Key information

Title: Production of hydrocarbon fuels from waste plastic
Application number: 20180957
Case type: National
Status: 15.03.2021 Patent meddelt (B1)
Filed: 06.07.2018
Effective date: 06.07.2018
Publicly available: 07.01.2020
Next annual fee due: 31.07.2026
Applicant: QUANTAFUEL AS (NO)
Owner: QUANTAFUEL AS (NO)
Inventor: Petter Kaalstad (NO) et al.
Agent: DEHNS NORDIC AS (NO)
Granted: 15.03.2021
Patent number: 345506
Expiry date: 06.07.2038

Abstract and drawing

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content.

The present invention relates to a method for producing fuel and additional hydrocarbons from waste plastic comprising the steps of providing at least one plastic material; exposing said at least one plastic material to a primary cracking to obtain a first hydrocarbon fluid; said first hydrocarbon fluid being a gas; exposing said first hydrocarbon gas to a catalytic hydrogenation to obtain a second hydrocarbon fluid; fractional separating said second hydrocarbon fluid to obtain at least one final product. The present invention further relates to a waste recycling system for recycling waste plastic into fluid hydrocarbon compounds.

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Date	Doc. No.	Process	Case number	In/Out	Journal description	To/from
02.12.2024	23-01	Saksbehandling	20180957(345506)	UT	PT Påminnelse om ikke betalt årsavgift (3329) (PT20180957)	DEHNS NORDIC AS
08.04.2021	02-01	Endring av fullmektig	2021/03898	UT	GH Forespørsel	DEHNS AS
22.03.2021	22-01	Saksbehandling	20180957(345506)	UT	PT Registreringsbrev Nasjonal Patent (15) (PT20180957)
18.03.2021	01-02	Endring av fullmektig	2021/03898	INN	20181011 Leogriff General PoA Quantafuel SIGNED	DEHNS AS
18.03.2021	01-01	Endring av fullmektig	2021/03898	INN	Generell henvendelse	DEHNS AS
27.01.2021	21-02	Saksbehandling	20180957	INN	2021-01-27 Patentstyret 20180957 kvittering Prioritetsdokument	DEHNS AS
27.01.2021	21-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
11.12.2020	20-01	Saksbehandling	20180957	UT	Intention to grant	DEHNS AS
18.11.2020	19-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
13.11.2020	18-07	Saksbehandling	20180957	INN	20180957 NORSK kravsett FILED	DEHNS AS
13.11.2020	18-06	Saksbehandling	20180957	INN	20180957 Figures	DEHNS AS
13.11.2020	18-05	Saksbehandling	20180957	INN	20180957 description MARKED	DEHNS AS
13.11.2020	18-04	Saksbehandling	20180957	INN	20180957 description CLEAN	DEHNS AS
13.11.2020	18-03	Saksbehandling	20180957	INN	20180957 CLAIMS amendments CLEAN	DEHNS AS
13.11.2020	18-02	Saksbehandling	20180957	INN	20180957 - response third OA	DEHNS AS
13.11.2020	18-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
10.11.2020	17-01	Saksbehandling	20180957	UT	Substantive examination	DEHNS AS
06.11.2020	16-05	Saksbehandling	20180957	INN	20180957 NORSK kravsett FILED	DEHNS AS
06.11.2020	16-04	Saksbehandling	20180957	INN	20180957 CLAIMS amendments MARKED	DEHNS AS
06.11.2020	16-03	Saksbehandling	20180957	INN	20180957 CLAIMS amendments CLEAN	DEHNS AS
06.11.2020	16-02	Saksbehandling	20180957	INN	20180957 - response second OA	DEHNS AS
06.11.2020	16-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
17.10.2020	15-01	Saksbehandling	20180957	UT	Substantive examination	DEHNS AS
17.10.2020	14-01	Saksbehandling	20180957	INN	Reply from patent agent 20190110	DEHNS AS
02.06.2020	13-01	Saksbehandling	20180957	UT	PT Varsel om betaling av første årsavgift (3317) (PT20180957)
15.11.2019	12-04	Saksbehandling	20180957	INN	Krav merket	DEHNS AS
15.11.2019	12-03	Saksbehandling	20180957	INN	Hovedbrev	DEHNS AS
15.11.2019	12-02	Saksbehandling	20180957	INN	Krav ren	DEHNS AS
15.11.2019	12-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
18.09.2019	11-01	Saksbehandling	20180957	UT	Generelt Brev Patent	DEHNS AS
13.09.2019	10-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	DEHNS AS
26.08.2019	09-02	Saksbehandling	20180957	INN	Skjema bestilling av pri.dok.	PLOUGMANN VINGTOFT NUF
26.08.2019	09-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	PLOUGMANN VINGTOFT NUF
11.07.2019	07-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	PLOUGMANN VINGTOFT NUF
11.07.2019	02-01	Endring av fullmektig	2019/08732	UT	GH Forespørsel	DEHNS AS
03.07.2019	08-02	Saksbehandling	20180957	INN	Fullmakt	PLOUGMANN VINGTOFT NUF
03.07.2019	08-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	PLOUGMANN VINGTOFT NUF
03.07.2019	01-02	Endring av fullmektig	2019/08732	INN	Fullmakt	DEHNS AS
03.07.2019	01-01	Endring av fullmektig	2019/08732	INN	Generell henvendelse	DEHNS AS
22.01.2019	06-02	Saksbehandling	20180957	UT	PT_report 02:06:41
22.01.2019	06-01	Saksbehandling	20180957	UT	Realitet patent	PLOUGMANN VINGTOFT NUF
08.01.2019	05-01	Saksbehandling	20180957	UT	Henv til fullmektig vedr kravsettene
11.10.2018	04-04	Saksbehandling	20180957	INN	Erklæring Søkers rett til oppfinnelse	PLOUGMANN VINGTOFT NUF
11.10.2018	04-03	Saksbehandling	20180957	INN	Fullmakt	PLOUGMANN VINGTOFT NUF
11.10.2018	04-02	Saksbehandling	20180957	INN	Fullmakt	PLOUGMANN VINGTOFT NUF
11.10.2018	04-01	Saksbehandling	20180957	INN	Korrespondanse (Hovedbrev inn)	PLOUGMANN VINGTOFT NUF
12.07.2018	03-01	Saksbehandling	20180957	UT	Formal Examination 1	PLOUGMANN VINGTOFT NUF
12.07.2018	02-01	Saksbehandling	20180957	UT	Infobrev til oppfinner	PLOUGMANN VINGTOFT NUF
06.07.2018	01-06	Saksbehandling	20180957	INN	Beskrivelse	PLOUGMANN VINGTOFT NUF
06.07.2018	01-05	Saksbehandling	20180957	INN	Krav	PLOUGMANN VINGTOFT NUF
06.07.2018	01-04	Saksbehandling	20180957	INN	Patenttegninger	PLOUGMANN VINGTOFT NUF
06.07.2018	01-03	Saksbehandling	20180957	INN	Sammendrag	PLOUGMANN VINGTOFT NUF
06.07.2018	01-02	Saksbehandling	20180957	INN	Søknadsskjema og tilleggsark oppfinnere	PLOUGMANN VINGTOFT NUF
06.07.2018	01-01	Saksbehandling	20180957	INN	Søknadsskjema Patent	PLOUGMANN VINGTOFT NUF

Description, claims and drawings

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content.

Description

PRODUCTION OF HYDROCARBON FUELS FROM WASTE PLASTIC

Field of the invention

This disclosure relates to the recycling of waste plastic and its transformation into hydrocarbon fuels, particulary diesel, and other hydrocarbon compounds by means of anaerobic thermal cracking and gas-phase catalytic hydrogenation, before fractional separation.

Background of the invention

Huge amounts of plastics end up in nature every year. The environmental consequences hereof have recently been realised. Not only does it destroy the esthetics of nature but it is realised that huge amount of microparticles are formed in particular in the oceans. These microparticles are taken up by fish and other organisms living in the ocean severely affecting their health.

At the same time, it is well known that the release of CO2 to the atmosphere could beneficially be reduced as CO2 is acknowledged to be a major factor in global heating. Advantageously, the extraction of petroleum products could be reduced in order to lower the CO2 outlet. One way of limiting this extraction could be by re-using and/or recirculating material made from petroleum products.

Thus, it would be beneficial for the environment if plastic materials were to be recycled and the release of additional CO2 into the atmosphere would be limited by lowering the extraction of petroleum products. This could be done for example by re-circulating the plastic material for producing hydrocarbon fuels from waste plastic.

WO 2018/055555 A1 discloses a method and a system for recycling waste plastic into fluid hydrocarbon compounds comprising a pyrolysis reactor for receiving a plastic material and producing a first hydrocarbon fluid, a catalytic hydrogenation reactor which produces a second hydrocarbon fluid by catalytic hydrogenation,

and a fractional separator which separates the second hydrocarbon fluid to

obtain at least one final product. The catalytic hydrogenation is energetic and designed to “hydrocrack” the large paraffins and aromatic hydrocarbons of the first hydrocarbon fluid.

US 2018/002609 A1 discloses a process similar to WO 2018/055555 A1 involving hydrocracking, with an additional Fluidised Catalytic Cracking (FCC) of the heavier fraction resulting from hydrocracking.

US 2016/264874 A1, with same assignee as WO 2018/055555 A1 and US 2018/002609 A1, discloses here a process similar to the one disclosed in the two first cited patents, involving “hydrocracking”, with a specific further cracking of the liquid fraction issued from pyrolysis.

JP 2009/242485 A seems (machine translation) to disclose a very energetic process where a hydrogenated pyrolysis is followed by a hydrocracking at very high pressure.

These patents disclose processes to re-cycle waste plastic materials into hydrocarbon fluids. However, they all include processes with repeated cracking, at pyrolysis level and at the following catalytic hydrogenation level, resulting in a higher selectivity towardslighter fractions, such as gas. An efficient process, preferably self-sufficient in terms of energy and directed for an optimal production of a bit heavier fuels, particularly diesel, is still needed.

Brief summary of the invention

An object of the present invention relates to a method and a system for re-using waste plastic to produce liquid fuel, gas and hydrocarbon compounds.

It is a further object of the present invention to re-use the energy obtained in the method for the method to be self-sufficient in terms of energy, for the method only to use a limited amount of extracted petroleum products thereby reducing potential human-produced CO2 emissions.

These objects are achieved according to the aspects and embodiments of the present invention as described herein.

In one aspect of the invention, a method for producing fuel, particularly diesel, and additional hydrocarbons from waste plastic is provided, comprising the steps of

- providing at least one plastic material;

- exposing said at least one plastic material to an anaerobic thermal cracking to obtain a first hydrocarbon fluid; said first hydrocarbon fluid being a gas; - exposing said first hydrocarbon gas to a catalytic hydrogenation to obtain a second hydrocarbon fluid;

- wherein said catalytic hydrogenation is performed at a pressure range of 0.1 to 10 bar, 10 preferably around 1 bar, and temperatures between 150-280oC, preferably between 190-230oC, such as around 200oC ;

- fractional separating said second hydrocarbon fluid to obtain at least one final product.

The method further comprises

- a further step of separating after said step of condensation, wherein said second hydrocarbon fluid is obtained at least via steps of catalytic hydrogenation, condensation and separation and wherein said second hydrocarbon fluid is a first hydrocarbon liquid obtained from said multiphase hydrocarbon fluid during separation.

Said separation further results in the formation of a first non-condensable hydrocarbon gas and wherein at least a part of said first non-condensable hydrocarbon gas is recirculated to and burnt in a gas burner to provide heat to said anaerobic thermal cracking.

In an embodiment, the method according to any of the preceding items further comprising a step of pre-hydrogenation catalytic cracking performed prior to the step of catalytic hydrogenation, and wherein said first hydrocarbon fluid is obtained at least via steps of anaerobic thermal cracking and pre-hydrogenation catalytic cracking.

In a further embodiment, the method further comprises a step of posthydrogenation catalytic cracking performed after the step of catalytic hydrogenation and wherein said second hydrocarbon fluid is obtained at least via steps of catalytic hydrogenation and post-hydrogenation catalytic cracking.

In a still further embodiment, the heavy fraction is recycled to the step of anaerobic thermal cracking, catalytic cracking and/or catalytic hydrogenation or to said holding tank.

In a still further embodiment, the heavy fraction is exposed to a step of heavy fraction cracking before being recycled to the step of anaerobic thermal cracking, catalytic cracking and/or catalytic hydrogenation or to said holding tank.

In a further aspect according to the invention, a waste recycling system for recycling waste plastic into fuel, particularly diesel, and additional hydrocarbon compounds is provided, comprising

- a anaerobic thermal cracking reactor capable of receiving at least one plastic material and producing a first hydrocarbon fluid from said at least one plastic material by an anaerobic thermal cracking, said first hydrocarbon fluid being a gas;

- a catalytic hydrogenation reactor capable of receiving said first hydrocarbon fluid and producing a second hydrocarbon fluid by catalytic hydrogenation,

- and a fractional separator capable of fractional separating said second hydrocarbon fluid to obtain at least one final product,

where said anaerobic thermal cracking reactor is in fluid connection with said catalytic hydrogenation reactor and said catalytic hydrogenation reactor is in fluid connection with said fractional separator.

The system further comprises

- a condenser for producing said second hydrocarbon fluid together with said catalytic hydrogenation reactor and resulting in said second hydrocarbon fluid being a multi-phase hydrocarbon fluid, and

- a separator for separating said multi-phase hydrocarbon fluid to provide a first hydrocarbon liquid and a first non-condensable hydrocarbon gas and - a gas burner for providing heat to said anaerobic thermal cracking reactor, said gas burner is fluidly connected with said separator.

In an embodiment, the system further comprises a post-fractional separation condenser, a non-condensable gas separator and a gas burner, said postfractional separation condenser being in fluidly connection with said fractional separator for receiving a light fraction obtained from the fractional separation process and wherein said post-fractional separation condenser is further fluidly connected with said non-condensable gas separator for separating a second noncondensable hydrocarbon gas; said non-condensable gas separator being further fluidly connected with said gas burner.

In a further embodiment, the system further comprises a pre-hydrogenation catalytic cracking reactor, wherein said anaerobic thermal cracking reactor is further fluidly connected with said catalytic hydrogenation reactor through said pre-hydrogenation catalytic cracking reactor.

In a still further embodiment, the system further comprises a post-hydrogenation catalytic cracking reactor, wherein said catalytic hydrogenation reactor is further fluidly connected with said fractional separator through said post-hydrogenation catalytic cracking reactor.

In a still further embodiment, the system further comprises a heavy fraction cracking reactor, said heavy fraction cracking reactor being in fluidly connection with said fractional separator for receiving a heavy fraction obtained from the fractional separation process and wherein said heavy fraction cracking reactor is further fluidly connected with said anaerobic thermal cracking reactor, said prehydrogenation catalytic cracking reactor, said post-hydrogenation catalytic cracking reactor and/or said catalytic hydrogenation reactor.

In a further aspect of the invention, the use of a system as described herein or a method as described herein for producing fuel and additional hydrocarbons from waste plastic is provided.

In a further use, the fluid hydrocarbon is diesel.

Brief description of the figures

The method and system for production of fuel and additional hydrocarbons from waste plastic according to the invention will now be described in more detail and with regard to the accompanying figures. The figures show one way of implementing the present invention and is not to be construed as being limiting to other possible embodiments falling within the scope of the invention.

Fig.1 shows a first embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation and fractional separation;

Fig.2 shows a second embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation, condensation and separation;

Fig.3 shows a third embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation and a pre-hydrogenation catalytic cracking;

Fig. 4 shows a fourth embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation and a post-hydrogenation catalytic cracking;

Fig.5 shows a fifth embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation and heavy fraction cracking, the product of which can be reinjected;

Fig.6 shows a sixth embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation and several paths for reinjection of the heavy fraction;

Fig. 7 shows a seventh embodiment of the invention presented as a process diagram comprising primary cracking, catalytic hydrogenation, fractional separation and re-circulation of a non-condensable gas isolated after fractional separation;

Fig. 8 shows an eight embodiment of the invention presented as a process diagram being a detailed embodiment according to the invention;

Fig. 9 shows a further embodiment of the invention presented as a process diagram comprising;

Fig. 10 shows an overview of an experimental set-up as used in experiment 1;

Fig. 11 shows the conversion results obtained in experiment 1 when initially screening alumina supported catalysts at 20 000 h-1 and 300oC;

Fig. 12 shows the carbon number distribution of the product obtained in experiment 2.

Detailed description of the invention

By “waste plastic” is to be understood waste, which is made entirely or primarily of plastic materials i.e. the level of non-plastic material in the waste should preferably be no more than 10 wt%.

By “plastic material” is to be understood a wide range of synthetic or semisynthetic organic polymers of high molecular mass such as polyolefins, acrylics, polyesters, silicones and polyurethanes. Examples of plastic materials are HDPE, LDPE, PP, PS, PET, ABS and PVC.

By “primary cracking” is to be understood a process where the molecules of the plastic materials are broken down to minor molecules. In one embodiment, the minor molecules are hydrocarbons primarily having a length of C1-C40, such as C1-C30. Primary cracking includes pyrolysis as well as other cracking types such as all types of anaerobic thermal cracking. Primary cracking is performed in a primary cracking reactor.

By “catalytic hydrogenation” is to be understood a process where hydrogen is used to saturate unsaturated hydrocarbons. The catalytic hydrogenation may or may not involve the action of catalysts. Catalytic hydrogenation is performed in a catalytic hydrogenation reactor.

By “catalytic cracking” is to be understood a process that cracks linear molecules to linear shorter molecules. It will normally have limited effect on aromatic compounds, and lighter molecules with carbon number lower than C7 are rarely cracked. The preferred embodiment for the so called “catalytic cracking” is with a catalyst. However, it covers the alternative use of a cracker without catalyst i.e. a non-catalysed cracking such as steam-cracking or delayed coking. Catalytic cracking is performed in a catalytic cracking reactor.

By “heavy fraction cracking” is to be understood a cracking process i.e. where linear molecules are cracked to linear shorter molecules on the heavy fraction from the fractional separation. This process can be performed with or without the addition of catalysts. Preferably, the process is performed without catalysts.

Heavy fraction cracking is performed in a heavy fraction cracking reactor.

By “residence time” is to be understood the time in which a particular molecule is present in the reactor i.e. from entering the reactor to exiting the reactor.

By “fractional separation” is to be understood a process for obtaining several fractions with a good degree of separation i.e. only having a minimal overlap of hydrocarbon chains having similar length in the fractions i.e. if a separated fraction comprises C6 to C10, the following fraction will comprise at the most 50 wt% C6 to C10, preferably at the most 25 wt% C6 to C10, such as at the most 20 wt% C6 to C10, like the most 15 wt% C6 to C10, more preferred at the most 10 wt% C6 to C10, like at the most 5 wt% C6 to C10. The fractional separation may be a distillation or a number of condensation steps. Fractional separation is performed in a fractional separator.

By “catalyst” is to be understood a substance that causes or accelerates a chemical reaction without itself being affected.

By “first hydrocarbon fluid” is to be understood a fluid i.e. a liquid or a gas entering the catalytic hydrogenation step in the catalytic hydrogenation reactor.

The first hydrocarbon fluid may comprise a water content of 50 wt% or less, like 45 wt% or less, such as 40 wt% or less, like 35 wt% or less, such as 30 wt% or less, like 25 wt% or less, such as 20 wt% or less, like 15 wt% or less, such as 10 wt% or less, like 5 wt% or less, such as 1 wt% or less.

By “second hydrocarbon fluid” is to be understood a fluid i.e. a liquid or a gas entering the fractional separation step in the fractional separator. The second hydrocarbon fluid may comprise a water content of 50 wt% or less, like 45 wt% or less, such as 40 wt% or less, like 35 wt% or less, such as 30 wt% or less, like 25 wt% or less, such as 20 wt% or less, like 15 wt% or less, such as 10 wt% or less, like 5 wt% or less, such as 1 wt% or less.

By “multi-phase hydrocarbon fluid” is to be understood a fluid having at least two phases such as for example a liquid phase and a gas phase, two liquid phases, two liquid phases and two gas phases, two liquid phases and one gas phase and two gas phases and one liquid phase.

The fluid may comprise a water content of 50 wt% or less, like 45 wt% or less, such as 40 wt% or less, like 35 wt% or less, such as 30 wt% or less, like 25 wt% or less, such as 20 wt% or less, like 15 wt% or less, such as 10 wt% or less, like 5 wt% or less, such as 1 wt% or less.

By “non-condensable gas” is to be understood a gas, which is not condensed given the particular setting (pressure and temperature) of the condensation and thus remains as a gas after the condensation process.

By “light fraction” is to be understood a fraction obtained from the fractional separation process, where the fraction includes the shortest hydrocarbon chains of the separation. This would often be hydrocarbon chains as present in gasoline. In one embodiment, the light fraction comprises mainly C6-C10 hydrocarbons. In a further embodiment, the light fraction comprises at least 99 wt% C6-C10 hydrocarbons, such as at least 98 wt% C6-C10 hydrocarbons, like 95 wt% C6-C10 hydrocarbons, such as at least 90 wt% C6-C10 hydrocarbons, like 85 wt% C6-C10 hydrocarbons, such as at least 80 wt% C6-C10 hydrocarbons, like 75 wt% C6-C10 hydrocarbons, such as at least 70 wt% C6-C10 hydrocarbons, like 65 wt% C6-C10 hydrocarbons, such as at least 60 wt% C6-C10 hydrocarbons, like 50 wt% C6-C10 hydrocarbons.

By “medium fraction” is to be understood a fraction obtained from the fractional separation process, where the fraction includes hydrocarbon chains of medium length when separated. This would often be hydrocarbon chains as present in diesel. In one embodiment, the medium fraction comprises mainly C11-C20 hydrocarbons, which is the standard length used in diesel. In a further embodiment, the medium fraction comprises at least 99 wt% C11-C20 hydrocarbons, such as at least 98 wt% C11-C20 hydrocarbons, like 95 wt% C11-C20 hydrocarbons, such as at least 90 wt% C11-C20 hydrocarbons, like 85 wt% C11-C20 hydrocarbons, such as at least 80 wt% C11-C20 hydrocarbons, like 75 wt% C11-C20 hydrocarbons, such as at least 70 wt% C11-C20 hydrocarbons, like 65 wt% C11-C20 hydrocarbons, such as at least 60 wt% C11-C20 hydrocarbons, like 50 wt% C11-C20 hydrocarbons.

By “heavy fraction” is to be understood a fraction obtained from the fractional separation process, where the fraction includes hydrocarbon chains of long length when separated. This fraction may also be mentioned as heavy oil. In one embodiment, the heavy fraction comprises mainly C21 and above hydrocarbons. In a further embodiment, the heavy fraction comprises at least 99 wt% C21 and above hydrocarbons, such as at least 98 wt% C21 and above hydrocarbons, like 95 wt% C21 and above hydrocarbons, such as at least 90 wt% C21 and above hydrocarbons, like 85 wt% C21 and above hydrocarbons, such as at least 80 wt% C21 and above hydrocarbons, like 75 wt% C21 and above hydrocarbons, such as at least 70 wt% C21 and above hydrocarbons, like 65 wt% C21 and above hydrocarbons, such as at least 60 wt% C21 and above hydrocarbons, like 50 wt% C21 and above hydrocarbons.

Feed material specifications, sorting and pre-treatment

In one embodiment, said at least one plastic material is pre-treated prior to said primary cracking. In a further embodiment, the system further comprises means for pre-treating said at least one plastic material prior to being received by said primary cracking reactor such as means for shredding and/or means for drying.

The desired plastic material is cleaned if it is contaminated in such grade that the intermediary or final products or by-products specifications do not respect requirements, and dried if necessary according to same principle criteria.

Contamination may be in the form of organic matter, glass, sand, earth particles or any other form of contamination found in e.g. household or industrial waste, or added to the material during collection, transport or handling and storage phases. The level of contamination should be as low as possible, and preferably no more than 10 wt%, even preferably less than 5 %, or even better less than 1 or 2 %.

The water content, mostly in the form of water on the surface of the plastic material, should be as low as possible and preferably not higher than 5 wt%, preferably less than 3 %, or even better less than 1 %. Should water content be too high, for example higher than 5 wt%, drying may be required. A high water content in the feedstock material such as 10 wt%, 15 wt%, 20 wt% or 25 wt% water would be possible, but the production capacity may end up to be lower due to a lower throughput of the plant.

Water entering the primary cracking reactor may be separated and extracted from the produced oil and gas in the process by means of a non-condensable gas separator or a Holding Tank.

In a still further embodiment, the at least one plastic material is HDPE, LDPE, PP and/or PS.

The plastic compositions desirable in the process are HDPE, LDPE, PP and PS. Plastics of the respective types PET, PVC and ABS are less desirable and preferably kept under 1 wt% fraction each in a standard plant, but may be higher if the plant is equipped with process units or chemical additives removing the additional unwanted chemical elements which the treatment of these plastic types may generate:

• PET contains oxygen that may lead to the formation of alcohols, acids, ketones, aldehydes, esters and other oxygenated compounds in the oil products.

• ABS, in addition to cyanides, amines and amides in the oil products, may produce dioxins when chlorine is present, and mercaptans (thiols) when Sulphur is present. It may also lead to an increase of NOx during combustion of non-condensable gases.

• PVC contains more than 50 wt% chlorine and may contribute to the formation of some of the molecules described above, plus HCl and Chlorine.

• In addition to generating unwanted molecules, PET, PVC and ABS will also reduce the capacity of the process by forming fewer alkanes.

In a still further embodiment, the at least one plastic material is pre-treated by shredding and/or sorting said at least one plastic material.

In one embodiment, the material may be shredded into manageable pieces, preferably in the size range of 5-500 mm, more preferably 10-250 mmm, even more preferably 10-100 mm.

In a further embodiment, the material may be stored in a buffer hopper, or filled in a hopper feeding for example a conveyor to the primary cracking reactor.

In one embodiment, the plastic material is fed after selection and optional pretreatment to a primary cracking reactor via a feeding system. The feeding system may comprise a dosing bin and the screw conveyer. Other feeding systems as known in the art may also be used.

In one embodiment, the screw conveyer may include, at one or several stage(s), compression of the plastic feed in order to reduce the amount of air fed into the primary cracking reactor.

Primary cracking

The step of primary cracking is performed in a primary cracking reactor. Primary cracking is to be understood as pyrolysis as well as other cracking types such as all types of anaerobic thermal cracking. In a preferred embodiment, primary cracking is pyrolysis. In a still further embodiment, the primary cracking reactor is a pyrolysis reactor.

The term pyrolysis is used interchangeably with the terms primary cracking and anaerobic thermal cracking throughout the description.

The main primary cracking reaction that provides a carbon distribution of alkanes and olefins primarily from C1-C40, such as C1-C30 is:

There is a primary cracking reaction side-reaction that produces carbon and hydrogen:

There will also be reactions that produce naphthenes (cyclic alkanes), but also aromatic and poly-aromatic hydrocarbons that are not listed here, as known in the art.

In the primary cracking process of cracking plastic, some by-products are formed in the shape of solid carbon particles, or char, as described in Reaction 2. The solid particles are preferably removed from the reactor and optionally cooled, to avoid self-ignition, before further handling. One of such handling may be combustion in order to generate heat for the primary cracking reactor.

Hydrogen is formed in parallel with carbon, and is consumed in the following process steps of the invention, mainly in the catalytic hydrogenation step.

The residence time in the primary cracking reactor may typically vary between 0.1 to 10 hours, preferably between 20 and 90 minutes, even more preferably 30 to 60 minutes.

The primary cracking reactor may also receive a complementary feed of a part or whole of a heavy fraction from the fractional separation.

The primary cracking may be performed with or without catalysts.

In one embodiment, the primary cracking is performed without catalysts.

In one embodiment, the primary cracking reactor does not contain catalysts (thermal cracking mode) modifying the composition of the hydrocarbons exiting the primary cracking reactor. The absence of catalysts will reduce the operating costs (opex) of the primary cracking as well as simplifying the design of the reactor (capex).

In another embodiment, the primary cracker contains catalysts, such as known zeolites or based on active metals, such as Ni, Cd, Mo etc.

In one embodiment, the reactor may contain silico-aluminates to reduce the optimal temperature of reaction. These are consumed and discharged with the solid char fraction. The reactor may also contain minerals such as CaO to capture Cl and S according to techniques known in the art. The resulting fraction is solid and will also be discharged with the char fraction. Silico-aluminates and calcium minerals mentioned above are not considered catalysts, as they are consumed in the process.

In one embodiment, the primary cracking reactor is operated at about 420oC, i.e. the temperature of produced hydrocarbons as measured at the terminal outlet of the reactor is about 420oC. More generally, the primary cracking reactor will be operated at temperatures from between 300°C to 550°C, preferably between 380oC and 460oC.

Throughout this description, the operating temperature of the primary cracking reactor is defined by the temperature at the terminal outlet, i.e. the outlet of the last zone of the reactor, before extraction to next process step.

Depending on the reactor design and operating parameters, different zones in the primary cracking reactor may have different temperatures. For example, some primary cracking reactors show an increasing gradient of temperature from the inlet where the at least one plastic material is received, to the outlet of the primary cracking reactor where the product formed, i.e. the first hydrocarbon fluid, exits the primary cracking reactor.

In one embodiment, plastic fed into the primary cracker is vapourised upon entry into the reactor. In another embodiment, the primary cracker comprises a first melting chamber with moderate temperature to produce an intermediary molten plastic product.

Some reactors may have several outlets, and several inlets, enabling for process optimisation extraction and/or injection/reinjection of the first hydrocarbon fluid or other gasses - such as the combustion gasses of the burner heating the primary cracker - in different zones of the reactor.

In one embodiment, the operating pressure will be kept around 1 bar. In another embodiment, the operating pressure is within a range of 0.1 and 10 bar, such as in the range from 0.5 to 5 bar, like in the range from 0.7 to 2 bar, such as in the range from 0.9 til 1.1 bar.

The optimal temperature and pressure of the product at the outlet will vary. It will depend i.e. on the nature of the feed and on the design of the primary cracker reactor.

The primary cracking will i.a. produce non-condensable gases – mainly alkanes with carbon length of 1 to 6. The non-condensable gas may be burned in a gas burner using air for combustion, thus providing heat to the primary cracking reactor. The production of non-condensable gas will depend on the nature of the feed such as type of plastic as well as the operations parameters of the primary cracking reactor such as temperature and pressure. The amount of noncondensable gases is preferably adjusted to be sufficient to heat the primary cracking reactor during running operation. If for any reason there is a shortage of non-condensable gas, increasing the temperature of the primary cracking reactor or the residence time of the plastic material in primary cracking reactor will increase the production of non-condensable gas, thus correcting the shortage.

Additionally and/or complementarily, additional fuel for combustion may be supplied from a commercial fuel source. The commercial fuel source is also designed for start-up of the primary cracking process: before reaching a stable running operation upon start, the primary cracking reactor will need to be heated up with readily burnable commercial fuels. This often needs to be performed for several hours. Examples of possible fuels are carbon, gasoline, diesel, any type of heavy oil, Liquefied Petroleum Gas (LPG), natural gas (NG), non-condensable gas etc.

Combustion gas from the gas burner (high temperature) will be mixed with returning exhaust gas (lower temperature after heat transfer to the primary cracking reactor) and recycled from the outlet of the primary cracking reactor to reduce the temperature and ensure a gas velocity enabling good heat transfer to the plastic inside the reactor.

In one embodiment, the recycling rate may tentatively vary from 10 to 70% of produced exhaust gas.

In a further embodiment, the temperature of the exhaust gas may vary from 400 to 800°C, preferably 500 to 600oC, more preferred about 550 °C. These temperatures will depend on a number of parameters, of which the plastic feed and the type of reactor.

In one preferred embodiment, the primary cracking reactor is of an indirect heating type, i.e. the main source of heat is not mixed with the waste plastic feed in the reactor.

Filtration and cooling after primary cracking

In a still further embodiment, the method further comprises filtering and optionally cooling after the step of primary cracking.

In one embodiment, the first hydrocarbon fluid leaving the primary cracking reactor after e.g. pyrolysis is filtered to remove carbon particles formed in the primary cracker and not discharged as solids e.g. char.

In order to protect the process units downstream, contaminants such as sand, glass, and unreacted plastic will also need to be either collected with char and solids at the bottom/end-part of the primary cracking reactor, or filtered when transported by the fluid exiting the primary cracker..

The particles borne by the first hydrocarbon fluid being a first hydrocarbon gas are expected to have sizes of one to several hundred µm. The amount of the particles are expected to vary with inlet water content, plastic type, contamination and the performance of the pyrolysis reactor.

Filtration methods known in the art may be used to this purpose. In one embodiment, filters will be designed to remove up to at least 95 % of particles larger than 5 microns. In a further embodiment, the filtration will be performed using a cyclone filter.

In a further embodiment, the gas temperature is adjusted to the temperature expected downstream, by means of heat exchangers. The temperature is preferably adjusted after filtering.

In a further embodiment, the gas pressure is adjusted to the pressure expected downstream by means of pressure reducing devices, such as a pressure control valve or other pressure control devices.

Hydrogenation Reactor

After the primary cracking and optional filtration, temperature and pressure adjustments, the first hydrocarbon fluid will undergo a catalytic hydrogenation in a catalytic hydrogenation reactor.

In principle, all unsaturated hydrocarbon molecules such as alkenes, alkynes, aromatics etc. containing a double or triple bond may react in the catalytic hydrogenation process, resulting in the molecules becoming saturated. An example of hydrogenation is shown below:

-CH=CH- H2 => -CH2-CH2- (3)

Olefin Hydrogen Alkane

The catalytic hydrogenation is run in gas phase. In one preferred embodiment, the process is run at conditions such as pressure and temperature above the Dew Point of the gas feed entering the catalytic hydrogenation reactor.

In a further embodiment, potential condensates in the gas are drained before entering the catalytic hydrogenation reactor i.e. upstream of the catalytic hydrogenation reactor.

The operating temperature at one bar will typically be between 150-280oC, preferably between 190-270oC. In one embodiment, the operating temperature will be around 190-200oC. In another embodiment, the operating temperature will be about 270oC.

In a still further embodiment, the catalytic hydrogenation is performed at an operating pressure of 1 bar and by temperatures between 150-280°C, preferably between 190-230°C, such as around 200°C.

In one embodiment, the catalytic hydrogenation is improved by adding hydrogen at several different locations along the catalytic hydrogenation reactor. Hereby, the concentration profile of the hydrogen through the catalyst is improved.

Hydrogen is often provided by the primary cracking reaction resulting from the decomposition as detailed in reaction 2. Thus, the first hydrocarbon fluid would be expected to hold some hydrogen. However, in some embodiments, addition of external hydrogen may be necessary.

Many types of reactors may be used for catalytic hydrogenation. In one embodiment, a packed-bed reactor is used. In another embodiment, a fixed-bed reactor is used, for example filled with a honeycomb structure. In a further embodiment, a fluidised-bed reactor is used.

In one embodiment, the Space Velocity (SV) of the reactor is in a range of from 50 000 to 200 h-1. The SV is calculated as the flow of the fluid to be processed divided by the bed volume of the reactor.

For a packed-bed reactor, the range is preferably from 50 000 to 10 000 h-1, such as from 50 000 to 30 000 h-1, like from 30 000 to 20 000 h-1, such as from 20 000 to 15 000 h-1, like from 15 000 to 10 000 h-1.

For a fixed-bed reactor, an expected range will be 10000 to 200 h-1, such as from 10 000 to 5 000 h-1, like from 5000 to 2 000 h-1, such as from 2 000 to 1 000 h-1, like from 1000 to 500 h-1, such as from 500 to 200 h-1.

The catalytic hydrogenation reactor may have an open structure. In one embodiment, flow openings will be of 0.1 to 10 mm, such as 0.5-8 mm, like 1-6 mm, such as 1.5-5 mm, preferably 2-4 mm.

Many catalysts are known to function well for hydrogenation and can be used in this application. For example a catalyst such as Cu-Mn/Al2O3 can be used for the catalytic hydrogenation. Other hydrogenation catalysts with good performances may also be used such as Ru/C, Pt/ASA or PtPd/ASA (where ASA is Amorphous Silica-Alumina) and CoMo/ɣ-Al2O3.

In one embodiment, the catalytic hydrogenation reactor receives a complementary feed of a heavy fraction from the fractional separator either directly from the fractional separator or after the heavy fraction has been exposed to a heavy fraction cracking.

The formation of coke or other impurities on the catalyst surface may deactivate the catalyst. Therefore, regeneration of the catalyst may be required.

In one embodiment, the catalytic hydrogenation reactor is equipped with an insitu cleaning/regenerating system, as known in the art.

In another embodiment, regeneration may be performed in a plant or in dedicated facilities after extraction of the catalyst from the reactor.

In one embodiment, the catalytic hydrogenation follows primary cracking and optionally filtration and cooling of the gas before entering the catalytic hydrogenation. In this embodiment, a heat exchanger cools the gas coming from primary cracking (preferred temperature of 420oC) before entering the catalytic hydrogenation (preferred temperature below 270oC).

In one embodiment, the required specification for the final product is EN590, and in some cases, the combination of the primary cracking and catalytic hydrogenation without further processing such as for example an additional catalytic cracking would not produce expected yield and quality.

Catalytic cracking

In a further embodiment, the gas may undergo an additional cracking step after primary cracking, and optionally filtration and cooling, this time a catalytic one. This additional step may be selected in order to improve productivity, and in particular in order to break long chain molecules such as C21 and above, like C21-C40, such as C21-C30 in the final product. The additional catalytic cracking step may take place before the catalytic hydrogenation (pre-hydrogenation catalytic cracking) or after (post-hydrogenation catalytic cracking).

Throughout the description catalytic cracking and catalytic cracking reactor will refer to both pre-hydrogenation catalytic cracking and post-hydrogenation catalytic cracking as well as pre-hydrogenation catalytic cracking reactor and posthydrogenation catalytic cracking reactor.

The catalytic cracking reactor will mainly crack linear molecules to linear shorter molecules. It will normally have limited effect on aromatic compounds, and lighter molecules with carbon number lower than C7 are rarely cracked. The catalyst will crack C-C bonds but may also give rise to isomerization of molecules.

In one embodiment, the temperature as measured in the catalytic cracking reactor is kept around 420°C, but the catalytic cracking reactor may also be operated at temperatures from between 350°C to 550°C, and preferably between 380 and 460°C.

In one embodiment, the operating pressure is around 1 bar. In a further embodiment, the operating pressure is in a range between 0.1 and 10 bar, such as in the range from 0.5 to 5 bar, like in the range from 0.7 to 2 bar, such as in the range from 0.9 til 1.1 bar.

Multiple types of reactor may be used. In one embodiment, a packed-bed reactor is used. In another embodiment, a fixed-bed reactor is used, for example filled with a honeycomb structure. In a further embodiment, a fluidised-bed reactor is used.

In one embodiment, the Space Velocity (SV) of the reactor may typically be within a range from 50 000 to 200 h-1.

For a packed-bed reactor, a typical range will be 50 000 to 10 000 h-1, such as from 50 000 to 30 000 h-1, like from 30 000 to 20 000 h-1, such as from 20 000 to 15 000 h-1, like from 15 000 to 10 000 h-1.

For a fixed-bed reactor, a typical range will be 10 000 to 200 h-1, such as from 10 000 to 5 000 h-1, like from 5 000 to 2 000 h-1, such as from 2 000 to 1 000 h-1, like from 1000 to 500 h-1, such as from 500 to 200 h-1.

The catalytic reactor may have an open structure. In one embodiment, flow openings will be of 0.1 to 10 mm, such as 0.5-8 mm, like 1-6 mm, such as 1.5-5 mm, preferably 2-4 mm.

Many catalysts are known to function well for catalytic cracking and can be used according to the invention for example ultrastable Y zeolite (USY) for catalytic cracking. Other catalytic cracking catalysts with good performances may also be used such as acid zeolite catalysts, where USY in an example. Mixed metal sulphides or noble metal catalysts are also used.

The formation of coke or other impurities on the catalyst surface will deactivate the catalyst. Because of this, regeneration of the catalyst is advantageously performed. In one embodiment, the reactor is equipped with an in-situ cleaning/regenerating system, as known in the art for example a system using air, water or inert gas mixture to regenerate the catalyst.

In another embodiment, regeneration may be performed in the plant or in dedicated facilities after extraction of the catalyst from the catalytic cracking reactor.

The pre- or post-hydrogenation catalytic cracker reactor may also receive a complementary feed of a part or whole of the heavy fraction from the fractional separator either directly i.e. without being further processed, from the fractional separator or after the heavy fraction has been exposed to a heavy fraction cracking.

In a further embodiment, a heavy fraction cracker may process the heavy fraction obtained from the fractional separator before re-injecting it upstream in the process. Hereby, the production of light and medium fractions obtained from fractional separation can be increased.

In one embodiment, the catalytic cracker is preferably run at higher temperature than the hydrogenation reactor, in particular in a range of temperature close to the one of the primary cracking reactor such as preferably at a temperature around 420 °C. Thus, from a point of view of the plant energy efficiency the catalytic cracking is preferably a pre-hydrogenation catalytic cracking. The gas flowing out of the primary cracking reactor will thus need no cooling – nor any pressure reduction - before entering the pre-hydrogenation catalytic cracking reactor. After pre-hydrogenation catalytic cracking, cooling may be required before entering the catalytic hydrogenation reactor, in order to bring the temperature of the first hydrocarbon fluid at the outlet of the pre-hydrogenation catalytic cracker from an operation temperature of for example 420°C, down to below 270°C.

In another embodiment, the catalytic cracking may be a post-hydrogenation catalytic cracking. This is advantageous for optimisation of hydrogen consumption. Catalytic hydrogenation consumes a high amount of hydrogen compared with catalytic cracking, and hydrogen is to come primarily from the primary cracking. In case the amount of hydrogen from the primary cracking reaction is limited, the catalytic cracking after hydrogenation can be a mean to reduce the consumption of the additional hydrogen to be purchased from an industrial gas supplier.

Using post-hydrogenation catalytic cracking may result in re-creation of unsaturated molecules and the necessity of heating up the gas obtained from the catalytic hydrogenation to a temperature required for catalytic cracking, which is energy consuming.

Condensation and separation

In one embodiment, a condenser is arranged after catalytic hydrogenation and/or post-hydrogenation catalytic cracking for the produced hydrocarbon fluid to flow into the condenser. In the condenser, the temperature is reduced to achieve condensation. From temperatures of for example 270°C or 200°C (outlet of the catalytic hydrogenation reactor) or 420°C, (outlet of the catalytic cracking reactor), the gas is cooled to preferably 100-130°C, more preferred 110°C, at a pressure in the range of 0.5-1 bar, most preferred 0.7-0.9 bar. Hereby, most of the gas is condensed and forms a multi-phase hydrocarbon fluid comprising at least a first non-condensable gas and a first hydrocarbon liquid.

In a further embodiment, the exit temperature of the condenser is 110oC, to keep water in vapour phase and facilitate water separation from hydrocarbon liquid (oil). Preferably, the temperature is kept above 60oC as at lower temperatures, for example below 60 °C, there is a risk of undesirable wax deposition.

In a further embodiment, the fluid after condensation i.e. the multi-phase hydrocarbon fluid passes through a separator, where the hydrocarbon liquid fraction (with a possible limited water fraction, of preferably max 0,2 %) is separated from the non-condensable gas fraction (which may contain a small fraction of water vapour).

In a further embodiment, the second hydrocarbon fluid, after optional cooling, and with optional purification (see below), is transferred to a Holding Tank. In one embodiment, the temperature of the Holding Tank is in a range of 60 to 80oC, preferably around 60oC.

In a further embodiment, the second hydrocarbon fluid is further purified before entering the Holding Tank.

In a still further embodiment, the separation further results in the formation of a first non-condensable hydrocarbon gas and wherein at least a part of said first non-condensable hydrocarbon gas is recirculated to and burnt in a gas burner to provide heat to said primary cracking.

In a still further embodiment, the at least a part of said first non-condensable hydrocarbon gas is exposed to further processing before being burnt such as further condensation and separation.

Purification of the hydrocarbon liquid

In a further embodiment, impurities are removed after catalytic hydrogenation and/or catalytic cracking. Impurities may be acids, alcohols, other oxygenated organic compounds, HCl and H2S to mention the most common ones. For the hydrocarbon liquid, such purification will take place at any location between the separator and the Holding Tank. In one embodiment, purification of the second hydrocarbon fluid will take place in the Holding Tank.

In one embodiment, small amounts of water/NaOH solution, alternatively any substance that neutralize acids such as CaO or Ca(OH)2 are added to the hydrocarbon liquid.

Some of the purification reactions that take place are listed below:

Alcohol:

R-OH NaOH = R-ONa H2O (4)

Acid:

R-COOH NaOH = R-COONa H2O (5)

Hydrogen sulfide:

H2S 2NaOH = Na2S 2H2O (6)

Hydrochloric acid:

HCl NaOH = NaCl H2O (7)

The formed sodium salts dissolve in water, which may be separated from hydrocarbon fluid in the Holding Tank.

Fractional separation

After catalytic hydrogenation optionally followed by further processing as described above, the second hydrocarbon fluid is fractional separated for segregation of different mixes of hydrocarbons.

The fractional separation process can be distillation or a number of condensation steps in order to obtain several fractions having a good degree of separation.

In one preferred embodiment, the second hydrocarbon fluid is fractional separated by distillation.

In a further embodiment, the second hydrocarbon fluid such as the first hydrocarbon liquid in the Holding Tank, being for example 60°C, is heated to for example 160°C before entering a fractional separator. This allows controlling of the final product fractions, based on their respective physical and chemical properties for example the boiling point. The previous primary cracking is expected to produce excess energy, a fraction of which may be available for fractional separation.

In a still further embodiment, the first hydrocarbon liquid is heated before fractional separation.

The fractional separator may use packed beds, sieve trays, clock bottoms, packing material or other material that ensure good gas/liquid contact. The quality of the contact is important to get good separation of the components in the tower. In one embodiment, packed beds may be used.

In one embodiment, it is envisaged to collect three fractions from the fractional separator, a light fraction, a medium fraction, and a heavy fraction. In a still further embodiment, three final products are obtained from said fractional separation step being a light fraction such as mainly C6 to C10; a medium fraction such as mainly C11 to C20 and a heavy fraction such as mainly C21 and above.

Typically, the light fraction is collected at the top of the column after being condensed. The medium fraction, typically a diesel product, is collected between the bottom and the top of the column where the quality is according to specifications. The heavy fraction is collected at a low point of the column.

The definitions of the fractions vary in literature and the industry, depending on the focus, but also because chemistry involved is not strictly segmented by the number of carbons. According to this invention, the fractions are to be understood as and defined by:

• light fraction: mainly C6 to C10

• Diesel (medium fraction): mainly C11 to C20.

• Heavy fraction: mainly C21 and higher.

In a still further embodiment, the light fraction is condensed and optionally separated resulting in at least a second non-condensable hydrocarbon gas, and wherein at least a part of said second non-condensable hydrocarbon gas is recirculated to and burnt in a gas burner to provide heat to said primary cracking.

In still further embodiments, the number of products (“fractions”) obtained from the fractional separator may be less or more than tree i.e. two, four, five or six. In In a still further embodiment, the ranges of carbon atoms may be different than as described above. For example C6 to C11, C12-C21 and C22 and higher.

The reboiler is located at the bottom of the tower. The reboiler supplies the necessary heat to the fractional separator, in particular consumed for evaporation.

In one embodiment, the fractional separator operates at vacuum, but may also be designed to operate at any pressure, typically up to 50 bar.

In a further embodiment, the fractional separator is designed to operate at vacuum, with the feed pre-heated to approximately 160 °C in a pre-heater before entering the fractional separator. At this temperature, the feed will be approximately 50/50 wt% split of vapour and liquid. Due to the mixed feed stream after heating, a flash vessel is introduced before the fractional separator to ensure adequate liquid-vapour separation so that the vapour does not create turbulence and disturb the equilibrium of the fractional separator.

In a further embodiment, the diameter of the column is 1000 mm and the height 15 000 mm.

In one embodiment, the top operating pressure of the column is 100 mbar to maintain bottom temperature at 290°C.

To provide some process flexibility to the fractional separator, the feed can be introduced to the fractional separator at different feed locations and also side draw locations can be adjusted. Such fractional separator will not be detailed further, as it is known to a person skilled in the art.

As previously described, the heavy fraction can be in part or in whole recirculated into the process. It can be fed into the primary cracking reactor, the prehydrogenation catalytic cracking reactor or as an alternative to the posthydrogenation catalytic cracking reactor without any significant treatment, or in several of these reactors at the same time when they are present in the process.

In one embodiment, the heavy fraction is recirculated into the reactors without specific chemical treatment. The fraction will though preferably be heated to vaporisation so as to obtain a hydrocarbon gas fraction. The heavy fraction may be returned in whole or in part to the primary cracking reactor in which case vaporisation may not be necessary. As an alternative, the heavy fraction may be returned in whole or in part to the catalytic cracker. These recirculation loops are typically designed and activated on the basis of modelled or observed process operation parameters. Recirculation may in turn require process adjustments as the load may vary to the different reactors, as is known in the process industry.

As an alternative, it can be fed to a dedicated heavy fraction catalytic cracker, as will be described below.

Heavy fraction cracking

In a further embodiment, the method comprises a step of heavy fraction cracking performed in a heavy fraction cracking reactor, which solely runs on the heavy fraction from the fractional separation. In doing so, the yield of diesel is increased as the longer hydrocarbon chains in the heavy fraction are cracked to shorter chains within the diesel range.

In one embodiment, this alternative is preferred to catalytic cracking of the whole hydrocarbon gas (pre- or post-hydrogenation) as undesired cracking of the potential “diesel fraction” of the gas into a lighter fraction are prevented when the gas is light.

In a further embodiment, the liquid heavy fraction is heated and vaporized to a temperature of close to 420°C before entering the heavy fraction catalytic cracker. The heavy fraction catalytic cracker may be operated at temperatures between 350°C and 550°C, and preferably between 380 and 460°C, where the temperature ranges are defined for operation at 1 bar. In one embodiment, the operating pressure is kept around 1 bar, but operation is considered at pressure range between 0.1 and 10 bar, such as in the range from 0.5 to 5 bar, like in the range from 0.7 to 2 bar, such as in the range from 0.9 til 1.1 bar.

The resultant stream from heavy fraction cracking is in one embodiment a gas phase, and may be introduced upstream the catalytic hydrogenation reactor or upstream the fractional separator.

When the stream resulting from the heavy fraction cracking is fed to the catalytic hydrogenation, it should be cooled to the temperature of the catalytic hydrogenation reactor, for example at below 270°C at 1 bar as described above.

If the resultant stream is introduced after the catalytic hydrogenation directly to fractional separator or into the Holding Tank, the stream will be cooled to the temperature of the Holding Tank, for example around 60 °C.

Furthermore, when performing a heavy fraction cracking, it is important to ensure there is sufficient hydrogen to ensure double bonds are not present after cracking, as heavy fraction cracking of the heavy fraction may else form double bonds during the reaction. Thus, in one embodiment, an additional source of industrial hydrogen gas may be added.

Non-Condensable Gas

During primary cracking and the additional treatments, non-condensable gas may be formed. The non-condensable gas fraction after primary cracking will contain alkanes, alkenes, alkynes and cyclic hydrocarbons with a carbon number mainly less or equal to 6. After separation following catalytic hydrogenation or catalytic cracking, it will mainly consist of alkanes with a carbon number from 1 to 6.

In the present context, “a carbon number mainly less or equal to 6” is to be understood as preferably at least 50 wt% has a carbon number below 6, such as at least 55 wt% has a carbon number below 6, like at least 60 wt% has a carbon number below 6, more preferred at least 65 wt% has a carbon number below 6, such as at least 70 wt% has a carbon number below 6, like at least 75 wt% has a carbon number below 6, for example at least 80 wt% has a carbon number below 6, most preferred at least 85 wt% has a carbon number below 6, such as at least 90 wt% has a carbon number below 6, like at least 95 wt% has a carbon number below 6, such as at least 97 wt% has a carbon number below 6, like at least 99 wt% has a carbon number below 6.

In one embodiment, the first non-condensable gas after separation is further cooled to partial condensation, generally producing a 3-phase fluid comprising gas, oil, and water. In one embodiment, the gas is cooled down to around 35oC. The fluid is then separated. An embodiment for the Non-Condensable Gas Separator is a modified cyclone within a tank, achieving a 3-phase separation, gas, oil and water.

In a further embodiment, the gas is transferred to a gas scrubber/filter as known in the art to ensure that the gas is clean and without contaminants like S and Cl, and running at about the same temperature (for example 35°C). The cleaned noncondensable gas will then be combusted in the gas burner to heat the primary cracking reactor during continuous and steady state operation.

Non-condensable gas separation after fractional separation

In a further embodiment, the multi-phase hydrocarbon composition obtained after condensation is fed directly to fractional separation. In such case, condensation may be milder, designed to bring the multi-phase composition to the pressure and temperature conditions required at the inlet of the fractional separator. In such case, the light fraction from the fractional separation is fed to a post-fractional separation condenser and then separated in the Non-Condensable Gas Separator. In still another embodiment, it is the the multi-phase hydrocarbon fluid composition exiting the catalytic hydrogenation or the post-hydrogenation catalytic cracking which is fed to fractional separation, optionally after some cooling.

Services and by-products

Heat management of the plant

Heat management is an important part of the process and operations management. Heat consumption will be optimized, according to good engineering principles, making use of heat exchangers.

In an embodiment, thermal oil is used to carry and exchange heat in a higher temperature range, while water is used for heat exchange in a lower temperature range.

Gas loops in the plant

The cleaned non-condensable gas is mixed with air and burnt to produce the necessary energy to operate the primary cracking reactor as described earlier. Non-condensable gas burnt in the gas burner, together with a recycled part of the primary cracking exhaust gas will provide the flue gas with levels of NOx to be below the local emission limits. The flue gas, will preferably be cooled before emission.

Waste water and Waste solids

There may be waste water from the optional inlet plastic drying plant, from the Non-Condensable Gas Separator, from the Holding Tank, and from plant operation. Waste water may also come from the non-condensable gas scrubber. There may also be water coming from the process of collection, transport and separation of carbon particles coming out of the primary cracker, of the particle cleaning filter after primary cracking, of the catalysis regeneration units etc.

Waste water will generally be treated using techniques as known in the art for such type of waste water.

Handling of solids

Produced solids, essentially char from primary cracking but also contaminant particles, rests of plastic, solid residues from cyclone-type and other filters etc. are collected, and further processed. This will preferably be transported to a specialised processing plant, outside of the scope of this description.

Material balance

The primary end product from the waste plastic method is diesel, with tentative conversion ratio of 20 to 80 wt% (weight %). Additionally, 5-50 wt% light liquid fraction and 3 - 25 wt% heavy liquid fraction are tentatively produced. During primary cracking some ash/carbon and non-condensable gases may be formed. Ash production may typically vary between 1 to 30 wt%, non-condensable gases may typically vary from 1 to 30 wt%. Permanent/non-condensable gases and ash/carbon may be re-used for energy production to heat the primary cracking reactors.

Feeding waste plastic after shredding to a continuously running process comprising primary cracking, catalytic hydrogenation in gas phase and fractional separation, provides high efficiency, high throughput, and a stable and predictable quality for the fuel. Furthermore when the light fraction of gas produced is used to heat the continuous primary cracking process, it results in an almost energy neutral method.

Additional method for producing hydrocarbons from waste plastic

In an additional method, fuel and additional hydrocarbons from waste plastic are produced by a method comprising the steps of

- providing at least one plastic material;

- exposing said at least one plastic material to a primary cracking to obtain a first hydrocarbon fluid; said first hydrocarbon fluid being a gas;

- fractional separating said first hydrocarbon fluid to obtain at least one product,

- exposing at least one of said at least one products to a catalytic hydrogenation to obtain a final product.

In a further aspect, a waste recycling system for recycling waste plastic into fluid hydrocarbon compounds comprising

- a primary cracking reactor capable of receiving at least one plastic material and producing a first hydrocarbon fluid from said at least one plastic material, said first hydrocarbon fluid being a gas;

- a fractional separator for fractional separation of said first hydrocarbon fluid to obtain at least one product, and

- a catalytic hydrogenation reactor capable of receiving at least one of said at least one products and producing a final product,

where said primary cracking reactor is in fluid connection with said fractional separator and said fractional separator is in fluid connection with said catalytic hydrogenation reactor is described.

The main benefit of this configuration is that hydrogen is not consumed in hydrogenating of light and heavy fractions before fractional separation. This reduces the amount of external hydrogen required and specific fractions obtained from the fractional separation such as the medium fraction comprising diesel can be selectively hydrogenated. It will also prevent cracking of the diesel (medium fraction) resulting in a larger percentage of in the light fraction, which will decrease the yield of the diesel fraction.

In one embodiment, the heavy fraction can be cracked in a heavy fraction cracking reactor as described above after fractional separation and the cracked heavy fraction product being recycled to the fractional separator to increase the diesel yield i.e. the yield of the medium fraction.

Such alternative configuration will increase the yield, but the diesel quality/composition will remain the same as the fractional separator can be expected to split the resultant fractions in about the same manner whether it is downstream or upstream of the hydrogenation reactor. Hydrogenation of this fraction will occur regardless of the configuration.

In a further embodiment, the light fraction may be further processed by a postfractional separation condenser and a non-condensable gas separator optionally after cooling in order to separate the non-condensable gas from the light fraction. The non-condensable gas can be used to heat the primary cracking reactor as described above and will result in similar amount of non-condensable gas for burning. The only difference is that in this embodiment, compared to other embodiments as described above, is that the non-condensable gas will not be saturated/hydrogenated and will thus contain olefins. The difference in heating value between light alkanes and olefins is negligible and thus, it is expected that a similar amount of heat will be provided to the primary cracking reactor.

Detailed description of the figures

Fig. 1 illustrates a first embodiment of the invention comprising a primary cracking reactor (20) capable of transforming at least one plastic material into a first hydrocarbon fluid being a gas by primary cracking. The first hydrocarbon fluid is directed via the fluid connection to a catalytic hydrogenation reactor (40) capable of transforming the first hydrocarbon fluid to a second hydrocarbon fluid by catalytic hydrogenation. The second hydrocarbon fluid is directed via the fluid connection to a fractional separator (80) for fractional separation of the second hydrocarbon fluid into three products being a light fraction (81), a medium fraction (82) and a heavy fraction (83).

Fig. 2 illustrates a second embodiment of the invention comprising a primary cracking reactor (20) followed by a catalytic hydrogenation reactor (40). The waste plastic is fed to the primary cracking reactor (20) producing a first hydrocarbon fluid. The first hydrocarbon fluid is then exposed to catalytic hydrogenation (40) forming a second hydrocarbon fluid. In an alternative embodiment, a filter such as illustrated in fig. 8 (no 27) at an outlet of the primary cracking reactor (20) is present (not shown in fig. 2). After catalytic hydrogenation (20), the hydrocarbon fluid is exposed to condensation in a condenser (60) and separation in a separator (65) resulting in a first noncondensable gas and a first hydrocarbon liquid as the second hydrocarbon fluid to enter the fractional separator. The first hydrocarbon liquid is fed to a fractional separator (80) and being separated into a light fraction (81), a medium fraction (82) and a heavy fraction (83).

In an alternative embodiment (not shown) the second embodiment further includes feeding the first hydrocarbon liquid to a Holding Tank and preheat it before entering the fractional separator (80).

The first non-condensable hydrocarbon gas obtained from the separator (65) is fed to a gas burner (19) in connection with the primary cracking reactor (20). Also, the first non-condensable hydrocarbon gas is preferably cooled in a second cooler (not shown) before entering a non-condensable gas separator (not shown) and being scrubbed in a scrubber before being sent to the gas burner (19). This is further elaborated upon in relation to fig. 8.

Variations familiar to the person skilled in the art of process engineering may also be part of these schematic process diagrams.

Fig.3 illustrates a third embodiment of the invention, where waste plastic is fed into a primary cracking reactor (20). The hydrocarbon fluid exiting the primary cracking reactor (20) is then exposed to a catalytic cracking in a prehydrogenation catalytic cracking reactor (30) before the first hydrocarbon fluid is catalytic hydrogenated in a catalytic hydrogenation reactor (40). The resulting hydrocarbon fluid is then condensed in a condenser (60) and separated in a separator (65) a first non-condensable hydrocarbon gas and a first hydrocarbon liquid. The first hydrocarbon liquid is fed to a fractional separator (80) for fractional separation of the second hydrocarbon fluid into three products being a light fraction /81), a medium fraction (82) and a heavy fraction (83). The first non-condensable hydrocarbon gas is re-circulated to a gas burner (19) heating up the primary cracking reactor (20).

Plastic is fed to the primary cracking reactor (20) producing a hydrocarbon fluid, which is fed to a pre-hydrogenation catalytic cracker (30). Alternatively (not shown), a particle filter at the outlet of the primary cracking reactor (20) as described in fig. 8 may also be included. After catalytic cracking (30), the first hydrocarbon fluid/gas is fed to the catalytic hydrogenation reactor (40).

Alternatively (not shown), a cooler at the outlet of the pre-hydrogenation catalytic cracking reactor (30) as described in fig. 8 may be included. After catalytic hydrogenation, the hydrocarbon fluid is condensed in a condenser (60) and separated in a separator (65).

Variations familiar to the person skilled in the art of process engineering may also be part of this schematic process diagram. In particular, the comparison of fig.8 and fig.3 process diagrams can give an indication of a number of units (in fig.8), which could be included in other embodiments based on the process diagrams shown in the figs. 1-7 and 9.

Fig.4 illustrates a fourth embodiment of the invention where post-hydrogenation catalytic cracking is performed. Plastic is fed to the primary cracking reactor (20) producing a first hydrocarbon fluid. The first hydrocarbon fluid is then fed to a catalytic hydrogenation reactor (40). Alternatively (not shown), a filter at the outlet of the primary cracking reactor (20) as described in fig. 8 may be included. After catalytic hydrogenation (40), the resulting hydrocarbon fluid is cracked in the post-hydrogenation catalytic cracker (50) before being fed to the condenser (60) and the separator (65) a first non-condensable hydrocarbon gas and a first hydrocarbon liquid. The first hydrocarbon liquid is fed to a fractional separator (80) for fractional separation of the second hydrocarbon fluid into three products being a light fraction /81), a medium fraction (82) and a heavy fraction (83). The first non-condensable hydrocarbon gas is re-circulated to a gas burner (19) heating up the primary cracking reactor (20).

Variations familiar to the person skilled in the art of process engineering may also be part of this schematic process diagram.

Fig. 5 illustrates a fifth embodiment of the invention where the catalytic hydrogenation reactor (40) may receive a complementary feed of the heavy fraction (83) after dedicated heavy fraction catalytic cracking in a heavy fraction cracking reactor (35).

A heavy fraction cracking reactor (35) may process the heavy fraction (83) before re-injecting it upstream in the process, with the advantage of increasing the production of light and medium fractions.

The resultant stream from heavy fraction cracking is in gas phase, and may be introduced upstream the catalytic hydrogenation reactor (40) or upstream the fractional separator (80).

This process is similar to the one in fig.2, but for the heavy fraction (83). Instead of being removed from the plant, or returned after optional heating to one or several of the reactors, a part of it is fed after optional heating to a heavy fraction cracking reactor (35), the outlet of which is then reintroduced into the main process flow, either upstream or downstream of the catalytic hydrogenation (40), or both. Recirculation may in turn require process adjustments as the load may vary to the different reactors, as is known in the process industry. Complementary process items (such as those represented in the detailed diagram of fig. 8) and variations familiar to the person skilled in the art are also part of the invention.

Fig. 6 illustrates a sixth embodiment according to the invention where the primary cracking reactor (20) receives a complementary feed of a part or whole of the heavy fraction (83) without significant treatment between the fractional separator (80) and the primary cracking reactor (20). This process is similar to the one in fig.3 but for the heavy fraction (83).

The catalytic hydrogenation reactor (40) may also receive a complementary feed of the heavy fraction (83) without any significant treatment.

The catalytic cracking reactor pre- or post- the catalytic hydrogenation reactor may also receive a complementary feed of a part or whole of the heavy fraction, without significant treatment between the fractional separator (80) and the primary cracking reactor (20).

This embodiment represents alternative recirculation of the heavy fraction (83) into the process without additional treatment. The heavy fraction (83) will though preferably be heated to vaporisation so as to obtain a hydrocarbon gas fraction. The heavy fraction (83) might be returned in whole or in part to the primary cracking reaction (20) in which case vaporisation may not be necessary. As an alternative, the heavy fraction (83) might be returned in whole or in part to the pre-hydrogenation catalytic cracking reactor (30). These recirculation loops are typically designed and activated on the basis of modelled or observed process operation parameters. Recirculation may in turn require process adjustments as the load may vary to the different reactors, as is known in the process industry.

Complementary process items (such as those represented in the detailed diagram of fig.8 ) and variations familiar to the person skilled in the art of process engineering may also be part of this schematic process diagram.

Fig. 7 illustrates a seventh embodiment of the invention where the multi-phase hydrocarbon composition obtained after condensation (60) from the condenser is fed directly to the fractional separator (80). In such case, condensation may be milder, designed to bring the multi-phase composition to the pressure and temperature conditions required at the inlet of fractional separation. The light fraction (81) is fed to a post-fractional separation condenser (85) before being separated in a Non-Condensable Gas Separator (95).

It is further illustrated that the waste plastic feed is processed and fed to the primary cracking reactor (20) where after the process is similar to the one described for fig.3 until the hydrocarbon fluid reaches the Condenser (60). The product of condensation (60) in this case is fed directly to the fractional separator (80) without separation. The light fraction (81) is condensed, and Non-Condensable Gas is separated at the Non-Condensable Gas Separator (95), and then fed to the gas burner (19). Alternatively, a scrubber cleans the Non-Condensable Gas on its way to the gas burner (19), as also described in fig.8. Complementary process items (such as those represented in the detailed diagram of fig.8) and variations familiar to the person skilled in the art of process engineering are also part of the invention.

Fig. 8 shows an eight embodiment of the invention illustrating a detailed diagram. In the eight embodiment, the waste plastic feed (10) is loaded in a hopper (11), emptied by a conveyor (12) feeding it to a primary cracking reactor (20). The heat will generally be generated via combustion of side products of the process, preferably non-condensable gas or char. During transition periods such as when starting the reactor, other commercial fuels can be burnt to generate heat. The noncondensable gas or any injected fuel is burnt in the combustion chamber. The resulting exhaust gas can be extracted (22) from one or several zones of the primary cracking reactor (20) and partly recirculated (23), the rest being rejected in the atmosphere as flue gas (24). Recirculation of exhaust gas enables fine tuning of heat transfer in the different areas of the primary cracking reactor (20). Note that in this embodiment, the primary cracking reactor (20) is of indirect heating type, this exhaust gas (22, 23, 24) is at no time in contact with the hydrocarbon phase exposed to cracking in the primary cracking reactor (20).

After primary cracking, the generated hydrocarbon gas is cleaned for particles in a filter (27) before flowing to a pre-hydrogenation catalytic cracker reactor (30), shortening the hydrocarbon molecules. The resulting hydrocarbon gas flows to a cooler (37) then enters the catalytic hydrogenation reactor (40). After hydrogenation, the hydrocarbon gas is condensed in a condenser (60) to produce at least a first non-condensable hydrocarbon gas (vapour phase) and a first hydrocarbon liquid (liquid oil phase), which are then separated in a separator (65).

The first hydrocarbon liquid (66) is pumped to the Holding Tank (70). The first hydrocarbon liquid may be the subject of purification with Ca or Na hydroxydes as known in the art. Oil (first hydrocarbon liquid) from the Holding Tank (70) is warmed up at the heat exchanger (77) before entering the fractional separator (80). The fractional separator (80) separates the first hydrocarbon liquid in three fractions of hydrocarbons: a light fraction (81), a medium fraction (82) and a heavy fraction (83).

The first non-condensable hydrocarbon gas (91) from the separator (65) comprises a mix of light “non-condensable” gases primarily from C1 to C6, steam, and a heavier hydrocarbon gas fraction. The first non-condensable hydrocarbon gas (91) is cooled in a second cooler (92), then fed to a non-condensable gas separator (95). In the second cooler (92), steam and the heavier hydrocarbon fraction condense into a water and a second hydrocarbon liquid (liquid oil fraction), respectively. The second hydrocarbon liquid (96) is then extracted in the non-condensable gas separator (95), and sent to the fractional separator (80) via the Holding Tank (70). Alternatively, the second hydrocarbon liquid is sent directly to the fractional separator (not shown). The water is extracted (195), and a refined first noncondensable hydrocarbon gas phase (97) is first fed to the scrubber (99), then to a gas burner (19) arranged in connection with the primary cracking reactor (20). When starting the primary cracking reactor (20), or in case of too low noncondensable gas production, a complementary supply (18) of commercial fuel can be supplied to the gas burner (19).

In the primary cracking process (20) of cracking plastic, some by-products are formed in the shape of solid carbon particles (120), or char. The solid particles (120) are removed from the reactor and preferably cooled before further handling to avoid self-ignition. These solids (120) may be used in a combustion process in order to generate heat for the primary cracking reactor (20).

In one embodiment, the primary cracking reactor (20) may contain silicoaluminates to reduce the optimal temperature of reaction. They are consumed and discharged with the solid fraction (120). The reactor (20) may also contain minerals such as CaO to capture Cl and S according to techniques known in the art. The resulting fraction is solid, and will also be discharged with the solid fraction (120). Silico-aluminates and calcium minerals mentioned above are not considered catalysts, as they are consumed in the process.

Produced solids, essentially solids such as char from the primary cracking reactor (120), but also contaminant particles, rests of plastic, solid residues from cyclonetype (127) and other filters etc. are collected, and further processed. This will preferably be transported to a specialised processing plant, outside of the scope of this description.

The waste plastic material feeding plant has been schematically represented in fig.8, by a hopper (11) and a conveyor (12). Although it has not been detailed in the figs. 1-7, it may also, in some embodiments, be part of the method as represented in these figures.

Filtration has been schematically represented in fig.8. Although it has not been represented in the figs. 1-7, it may also, in some embodiments, be part of the method as represented in these figures.

Fig. 9 shows a further embodiment of the method of producing fuel and additional hydrocarbons from waste plastic. The waste plastic is exposed to primary cracking such as pyrolysis (20) resulting in a first hydrocarbon fluid being a gas. The first hydrocarbon fluid is fed to a fractional separator (80) separating the fluid in three different fractions – a light fraction (81p), a medium fraction (82p) and a heavy fraction (83p). The light fraction (81p) is recirculated, in part or in whole, to a post-fractional separation condenser (85) and a non-condensable gas separator (95) for extracting water (195) and non-condensable gas, which is used in a gas burner (19) for heating said primary cracking reactor (20).

The medium fraction (82p) - corresponding to Diesel carbon chains but likely having too high a rate of olefins to be considered as diesel – is exposed to catalytic hydrogenation (40) to reduce the quantity of unsaturated bonds resulting in a useable diesel product (82). The heavy fraction (83p) can be utilized as such, or sent back into the process upstream the fractional separator (80) after heavy fraction cracking (35) as described elsewhere in the application.

In this embodiment, water is not removed from the first hydrocarbon fluid before fractional separation, which is why a large quantity of steam will have to be taken into account in the design of the fractional separator.

It is to be understood that even though the same numbering is retained throughout the description of the figures, the design of the components in the different embodiments may be different as long as the described process occurs.

Experiments

The processes as described above have been the object of experiments.

Experiment 1: Catalytic hydrogenation of a model gas mixture

In a first experiment, catalytic hydrogenation feasibility and various catalysts were tested in a lab on a model gas mixture.

In this experiment, catalytic hydrogenation of a (diluted) model gas was tested on different catalysts. The model gas was chosen to be an olefin mixture containing ethylene and propylene in order to measure the catalysts activity. Conversion rates were measured for these two olefins.

In the experimental set-up as illustrated in fig. 10, the gas mix from the gas vessel (1) is mixed with water from the liquid vessel (2) and passed through a pre-heater (3). Thereafter, the gas/steam mixture is passed through the catalytic hydrogenation reactor (packed-bed reactor)(4) and then onto a steam condensation (5) and gas separation unit (6) before the gas is analysed in a Micro-GC (9) and the water is collected in a collection vessel (13).

The gas from the gas vessel (1) is entered into the hot-zone of the pre-heater (3), in which it is mixed with the water from the liquid vessel (2), which is evaporated to steam almost instantaneously. The flow of the gas is controlled by a MFC (Mass Flow Controller) (7) and the water flow by an HPLC-pump (8). The water that is used is de-ionized using a Millipore Milli-DI system and fed from a vessel. The preheater (3) and the reactor (4) are situated in a vertically divisible, two-zone tube furnace.

The two temperature-zones in the furnace are controlled independently of each other and the temperatures are set such that the inlet temperature of the catalyst bed is as close as possible to the desired temperature. The temperatures are monitored by four thermocouples, two in the preheater (3) and two in the reactor (4). The inlet temperature is measured where the catalyst bed starts and the outlet temperature is measured were the bed ends.

The experiments were performed at the temperatures 150°C, 200°C, 250°C and 300°C and at ambient pressure; in some instances, also 350 °C was investigated.

Table I: Model gas composition

The catalysts investigated were tested at a space velocity of 20 000 h-1. To avoid gradients in the bed, the catalyst bed was diluted 6 times using sintered -alumina. When steady-state operation was reached and verified at each test point a minimum of three gas-samples were extracted. If the three consecutive gas chromatograph analyses were found to be identical (with a minimum time interval of 10 minutes in-between), the conditions were considered to be stable and the experimental conditions were changed to a new test point. The gas analysis was performed using a Varian CP-4900 2-Channel Micro Gas Chromatograph (one molecular-sieve 5A PLOT column and one PoraPlot column, with double TCD detectors).

The catalysts were prepared by incipient wetness method known in the art.

A series of supported metals on δ-alumina was prepared and tested for the hydrogenation of ethylene and propylene in a gas mixture mimicking an envisioned feed representing the plastics pyrolysis reactor.

Conclusion: Good conversion rates were observed, especially for the Cu-Mn/Al2O3 catalyst as illustrated in fig. 11.

Exp 2: catalytic hydrogenation of a pyrolysis reactor hydrocarbon gas

In this experiment, we tested hydrogenation on a fraction of a pyrolysis product (hydrocarbon fluid) produced from a demo plant with 5 tonnes plastic per day capacity. The hydrocarbon gas obtained from the pyrolysis reaction was then fractional separated in a demo batch distillation column with focus on the temperature range typical for a diesel fuel i.e. 140-380oC in order to provide a hydrocarbon composition made mostly of diesel C10-C20, as illustrated in fig.12.

One part of the distillate was hydrogenated in gas phase in the experimental setup similar to the set-up as illustrated in fig. 10 using catalysts as in Experiment 1, The remaining part of the distillate was left untreated. Referring to the experimental set up , the gas in the gas vessel (1) is hydrogen, whereas the liquid in the liquid vessel (2) is the distillate.

The two hydrocarbon samples – one hydrogenated, the other one untreated (nonhydrogenated), were analysed for hydrocarbon types by fluorescent indicator adsorption as indicated in Table II. The results are presented in the table II.

Table II

Conclusion: From Table II, it can be seen that the olefin level is strongly reduced in the hydrogenated product. Thus, hydrogenation contributed to increase significantly the saturated fraction of the hydrocarbons.

Reference numbers

1: gas vessel

2: liquid vessel

3: pre-heater

4: catalytic hydrogenation reactor

5: condenser

6: separator

7: MFC

8: HPLC-pump

9: micro-GC

10: waste plastic feed

11: hopper

12: conveyor

13: collection vessel

18: complementary supply

19: gas burner

20: primary cracking reactor

22: primary cracking reactor gas extractions

23: primary cracking reactor extracted gas for recirculation 25: rejected flue gas

27: filter

30: pre-hydrogenation catalytic cracking reactor

35: heavy fraction cracking reactor

37: cooler

40: catalytic hydrogenation reactor

50: post-hydrogenation catalytic cracking reactor

60: condenser

65: separator

66: first hydrocarbon liquid

70: Holding Tank

77: heat exchanger

80: fractional separator

81: light fraction

81p: light fraction with a higher a rate of olefins

82: medium fraction (diesel)

82p:medium fraction with a higher a rate of olefins

83: heavy fraction

83p: heavy fraction with a higher rate of olefins

85:post-fractional separation condenser

91: first non-condensable hydrocarbon gas

92: second cooler

95: Non-Condensable Gas Separator

96: second hydrocarbon liquid

97: refined first non-condensable hydrocarbon gas

99: scrubber

120: solids from the primary cracking reactor (char) 127: solids from filtration

170: water and purification fluids extracted from Holding Tank 195: water extracted from Non-Condensable Gas Separator

Claims

1. A method for producing fuel, particularly diesel, and additional hydrocarbons from waste plastic comprising the steps of

- providing at least one plastic material;

- exposing said at least one plastic material to a anaerobic thermal cracking to obtain a first hydrocarbon fluid; said first hydrocarbon fluid being a gas;

- exposing said first hydrocarbon gas to a catalytic hydrogenation to obtain a second hydrocarbon fluid; wherein said catalytic hydrogenation is performed at a pressure range of 0.1 to 10 bar, preferably around 1 bar, and temperatures between 150-280oC, preferably between 190-230oC, such as around 200oC;

- fractional separating said second hydrocarbon fluid to obtain at least one final product;

wherein the method further comprises

- a step of condensation after said step of catalytic hydrogenation, wherein said second hydrocarbon fluid is obtained via at least said steps of catalytic hydrogenation and condensation and wherein said second hydrocarbon fluid is a multi-phase hydrocarbon fluid, and - a further step of separating after said step of condensation, wherein said second hydrocarbon fluid is obtained at least via said steps of catalytic hydrogenation, condensation and separation and wherein said second hydrocarbon fluid is a first hydrocarbon liquid obtained from said multi-phase hydrocarbon fluid during separation ; and wherein said separation further results in the formation of a first non-condensable hydrocarbon gas and wherein at least a part of said first non-condensable hydrocarbon gas is recirculated to and burnt in a gas burner to provide heat to said anaerobic thermal cracking.

2. The method according to claim 1 further comprising a step of prehydrogenation catalytic cracking performed prior to the step of catalytic hydrogenation, and wherein said first hydrocarbon fluid is obtained at least via steps of anaerobic thermal cracking and pre-hydrogenation catalytic cracking and/or a step of post-hydrogenation catalytic cracking performed after the step of catalytic hydrogenation and wherein said second hydrocarbon fluid is obtained at least via steps of catalytic hydrogenation and post-hydrogenation catalytic cracking.

3. The method according to any of the claims 1-2, wherein the second hydrocarbon fluid is subject to fractional separation for segregation of three final products : a light fraction such as mainly C6 to C10; a medium fraction such as mainly C11 to C20 and a heavy fraction such as mainly C21 and above.

4. The method according to claim 3, wherein said light fraction is condensed and optionally separated resulting in at least a second non-condensable hydrocarbon gas, and wherein at least a part of said second non-condensable hydrocarbon gas is recirculated to and burnt in a gas burner to provide heat to said anaerobic thermal cracking.

5. The method according to any of the preceding claims, wherein said anaerobic thermal cracking is performed without catalysts.

6. The method according to any one of the claims 3-4, wherein said heavy fraction is recycled to the step of anaerobic thermal cracking, catalytic cracking and/or catalytic hydrogenation or to a holding tank.

7. The method according to claim 6, wherein said heavy fraction is exposed to a step of heavy fraction cracking before being recycled to the step of anaerobic thermal cracking, catalytic cracking and/or catalytic hydrogenation or to said holding tank.

8. A waste recycling system for recycling waste plastic into fuel, particularly diesel, and additional hydrocarbons comprising

- a anaerobic thermal cracking reactor capable of receiving at least one plastic material and producing a first hydrocarbon fluid from said at least one plastic material by anaerobic thermal cracking, said first hydrocarbon fluid being a gas;

- a catalytic hydrogenation reactor capable of receiving said first hydrocarbon fluid and producing a second hydrocarbon fluid by catalytic hydrogenation,

- and a fractional separator capable of fractional separating said second hydrocarbon fluid to obtain at least one final product,

wherein said system further comprises a condenser for producing said second hydrocarbon fluid together with said catalytic hydrogenation reactor and resulting in said second hydrocarbon fluid being a multi-phase hydrocarbon fluid, and a separator for separating said multi-phase hydrocarbon fluid to provide a first hydrocarbon liquid and a first non-condensable hydrocarbon gas, said wherein said catalytic hydrogenation reactor is further fluidly connected with said fractional separator through said condenser and said separator; and

wherein said system further comprises a gas burner for providing heat to said anaerobic thermal cracking reactor, said gas burner is fluidly connected with said separator.

9. The system according to claim 8, wherein the system further comprises a postfractional separation condenser, a non-condensable gas separator and a gas burner, said post-fractional separation condenser being in fluidly connection with said fractional separator for receiving a light fraction obtained from the fractional separation process and wherein said post-fractional separation condenser is further fluidly connected with said non-condensable gas separator for separating a second non-condensable hydrocarbon gas; said non-condensable gas separator being further fluidly connected with said gas burner.

10. The system according to claims 8 or 9, wherein said system further comprises a prehydrogenation catalytic cracking reactor, wherein said anaerobic thermal cracking reactor is further fluidly connected with said catalytic hydrogenation reactor through said prehydrogenation catalytic cracking reactor.

11. The system according to any of the claims 8-10, wherein said system further comprises a post-hydrogenation catalytic cracking reactor, wherein said catalytic hydrogenation reactor is further fluidly connected with said fractional separator through said post-hydrogenation catalytic cracking reactor.

12. The system according to any of the claims 8-11, wherein the system further comprises a heavy fraction cracking reactor, said heavy fraction cracking reactor being in fluidly connection with said fractional separator for receiving a heavy fraction obtained from the fractional separation process and wherein said heavy fraction cracking reactor is further fluidly connected with said anaerobic thermal cracking reactor, said pre-hydrogenation catalytic cracking reactor, said post-hydrogenation catalytic cracking reactor and/or said catalytic hydrogenation reactor.

13. Use of a system as described in any of the claims 8-12 or a method as described in any of the claims 1-7 for producing fuel and additional hydrocarbons from waste plastic, wherein said fluid hydrocarbon is diesel.

Krav

1. En fremgangsmåte for å produsere drivstoff, spesielt diesel og øvrige hydrokarboner, fra avfallsplast som inneholder følgende trinn

- skaffe minst en type plastmateriale;

- utsette nevnte plastmateriale for anaerob termisk cracking for å produsere et første fluid av hydrokarboner; nevnte første fluid av hydrokarboner er en gass;

- utsette nevnte første gass av hydrokarboner for katalytisk hydrogenering for å produsere et andre fluid av hydrokarboner, hvori nevnte katalytiske hydrogenering blir gjennomført ved trykk mellom 0.1 til 10 bar, der omtrent 1 bar trykk er foretrukket, og ved en temperatur mellom 150 og 280 °C, der temperature mellom 190 og 230°C er foretrukket, eksempelvis ved omtrent 200 °C;

- fraksjonell separasjon av nevnte andre fluid av hydrokarboner for å produsere minst ett sluttprodukt;

hvori fremgangsmåten videre inneholder

- et kondenseringstrinn etter nevnte katalytiske hydrogenering, der nevnte andre fluid av hydrokarboner blir produsert via minst nevnte trinn av katalytisk hydrogenering og kondensering og der nevnte andre fluid av hydrokarboner er et multifase fluid av hydrokarboner, og

- et videre trinn av separering etter nevnte kondenseringstrinn, der nevnte andre fluid av hydrokarboner blir produsert via minst nevnte trinn av katalytisk hydrogenering, kondensering og separering og der nevnte andre fluid av hydrokarboner er en første væske av hydrokarboner generert fra nevnte multifase fluid av hydrokarboner ved separasjon, og der nevnte separasjon videre resulterer i dannelse av en første ikke-kondenserbar gass av hydrokarboner og der minst en del av nevnte første ikke-kondenserbare gass av hydrokarboner blir resirkulert og brent i en gassbrenner for å gi varme til nevnte anaerobe termiske cracking.

2. Fremgangsmåten i henhold til krav 1 som videre inneholder et trinn av prehydrogenerings katalytisk cracking utført før det katalytiske hydrogeneringstrinnet, og der første fluid av hydrokarboner blir produsert minst via trinnene anaerob termisk cracking og pre-hydrogenerings katalytisk cracking og/eller et trinn bestående av posthydrogenerings katalytisk cracking utført etter trinnet bestående av katalytisk hydrogenering og der nevnte andre fluid av hydrokarboner blir produsert via minst trinnene bestående av katalytisk hydrogenering og post-hydrogenerings katalytisk cracking.

3. Fremgangsmåten i henhold til kravene 1 eller 2, hvori andre fluid av hydrokarboner blir utsatt for fraksjonell separering for segregering av tre sluttprodukter: en lettfraksjon som hovedsakelig inneholder C6 til C10; en mellomfraksjon som hovedsakelig inneholder C11 til C20 og en tungfraksjon som hovedsakelig inneholder C21 og høyere.

4. Fremgangsmåten i henhold til krav 3, hvori nevnte lettfraksjon blir kondensert og om ønskelig separert slik at minst en andre ikke-kondenserbar gass av hydrokarboner blir produsert, og der minst en del av nevnte andre ikke-kondenserbare gass av hydrokarboner blir resirkulert til og brent i en gassbrenner for å gi varme til nevnte anaerobe termiske cracking.

5. Fremgangsmåten i henhold til hvilken som helst av foregående krav, hvori nevnte anaerobe termiske cracking blir utført uten katalysator.

6. Fremgangsmåten i henhold til krav 3 eller 4, hvori nevnte tungfraksjon blir resirkulert til trinnet bestående av anaerob termisk cracking, katalytisk cracking og/eller katalytisk hydrogenering eller til en lagertank.

7. Fremgangsmåten i henhold til krav 6, hvori nevnte tungfraksjon blir utsatt for et trinn av tungfraksjonscracking før tungfraksjonen blir resirkulert til trinnet bestående av anaerob termisk cracking, katalytisk cracking og/eller katalytisk hydrogenering eller til nevnte lagertank.

8. Et system for avfallsresirkulering der avfallsplast blir resirkulert til drivstoff, spesielt diesel og øvrige hydrokarboner, som omfatter

- en reaktor for anaerob termisk cracking som kan motta minst en type plastmateriale og produsere en første fluid av hydrokarboner fra nevnte plastmateriale ved anaerob termisk craking, der nevnte første fluid av hydrokarboner er en gass;

- en reaktor for katalytisk hydrogenering som kan motta nevnte første fluid av hydrokarboner og som kan produsere et andre fluid av hydrokarboner via katalytisk hydrogenering,

- og en fraksjonsseparator som kan fraksjonelt separere nevnte andre fluid av hydrokarboner for å produsere minste ett sluttprodukt,

hvori nevnte reaktor for anaerob termisk cracking er flyttende forbundet med nevnte reaktor for katalytisk hydrogenering og der nevnte reaktor for katalytisk hydrogenering er flyttende forbundet med nevnte fraksjonsseparator;

hvori nevnte system videre omfatter en kondensator for produksjon av nevnte andre fluid av hydrokarboner sammen med nevnte reaktor for katalytisk hydrogenering og som resulterer i at nevnte andre fluid av hydrokarboner er et multifase fluid av hydrokarboner, og en separator for separasjon av nevnte multifase fluid av hydrokarboner for å generere en første væske av hydrokarboner og en første ikke-kondenserbar gass av hydrokarboner, der nevnte reaktor for katalytisk hydrogenering videre er flyttende forbundet med nevnte fraksjonsseparator via nevnte kondensator og nevnte separator; og der nevnte system videre omfatter en gassbrenner for generering av varme til nevnte reaktor for anaerob termisk cracking, nevnte gassbrenner er flyttende forbundet med nevnte separator.

9. Systemet i henhold til krav 8, hvori systemet videre omfatter en postfraksjonsseparator kondensator, en separator for ikke-kondenserbar gass og en gassbrenner, der nevnte post-fraksjonsseparator kondensator er flyttende forbundet med nevnte fraksjonsseparator slik at den kan motta en lettfraksjon fra den fraksjonelle separeringsprosessen og der nevnte post-fraksjonsseparator kondensator er videre flyttendeforbundet med nevnte separator for ikke-kondenserbar gass, nevnte separator for ikke-kondenserbar gass er videre flyttende forbundet med nevnte gassbrenner.

10. Systemet i henhold til krav 8 eller 9, hvori nevnte system videre omfatter et trinn bestående av en reaktor for pre-hydrogenerings katalytisk cracking, der nevnte reaktor for anaerob termisk cracking er videre flyttende forbundet med nevnte reaktor for katalytisk hydrogenering via nevnte reaktor for pre-hydrogenerings katalytisk cracking.

11. Systemet i henhold til hvilken som helst av kravene 8-10, hvori nevnte system videre omfatter en reaktor for post-hydrogenering katalytisk cracking, der nevnte reaktor for katalytisk hydrogenering er videre flyttende forbundet med nevnte fraksjonsseparator via nevnte reaktor for post-hydrogenering katalytisk cracking.

12. Systemet i henhold til hvilken som helst av kravene 8-11, hvori systemet videre omfatter en reaktor for cracking av tungfraksjon, der nevnte reaktor for cracking av tungfraksjon er flyttende forbundet med nevnte fraksjonsseparator for å kunne motta tungfraksjon produsert fra fraksjonsseparasjonsprosessen og der nevnte reaktor for cracking av tungfraksjon er videre flyttende forbundet med nevnte reaktor for anaerob katalytisk cracking, nevnte reaktor for pre-hydrogenerings katalytisk cracking, nevnte reaktor for post-hydrogenerings katalytisk cracking og/eller nevnte reaktor for katalytisk hydrogenering.

13. Bruk av et system som beskrevet i hvilken som helst av kravene 8-12 eller en fremgangsmåte som beskrevet i hvilken som helst av kravene 1-7 for produksjon av drivstoff og øvrige hydrokarboner fra avfallsplast, hvori nevnte fluid av hydrokarboner er diesel.

Drawings

Priority

No priority

Patent classes

IPC classes

C10G 1/10

C10G 1/02

CPC classes

C10G 1/10

C10G 1/02

Citations

WO 2018055555 A1 (A1)

US 2018002609 A1 (A1)

JP 2009242485 A (A)

US 2016264874 A1 (A1)

WO 2013015819 A1 (A1)

Applicants, owners and inventors

Owners

QUANTAFUEL AS

Vollsveien 13 H

1366 LYSAKER

NO (BÆRUM Municipality, Akershus county)

Org. number: 915119484

Inventors

Petter Kaalstad

Ingelbrecht Knudssøns gate 1

0365 OSLO

NO (OSLO Municipality, Oslo county)

Erik Fareid

Kjærlighetstien 16

3970 LANGESUND

NO (BAMBLE Municipality, Telemark county)

Arnstein Norheim

Ullandsvegen 754

3614 KONGSBERG

NO (KONGSBERG Municipality, Buskerud county)

Lars Erik Fareid

Henrik Ibsens gate 7

3022 DRAMMEN

NO (DRAMMEN Municipality, Buskerud county)

Tarjei Thorrud

Myrehagen 58

3025 DRAMMEN

NO (DRAMMEN Municipality, Buskerud county)

Agent

DEHNS NORDIC AS

Gaustadalléen 21

0349 OSLO

NO (OSLO Municipality, Oslo county)

Org. number: 925704261

Reference: -

Status history

Payment history

Oppositions and appeals

No oppositions or appeals

Administrative limitation

No administrative limitation

Liens and licences

No liens or licenses registered

Gazette entries

No Gazette entries found

Only events from 2024.03.04 and onwards are shown.

Production of hydrocarbon fuels from waste plastic

Key information

Abstract and drawing

Publications

Documents

Description, claims and drawings

Priority

Patent classes

Citations

Applicants, owners and inventors

Agent

Status history

Payment history

Oppositions and appeals

Administrative limitation

Liens and licences

Gazette entries