Key information

Title
Hydrate inhibitor recovery system
Application number
20162051
Case type
National
Status
31.12.2021 Ikke betalt årsavgift
Filed
23.12.2016
Effective date
23.12.2016
Publicly available
25.06.2018
Applicant
NOV Process & Flow Technologies AS (NO)
Owner
NOV Process & Flow Technologies AS (NO)
Inventor
Dieter Müller (NO)
Agent
ONSAGERS AS (NO)
Granted
25.06.2018
Patent number
342676

Abstract and drawing

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content.
A hydrate inhibitor recovery system and a Method of operating the system is disclosed. The system comprises- a flash separator (32) with a main stream rich hydrate inhibitor inlet (29), - a recycle heating loop (35, 44, 46, 37); - a salt separator (48) in fluid communicationwith the recycle heating loop, and - a main stream vapour outlet with an unidirectional fluid connection to a distillation column (34) with a main stream vapour inlet, wherein the distillation column comprises a Rich hydrate inhibitor slip stream inlet (53), a reflux inlet (39), a steam outlet (31) and a lean hydrate inhibitor outlet (33).

Publications

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Documents

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Date
 Date Doc. No. Process Case number In/Out Journal description To/from
 18.07.2022 13-01 Saksbehandling 20162051(342676) UT PT Opphørt Patent - for ikke betalt årsavgift (3311)
02.05.2022 12-01 Saksbehandling 20162051(342676) UT PT Påminnelse om ikke betalt årsavgift (3329) (PT20162051)
01.11.2018 11-01 Saksbehandling 20162051 UT PT Varsel om betaling av første årsavgift (3317) (PT20162051)
26.06.2018 10-01 Saksbehandling 20162051 UT PT Registreringsbrev Nasjonal Patent (15)
14.05.2018 09-01 Saksbehandling 20162051 UT Intention to grant ONSAGERS AS
 08.01.2018 07-01 Saksbehandling 20162051 UT Bekreftelse på patentsøknad Onsagers AS
 04.01.2018 08-01 Saksbehandling 20162051 INN Korrespondanse (Hovedbrev inn) Onsagers AS
 22.12.2017 06-05 Saksbehandling 20162051 INN Krav Onsagers AS
 22.12.2017 06-04 Saksbehandling 20162051 INN Beskrivelse ME Onsagers AS
 22.12.2017 06-03 Saksbehandling 20162051 INN Beskrivelse Onsagers AS
 22.12.2017 06-02 Saksbehandling 20162051 INN Hovedbrev Onsagers AS
 22.12.2017 06-01 Saksbehandling 20162051 INN Korrespondanse (Hovedbrev inn) Onsagers AS
 05.10.2017 02-01 Overdragelse av søknad/rettighet 2017/12769 UT GH Forespørsel Onsagers AS
 03.10.2017 01-03 Overdragelse av søknad/rettighet 2017/12769 INN Endringsskjema, fullmakt Onsagers AS
 03.10.2017 01-02 Overdragelse av søknad/rettighet 2017/12769 INN Fullmakt Onsagers AS
 03.10.2017 01-01 Overdragelse av søknad/rettighet 2017/12769 INN Generell henvendelse Onsagers AS
 23.06.2017 05-02 Saksbehandling 20162051 UT PT report 09:57:15
23.06.2017 05-01 Saksbehandling 20162051 UT Realitet patent Onsagers AS
 02.03.2017 04-01 Saksbehandling 20162051 UT Infobrev til oppfinner Onsagers AS
 28.02.2017 03-03 Saksbehandling 20162051 INN Erklæring Søkers rett til oppfinnelse Onsagers AS
 28.02.2017 03-02 Saksbehandling 20162051 INN Hovedbrev Onsagers AS
 28.02.2017 03-01 Saksbehandling 20162051 INN Korrespondanse (Hovedbrev inn) Onsagers AS
 06.01.2017 02-01 Saksbehandling 20162051 UT Formalia 1 Onsagers AS
 23.12.2016 01-05 Saksbehandling 20162051 INN Beskrivelse Onsagers AS
 23.12.2016 01-04 Saksbehandling 20162051 INN P25153NO00 Figures Onsagers AS
 23.12.2016 01-03 Saksbehandling 20162051 INN Annet dokument Onsagers AS
 23.12.2016 01-02 Saksbehandling 20162051 INN Fullmakt Onsagers AS
 23.12.2016 01-01 Saksbehandling 20162051 INN Søknadsskjema Patent Onsagers AS

Description, claims and drawings

Disclaimer: This text has been machine-scanned and may contain errors – please refer to "Publications" for legally binding content. Description
Hydrate inhibitor recovery systemThe present invention relates to a system for recovery of hydrate inhibitor, especially an improved system for reclamation and re-concentration of hydrate inhibitor including the use of flash separation.BackgroundGlycol based hydrate inhibitors such as Mono Ethylene Glycol (MEG), Di-ethylene glycol (DEG), or tri-ethylene glycol (TEG) are used in hydrocarbon gas and/or condensate pipelines e.g. in gas fields, to absorb moisture and prevent formation of hydrate in the pipeline and other equipment. Typically the MEG is injected into the upstream end of the pipeline and is separated from the hydrocarbon flow at downstream end. The separated MEG (approximately 50 % MEG, 50 % water), denoted as rich MEG, carries the absorbed water. This rich MEG is re-concentrated by a water removal process to produce “lean MEG” (approximately 90 % MEG, 10 %water) for re-use. Water removal is normally performed by evaporation of the water. The MEG is also contaminated with other components from the well and the pipeline. Pipeline corrosion products, scale and other contaminants such as hydrocarbons, salts from formation water or production chemicals including other types of hydrate inhibitors are present. These impurities have to be fully or partially removed in the reclamation process otherwise the concentration of these compounds would be increase every time the inhibitor is recycled.Herein the present invention is exemplified by referring to MEG as the glycol based hydrate inhibitor, however a person skilled in the art will understand that the invention is equally applicable for other types of inhibitors comprising glycol inhibitors and the invention is not limited to the recovery of MEG.Prior artWO 2013/093789 discloses a stream processing system with stream of a glycol based hydrate inhibitor and a kinetic hydrate inhibitor. The system further comprises thermal oxidation unit and a processing unit comprising a stream inlet, a fluid inlet and a mixture outlet in fluid communication with the thermal oxidation unit.WO 2010/080038 discloses a method for regeneration and reclamation of Mono Ethylene Glycol (MEG) comprising the steps of a) re-concentrating the rich MEG to lean MEG by water boiling; and b) reclaiming a part of the lean MEG, wherein both the re-concentration and the reclamation step is performed at conditions below atmospheric pressure. The re-concentration and reclaiming steps are performed in separate units and the step of re-concentration of rich MEG to lean MEG is carried out at a temperature below the evaporation temperature of pure MEG. Salts are removed from part of the lean MEG, the Slip Stream, in a reclamation unit. The temperature in step a) is below the evaporation temperature of pure MEG at said pressure.In WO 2007/073204 A1 a process and a plant is described for regeneration of glycol from a mixture comprising glycol, water and salts, the salts comprising carbonate and/or bicarbonate ions. The mixture is flash distilled to obtain a salt-free solution of glycol and water. This solution is condensed and distilled to obtain glycol with reduced water content. The salts are concentrated in the vacuum boiler and removed from a sub-stream taken out of a return circuit to the vacuum boiler.US 2005/0072663 disclose a method of regenerating a glycol solution containing water, hydrocarbons and salts. The glycol solution is expanded in a drum, then distilled in a column. The concentrated glycol collected at the level of a reboiler is placed under vacuum to vaporize the water and to precipitate the salts. The salts are separated from the glycol in a separation device. The concentrated glycol feed of the salts is stored in capacity.In industry two main types of systems are commonly used for MEG reclamation and re-concentration: the Full Stream system and the Slip Stream system. WO 2007/073204 and US 2005/0072663 referred to above are specific examples of these two main systems respectively.By re-concentration is meant concentrating the rich MEG to lean MEG, and by reclamation is meant removing contaminants as salts and corrosion products. In a Slip Stream system the MEG is only partly reclaimed, meaning only a partial stream undergoes reclamation to control the level of impurities like salts in the lean MEG being reintroduced to the well stream, whereas the rest of the rich MEG only undergoes re-concentration.Objectives of the inventionThe main objective of the present invention is to provide more energy efficient recovery system and method. Wherein the system has a compact design, and the improvement reduces the weight and amount of equipment compared to a tradition slip stream system. Therefore the invention may reduce both the investment and operation costs.The present invention provides a hydrate inhibitor recovery system comprising - a flash separator with a main stream rich hydrate inhibitor inlet,- a recycle heating loop,- a salt separator in fluid communication with the recycle heating loop, and - a main stream vapour outlet with an unidirectional fluid connection to a distillation column with a main stream vapour inlet,wherein the distillation column comprises a rich hydrate inhibitor slip stream inlet, a reflux inlet, a steam outlet and a lean hydrate inhibitor outlet.The recycle heating loop on the flash separator will normally comprise a recycle loop outlet in fluid communication with the flash separator, a recycle loop pump with an inlet in fluid communication with the recycle loop outlet and a pump outlet in fluid communication with an inlet to a recycle heater comprising an outlet in fluid communication with a recycle loop inlet arranged on the flash separator.In second aspect of the hydrate inhibitor recovery system the main stream vapour outlet is fluidly connected to the distillation column through a chimney tray. In one aspect, the chimney height of the chimney tray is taller than 400mm-1000mm or 0.3-0.7 times the inner diameter of the distillation column.In one aspect of the hydrate inhibitor recovery system, the distillation column comprises a further tray between chimney tray and the slip stream inlet. This further tray may be a further chimney tray of a perforated tray.In a further aspect of the hydrate inhibitor recovery system the rich hydrate inhibitor slip stream inlet is arranged above the chimney tray and a deflector is arranged at the inlet for deflecting the rich hydrate inhibitor slip stream towards the chimney tray or the further tray.In yet another aspect of the hydrate inhibitor recovery system the system comprises a heat exchanger connected to the lean hydrate inhibitor outlet and the rich hydrate inhibitor slip stream to transfer heat from the lean stream to the slip stream.In another aspect of the hydrate inhibitor recovery system, the system further comprises a slip stream valve and a salt content analyser in fluid connection with the rich hydrate inhibitor main stream inlet, wherein the analyser is in signal communication with a control unit and wherein the slip stream valve is controllably connected to the control unit which is adapted to control the valve depending on the salt content. If the salt content increases the slip stream feed rate can be reduced to avoid formation of solids or scaling on the chimney tray. In yet a further aspect the system comprises a reflux valve upstream the reflux inlet controllably connected to the control unit for controlling the reflux and thereby temperature in the distillation column and water content in a lean hydrate inhibitor stream obtained from the lean hydrate inhibitor outlet. If the slip stream feed rate is reduced the reflux feed rate can be increase to adjust the water content in the lean hydrate inhibitor product. If there are expected gas production periods were the salt levels in the rich hydrate inhibitor are so low that there would be negligible salt accumulation in the flash separator, the hydrate inhibitor recovery system may then comprise a reversibly closable lean return stream conduit fluidly connecting the lean hydrate inhibitor outlet with the flash separator. The lean hydrate inhibitor product may then be obtained directly from the recycle heating loop, hereinafter referred to as a salt free mode. One example of such periods could be when there are nil, or extremely low formation water being produced from the reservoirs, where basically the only water being produced is condensed water from the produced gas. One example of negligible salt levels could be when the ppm level of total dissolved salt ions are below 20 ppm. Another example of negligible salt levels could be when the ppm when the divalent ions are below 1ppm, but where the monovalent salts ions are above 20ppm, allowing some accumulation of monovalent salts in the lean hydrate inhibitor injected to pipeline. When the salt accumulation of the salts in the lean hydrate inhibitor injected to the pipeline reaches an insignificant or pre-set value, then the lean return stream would be closed for a period. The present invention further provides a method to operate a hydrate inhibitor recovery system according to the present invention, wherein the rich hydrate inhibitor slip stream feed rate is in the range of 1% to 35% of the feed rate of the rich hydrate inhibitor main stream. Preferably, in the hydrate inhibitor recovery system according to the present invention the slip stream is in the range of 27% to 33% of the feed rate of the rich hydrate inhibitor main stream.In one aspect of the method, it comprises:analysing the salt content of the rich hydrate inhibitor main stream;adjusting the rich hydrate inhibitor slip stream feed rate depending on the salt content; andadjusting the reflux stream feed rate depending on the slip stream feed rate.In a further aspect the method comprises deflecting the slip stream on the inside of the tank, collecting non- flashed liquids from this deflected slip stream collected on a perforated tray below, where at least a portion of this non-flashed liquid spills downwards into the section of the chimney tray through the perforations.In yet another aspect one or more chimney tray hats deflects the evaporated flow from the mainstream into a flow pattern so it heats the non flashed liquid that is spilled downwards into the section of the chimney tray.In a further aspect the hydrate inhibitor recovery system is operated in batches of in various modes ofa) full stream modeb) slip stream-full stream hybrid mode.In yet a further aspect the system is operated in a salt free mode wherein the method comprises adjusting the slip stream feed rate to nil and returning lean hydrate inhibitor to the flash separator via an open and closable lean return stream conduit and producing the lean hydrate inhibitor from the liquid phase in the flash separator. The salt content analyser and the control unit may depending on the stability of the well stream treated with the hydrate inhibitor be applied only initially to adjust the system to the well. Alternatively it may be used more regularly if there are significant variations in the salt content.The rich hydrate inhibitor pump may also be connected controllably to the control unit so that this may control the overall feed rate into the recovery system.The present invention may also be referred to as hybrid reclamation. When the invention is employed on a MEG system the Rich MEG is fed to the flash separator while a smaller slip stream is sent directly to the bottom stage of the distillation column below the packing and above the chimney tray. Similar to a full stream design, both the reclamation system (i.e. the flash separator) and re-concentration system (i.e. distillation column) are operating under vacuum. The advantage to the hybrid configuration is that only a partial stream is sent to the reclamation for removing and controlling the salt levels while the slip stream is sent directly to the distillation column for distillation obtaining the lean MEG product, thereby reducing the total energy usage and optimizing on equipment size and weight. This allows the reclamation (i.e. flash separator, recycle heater and pump) to be smaller. The vapour from the flash separator is providing the re-boiling heat in the column for the distillation of the MEG. The concept of removing a portion of salts is similar to the slip stream design whereby the salt levels in the MEG loop are controlled however, the difference being that the slip stream for reclamation is taken from the front of the process as rich MEG instead of the lean MEG product.One essential feature for the latent heat of vaporized fluid from the main stream to be able to evaporate the slip stream, is to set up the system to a thermodynamic equilibrium where there still is some remaining water content in the produced Lean MEG, typically 10%wt water, i.e. 90% MEG.According to one aspect of the invention the lean hydrate inhibitor contains above 5 wt.% water, preferably above 7 wt.% water, or in another aspect it contains in the range of 7-15 wt.% water, specifically around.10 wt.% water.Brief description of the drawingsThe present invention will be described in further detail with reference to the enclosed figures, wherein:Figure 1 is a schematic illustration of an embodiment of the system according to the present invention. Figure 2 is a schematic illustration of an embodiment of the system according to the present invention including a control unit.Figure 3 is a schematic view of an embodiment with separate flash separator and distillation column.Figure 4 is a schematic illustration of an embodiment of the system according to the present invention comprising additional heat exchange.Figure 5a, 5b, 5c, 5d illustrated different configurations of the lower section of the distillation column of the combined flash separator and distillation column containing the chimney tray and the slip stream inlet.Figure 6 is schematic illustration of a recovery system according to the present invention including injections to control and minimize precipitation. adjustment Figure 7 is schematic illustration of a recovery system according to the present invention including alternative injections to control and minimize precipitation. adjustmentFigure 8 is schematic illustration of a recovery system according to the present invention including injections to control and minimize precipitation. Adjustment and an additional tray.Figure 9 illustrates an embodiment especially adapted to a “salt free” rich MEG stream.Principal description of the inventionIn the drawings equal reference numbers refer to equal equipment. All the reference numbers are listed in a table at the end of the description to provide a full overview. Although the figures illustrate different embodiments of the invention a person skilled in the art will appreciate that the different embodiments can be combined to form alternative embodiments of the invention.Figure 1 illustrates one embodiment of the present invention, it should be understood that the invention primarily relates to the flash separation and reconcentration system and that this inventive central part can be combined with other known methods of regeneration of hydrate inhibitor and treatment of a well stream. Illustrated on figure 1 is a formation 1, with a seafloor 2 and a sea surface 3. A well stream 11 is obtained from the formation that contains natural gas, water and salts, but which may also comprise condensate, liquid hydrocarbons and production chemicals. The well stream is mixed with lean hydrate inhibitor from conduit 13 before it is past through the pipeline 10, thereby avoiding and/or minimising formation of hydrates during transport in the pipeline. Via conduit/riser 15 the inhibited well stream is fed to a hydrocarbon separator 12 providing a hydrocarbon gas stream 17 and a rich hydrate inhibitor stream 19. By separator pump 14 the rich hydrate inhibitor is fed to a rich hydrate inhibitor storage tank 16. Via rich hydrate inhibitor conduit 21 and rich hydrate inhibitor pump 18 the rich hydrate inhibitor is fed via pressurised rich hydrate inhibitor conduit 23 to the recovery system. A main stream 25 passes valve 20 and enters the flash separator 32 of the combined flash separator and distillation column 30 via main stream inlet 29. A rich hydrate inhibitor slip stream 27 passes valve 22 and enters the distillation column 34 of the combined flash separator and distillation column 30 via slip stream inlet 53. The slip stream feed rate is between 1 and 30% of the mainstream feed rate. The combined separator and column 30 is operated under vacuum. Separating the flash separator 32 and the distillation column 34 is a chimney tray 38 which allows vapour to pass from the flash separator 32 to the distillation column 34 and which collects the flashed and distilled lean hydrate inhibitor and directs it out trough lean hydrate inhibitor outlet 33. The lean hydrate inhibitor pump 42 transfers the lean hydrate inhibitor via conduit 45 to the lean hydrate inhibitor tank 50 from where it via lean hydrate inhibitor pump 52 can be supplied to conduit 13.To provide heat to the flash separator and to the distillation column a recycle heating loop is installed. The loop comprises a recycle loop outlet 35 in fluid communication with a bottom section of the flash separator 32, a recycle loop pump 44 with an inlet in fluid communication with the recycle loop outlet 35 and a pump outlet in fluid communication with an inlet to a recycle heater 46 comprising an outlet in fluid communication with a recycle loop inlet 37 on arranged on the flash separator in a section above the liquid filled bottom section. To remove salts a salt removal slip stream 47 is removed from the recycle heating loop and passed to a salt remover 48 where the salts are separated out through a salt outlet 49. The salt remover can be any type of equipment known for separation of solid salt particles from a fluid stream including equipment such as centrifuges and filters.The distillation column is further equipment with a reflux loop. Steam is removed trough the steam/vapour outlet 31 arranged in the top of the column. It is cooled by passing through cooler 24 and water is condensed in condenser 26. Remaining vapour leaves through vapour outlet 41. The condensed water is past via reflux pump 28, then reflux valve 40 and to recycle inlet 39 into the distillation column. As the purpose of the distillation is to remove water to concentrate the hydrate inhibitor water is removed through water outlet 43.Figure 2 shows an embodiment similar to figure 1 but further comprising a salt content analyser 54 connected to a control unit 56. The control unit is connected to the rich hydrate inhibitor pump 18, slip stream valve 22 and reflux valve 40. and can control these based on the input from the analyser. The embodiment illustrated on figure 3 contains the same control units as the one illustrated on figure 2 but in this embodiment the flash separator 32 and the distillation column 34 are separate units. Lean hydrate inhibitor is collected in the bottom of the separate distillation column and no chimney tray is therefore required. The embodiment illustrated on figure 4 is equivalent to figure 1 except that a heat exchanger 58 is installed on the slip stream conduit wherein the slip stream is heated by indirect heat exchange with the lean hydrate inhibitor stream coming from the lean hydrate inhibitor outlet 33.Figures 5a, 5b, 5c, 5d illustrate different configurations of the lower section of the distillation column of the combined flash separator and distillation column containing the chimney tray and the slip stream inlet.In figure 5a the rich hydrate inhibitor slip stream inlet 53 is arranged near the bottom of the chimney tray providing a submerge inlet. The vapour will flash when entering the column at vacuum conditions and proceed through the lean hydrate inhibitor liquid collected on the chimney tray 38 and continue upwards through the packing 36 of the distillation column.In figure 5b the inlet 53 is arranged higher up and a second chimney tray 60 is arranged above the main chimney tray 38 but below the inlet. The slip stream will flash when entering this section and liquid collected by the second tray is allowed to spill down onto the main chimney tray 38.In figure 5c the slip stream inlet 53 is arranged high above the chimney tray 38 and a deflector 64 is arranged above the inlet deflecting the slip stream downwards to provide for mainly the vapour phase to enter the packing 36 of the distillation column.In figure 5d the configuration is similar to the configuration in figure 5b but here the second tray 160 is a perforated plate without chimney hats.In figure 5b and 5d the slipstream is deflected on the inside of the lower section of the distillation column, where non- flashed liquids from this deflected slip stream is collected on a second tray 60,160 below, where at least a portion of this non-flashed liquid spills downwards into the section of the chimney tray 38 through the perforations. It is believed that when one or more chimney tray hats deflects the evaporated flow from the mainstream into a flow pattern, it heats the non flashed liquid that is spilled downwards from the second tray 60,160 into the section of the chimney tray 38.Figure 6 illustrate an embodiment comprising acid injection in slip stream 61 upstream injection into evaporating tank 62 to suppress precipitation of divalent ions from the slip stream by shifting the solubility product of the divalent salts as a function of the following feed conditions-salt concentrations-pH-alkalinity-temperature- MEG concentrationAcid injection 61 is supplied to the slip stream 27 in a treated slip stream tank 62 resulting in a pH of 4-6 or lower in the slip stream past though inlet 153. The lean hydrate inhibitor is at least partly neutralized by injecting base through base injection inlet 59, providing the lean hydrate inhibitor with a pH of approximately 6-7. This reduces or eliminates the scaling and salt precipitation on the chimney tray. In the illustrated embodiment there is also provided for adding chemicals to the main stream via inlet 57, where such chemicals that minimise scaling in the flash separator and control the salt precipitation could be injected here. The mainstream including chemicals are referred to as 129.Figure 7 illustrates a similar system to figure 6 but here the acid 61 is injected directly into the slip stream.In figure 8 the injection systems are equivalent to figure 7 but here a deflector according to figure 5c and a perforated plate according to figure 5d are installed in the distillation column.Figure 9 is an illustration of the “salt free” mode, were in the embodiment of figure 8 a lean return stream conduit 63 is included directing the lean hydrate inhibitor down into the flash separator. The valves 22 controlling the slip stream 27 and the valve on the acid injection 61 are closed during this mode. As there are no salts the recovered lean hydrate inhibitor can be removed from the recycle heating loop as stream 65. Reference numbers
Claims
CLAIMS1. Hydrate inhibitor recovery system comprising- a flash separator (32) with a main stream rich hydrate inhibitor inlet (29),- a recycle heating loop,- a salt separator in fluid communication with the recycle heating loop, and- a main stream vapour outlet (55) with an unidirectional fluid connection to a distillation column (34) with a main stream vapour inlet,characterized in that the distillation column (34) comprises a rich hydrate inhibitor slip stream inlet (53), a reflux inlet (39), a steam outlet (31) and a lean hydrate inhibitor outlet (33).2. Hydrate inhibitor recovery system according to claim 1 characterized in that the main stream vapour outlet (55) is fluidly connected to the distillation column (34) through a chimney tray (38).3. Hydrate inhibition recovery system according to claim 2, characterized in that the chimney height is taller than 400mm-1000mm or 0.3-0.7 times the diameter of the distillation column (34).4. Hydrate inhibitor recovery system according to claim 2 characterized in that the distillation column (34) comprises a further tray (60) between chimney tray (38) and the slip stream inlet (53).5. Hydrate inhibitor recovery system according to any one of the claims 2-4, characterized in that the rich hydrate inhibitor slip stream inlet (53) is arranged above the chimney tray (38) and a deflector (64) is arranged at the inlet (53) for deflecting the rich hydrate inhibitor slip stream towards the chimney tray (38) or the further tray (60).6. Hydrate inhibitor recovery system according to any one of the claims 4-5, characterized in that the further tray (60) has perforations.7. Hydrate inhibitor recovery system according to any one of the claims 2-6, characterized in that the system comprises a heat exchanger (58) connected to the lean hydrate inhibitor outlet (33) and the rich hydrate inhibitor slip stream to transfer heat from the lean stream to the slip stream.8. Hydrate inhibitor recovery system according to any one of the claims 2-7, characterized in that it further comprises a slip stream valve (22) and a salt content analyser (54) in fluid connection with the rich hydrate inhibitor main stream inlet (29), wherein the analyser (54) is in signal communication with a control unit (56) and wherein the slip stream valve (22) is controllably connected to the control unit (56) which is adapted to control the valve (22) depending on the salt content.9. Hydrate inhibitor recovery system according to claim 8, characterized in that the system comprises a reflux valve (40) upstream the reflux inlet (39) controllably connected to the control unit (56) for controlling the reflux and thereby temperature in the distillation column (34) and water content in a lean hydrate inhibitor stream obtained from the lean hydrate inhibitor outlet (33).10. Hydrate inhibitor recovery system according to any one of the claims 1-9, characterized in that it further comprises a reversibly closable lean return stream conduit (63) fluidly connecting the lean hydrate inhibitor outlet (33) with the flash separator (32).11. Method to operate a hydrate inhibitor recovery system according to any one of the claims 1-10, characterized in that the rich hydrate inhibitor slip stream feed rate is in the range of 1% to 35% of the feed rate of the rich hydrate inhibitor main stream.12. Method according to claim 11, characterized in that the method comprises analysing the salt content of the rich hydrate inhibitor main stream;adjusting the rich hydrate inhibitor slip stream feed rate depending on the salt content; andadjusting the reflux stream feed rate depending on the slip stream feed rate.13. Method according to claim 11 or 12, characterized in that the method comprises deflecting the slip stream on the inside of the lower section of the distillation column (34), collecting non-flashed liquids from this deflected slip stream collected on a perforated tray (60) below, where at least a portion of this non-flashed liquid spills downwards into the section of the chimney tray (38) through the perforations.14. Method according to claim 13, characterized in that one or more chimney tray hats deflects the evaporated flow from the main stream into a flow pattern so it heats the non flashed liquid that is spilled downwards into the section of the chimney tray (38).15. Method according to claim 11, 12, 13 or 14, characterized in that the hydrate inhibitor recovery system is operated in batches of in various modes ofa) full stream modeb) slip stream-full stream hybrid mode.16. Method according to any one of the claims 11-15, characterized in that in a salt free mode the method comprises adjusting the slip stream feed rate to nil and returning lean hydrate inhibitor to the flash separator (32) via an open and closable lean return stream conduit (63) and producing the lean hydrate inhibitor from the liquid phase in the flash separator (32).KRAV1. Hydratinhibitorgjenvinningssytem som omfatter:- en flashseparator (32) med et hovedstrømsinntak (29) for rik hydratinhibitor, - en resirkuleringsoppvarmingssløyfe,- en saltseparator i fluidkommunikasjon med resirkuleringsoppvarmingssløyfen, og- et hovedstrømsdamputløp (55) med en ensrettet fluidkobling til en destillasjonskolonne (34) med et hovedstrømsdampinntak,karakterisert ved at destillasjonskolonnen (34) omfatter et delstrøminntak (53) for rik hydratinhibitor, et refluksinntak (39), et damputløp (31), og et utløp for mager hydratinhibitor (33).2. Et hydratinhibitorgjenvinningssytem ifølge krav 1, karakterisert ved at hovedstrømdamputløpet (55) er fluidmessig forbundet med destillasjonskolonnen (34) gjennom et skorsteinsbrett (38).3. Et hydratinhibitorgjenvinningssytem ifølge krav 2, karakterisert ved at skorsteinshøyden er høyere enn 400mm – 1000mm eller 0,3 til 0,7 ganger diameteren på destillasjonskolonnen (34).4. Et hydratinhibitorgjennvinningssytem ifølge krav 2, karakterisert ved at destillasjonskolonnen (34) omfatter et ytterligere brett (60) mellom skorsteinsbrettet (38) og delstrøminntaket (53).5. Et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 2 til 4, karakterisert ved at delstrøminntaket (53) for den rike hydratinhibitoren er anlagt over skorsteinsbrettet (38) og en deflektor (64) er anbrakt ved inntaket (53) for avledning av den rike hydratinnhibitordelstrømmen mot skorsteinsbrettet (38) eller det ytterligere brettet (60).6. Et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 2 til 5, karakterisert ved at det ytterligere brettet (60) har perforeringer.7. Et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 2 til 6, karakterisert ved at systemet omfatter en varmeveksler (58) som er koblet til uttaket (33) for den magre hydratinhibitoren og den rike hydratinhibitordelstrømmen for å overføre varme fra den magre strømmen til delstrømmen.8. Et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 2 til 7, karakterisert ved at det ytterligere omfatter en delstrømventil (22) og en saltinnholdsanalysator (54) som står i fluidkobling med hovedstrømsinntaket (29) for den rike hydratinhibitoren, der analysatoren (54) er i signalkommunikasjon med en styringsenhet (56) og der delstrømventilen (22) er styrbart koblet til styringsenheten (56) som er tilpasset å styre styringsventilen (22) avhengig av saltinnholdet.9. Et hydratinhibitorgjenvinningssytem ifølge krav 8, karakterisert ved at systemet omfatter en refluksventil (40) oppstrøms for refluksinntaket (39) som er styrbart koblet til styringsenheten (56) for å styre refluksen og dermed temperaturen i destillasjonskolonnen (34) og vanninnholdet i den magre hydratinhibitorstrømmen som er oppnådd fra utløpet (33) til den magre hydratinhibitoren.10. Et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 1 til 9, karakterisert ved at det ytterligere omfatter en reversibelt stengbar kanal (63) for mager returstrøm som fluidkobler utløpet (33) til den magre hydratinhibitoren med flashseparatoren (32).11. Metode for å drive et hydratinhibitorgjenvinningssytem ifølge ethvert av kravene 1 til 10, karakterisert ved at tilførselsraten av delstrømmen til den rike hydratinhibitoren er i området 1-35% av tilførselsraten av hovedstrømmen av den rike hydratinhibitoren.12. Metoden ifølge krav 11, karakterisert ved at metoden omfatter å analysere saltinnholdet i hovedstrømmen av den rike hydratinhibitoren;justere tilførselsraten til delstrømmen av den rike hydratinhibitoren avhengig av saltinnholdet og justere tilførselsraten av refluksstrømmen avhengig av tilførselsraten av delstrømmen.13. Metoden ifølge krav 11 eller 12, karakterisert ved at metoden omfatter å avlede delstrømmen på innsiden av den nedre delen av destillasjonskolonnen (34), samle opp ikke-flashede væsker fra denne avledede delstrømmen som er oppsamlet på et perforert brett (60) nedenfor, der i det minste en del av denne ikke-flashede væsken lekker nedover inn i området til skorsteinsbrettet (38) gjennom perforeringene.14. Metoden ifølge krav 13, karakterisert ved at en eller flere skorsteinsbretthatter avleder den avdampede strømmen fra hovedstrømmen inn i et strømningsmønster slik at det varmer opp den ikke-flashede væsken som lekker nedover inn i området til skorsteinsbrettet (38).15. Metoden ifølge krav 11,12,13 eller 14, karakterisert ved at hydratinhibitorgjenvinningssytemet blir drevet i ladninger i ulike modus av a) fullstrømsmodusb) delstrøms-fullstrøms hybridmodus.16. Metoden ifølge ethvert av kravene 11til 15, karakterisert ved at metoden i en saltfri modus omfatter å justere delstrømstilførselsraten til null, og returnere mager hydratinhibitor til flashseparatoren (32) mellom en åpen og lukkbar kanal (63) for mager returstrøm og produsere den magre hydratinhibitoren fra den flytende fasen i flashseparatoren (32).
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IPC classesB01D 3/10C07C 29/80C07C 29/76CPC classesB01D 3/10C07C 29/80C07C 29/76

Citations

WO 2013093789 A2 (A2)WO 2010080038 A1 (A1)WO 2015036614 A1 ( A1)

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NOV Process & Flow Technologies AS
Snarøyveien 36 1364 FORNEBU NO (BÆRUM Municipality, Akershus county)Org. number: 918094180Inventors
Dieter Müller
Bjerregaards Gata 56 C 0174 OSLO NO (OSLO Municipality, Oslo county)

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