WO2010080038A1 - Method for regeneration and reclamation of mono ethylene glycol using a vacuum slip stream - Google Patents

Method for regeneration and reclamation of mono ethylene glycol using a vacuum slip stream Download PDF

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Publication number
WO2010080038A1
WO2010080038A1 PCT/NO2010/000006 NO2010000006W WO2010080038A1 WO 2010080038 A1 WO2010080038 A1 WO 2010080038A1 NO 2010000006 W NO2010000006 W NO 2010000006W WO 2010080038 A1 WO2010080038 A1 WO 2010080038A1
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Prior art keywords
reclamation
meg
concentration
stream
slip stream
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PCT/NO2010/000006
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French (fr)
Inventor
Lucie Addicks
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Fjords Processing AS
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Aker Process Systems AS
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/86—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by liquid-liquid treatment

Definitions

  • the present invention relates to a method for regeneration and reclamation of Mono 5 Ethylene Glycol.
  • Hydrate inhibitors such as Mono Ethylene Glycol (MEG) are used in hydrocarbon gas and/or condensate pipelines e.g. in gas fields, to absorb moisture and prevent hydrate forming in the pipeline.
  • MEG Mono Ethylene Glycol
  • the MEG is injected into the upstream0 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.
  • the MEG is also contaminated with other components from the well and5 the pipeline. Pipeline corrosion products, scale and other contaminants such as hydrocarbons, salts from formation water or production chemicals are present, and those impurities are fully or partially removed in the reclamation process.
  • WO 2007/073204 a process and a plant is described for regeneration of glycol from a mixture comprising glycol , water and salts, the salts comprising carbonate0 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 containing5 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. 0
  • two main types of systems are commonly used for MEG reclamation and re-concentration: the Full Stream concept and the Slip Stream concept. These two concepts are schematically shown in figures 2A and 2B respectively.
  • WO 2007/073204 and US 2005/0072663 referred to above are specific examples of these two main systems respectively.
  • re-concentration is meant concentrating the rich MEG to lean MEG, and by reclamation is meant removing contaminants as salts and corrosion products.
  • Slip Stream as used herein is meant that the MEG is only partly reclaimed.
  • all the rich MEG (C) first enters the reclamation part (A), wherein all the rich MEG is evaporated by vacuum boiling and all the salts (D) are removed in a single step.
  • the evaporated rich MEG is then re-concentrated (B) to lean MEG (F) downstream the reclamation part by means of distillation under vacuum.
  • the MEG reclamation and re-concentration are energy demanding processes and reducing the energy consumption would lead to large savings.
  • Figure 1 is a schematic illustration of an embodiment of the present invention.
  • Figure IA is a schematic illustration of an embodiment of the present invention.
  • Figure 2A is schematically showing state of the art Full Stream concept
  • Figure 2B shows the Slip Stream concepts.
  • Figure 3 is a table showing the electrical power consumption (work) in the real case simulation in the Example.
  • Figure 4 is a table showing the heating medium consumption in the real case simulation in the Example.
  • Figure 5 is a table showing the cooling medium consumption in the real case simulation in the Example. DETAILED DESCRIPTION OF THE INVENTION
  • the present invention concerns a method for re-concentration and reclamation of Mono Ethylene Glycol 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.
  • water is evaporated at a pressure below atmospheric pressure and at a temperature below the evaporation temperature of MEG at said pressure.
  • the operating temperatures in both step a) and b) are below the degeneration temperature of MEG.
  • the concept according to the invention provides an energy effective system for large capacities.
  • the whole inlet stream, rich MEG is evaporated under vacuum. This is a process with high energy demand as the total inlet flow, i.e. water and MEG, has to be evaporated.
  • the whole inlet stream, rich MEG is re-concentrated by atmospheric water boiling; i.e. only water, not MEG, is boiled off from the main stream.
  • the boiling is done at atmospheric pressure, i.e. at higher pressure than in Full Stream, the boiling temperature of the liquid is higher then in Full Stream and the energy savings by boiling off water only may be relatively small.
  • the full rich MEG (3) stream is first re-concentrated (1) to lean MEG (6) in that water (5) is boiled off.
  • the re- concentration unit is connected to vacuum and the boil off is performed at conditions below atmospheric pressure.
  • water is boiled off under vacuum the boiling temperature is lowered and the energy needed for boil off of water is considerable reduced. This will allow the building of high capacity trains with very low energy demand as only the water is boiled off at low pressure and temperature.
  • the reclamation unit is connected to vacuum and the reclamation is performed by vacuum boiling.
  • the amount of lean MEG sent as Slip Stream part to the reclamation unit is regulated such that the salt concentration in the full lean MEG stream is kept below a certain maximum level which is acceptable for subsea processing.
  • the re-concentration and reclamation parts may be connected to separate or common vacuum systems.
  • the reclamation unit may be off line. The energy savings is even more considerable when the reclamation unit is put off line.
  • the acceptable salt concentration for subsea processing varies from system to system, but would be about 50 g/L maximum, but varies for each case. Acceptable salt concentrations varies in a range from 0 g/L to a maximum of 20-30g/L or as high as 40-50 g/L depending on the system.
  • Figure IA illustrates a particular embodiment of the present invention wherein the rich MEG (3) stream is first re-concentrated to lean MEG (6) in a re-concentration unit (1) where water (5) is boiled off under vacuum.
  • the re-concentration unit is connected to vacuum and the boil off is performed at conditions below atmospheric pressure.
  • the reclamation unit is connected to vacuum and the reclamation is performed by vacuum boiling.
  • the tables in figures 3, 4 and 5 are base on real case simulations, looking at electrical power consumption (work), heating medium consumption and cooling medium consumption.
  • the re-concentration process (1) is typically performed at a pressure of 15-20 kPa absolute and an operating temperatures are typically in the range of 84-91 °C for the re-concentrated (lean) MEG and 51-58 °C for the separated water phase.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Nitrogen Condensed Heterocyclic Rings (AREA)

Abstract

The present invention discloses a novel method for regeneration and reclamation of Mono Ethylene Glycol (MEG).

Description

METHOD FOR REGENERATION AND RECLAMATION OF MONO ETHYLENE GLYCOL USING A VACUUM SLIP STREAM
FIELD OF INVENTION
The present invention relates to a method for regeneration and reclamation of Mono 5 Ethylene Glycol.
BACKGROUND OF INVENTION
Hydrate inhibitors such as Mono Ethylene Glycol (MEG) are used in hydrocarbon gas and/or condensate pipelines e.g. in gas fields, to absorb moisture and prevent hydrate forming in the pipeline. Typically the MEG is injected into the upstream0 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. The MEG is also contaminated with other components from the well and5 the pipeline. Pipeline corrosion products, scale and other contaminants such as hydrocarbons, salts from formation water or production chemicals are present, and those impurities are fully or partially removed in the reclamation process.
In WO 2007/073204 Al a process and a plant is described for regeneration of glycol from a mixture comprising glycol , water and salts, the salts comprising carbonate0 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 containing5 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. 0 In industry two main types of systems are commonly used for MEG reclamation and re-concentration: the Full Stream concept and the Slip Stream concept. These two concepts are schematically shown in figures 2A and 2B respectively. WO 2007/073204 and US 2005/0072663 referred to above are specific examples of these two main systems respectively. 5 By re-concentration is meant concentrating the rich MEG to lean MEG, and by reclamation is meant removing contaminants as salts and corrosion products. By Slip Stream as used herein is meant that the MEG is only partly reclaimed. In the Full Stream concept all the rich MEG (C) first enters the reclamation part (A), wherein all the rich MEG is evaporated by vacuum boiling and all the salts (D) are removed in a single step. The evaporated rich MEG is then re-concentrated (B) to lean MEG (F) downstream the reclamation part by means of distillation under vacuum. Water (E) is distilled off in the re-concentration process. The Full Stream is suited for production with high solids load but has limitation with respect to capacities. This is resulting in parallel process trains for handling of larger volumes. The process is also highly energy demanding as both MEG and water needs to be evaporated. In the Slip Stream concept the rich MEG (C) is first re-concentrated (B') to lean
MEG (F')in the re-concentration part (B') by distillation at atmospheric pressure. In the re-concentration process water (E') is distilled off. Downstream the re- concentration a slip stream from the lean MEG is send to reclamation part (A') for salt (D') removal. This means that the in the slip stream concept the MEG is only partly reclaimed. The total salt concentration in the lean MEG loop must however be kept under a certain max level which is acceptable for the subsea processing. The reclamation part is again performed by means of vacuum boiling. The Slip Stream can be built in larger capacities per process train and it is more energy effective, especially if the reclamation part can be off line during the low salt production period.
The MEG reclamation and re-concentration are energy demanding processes and reducing the energy consumption would lead to large savings.
BRIEF DESCRIPTION OF THE DRAWINGS
Figure 1 is a schematic illustration of an embodiment of the present invention. Figure IA is a schematic illustration of an embodiment of the present invention.
Figure 2A is schematically showing state of the art Full Stream concept, and Figure 2B shows the Slip Stream concepts.
Figure 3 is a table showing the electrical power consumption (work) in the real case simulation in the Example.
Figure 4 is a table showing the heating medium consumption in the real case simulation in the Example.
Figure 5 is a table showing the cooling medium consumption in the real case simulation in the Example. DETAILED DESCRIPTION OF THE INVENTION
The present invention concerns a method for re-concentration and reclamation of Mono Ethylene Glycol 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 the present invention water is evaporated at a pressure below atmospheric pressure and at a temperature below the evaporation temperature of MEG at said pressure. The operating temperatures in both step a) and b) are below the degeneration temperature of MEG.
The concept according to the invention provides an energy effective system for large capacities. In the Full Stream the whole inlet stream, rich MEG, is evaporated under vacuum. This is a process with high energy demand as the total inlet flow, i.e. water and MEG, has to be evaporated. In the Slip Stream concept the whole inlet stream, rich MEG, is re-concentrated by atmospheric water boiling; i.e. only water, not MEG, is boiled off from the main stream. However since the boiling is done at atmospheric pressure, i.e. at higher pressure than in Full Stream, the boiling temperature of the liquid is higher then in Full Stream and the energy savings by boiling off water only may be relatively small.
In the method according to the present invention the full rich MEG (3) stream is first re-concentrated (1) to lean MEG (6) in that water (5) is boiled off. The re- concentration unit is connected to vacuum and the boil off is performed at conditions below atmospheric pressure. When water is boiled off under vacuum the boiling temperature is lowered and the energy needed for boil off of water is considerable reduced. This will allow the building of high capacity trains with very low energy demand as only the water is boiled off at low pressure and temperature.
A part of the re-concentrated lean MEG, the Slip Stream, is then sent to the reclamation unit (2) for removal of salts (4). The reclamation unit is connected to vacuum and the reclamation is performed by vacuum boiling. The amount of lean MEG sent as Slip Stream part to the reclamation unit is regulated such that the salt concentration in the full lean MEG stream is kept below a certain maximum level which is acceptable for subsea processing. The re-concentration and reclamation parts may be connected to separate or common vacuum systems.
In periods of low salt production when salt concentration in the full lean MEG stream leaving the re-concentration unit is below the certain maximum level which is acceptable for subsea processing, the reclamation unit may be off line. The energy savings is even more considerable when the reclamation unit is put off line.
The acceptable salt concentration for subsea processing varies from system to system, but would be about 50 g/L maximum, but varies for each case. Acceptable salt concentrations varies in a range from 0 g/L to a maximum of 20-30g/L or as high as 40-50 g/L depending on the system.
Figure IA illustrates a particular embodiment of the present invention wherein the rich MEG (3) stream is first re-concentrated to lean MEG (6) in a re-concentration unit (1) where water (5) is boiled off under vacuum. The re-concentration unit is connected to vacuum and the boil off is performed at conditions below atmospheric pressure.
A part of the re-concentrated lean MEG, the Slip Stream (11), is then sent to the reclamation unit (2) for removal of salts (4). The reclamation unit is connected to vacuum and the reclamation is performed by vacuum boiling.
In this particular embodiment of the invention re-concentration (1) and reclamation (2) shear the vacuum system (16).
Reference numbers in figure IA refers to the following components;
1 Re-concentration unit
2 Reclamation unit
3 Rich MEG stream 4 Salt removal
5 Produced water
6 Lean MEG stream
7 Storage tank
8 Distillation column 9 Condensers
10 Vacuum receivers
11 Lean MEG Slip Stream to reclamation
12 Flash separator
13 MEG return stream 14 Off gas
15 Drain vessel
16 Liquid ring vacuum system EXAMPLE:
An example was made for a system with rich MEG flow 32 m3/h, regenerating and reclaiming MEG in
A) Full Stream concept
B) Slip Stream Concept (with 25 % Slip Stream Reclaimer, re-concentration at atmospheric pressure, reclamation under vacuum) C) Vacuum Slip Stream Concept (with 25 % Slip Stream Reclaimer, both the
Re-concentration and reclamation done under vacuum)
The tables in figures 3, 4 and 5 are base on real case simulations, looking at electrical power consumption (work), heating medium consumption and cooling medium consumption.
With respect to C) above the re-concentration process (1) is typically performed at a pressure of 15-20 kPa absolute and an operating temperatures are typically in the range of 84-91 °C for the re-concentrated (lean) MEG and 51-58 °C for the separated water phase.

Claims

1. Method for re-concentration and reclamation of Mono Ethylene Glycol 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, characterized in that both the re-concentration and the reclamation step is performed at conditions below atmospheric pressure.
2. Method according to claim 1, characterized in that the temperature in step a) is below the evaporation temperature of pure MEG at said pressure.
3. Method according to any one of claims 1 to 2, characterized in that when the re-concentration is done in a re- boiler or similar followed by a distillation column or similar, both operating at conditions below atmospheric pressure.
4. Method according to any one of claims 1 to 3, characterized in that when the reclamation is done in a slip stream, then the reclamation is performed at conditions below atmospheric pressure.
5. Method according to any one of claims 1 to 4, characterized in that the reclamation slip stream is off line when the salt concentration is acceptable for the subsea processing.
6. Method according to any one of claims 1 to 5, characterized in that the reclamation and re-concentration parts are connected to separate vacuum systems.
7. Method according to any one of claims 1 to 5, characterized in that the reclamation and re-concentration parts are connected to a common vacuum system.
PCT/NO2010/000006 2009-01-08 2010-01-07 Method for regeneration and reclamation of mono ethylene glycol using a vacuum slip stream Ceased WO2010080038A1 (en)

Applications Claiming Priority (2)

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NO20090115A NO332854B1 (en) 2009-01-08 2009-01-08 Process for the re-concentration and recovery of monoethylene glycol

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Cited By (21)

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Publication number Priority date Publication date Assignee Title
US20130118989A1 (en) * 2011-11-14 2013-05-16 Luis Eduardo Caires Fernandez Process Scheme to improve Divalent Metal Salts Removal from Mono Ethylene Glycol (MEG)
EP2860168A1 (en) * 2013-10-10 2015-04-15 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (meg) water streams by acidification and vaporization under vacuum
FR3013710A1 (en) * 2013-11-22 2015-05-29 Prosernat FLEXIBLE PROCESS FOR THE TREATMENT OF SOLVENT, SUCH AS MONOETHYLENE GLYCOL, FOR THE EXTRACTION OF NATURAL GAS
WO2015195361A1 (en) * 2014-06-17 2015-12-23 Cameron Solutions, Inc. Salt removal and transport system for use in a monoethyleneglycol (meg) reclamation process
WO2015195362A1 (en) * 2014-06-17 2015-12-23 Cameron Solutions, Inc. Salt removal and transport system for use in a monoethyleneglycol (meg) reclamation procesjs
WO2015198212A1 (en) * 2014-06-27 2015-12-30 Reliance Industries Limited A system for regenerating mono ethylene glycol and a method thereof
KR20160001448A (en) * 2014-06-27 2016-01-06 삼성중공업 주식회사 Apparatus for recovering MEG
US20160101403A1 (en) * 2014-09-29 2016-04-14 Cameron Solutions, Inc. System and Method For PH Control Of Lean MEG Product From MEG Regeneration and Reclamation Packages
KR20160095443A (en) 2015-02-03 2016-08-11 대우조선해양 주식회사 Salts Removing Method by Water Flushing of MEG Regeneration Process and System Thereof
KR101670878B1 (en) * 2015-01-16 2016-10-31 대우조선해양 주식회사 MEG Regeneration System
US9718752B2 (en) 2013-05-31 2017-08-01 Shell Oil Company Process for the separation of an alkylene glycol
KR101805491B1 (en) * 2015-11-23 2017-12-07 대우조선해양 주식회사 MEG Regeneration System
US9932284B2 (en) 2013-05-31 2018-04-03 Shell Oil Company Process for the separation of 1,4-butanediol and co-products
NO20162051A1 (en) * 2016-12-23 2018-06-25 Nov Process & Flow Tech As Hydrate inhibitor recovery system
US10099980B2 (en) 2013-05-31 2018-10-16 Shell Oil Company Glycol recovery with solvent extraction
US10221116B2 (en) 2014-04-02 2019-03-05 Shell Oil Company Process for the separation of monoethylene glycol and 1,2-butanediol
KR20190124471A (en) * 2018-04-26 2019-11-05 삼성중공업 주식회사 Meg regeneration apparatus
KR20190125637A (en) * 2018-04-30 2019-11-07 삼성중공업 주식회사 Meg regeneration apparatus
WO2020104461A1 (en) 2018-11-19 2020-05-28 Nov Process & Flow Technologies As Hydrate inhibitor recovery system
RU2767520C1 (en) * 2020-10-26 2022-03-17 Публичное акционерное общество "Газпром" Method for regenerating aqueous solution of ethylene glycol and purifying thereof from salts
US20230002298A1 (en) * 2019-12-02 2023-01-05 Schlumberger Technology Corporation Reducing energy consumption in meg reclamation

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US9790153B2 (en) * 2011-11-14 2017-10-17 Cameron International Corporation Process scheme to improve divalent metal salts removal from mono ethylene glycol (MEG)
US20130118989A1 (en) * 2011-11-14 2013-05-16 Luis Eduardo Caires Fernandez Process Scheme to improve Divalent Metal Salts Removal from Mono Ethylene Glycol (MEG)
US11203560B2 (en) 2011-11-14 2021-12-21 Cameron International Corporation Process scheme to improve divalent metal salts removal from mono ethylene glycol (MEG)
US9718752B2 (en) 2013-05-31 2017-08-01 Shell Oil Company Process for the separation of an alkylene glycol
US9932284B2 (en) 2013-05-31 2018-04-03 Shell Oil Company Process for the separation of 1,4-butanediol and co-products
US10099980B2 (en) 2013-05-31 2018-10-16 Shell Oil Company Glycol recovery with solvent extraction
US10934237B2 (en) 2013-10-10 2021-03-02 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (MEG) water streams by acidification and vaporization under vacuum
US10308578B2 (en) 2013-10-10 2019-06-04 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (MEG) water streams by acidification and vaporation under vacuum
US11807595B2 (en) 2013-10-10 2023-11-07 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (MEG) water streams by acidification and vaporization under vacuum
US10005708B2 (en) 2013-10-10 2018-06-26 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (MEG) water streams by acidification and vaporization under vacuum
US12247003B2 (en) 2013-10-10 2025-03-11 Cameron International Corporation System and process for removal of organic carboxylates from mono ethylene glycol (MEG) water streams by acidification and vaporization under vacuum
EP2860168A1 (en) * 2013-10-10 2015-04-15 Cameron Solutions, Inc. System and process for removal of organic carboxylates from mono ethylene glycol (meg) water streams by acidification and vaporization under vacuum
EP2878589A1 (en) * 2013-11-22 2015-06-03 Prosernat Flexible method for the treatment of a solvent, such as monoethylene glycol, used in the extraction of natural gas
US9943775B2 (en) 2013-11-22 2018-04-17 Prosernat Flexible process for treating solvent, such as monoethylene glycol, used in natural gas extraction
FR3013710A1 (en) * 2013-11-22 2015-05-29 Prosernat FLEXIBLE PROCESS FOR THE TREATMENT OF SOLVENT, SUCH AS MONOETHYLENE GLYCOL, FOR THE EXTRACTION OF NATURAL GAS
US10221116B2 (en) 2014-04-02 2019-03-05 Shell Oil Company Process for the separation of monoethylene glycol and 1,2-butanediol
US9272972B2 (en) 2014-06-17 2016-03-01 Cameron Solutions, Inc. Salt removal and transport system and method for use in a mono ethylene glycol reclamation process
US10252182B2 (en) 2014-06-17 2019-04-09 Cameron Solutions, Inc. Salt removal and transport system and method for use in a mono ethylene glycol reclamation process
US11058968B2 (en) 2014-06-17 2021-07-13 Cameron Solutions, Inc. Salt removal and transport system and method for use in a mono ethylene glycol reclamation process
US9914685B2 (en) 2014-06-17 2018-03-13 Cameron Solutions, Inc. System for removing salt from a rich mono ethylene glycol stream
WO2015195361A1 (en) * 2014-06-17 2015-12-23 Cameron Solutions, Inc. Salt removal and transport system for use in a monoethyleneglycol (meg) reclamation process
US9630122B2 (en) 2014-06-17 2017-04-25 Cameron Solutions, Inc. Salt removal and transport system and method for use in a mono ethylene glycol reclamation process
US9522865B2 (en) 2014-06-17 2016-12-20 Cameron Solutions, Inc. System for removing salt from a rich mono ethylene glycol stream
WO2015195362A1 (en) * 2014-06-17 2015-12-23 Cameron Solutions, Inc. Salt removal and transport system for use in a monoethyleneglycol (meg) reclamation procesjs
KR101652494B1 (en) * 2014-06-27 2016-08-30 삼성중공업 주식회사 Apparatus for recovering MEG
KR20160001448A (en) * 2014-06-27 2016-01-06 삼성중공업 주식회사 Apparatus for recovering MEG
WO2015198212A1 (en) * 2014-06-27 2015-12-30 Reliance Industries Limited A system for regenerating mono ethylene glycol and a method thereof
US9926250B2 (en) 2014-06-27 2018-03-27 Reliance Industries Limited System for regenerating mono ethylene glycol and a method thereof
US20160101403A1 (en) * 2014-09-29 2016-04-14 Cameron Solutions, Inc. System and Method For PH Control Of Lean MEG Product From MEG Regeneration and Reclamation Packages
US10232340B2 (en) 2014-09-29 2019-03-19 Cameron Solutions, Inc. System and method for pH control of lean MEG product from MEG regeneration and reclamation packages
US9757708B2 (en) * 2014-09-29 2017-09-12 Cameron Solutions, Inc. System and method for pH control of lean MEG product from MEG regeneration and reclamation packages
KR101670878B1 (en) * 2015-01-16 2016-10-31 대우조선해양 주식회사 MEG Regeneration System
KR20160095443A (en) 2015-02-03 2016-08-11 대우조선해양 주식회사 Salts Removing Method by Water Flushing of MEG Regeneration Process and System Thereof
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