CA2187066A1 - Process for desalting glycol-derived solvents for gas scrubbers - Google Patents
Process for desalting glycol-derived solvents for gas scrubbersInfo
- Publication number
- CA2187066A1 CA2187066A1 CA 2187066 CA2187066A CA2187066A1 CA 2187066 A1 CA2187066 A1 CA 2187066A1 CA 2187066 CA2187066 CA 2187066 CA 2187066 A CA2187066 A CA 2187066A CA 2187066 A1 CA2187066 A1 CA 2187066A1
- Authority
- CA
- Canada
- Prior art keywords
- water
- scrubbing liquid
- scrubbing
- glycol
- aqueous phase
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Abandoned
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/52—Hydrogen sulfide
- B01D53/523—Mixtures of hydrogen sulfide and sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/26—Treatment of water, waste water, or sewage by extraction
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Environmental & Geological Engineering (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Hydrology & Water Resources (AREA)
- Water Supply & Treatment (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
The invention relates to a process for removing salts or water-soluble substances from a nonaqueous, water-miscible scrubbing liquid in gas scrubbers, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
The advantages of the process according to the invention are essentially that it circumvents the salting of the scrubbing media by a continuous removal of salts from such scrubbing processes.
Alkyl ethers particularly suitable for the process are, for example, the polyethylene glycol dimethyl ethers having a mean molar weight between 200 and 700, preferably 250 to 550. Corresponding compounds are sold, for example, by Hoechst AG (D-65926 Frankfurt am Main) under the trade name Genosorb.
The advantages of the process according to the invention are essentially that it circumvents the salting of the scrubbing media by a continuous removal of salts from such scrubbing processes.
Alkyl ethers particularly suitable for the process are, for example, the polyethylene glycol dimethyl ethers having a mean molar weight between 200 and 700, preferably 250 to 550. Corresponding compounds are sold, for example, by Hoechst AG (D-65926 Frankfurt am Main) under the trade name Genosorb.
Description
HOECHST AKTIENGESELLSCHAFT HOE 95 /F 228 Dr.PP/gp Description 5 Process for desalting glycol-derived solvents for gas scrubbers The invention relates to a process for removing salts or water-soluble substances from a nonaqueous water-miscible scrubbing liquid in gas scrubbers.
The use of organic solvents for removing undesirable acidic constituents, such as H2S and SO2 and CO2, from natural gases, synthesis gases and flue gases is known. These processes play an important part in keeping the environment clean by retaining pollutant 15 gases from industrial processes. Many such gas cleaning processes are based on the use of glycol-derived solvents - in this context, termed scrubbing liquids - as, for example, pure substances or mixtures of polyglycol dialkyl ethers or polyethylene glycol compounds containing 2 - 12 [CH2-CH2-O] units or corresponding mono- and diether compounds 20 containing up to 16 [CH2-CH2-O] units. These scrubbing liquids offer a number of advantages. Thus, they have a high and frequently specific solubilizing power for gases such as H2S, SO2 and CO2, have, in particular in the case of longer-chain compounds, only low vapor pressures and have low viscosities, which qualify them for use in 25 scrubbers or absorbers. The german VDI/DIN Commission on Air Pollution reports regularly on the prior art; VDI-Bericht 1034 of March 1993 may be mentioned as representative.
The literature describes numerous process variants of such scrubbing processes, which generally comprise an absorber stage for depleting 30 the undesirable substances in the gas stream and a desorption or regeneration stage for removing the substances from the laden solvent and converting the same into a utilizable or landfillable form. The ~Solinox process of the german Linde AG for removing SO2 is mentioned as an example. Other processes exploit chemical reactions of the dissolved gases in the scrubbing liquid, catalytically active substances or oxidants being added. Examples of this which can be mentioned are a process according to DOS 2158072, which uses a 5 catalytic Claus reaction, which proceeds in the solvent phase, between H2S and SO2 to give sulfur, and a process according to EP-A O 066 306, in which Fe(lll) chelates are used to oxidize H2S to sulfur, with a downstream oxidation of the resulting Fe(ll) chelates by atmospheric oxygen.
10 Other processes are also based on the specific action of certain glycol compounds. Thus, it is known, that methyl isopropyl ethers of ethylene glycols have the advantage of a particularly high solution rate for H2S
and C2 for gas scrubbers (DOS 26 11 613).
15 All these processes have in common a circulation of the scrubbing liquids used, which proceeds virtually quantildli~/ely, just from economic considerations. This is accompanied by a critical disadvantage. Compounds of low volatility such as sulfur, hydrocarbons, glycols or inorganic salts, under some circumstances, are 20 not removed in the regeneration stage and accumulate in the scrubbing liquid. This can have adverse consequences for the performance of the absorber or can require frequent replacement of the scrubbing liquid. In order to counteract this circumstance, processes for removing sulfur from the scrubbing liquid using carbon disulfide (USP 3 915 674) or for 25 removing glycols from dialkyl ether polyglycol scrubbing solutions (USP 4 962 238) and liquid hydrocarbons-polyether solvents (USP 4 334 102) have been developed. The accumulation of salts is particularly problematic, since, after reaching the saturation limit, salts begin to sediment in the apparatuses and to impair operation. The origin 30 of such salts is explained, for example, by entry in the form of flue dust or from additions of catalyst and buffer, but principally by the absorption of trace contaminants such as SO3 and reactions such as the formation of sulfate due to SO2 oxidation by traces of NOX.
Frequently, there must therefore be an additional outlay to avoid trace gases such as NOX. A typical example of this problem is the process according to DOS 2158072, in which after an operating period of 5 several months, the plant must occasionally be closed down for several weeks for cleaning.
The object therefore underlying the invention was to provide a process which enables the desalting of the scrubbing liquid, in order by this 10 means to avoid said disadvantages.
It is known that alkyl ether compounds of polyglycols having the composition as used as scrubbing liquids in gas scrubbers are compounds which are completely miscible with water or at least 15 miscible in very broad ratios. However, it was surprisingly found that various alkyl ether polyglycols which had been charged with salts in concentrations near the saturation limit or above it form two liquid phases as a result of the addition of only very little water or moderately conce"l~dted aqueous salt solution at certain temperatures, which 20 phases can be readily separated. One of the two phases in this case is aqueous and contains a majority of the salts from the scrubbing liquid in dissolved form. The other of these phases contains the scrubbing liquid depleted in salts and only low amounts of water. The aqueous phase, in addition to the salts, only contains small amounts of solvent 25 and has a higher specific gravity than the nonaqueous phase.
Conventional non-alkylated polyglycols which have hitherto primarily been used for gas scrubbers in absorbers, in contrast, do not exhibit this property of a phase separation.
30 The object is thus achieved by a process of the type mentioned at the outset, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
The invention therefore relates to a process for removing salts or water-soluble substances from a nonaqueous, water-miscible scrubbing liquid in gas scrubbers, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
Further embodiments are given by claims 2 to 6. Individual or a plurality of the individual features described in the claims can also each represent per se independent solutions according to the invention and the features of the embodiments can also be combined as desired.
The advantages of the process according to the invention are essentially that it circumvents the salting of the scrubbing media by a continuous removal of salts from such scrubbing processes.
Alkyl ethers particularly suitable for the process are, for example, polyethylene glycol dimethyl ethers having a mean molar weight between 200 and 700, preferably 250 to 550. Corresponding compounds are sold, for example, by Hoechst AG ~D-65926 Frankfurt am Main) under the trade name Genosorb.
Since alkylated polyglycol compounds have, with respect to non-alkylated polyglycols, improved solution and absorption properties for the off-gases in question, with comparable fluid-dynamic properties, conventional plants operated with polyethylene glycols can frequently be changed over to alkyl ether polyglycols and to the process of the invention even with the advantage of a higher efficiency.
The process of the invention can be utilized in such a manner that the circulated scrubbing liquid is withdrawn from the process at a suitable point and, at a temperature between 20 and 100C, preferably between 60 and 100C, particularly preferably between 80 and 100C, and very particularly preferably between 90 and 100C, is mixed with a suitable amount of water. If the salt content in the scrubbing liquid is not sufficient for a phase separation, it is expedient to add additional salt. After settling and separating the phases, the aqueous and organic phases are divided. The organic phase, if appropriate after passing through a drying stage to evaporate undesirable moisture, can be recycled to the scrubbing process. The aqueous salt solution is ejected.
The process of the invention can be carried out with all of the scrubbing liquid, but preferably with part-streams, for example via a bypass stream.
The process of the invention can be carried out batchwise or continuously. For the batchwise procedure, for example, a simple heatable stirred tank is suitable, which acts as a mixer and simultaneously as a settler. Continuous processes can be operated with mixer-settler devices, decanters or separators.
A possible embodiment of the process is described in more detail below with reference to the process flow diagram shown in the figure.
An off-gas is fed via a pipe 1 to a vertically upright gas scrubber 3 in the lower third and, on the way up to the exit 4, is scrubbed with a glycol-derived solvent. The solvent is introduced at the top into the gas scrubber 3 by pumps 7, 9 via pipes 5, 11, 12 and then collects in the bottom part of the gas scrubber 3 as liquid column 2 on a sulfur melt 17, which is due to the Claus reaction mentioned at the outset. From there the solvent can be fed in whole or in part via a pump 8 and pipes 5, 6, 19 to a vessel 10, in which it is then admixed with water via a feed 16, whereupon an aqueous phase 15 separates out, which is enriched with salts and is taken off via an outlet 13. The desalted 21 87U6~
solvent phase 14 can be taken off batchwise or continuously via outlets 20 by the pump 9 and recycled to the gas scrubber 3. The sulfur melt 17 can be taken off via a line 18 from the bottom of the gas scrubber 3.
The following examples serve for further explanation of the process.
Example 1 500 9 of polyethylene glycol dimethyl ether having a mean molar weight of 500 kg/kmol were admixed with 15 9 of sodium chloride and 100 ml of water and brought into solution at 90C. The water was then completely taken off via a waterjet vacuum and the solvent was thus made supersaturated with salt. Water was then added stepwise and the behavior was observed. After addition of 105 9 of water, a phase separation occurred. The top and bottom phases were separated from one another. The top phase (545 9) comprised the polyglycol ether and contained, in addition to 15 % water, only 1 % of NaCI
(5.5 9). The bottom phase (35 9) comprised a concenlldted salt brine of composition 74 % water and 26 % salt (9.1 9).
Comparison Example 1 The same experiment of Example 1 was carried out with 500 9 of polyethylene glycol having a mean molar weight of 400 kg/kmol instead of the polyethylene glycol dimethyl ether. In the stepwise addition of water, instead of a phase separation, after addition of 65 9 of water, complete solubility was observed. Phase separation did not occur.
Example 2 500 9 of polyethylene glycol dimethyl ether having a mean molar weight of 500 kg/kmol were admixed with 25 9 of sodium chloride and 100 ml of water and brought into solution at 90C. The water was then completely taken off via a waterjet vacuum and the solvent was thus made supersaturated with salt. Water was then added stepwise and the behavior was observed. After addition of 125 9 of water, a phase separation occurred. The top and bottom phases were separated from one another. The top phase (570 g) comprised the polyglycol 5 ether and contained, in addition to 13 % water, only 1 % of NaCI
(5.5 9). The bottom phase (68 9) comprised a concentrated salt brine of composition 74.5 % water and 25.5 % salt (17.3 9).
Comparison Example 2 The same experiment of Example 2 was carried out with 500 9 of polyethylene glycol having a mean molar weight of 400 kg/kmol instead of the polyethylene glycol dimethyl ether. In the stepwise addition of water, instead of a phase separation, after addition of 95 9 of water, complete solubility was observed. Phase separation did not occur.
The use of organic solvents for removing undesirable acidic constituents, such as H2S and SO2 and CO2, from natural gases, synthesis gases and flue gases is known. These processes play an important part in keeping the environment clean by retaining pollutant 15 gases from industrial processes. Many such gas cleaning processes are based on the use of glycol-derived solvents - in this context, termed scrubbing liquids - as, for example, pure substances or mixtures of polyglycol dialkyl ethers or polyethylene glycol compounds containing 2 - 12 [CH2-CH2-O] units or corresponding mono- and diether compounds 20 containing up to 16 [CH2-CH2-O] units. These scrubbing liquids offer a number of advantages. Thus, they have a high and frequently specific solubilizing power for gases such as H2S, SO2 and CO2, have, in particular in the case of longer-chain compounds, only low vapor pressures and have low viscosities, which qualify them for use in 25 scrubbers or absorbers. The german VDI/DIN Commission on Air Pollution reports regularly on the prior art; VDI-Bericht 1034 of March 1993 may be mentioned as representative.
The literature describes numerous process variants of such scrubbing processes, which generally comprise an absorber stage for depleting 30 the undesirable substances in the gas stream and a desorption or regeneration stage for removing the substances from the laden solvent and converting the same into a utilizable or landfillable form. The ~Solinox process of the german Linde AG for removing SO2 is mentioned as an example. Other processes exploit chemical reactions of the dissolved gases in the scrubbing liquid, catalytically active substances or oxidants being added. Examples of this which can be mentioned are a process according to DOS 2158072, which uses a 5 catalytic Claus reaction, which proceeds in the solvent phase, between H2S and SO2 to give sulfur, and a process according to EP-A O 066 306, in which Fe(lll) chelates are used to oxidize H2S to sulfur, with a downstream oxidation of the resulting Fe(ll) chelates by atmospheric oxygen.
10 Other processes are also based on the specific action of certain glycol compounds. Thus, it is known, that methyl isopropyl ethers of ethylene glycols have the advantage of a particularly high solution rate for H2S
and C2 for gas scrubbers (DOS 26 11 613).
15 All these processes have in common a circulation of the scrubbing liquids used, which proceeds virtually quantildli~/ely, just from economic considerations. This is accompanied by a critical disadvantage. Compounds of low volatility such as sulfur, hydrocarbons, glycols or inorganic salts, under some circumstances, are 20 not removed in the regeneration stage and accumulate in the scrubbing liquid. This can have adverse consequences for the performance of the absorber or can require frequent replacement of the scrubbing liquid. In order to counteract this circumstance, processes for removing sulfur from the scrubbing liquid using carbon disulfide (USP 3 915 674) or for 25 removing glycols from dialkyl ether polyglycol scrubbing solutions (USP 4 962 238) and liquid hydrocarbons-polyether solvents (USP 4 334 102) have been developed. The accumulation of salts is particularly problematic, since, after reaching the saturation limit, salts begin to sediment in the apparatuses and to impair operation. The origin 30 of such salts is explained, for example, by entry in the form of flue dust or from additions of catalyst and buffer, but principally by the absorption of trace contaminants such as SO3 and reactions such as the formation of sulfate due to SO2 oxidation by traces of NOX.
Frequently, there must therefore be an additional outlay to avoid trace gases such as NOX. A typical example of this problem is the process according to DOS 2158072, in which after an operating period of 5 several months, the plant must occasionally be closed down for several weeks for cleaning.
The object therefore underlying the invention was to provide a process which enables the desalting of the scrubbing liquid, in order by this 10 means to avoid said disadvantages.
It is known that alkyl ether compounds of polyglycols having the composition as used as scrubbing liquids in gas scrubbers are compounds which are completely miscible with water or at least 15 miscible in very broad ratios. However, it was surprisingly found that various alkyl ether polyglycols which had been charged with salts in concentrations near the saturation limit or above it form two liquid phases as a result of the addition of only very little water or moderately conce"l~dted aqueous salt solution at certain temperatures, which 20 phases can be readily separated. One of the two phases in this case is aqueous and contains a majority of the salts from the scrubbing liquid in dissolved form. The other of these phases contains the scrubbing liquid depleted in salts and only low amounts of water. The aqueous phase, in addition to the salts, only contains small amounts of solvent 25 and has a higher specific gravity than the nonaqueous phase.
Conventional non-alkylated polyglycols which have hitherto primarily been used for gas scrubbers in absorbers, in contrast, do not exhibit this property of a phase separation.
30 The object is thus achieved by a process of the type mentioned at the outset, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
The invention therefore relates to a process for removing salts or water-soluble substances from a nonaqueous, water-miscible scrubbing liquid in gas scrubbers, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
Further embodiments are given by claims 2 to 6. Individual or a plurality of the individual features described in the claims can also each represent per se independent solutions according to the invention and the features of the embodiments can also be combined as desired.
The advantages of the process according to the invention are essentially that it circumvents the salting of the scrubbing media by a continuous removal of salts from such scrubbing processes.
Alkyl ethers particularly suitable for the process are, for example, polyethylene glycol dimethyl ethers having a mean molar weight between 200 and 700, preferably 250 to 550. Corresponding compounds are sold, for example, by Hoechst AG ~D-65926 Frankfurt am Main) under the trade name Genosorb.
Since alkylated polyglycol compounds have, with respect to non-alkylated polyglycols, improved solution and absorption properties for the off-gases in question, with comparable fluid-dynamic properties, conventional plants operated with polyethylene glycols can frequently be changed over to alkyl ether polyglycols and to the process of the invention even with the advantage of a higher efficiency.
The process of the invention can be utilized in such a manner that the circulated scrubbing liquid is withdrawn from the process at a suitable point and, at a temperature between 20 and 100C, preferably between 60 and 100C, particularly preferably between 80 and 100C, and very particularly preferably between 90 and 100C, is mixed with a suitable amount of water. If the salt content in the scrubbing liquid is not sufficient for a phase separation, it is expedient to add additional salt. After settling and separating the phases, the aqueous and organic phases are divided. The organic phase, if appropriate after passing through a drying stage to evaporate undesirable moisture, can be recycled to the scrubbing process. The aqueous salt solution is ejected.
The process of the invention can be carried out with all of the scrubbing liquid, but preferably with part-streams, for example via a bypass stream.
The process of the invention can be carried out batchwise or continuously. For the batchwise procedure, for example, a simple heatable stirred tank is suitable, which acts as a mixer and simultaneously as a settler. Continuous processes can be operated with mixer-settler devices, decanters or separators.
A possible embodiment of the process is described in more detail below with reference to the process flow diagram shown in the figure.
An off-gas is fed via a pipe 1 to a vertically upright gas scrubber 3 in the lower third and, on the way up to the exit 4, is scrubbed with a glycol-derived solvent. The solvent is introduced at the top into the gas scrubber 3 by pumps 7, 9 via pipes 5, 11, 12 and then collects in the bottom part of the gas scrubber 3 as liquid column 2 on a sulfur melt 17, which is due to the Claus reaction mentioned at the outset. From there the solvent can be fed in whole or in part via a pump 8 and pipes 5, 6, 19 to a vessel 10, in which it is then admixed with water via a feed 16, whereupon an aqueous phase 15 separates out, which is enriched with salts and is taken off via an outlet 13. The desalted 21 87U6~
solvent phase 14 can be taken off batchwise or continuously via outlets 20 by the pump 9 and recycled to the gas scrubber 3. The sulfur melt 17 can be taken off via a line 18 from the bottom of the gas scrubber 3.
The following examples serve for further explanation of the process.
Example 1 500 9 of polyethylene glycol dimethyl ether having a mean molar weight of 500 kg/kmol were admixed with 15 9 of sodium chloride and 100 ml of water and brought into solution at 90C. The water was then completely taken off via a waterjet vacuum and the solvent was thus made supersaturated with salt. Water was then added stepwise and the behavior was observed. After addition of 105 9 of water, a phase separation occurred. The top and bottom phases were separated from one another. The top phase (545 9) comprised the polyglycol ether and contained, in addition to 15 % water, only 1 % of NaCI
(5.5 9). The bottom phase (35 9) comprised a concenlldted salt brine of composition 74 % water and 26 % salt (9.1 9).
Comparison Example 1 The same experiment of Example 1 was carried out with 500 9 of polyethylene glycol having a mean molar weight of 400 kg/kmol instead of the polyethylene glycol dimethyl ether. In the stepwise addition of water, instead of a phase separation, after addition of 65 9 of water, complete solubility was observed. Phase separation did not occur.
Example 2 500 9 of polyethylene glycol dimethyl ether having a mean molar weight of 500 kg/kmol were admixed with 25 9 of sodium chloride and 100 ml of water and brought into solution at 90C. The water was then completely taken off via a waterjet vacuum and the solvent was thus made supersaturated with salt. Water was then added stepwise and the behavior was observed. After addition of 125 9 of water, a phase separation occurred. The top and bottom phases were separated from one another. The top phase (570 g) comprised the polyglycol 5 ether and contained, in addition to 13 % water, only 1 % of NaCI
(5.5 9). The bottom phase (68 9) comprised a concentrated salt brine of composition 74.5 % water and 25.5 % salt (17.3 9).
Comparison Example 2 The same experiment of Example 2 was carried out with 500 9 of polyethylene glycol having a mean molar weight of 400 kg/kmol instead of the polyethylene glycol dimethyl ether. In the stepwise addition of water, instead of a phase separation, after addition of 95 9 of water, complete solubility was observed. Phase separation did not occur.
Claims (8)
1. A process for removing salts or water-soluble substances from a nonaqueous, water-miscible scrubbing liquid in gas scrubbers, which comprises feeding water to the scrubbing liquid until an aqueous phase separates out from the scrubbing liquid, and taking off this aqueous phase.
2. The process as claimed in claim 1, wherein the water is fed or the aqueous phase is taken off continuously or batchwise.
3. The process as claimed in claim 1 or 2, wherein the water is fed at a temperature between 20°C, preferably 60°C, particularly preferably 80°C, very particularly preferably 90°C, and 100°C.
4. The process as claimed in one or more of claims 1 to 3, wherein the scrubbing liquid contains a glycol-derived solvent.
5. The process as claimed in claim 4, wherein the glycol-derived solvent contains a mono- or dialkyl ether of a polyethylene glycol.
6. The process as claimed in claim 4 or 5, wherein the glycol-derived solvent has a mean molar weight of 200 to 700, preferably of 250 to 550.
7. Use of a glycol-derived solvent for carrying out the process as claimed in one or more of claims 1 to 3.
8. An apparatus for carrying out the process as claimed in one or more of claims 1 to 6, the apparatus containing a gas scrubber and a vessel which has an inlet and an outlet at the bottom, wherein the bottom part of the gas scrubber is connected to the top part of the gas scrubber and the inlet at the bottom of the vessel, and the outlet at the bottom of the vessel is connected to the top part of the gas scrubber.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE1995136941 DE19536941A1 (en) | 1995-10-04 | 1995-10-04 | Process for the desalination of glycol-based solvents for gas scrubbing |
| DE19536941.6 | 1995-10-04 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA2187066A1 true CA2187066A1 (en) | 1997-04-05 |
Family
ID=7773992
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA 2187066 Abandoned CA2187066A1 (en) | 1995-10-04 | 1996-10-03 | Process for desalting glycol-derived solvents for gas scrubbers |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP0766986A1 (en) |
| JP (1) | JPH09108528A (en) |
| CA (1) | CA2187066A1 (en) |
| DE (1) | DE19536941A1 (en) |
| NO (1) | NO964196L (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2877858B1 (en) * | 2004-11-12 | 2007-01-12 | Inst Francais Du Petrole | METHOD FOR DEACIDIFYING A GAS WITH A FRACTIONED REGENERATION ABSORBENT SOLUTION |
| KR200448532Y1 (en) * | 2008-01-31 | 2010-04-21 | 박재성 | Device for separating oil and water used of solvent collector for washing dryer system |
| CN111318153A (en) * | 2020-03-09 | 2020-06-23 | 众升清源（天津）环保科技有限公司 | Full-automatic wet oxidation hydrogen sulfide removal control system and use method |
| CN112121452A (en) * | 2020-09-27 | 2020-12-25 | 江苏科技大学 | Desalination system and desalination method for ethylene glycol barren solution containing high-solubility salt in deep sea natural gas exploitation |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5663927A (en) * | 1979-10-26 | 1981-05-30 | Kuraray Co Ltd | Method for carrying out grignard reaction |
| US4334102A (en) * | 1981-04-02 | 1982-06-08 | Allied Corporation | Removing liquid hydrocarbons from polyether solvents |
| DE3908422A1 (en) * | 1989-03-15 | 1990-09-20 | Forschungszentrum Juelich Gmbh | METHOD FOR THE EXTRACTION OF PROTEINS FROM AQUEOUS BIOMASS SUSPENSIONS |
-
1995
- 1995-10-04 DE DE1995136941 patent/DE19536941A1/en not_active Withdrawn
-
1996
- 1996-09-12 EP EP96114573A patent/EP0766986A1/en not_active Withdrawn
- 1996-10-02 JP JP8261549A patent/JPH09108528A/en active Pending
- 1996-10-03 NO NO964196A patent/NO964196L/en unknown
- 1996-10-03 CA CA 2187066 patent/CA2187066A1/en not_active Abandoned
Also Published As
| Publication number | Publication date |
|---|---|
| EP0766986A1 (en) | 1997-04-09 |
| NO964196D0 (en) | 1996-10-03 |
| JPH09108528A (en) | 1997-04-28 |
| DE19536941A1 (en) | 1997-04-10 |
| NO964196L (en) | 1997-04-07 |
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