CN1048204A - Reclaim improving one's methods of sour gas - Google Patents
Reclaim improving one's methods of sour gas Download PDFInfo
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- CN1048204A CN1048204A CN89103780A CN89103780A CN1048204A CN 1048204 A CN1048204 A CN 1048204A CN 89103780 A CN89103780 A CN 89103780A CN 89103780 A CN89103780 A CN 89103780A CN 1048204 A CN1048204 A CN 1048204A
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- China
- Prior art keywords
- aqueous solution
- alkanolamine
- regenerated
- carbon dioxide
- carbonic acid
- Prior art date
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Links
- 238000000034 method Methods 0.000 title claims abstract description 34
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 title abstract description 31
- 239000007864 aqueous solution Substances 0.000 claims abstract description 40
- 230000008929 regeneration Effects 0.000 claims abstract description 9
- 238000011069 regeneration method Methods 0.000 claims abstract description 9
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 70
- HZAXFHJVJLSVMW-UHFFFAOYSA-N 2-Aminoethan-1-ol Chemical compound NCCO HZAXFHJVJLSVMW-UHFFFAOYSA-N 0.000 claims description 40
- 239000000243 solution Substances 0.000 claims description 27
- 235000011089 carbon dioxide Nutrition 0.000 claims description 24
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 23
- 239000001569 carbon dioxide Substances 0.000 claims description 23
- 238000009395 breeding Methods 0.000 claims description 18
- 230000001488 breeding effect Effects 0.000 claims description 18
- 239000007788 liquid Substances 0.000 claims description 16
- 238000013459 approach Methods 0.000 claims description 13
- 241000282326 Felis catus Species 0.000 claims description 6
- 230000008676 import Effects 0.000 claims description 3
- 230000008569 process Effects 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 16
- 238000010521 absorption reaction Methods 0.000 description 15
- 239000006096 absorbing agent Substances 0.000 description 6
- 239000000047 product Substances 0.000 description 5
- 239000002253 acid Substances 0.000 description 4
- 230000006872 improvement Effects 0.000 description 4
- -1 triacontanol amine Chemical class 0.000 description 4
- REZQBEBOWJAQKS-UHFFFAOYSA-N triacontyl alcohol Natural products CCCCCCCCCCCCCCCCCCCCCCCCCCCCCCO REZQBEBOWJAQKS-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000011521 glass Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000001172 regenerating effect Effects 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 239000013256 coordination polymer Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 150000002169 ethanolamines Chemical class 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 1
- 206010022000 influenza Diseases 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000005204 segregation Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229960004418 trolamine Drugs 0.000 description 1
Images
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2
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- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
A kind ofly be used for separating and reclaiming improving one's methods of the contained sour gas of mixed airflow.Comprise, the regenerated alkanolamine aqueous solution in technological process that will contain the most about 20% (weight) of alkanolamine concentration range is cooled to the highest about 35 ℃ temperature range, and above-mentioned chilled regeneration soln is imported the uptake zone make it to contact with the mixed airflow that contains sour gas, this regenerated alkanolamine aqueous solution remains essentially in that temperature that it is cooled in most of zone of uptake zone.
Description
The present invention relates to separate and reclaim the improvement of the method for sour gas contained in the mixed airflow, the processing that especially relates to the stack gas that contains carbonic acid gas reaches from wherein separating and reclaim the innovative approach of the method for carbonic acid gas.
There have been many kinds from mixed airflow, to separate the method that for example resembles carbonic acid gas, sulfurous gas, hydrogen sulfide and so on sour gas.The method of these sour gas of separation of a kind of success especially and widespread use is usually said " girbotol process ".This method (is seen Kirk-Othmer except that being used for selexol process, Encyclopedia of Chemical Technology Vol.1,2ed＜1969〉the 821-822 page or leaf), also be used for separating and to reclaim the carbonic acid gas of stack gas (the same, Vol.4,2ed＜1969 〉, 362 pages).Issued September 26 at U.S. Patent No. RE 18985(1933) in can find more complete and detailed description about this method.
Put it briefly " girbotol process " can regard a kind of two step method as, in first step, the gas mixture inlet air flow that contains sour gas contacts with alkanolamine or chain triacontanol amine solution at a suitable uptake zone.This contact is carried out in a certain temperature and pressure operational condition scope.No matter final purpose is to reclaim sour gas contained in the mixed airflow or only to the mixed airflow desulfurization etc., the specified conditions that are used for this contact will depend on the character and the employed alkanolamine of the mixed airflow through being subject to processing.About this point, already used operational condition in the first step of this method of realization, the temperature of for example have an appointment 80 (26 ℃) to about 150 (65 ℃) reaches from normal atmosphere to about 1000 pounds of/square inch (70.3kg/cm
2) pressure (see Kirk-Othmer, Encyclopedia of Chemical Technology, Vol.1,2ed,＜1969〉822 page).Under these conditions, sour gas combines sour gas/alkanolamine product that formation dissolves in alkanolamine with alkanolamine, thereby sour gas is separated from the mixed airflow through being subject to processing.
In second step of this method, sour gas/alkanolamine product discharges and is input to a suitable alkanolamine or chain triacontanol amine solution breeding blanket from the uptake zone.In this breeding blanket, the sour gas that produces in the uptake zone/alkanolamine product is decomposed, each sour gas and alkanolamine or chain triacontanol amine solution obtain regeneration simultaneously, and this regeneration step is to realize by sour gas/alkanolamine product being heated to the temperature of using in the first step (being absorption step) that is much higher than this method.The most frequently used temperature range is that about 220 °F (104 ℃) are to 240 °F (115 ℃) in second step.Through sending the uptake zone back to after regenerated alkanolamine or the chain triacontanol amine solution cooling, in the uptake zone, be used to handle the next batch mixed airflow.Sour gas can emit, if carbonic acid gas then can reclaim for further handling.
Usually, design and make the equipment that is used for aforesaid method according to predetermined operational condition.These conditions comprise: the composition of pending mixed gas inlet air flow and character, used alkanolamine and the concentration when using in solution thereof, temperature and pressure or the like.After these operational conditions are determined, just can be easy to determine the parts of the needed suitable dimension of this equipment.But in case build up, the maximum capacity of aforesaid device is relatively-stationary, just can not increase its maximum capacity if do not carry out bigger transformation.Therefore, in aforesaid method, can increase any innovative approach that sour gas in the gas separates and don't need carry out the equipment based on aforesaid method bigger reconstruction, all be the marked improvement in this technical field.
The present invention relates to from a kind of mixed gas inlet air flow to separate and to reclaim the innovative approach of the continuation method of sour gas, especially relate to the improvement of following continuation method: isolate sour gas by the mixed gas inlet air flow is contacted with the regenerated alkanolamine aqueous solution in the uptake zone in the method.This contact causes forming the rich sour gas effluent liquid stream that contains sour gas/alkanolamine product.The effluent liquid stream of this rich sour gas reclaims and delivers into the breeding blanket from the uptake zone.In the breeding blanket, this effluent liquid stream is heated to above the temperature of zone of action, thereby makes the sour gas/alkanolamine reaction product decomposes generation sour gas that generates in the zone of action and make the regeneration of the alkanolamine aqueous solution.Sour gas reclaims from the breeding blanket as the cat head effluent stream, and the regenerated alkanolamine aqueous solution reclaims from the breeding blanket as effluent liquid stream.A kind of liquid stream in back is recovered and is recycled to the uptake zone, is used for handling the charge air flow of next batch acid gas-containing.
Innovative approach of the present invention relates to the absorption stage of aforesaid method.Itself comprises innovative approach, the regenerated alkanolamine aqueous solution is imported the uptake zone, the above-mentioned regenerated alkanolamine aqueous solution contains the most about 20%(weight of alkanolamine concentration range), this regenerated alkanolamine aqueous solution is remained on be not more than about 35 ℃ temperature range.Use the result who improves one's methods of the present invention, improved the segregation ratio of sour gas, thereby improved the actual quantity of separation and restored acid gas.
Unique accompanying drawing represent in the method general step and the schematic illustration of material flow.Innovative approach of the present invention is to be fit to this method.
Have now found that, implement innovative approach of the present invention and can improve containing certain sour gas or some and plant the uptake rate of this sour gas in the air-flow of sour gas or acid gas mixture.Put it briefly, of the present invention improving one's methods comprises, that use produces in technological process, have alkanolamine concentration range maximum and be about 20%(weight) preferably about 15% to about 20%(weight) the alkanolamine aqueous solution, be cooled to be enough to make this solution in most of uptake zone, to remain on the highest about 35 ℃ temperature as absorption agent and with the regenerated alkanolamine aqueous solution.
Describe in more detail with reference to the accompanying drawings and constitute step of the present invention and innovative approach.For convenience of explanation, just utilize the regenerated monoethanolamine aqueous solution in the technological process to come about 135 ℃ of the situations of temperature ranges that the present invention is described below to about 140 ℃ carbon dioxide enriched boiler flues as absorption agent.This stack gas is through the bottom of piping 12 input uptake zones 14, and the bottom of stack gas input uptake zone 14 also upwards flows through uptake zone 14, and it contacts with the regenerated monoethanolamine water solution flow that flows downward at this.The stack gas of adverse current is carried out among a pair of absorber portion 15 and 16 that is positioned at 14 tops, uptake zone with effective the contact in fact between the regenerated monoethanolamine aqueous solution.Usually, absorber portion 15 and 16 comprises the various packing materials that are supported, for example labor Shen (Raushing) ring, Lai Xin (Lessing) ring, Bel (Berl) saddle packing, Ying Teluokesi (Intalox) saddle packing etc. or a series of tower tray, for example bubble-cap and screen tray.
The regenerated monoethanolamine aqueous solution is by pipeline 32 and a top that is set directly at the dispenser device (not shown) importing uptake zone 14 of absorber portion 15 tops.According to innovative approach of the present invention, the regenerated monoethanolamine aqueous solution will be cooled to a certain temperature and be imported into uptake zone 14 under this temperature.Said temperature remains unchanged basically in most of zone of uptake zone 14.About this point, when the regenerated monoethanolamine aqueous solution is cooled to the temperature range of about 80 (26 ℃) to about 95 (35 ℃) by pipeline 32 input uptake zones 14 and dispenser device (not shown), this solution will remain in this temperature range in the major part of uptake zone 14.Mean that according to " major part " term the moisture monoethanolamine solution of regeneration remains in the said temperature scope in the absorber portion of uptake zone accounts for overall 50% scope at least.With reference to the accompanying drawings, this " major part " is equivalent to the whole absorber portion 15 of uptake zone 14.Temperature by the moisture monoethanolamine solution of regeneration in the whole absorber portion 15 of uptake zone 14 remains within the said temperature scope, improves the carbon dioxide absorption rate that is mixed in the carbon dioxide enriched boiler flue by the moisture monoethanolamine solution of regeneration.Especially found through experiments, temperature by the moisture monoethanolamine solution of regenerating is maintained at about 26 ℃ to about 35 ℃ temperature range, and the specific absorption of using this solution to obtain than when being higher than 36 ℃ by this solution carbon dioxide absorption rate can improve about 5% to 10%.According to the result of the above-mentioned raising specific absorption that obtains, do not need the equipment sequence that is used for implementing present method is carried out the actual quantity that bigger expansion just can improve the carbonic acid gas of recovery.
As mentioned above, 14 cause generating soluble carbonic acid gas/monoethanolamine reaction product by the moisture monoethanolamine solution absorbing carbon dioxide of regenerating in the uptake zone, and the result forms a kind of poor carbonic acid gas overfire air stream and a kind of carbon dioxide enriched effluent liquid stream.14 discharges also can enter the atmosphere by pipeline 17 poor carbonic acid gas overfire air stream from the uptake zone by a pipeline 17.Carbon dioxide enriched effluent liquid stream 14 is discharged and is transported to heat exchange zone 20 by pipeline 18 from the uptake zone by a pipeline 18, transfers to the top of breeding blanket 24 again by pipeline 22.
Effluent liquid stream carbon dioxide enriched in breeding blanket 24 decomposes and separates by the temperature range that is heated to about 220 (104 ℃) to about 240 (115 ℃).Decomposing required heat can provide by the stream that boils again of discharging from the monoethanolamine aqueous solution storage tank of the poor carbonic acid gas that is arranged in 24 bottoms, breeding blanket.Boil circulation piping 36 again and from this storage tank, discharge, behind reboiler 38, return breeding blanket 24 by pipeline 44 again.The steam that utilization is reclaimed from reboiler by steam-pipe 40 input reboilers 38 and by steam condenser pipe 42 is to boiling the stream heat supply again, boil again stream be heated to from about 104 ℃ to about 115 ℃ temperature range, when it turns back to breeding blanket 24 by pipeline 44, just provide the carbon dioxide enriched effluent liquid of decomposition to flow needed heat.
As mentioned above, carbon dioxide enriched effluent liquid stream resolves into the effluent liquid stream of carbon dioxide enriched cat head effluent stream and poor carbonic acid gas in breeding blanket 24.Carbon dioxide enriched overhead streams goes out air communication piping 46 discharges on 24 tops from the breeding blanket, by condenser 48 so that the monoethanolamine solution condensation of wherein carrying secretly enters reception area 50 then.The monoethanolamine solution that contains and be condensed in carbon dioxide enriched cat head effluent stream is collected in the reception area 50.The monoethanolamine of condensation turns back to the top of breeding blanket 24 from reception area 50 by pipeline 52.Carbonic acid gas in the uncooled cat head effluent stream that is included in carbonic acid gas reclaims from reception area 50 by pipeline 54.
The monoethanolamine aqueous solution that the regenerated monoethanolamine aqueous solution accumulates in the bottom of breeding blanket 24 and forms above-mentioned poor carbonic acid gas is accumulated.This accumulating further provides regenerated monoethanolamine aqueous solution source, and this solution is recycled to uptake zone 14 and is used therein.This regenerated monoethanolamine aqueous solution is delivered to heat exchange zone 20 by pipeline 26 24 discharges from the breeding blanket, it and the carbon dioxide enriched effluent liquid stream generation indirect heat exchange that flows into by pipeline 18 at this.Resulting refrigerative monoethanolamine solution is discharged from heat exchange zone 20 by pipeline 28, and imports the top of uptake zone 14 again by pump 30 and pipeline 32.
Will be before the overcooled regeneration monoethanolamine aqueous solution imports uptake zone 14 again, by a water cooler 34 make its further be cooled to about 26 ℃ to about 35 ℃ temperature range.In addition, regulate the monoethanolamine concentration in the regenerated monoethanolamine aqueous solution as required, to provide required about 15% to about 20%(weight) monoethanolamine concentration.If need to add monoethanolamine, it can be in this system arbitrary position between uptake zone 14 and the breeding blanket 24 be input in the backhaul of the regenerated monoethanolamine aqueous solution (not shown equipment therefor).
Find that in the embodiment of this invention the regenerated monoethanolamine aqueous temperature in uptake zone 14 was very important, the concentration of this solution also was very crucial.For example have been found that in the present invention under the lesser temps that uses, if the monoethanolamine concentration of aqueous solution surpasses about 20%(weight) then the per-cent variation of absorption rate of carbon dioxide begin to reduce.According to instruction among the United States Patent (USP) NO.RE18985 and hint, this discovery is unexpected.This patent is pointed out clearly, preferentially selects the alkanolamine of viscosity higher for use, and trolamine for example is because this viscosity higher helps to obtain higher acid gas absorption speed.The meaning below implying in this patent, the low viscosity alkanolamine of the use high density for example solution of monoethanolamine also helps to obtain higher uptake rate.But shown in following data, though actual absorption speed improves with strength of solution, the concentration that the per-cent of carbon dioxide absorption rate changes with the monoethanolamine aqueous solution surpasses about 20%(weight) and significantly reduce.
The following examples only provide for the present invention is described, are not to be used for limiting the scope of the invention.In these embodiments, all umbers or percentage ratio all are meant weight except as otherwise noted.
Embodiment
To the monoethanolamine aqueous solution that the saturated chamber adding of the round shape gas 25ml of sintered glass dividing plate is housed in its underpart.This chamber and the monoethanolamine aqueous solution that is mounted in it equilibrate to a steady temperature in a constant temperature oil bath.After reaching temperature equilibrium, carbonic acid gas is imported in this chamber continuously by the inlet mouth that is arranged on sintered glass dividing plate below.Unabsorbed carbonic acid gas is discharged by the air outlet that is arranged on this top, chamber.The time that carbonic acid gas is transfused to this chamber is one hour.
When the above-mentioned time finished, the chamber of containing the monoethanolamine aqueous solution was cooled to room temperature, reclaims this monoethanolamine aqueous solution and analyzes carbon dioxide content.
As mentioned above, a series of experimental results that the monoethanolamine aqueous solution of use different concns carries out under differing temps are listed in table I and II.The table III comprises the viscosity data about the monoethanolamine aqueous solution that uses under above-mentioned differing temps.
The carbonic acid gas of table I when monoethanolamine solution concentration (weight %) is following numerical value
Specific absorption (Grams Per Minute)
Sequence number temperature ℃ 15 20 25 30
A 49 2.65 3.47 3.88 4.01
B 39 2.69 3.54 3.90 4.05
C 35 2.84 3.81 4.11 4.21
The table II increase 5%(weight one by one in monoethanolamine concentration) between carbonic acid gas
The per-cent of specific absorption changes
Sequence number temperature ℃ 15-20 20-25 25-30
A 49 30.9 11.8 3.3
B 39 31.6 10.2 3.8
C 35 34.0 7.9 2.4
Viscosity (CP) * of the monoethanolamine solution of table III when concentration (weight %) is following numerical value
Sequence number temperature ℃ 15 20 25 30
A 49 0.94 1.08 1.22 1.42
B 39 1.14 1.22 1.54 1.79
C 35 1.22 1.42 1.66 1.99
* the CP-centipoise is measured under 60 rev/mins of operations with the Brookfield viscometer (DV-2 type) of a ultralow adapter is housed.
Can find out obviously that from the data of table II and III the per-cent of carbon dioxide absorption rate changes with strength of solution and increases (increasing with soltion viscosity) and reduce significantly especially that strength of solution surpasses about 20%(weight) time.
Though according to be considered to preferred specific embodiments described constitute method of the present invention self-evident can be under the situation that does not exceed the spirit and scope of the present invention to its changes and improvements.
Claims (4)
1, a kind of continuation method that from carbon dioxide enriched air-flow, reclaims carbonic acid gas, this air-flow is contacted with a kind of alkanolamine aqueous solution in the uptake zone, form the cat head effluent stream of poor carbonic acid gas and carbon dioxide enriched effluent liquid stream, carbon dioxide enriched effluent liquid stream is heated in the breeding blanket, form the effluent liquid stream of carbon dioxide enriched cat head effluent stream and poor carbonic acid gas, above-mentioned poor carbonic acid gas effluent liquid stream contains the regenerated alkanolamine aqueous solution, this regenerated alkanolamine aqueous solution is sent back in the uptake zone again, and the innovative approach of this method comprises:
Make the regenerated alkanolamine aqueous solution be cooled to be enough to make this solution in most uptake zone, to remain on and be not higher than about 35 ℃ temperature, the most about 20% (weight) of concentration that the above-mentioned regenerated alkanolamine aqueous solution contains alkanolamine, and will import the uptake zone through the overcooled regeneration alkanolamine aqueous solution, so that it contacts above-mentioned carbon dioxide enriched air-flow and from wherein removing carbonic acid gas.
2, according to the innovative approach of claim 1, wherein the regenerated alkanolamine aqueous solution be cooled to about 26 ℃ to about 35 ℃ temperature range.
3, according to the innovative approach of claim 1, wherein the alkanolamine in the regenerated alkanolamine aqueous solution is a monoethanolamine.
4, according to the innovative approach of claim 1, the alkanolamine concentration in the wherein above-mentioned regenerated alkanolamine aqueous solution is to about 20%(weight about 15%) scope.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/190,838 US4869884A (en) | 1988-05-06 | 1988-05-06 | Process for recovering acidic gases |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1048204A true CN1048204A (en) | 1991-01-02 |
| CN1073049C CN1073049C (en) | 2001-10-17 |
Family
ID=22703003
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN89103780A Expired - Fee Related CN1073049C (en) | 1988-05-06 | 1989-06-17 | Improved process for recovering acidic gases |
Country Status (4)
| Country | Link |
|---|---|
| CN (1) | CN1073049C (en) |
| BG (1) | BG60008B2 (en) |
| BR (1) | BR8907421A (en) |
| RO (1) | RO105105B1 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1747774B (en) * | 2003-02-04 | 2011-12-07 | 新日本制铁株式会社 | Method and apparatus for separating and recovering carbon dioxide |
| CN102351624A (en) * | 2011-08-24 | 2012-02-15 | 西安交通大学 | System for preparing low-carbon olefins by CO2 hydrogenation |
| CN101837236B (en) * | 2009-12-29 | 2013-02-27 | 中国恩菲工程技术有限公司 | Flue gas desulfurization method |
-
1989
- 1989-04-24 BR BR898907421A patent/BR8907421A/en not_active IP Right Cessation
- 1989-06-17 CN CN89103780A patent/CN1073049C/en not_active Expired - Fee Related
- 1989-11-13 RO RO142476A patent/RO105105B1/en unknown
-
1990
- 1990-10-24 BG BG093080A patent/BG60008B2/en unknown
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1747774B (en) * | 2003-02-04 | 2011-12-07 | 新日本制铁株式会社 | Method and apparatus for separating and recovering carbon dioxide |
| CN101837236B (en) * | 2009-12-29 | 2013-02-27 | 中国恩菲工程技术有限公司 | Flue gas desulfurization method |
| CN102351624A (en) * | 2011-08-24 | 2012-02-15 | 西安交通大学 | System for preparing low-carbon olefins by CO2 hydrogenation |
| CN102351624B (en) * | 2011-08-24 | 2013-12-11 | 西安交通大学 | System for preparing low-carbon olefins by CO2 hydrogenation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1073049C (en) | 2001-10-17 |
| BR8907421A (en) | 1991-05-07 |
| RO105105B1 (en) | 1994-12-10 |
| BG60008B2 (en) | 1993-06-30 |
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