CN105536437B - A kind of MDEA composite absorbers and separation method for sour gas separation - Google Patents
A kind of MDEA composite absorbers and separation method for sour gas separation Download PDFInfo
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- CN105536437B CN105536437B CN201610035154.3A CN201610035154A CN105536437B CN 105536437 B CN105536437 B CN 105536437B CN 201610035154 A CN201610035154 A CN 201610035154A CN 105536437 B CN105536437 B CN 105536437B
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- 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
- B01D53/1493—Selection of liquid materials for use as absorbents
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- 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
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- 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
- B01D53/1456—Removing acid components
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/20478—Alkanolamines
- B01D2252/20489—Alkanolamines with two or more hydroxyl groups
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
- B01D2252/504—Mixtures of two or more absorbents
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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
- 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
Abstract
A kind of MDEA composite absorbers and separation method for sour gas separation belongs to gas separation technique field.For MDEA composite absorbers containing MDEA and the immiscible alcohols of water and water, the mass percent of MDEA is 10-60%, and the mass percent with the immiscible alcohols of water is 10%-60%, and the mass percent of water is 10%-80%；It is homogeneous before absorption sour gas due to the hydrotropy effect of MDEA, forms liquid-liquid two-phase after absorbing sour gas, liquid phase is the lean solution phase of supported acidic gas, and lower liquid phase is the rich solution phase of supported acidic gas, and only rich solution reduces desorption energy consumption mutually into desorption unit.Formation liquid-liquid two-phase is easily isolated after the composite absorber of the present invention absorbs sour gas, by adjusting the composition ratio of absorbent to obtain the load capacity of the volume of the optimal upper and lower liquid phase for being adapted to the process when absorbent, it is lowered into the amount of the rich solution phase of desorption unit, reduces desorption energy consumption.
Description
Technical field
The invention belongs to gas separation technique fields, and in particular to a kind of MDEA composite absorptions for sour gas separation
Agent.
Background technology
The energy resource structure of energy demand and China based on the fossil fuels such as coal caused by industrialization fast development, is caused
A large amount of CO2Discharge, ecological environment is caused to seriously affect, causes Global Greenhouse Effect, extreme weather continuously emerges, glacier
Melt, the problems such as sea level rise, species extinction it is increasingly serious.Reduce CO2Discharge be inhibit global warming it is effective
Approach.By CO2Carry out efficient trapping and seal (CCS) up for safekeeping to be presently the most feasible CO2Discharge-reducing method.
Chemical absorption method is currently used CCS technologies.Since the energy consumption of desorption process accounts for very in CCS process total energy consumptions
Big proportion, Devoting Major Efforts To Developing New Absorbent is to reduce the research hotspot that the energy consumption during CCS is current.N methyldiethanol amine
(MDEA) absorbent is because it is with higher CO2Absorbing load and lower chemical reaction heat close as those skilled in the art
The hot spot of note.
Chinese invention patent " a kind of novel high-efficient compound decarbonization solvent " (application number 201010161302.9, publication date
On September 1st, 2010) with MDEA it is main to absorb ingredient, addition N- hydroxyethyl morpholines, the composite absorption of AMP, PZ as activator
Agent；Chinese invention patent " polyamine process removes carbon dioxide in gas and sulfide " (application number 93110579.X, publication date 1994
On August 31) based on MDEA aqueous solutions, addition activator is for carbon dioxide removal or the carbon dioxide body of sulfur compound
System；Chinese invention patent " the double amino ionic liquid-MDEA composite absorbers for being used for collecting carbonic anhydride " (application number
201310362336.8, publication date on March 18th, 2015) propose that the absorbent for compounding MDEA with double amino ionic liquids is used for
The addition of collecting carbonic anhydride, ionic liquid can reduce CO2Separating energy consumption.The above patent is the CO by improving absorbent2Load
Amount or increase absorbent are to CO2The mode of absorption rate reduce CO2Separating energy consumption, but water evaporation in desorption process is not reduced
With the energy consumption of absorbent heating.
Chinese patent application " a kind of amine absorbent and trapping CO2Method " (application number 201280031688.9, publication date
On May 28th, 2014) propose a kind of amine absorbent and trapping CO2Method, absorbent DIPAE/MAPA, DIPAE/DAB, N-
TBDEA/DiAP, DEEA/DMPDA absorb CO2After form two-phase, load C O2Enrichment phase enter desorption unit, reduce desorption
Liquid measure, reduce desorption energy consumption, the method for the patent application can reduce the energy consumption of the evaporation energy consumption and absorbent heating of water simultaneously,
But concentration of absorbing is high, viscosity is big and expensive, is not easily-synthesized, and is unfavorable for its application in industry.Chinese patent application " is used
In CO2The joint CO of piece-rate system2Phase transformation absorbent " (application number 201310212240.3, publication date on December 28th, 2013) carries
Go out a kind of amino-silicone absorbent, which absorbs CO2Solid-liquid two-phase is formed afterwards, and solid is carbamate, is being desorbed
The regeneration of absorbent can be realized in heating solid carbamate in the process, easily stifled due to generating solid in the absorption process
Pipeline is filled in, is made troubles for commercial Application.Chinese patent application " the concentration absorbent certainly for sour gas separation " (application number
201080019279.8, publication date on July 25th, 2012) disclose it is a kind of for the admixture of gas depickling containing acid gas
Method, absorbent used by this method include the amine of dissolving in a solvent, and the absorbent is after absorbing sour gas, absorption
Dosage form is at concentration amine phase, and concentration amine mutually can be mechanically decoupled with remaining absorbent and enters regeneration unit, remaining absorption
Absorptive unit is recycled and is returned in agent, and absorbent is the isooctanol solution of MEA used by unique example, and does not specify sour gas
The removal effect of body and the contribution that energy consumption is reduced.United States Patent (USP) " PHASE TRANSITRONAL ABSORPTION METHOD "
(application number 11/279095, patent No. US7541011B2, publication number September in 2009 2 days) discloses a kind of using containing at least
The method that the absorbent of a kind of activator and at least one solvent detaches gas from admixture of gas, the absorbent of unique instances
For the aqueous mixture of DEA and potassium carbonate, the above patent, which does not indicate, causes expected phase separation solvent, and unknown in embodiment
The concentration of true absorbent composition and each component, experiment show that most of absorbent of different compositions absorbs nothing after gas to be absorbed
There is phenomenon of phase separation in method, has no way of implementing.
Described in summary, evaporation energy consumption a kind of maturation based on commercial Application of exploitation and that water can be reduced and absorbent heating
Energy consumption absorbent it is significant.
Invention content
In view of the deficiencies in the prior art, the object of the present invention is to provide a kind of MDEA for sour gas separation
Composite absorber, which can spontaneously form liquid-liquid two-phase after absorbing sour gas, and liquid-liquid two-phase is easily isolated,
And can be according to absorbed sour gas the characteristics of, by adjusting the composition ratio of absorbent to obtain being adapted to the process most
The load capacity of the volume of excellent upper and lower liquid phase when absorbent, to reduce the rich solution phase for entering desorption unit under industrial environment
Amount, to reduce the energy consumption in desorption process as much as possible.
To achieve the above objectives, the technical solution adopted by the present invention is：A kind of MDEA for sour gas separation is compound
Absorbent, wherein MDEA composite absorbers include MDEA and the immiscible alcohols of water and water, and the wherein mass percent of MDEA is
10-60%, the mass percent with the immiscible alcohols of water are 10-60%, and the mass percent of water is 10-80%.It is described multiple
Hydrotropy effect of the absorbent due to MDEA is closed, is homogeneous body before absorption sour gas, liquid-liquid is spontaneously formed after absorbing sour gas
Two-phase, liquid phase are the lean solution phase of supported acidic gas, and lower liquid phase is the rich solution phase of supported acidic gas.
In MDEA composite absorbers described further, the mass percent of MDEA is 20%-40%, with the immiscible alcohol of water
The mass percent of class is 20%-60%, and the mass percent of water is 20%-60%.
Further, the combination of any one or more of the alcohols of C4-C8 is selected from the immiscible alcohols of water.
Further, the C4-C8 alcohol is selected from n-butanol, isobutanol, amylalcohol, hexanol, enanthol and octanol and its with point different
The group that the alcohol of structure body is formed.
Method for absorbing and separating includes the following steps：By sour gas and MDEA composite absorber haptoreactions, MDEA is compound
Absorbent due to MDEA hydrotropy effect, absorb sour gas before be homogeneous body, absorb sour gas after spontaneously form liquid-liquid two
Phase, liquid phase are the lean solution phase of supported acidic gas, and lower liquid phase is the rich solution phase of supported acidic gas, detaches rich solution phase, only makes
Rich solution mutually enters follow-up desorption unit and carries out sour gas desorption, completes to use again after absorbent and lean solution after desorption mix
In absorption process.
The salt generated, most of water, one are reacted with sour gas comprising major part MDEA in the above-mentioned rich solution phase of the present invention
The unreacted MDEA in part and with the immiscible alcohols of water；Lean solution include mutually it is most of with the immiscible alcohols of water, a part not
MDEA, fraction water and the fraction MDEA of reaction react the salt generated with sour gas.Therefore, in the liquid-using the present invention
After liquid phase becomes absorbent completion sour gas absorption, rich solution phase is detached, so that rich solution is mutually entered follow-up desorption unit and carries out acidity
Gas desorption completes that after absorbent and lean solution after desorption mix absorption process can be reused for.
Further, by adjusting MDEA composite absorber composition ratio, the composite absorber absorb after sour gas from
The volume ratio for sending out the liquid phase and lower liquid phase formed is (0.10-4.50):1.
Further, the composite absorber absorbs the volume ratio of the liquid phase and lower liquid phase that are spontaneously formed after sour gas
For (0.50-4.00):1.
Further, the absorption temperature that the composite absorber is used to absorb sour gas is 20-80 DEG C, and absorption pressure is
0.1-8MPa。
Further, the sour gas is to include CO2、H2S、SO2In one or more flue gases, natural gas, transformation
Gas or synthesis gas.
It is had the following advantages provided by the present invention for the composite absorber of sour gas separation：
The first, composite absorber of the invention forms liquid-liquid two-phase after absorbing sour gas, with CO2For, above and below
Liquid phase CO2Load capacity concentration ratio is 0.05-0.40:1, and since liquid phase (i.e. lean solution phase) loads minimal amount of sour gas,
It only needs to desorb the lower liquid phase (i.e. rich solution phase) of supported acidic gas, can be inhaled in this way according to industrial needs by adjusting
The proportioning of agent is received to change the volume ratio for being formed by upper and lower liquid phase, to reduce the amount of liquid for entering desorption unit, can be dropped
The heating sensible heat of absorbent in low desorption process, and then reduce the desorption energy consumption of sour gas.
The second, composite absorber using the present invention, can be according to industrial needs, by adjusting the proportioning of absorbent to change
The concentration ratio of upper and lower solid supported reagents sour gas, to can be improved into the negative of the rich solution phase load sour gas of desorption unit
Carrying capacity, and the concentration of salt formed in rich solution phase is improved, the activity of water in rich solution phase is reduced, so as to reduce desorption process
The evaporation capacity of middle water, and then reduce the desorption energy consumption of sour gas.
There are organic solvents in third, composite absorber of the invention, and CO is improved in absorption process2Absorption speed
Rate, the load capacity in addition entering sour gas in the rich solution phase of desorption unit are higher and organic molten containing that can promote to desorb on a small quantity
Agent can improve CO2Desorption efficiency and circular treatment amount (be defined as " enter the forward and backward institute's supported acidic gas of desorption unit amount
Difference "), to reduce the desorption energy consumption of sour gas.
Description of the drawings
Fig. 1 is the CO of different absorbents2Absorption rate compares figure.
Specific implementation mode
The invention will be further described With reference to embodiment, but is not limited to following embodiment.
It should be noted that due to some sour gas such as H2S、SO2Deng, there is toxicity or corrosivity, it is therefore, real below
Example is applied to absorb CO2For come illustrate the present invention liquid-liquid decomposition absorbent the characteristics of and advantage, it is not intended that of the invention
The liquid-liquid absorbent of offer is only applicable to absorb CO2。
Embodiment 1
MDEA, n-butanol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 30%, n-butanol
Mass fraction be 50%, the mass fraction of water is 20%.Then, in 20 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 35.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.408mol/L；Lower liquid phase is 9.0mL CO2The rich solution phase of high load, CO2Load capacity is 3.586mol/L.
Obviously, upper and lower liquid volume ratio is 3.89:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.11:1.
Embodiment 2
MDEA, n-butanol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 30%, n-butanol
Mass fraction be 40%, the mass fraction of water is 30%.Then, in 20 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 23.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.279mol/L；Lower liquid phase is 20.0mL CO2The rich solution phase of high load, CO2Load capacity is 3.078mol/L.
Obviously, upper and lower liquid volume ratio is 1.15:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.09:1.
Embodiment 3
MDEA, isoamyl alcohol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 30%, isoamyl alcohol
Mass fraction be 40%, the mass fraction of water is 30%.Then, in 20 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 22.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.205mol/L；Lower liquid phase is 20.0mL CO2The rich solution phase of high load, CO2Load capacity is 2.492mol/L.
Obviously, upper and lower liquid volume ratio is 1.1:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.08:1.
Embodiment 4
MDEA, tert-pentyl alcohol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 30%, tert-pentyl alcohol
Mass fraction be 30%, the mass fraction of water is 40%.Then, in 20 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 15.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.188mol/L；Lower liquid phase is 25.5mL CO2The rich solution phase of high load, CO2Load capacity is 2.438mol/L.
Obviously, upper and lower liquid volume ratio is 0.59:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.08:1.
Embodiment 5
MDEA, n-butanol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 30%, n-butanol
Mass fraction be 30%, the mass fraction of water is 40%.Then, in 20 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 16.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.250mol/L；Lower liquid phase is 26.0mL CO2The rich solution phase of high load, CO2Load capacity is 2.922mol/L, upper and lower liquid
Phase volume ratio is 0.62:1, upper and lower liquid phase CO2The ratio 0.09 of load capacity:1；Then, by lower liquid phase under 80 DEG C of temperature, normal pressure
It is desorbed, CO in lower liquid phase after desorption2Load capacity be 0.538mol/L, therefore, the repeated loading amount of absorbent is
2.384mol/L。
The lean solution of lower liquid phase and former absorbent after desorption is mixed, mixed solution restores homogeneously.
Embodiment 6
MDEA, n-butanol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 10%, n-butanol
Mass fraction be 60%, the mass fraction of water is 30%.Then, in 40 DEG C of temperature, CO is absorbed using the absorbent under normal pressure2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 35.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.121mol/L；Lower liquid phase is 11.0mL CO2The rich solution phase of high load, CO2Load capacity is 1.791mol/L.
Obviously, upper and lower liquid volume ratio is 3.18:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.07:1.
Embodiment 7
MDEA, n-octyl alcohol and water is compound, it is configured to absorbent 40g, the wherein mass fraction of MDEA is 60%, n-octyl alcohol
Mass fraction be 20%, the mass fraction of water is 20%.Then, under temperature 50 C, normal pressure CO is absorbed using the absorbent2
To saturation；Absorb CO2Absorbent afterwards forms liquid-liquid two-phase, and liquid phase is 18.0mL CO2The lean solution phase of low-load, CO2Load
Amount is 0.527mol/L；Lower liquid phase is 23.0mL CO2The rich solution phase of high load, CO2Load capacity is 1.331mol/L.
Obviously, upper and lower liquid volume ratio is 0.78:1, upper and lower liquid phase CO2Loading concentrations ratio is 0.39:1.
Embodiment 8
The mass fraction that absorbent and MDEA that MDEA mass fractions are 30% is respectively configured is 30%, the quality of n-butanol
Score is 30%, and the mass fraction of water is 40% composite absorber, each 40g.Then, slowly logical under normal pressure in 20 DEG C of temperature
Enter CO2Gas, control flow are 300mL/min.Two kinds of absorbents, which are measured, with soap bubble flowmeter absorbs CO2Rate, specific data
As shown in Figure 1, the CO of MDEA- n-butanol-water composite absorbers2Absorption rate is more than the MDEA that mass fraction is 30% and absorbs
Agent.
Above-described embodiment is to the present invention for example, the present invention can also be with other ad hoc fashions or others
Particular form is implemented, without departing from the gist of the invention or substantive characteristics.Therefore, from the point of view of the embodiment of description is in terms of any
It is regarded as illustrative and non-limiting.The scope of the present invention should illustrate by appended claims, any and claim
Intention and the equivalent variation of range should also be included in the scope of the present invention.
Claims (6)
1. it is a kind of for sour gas separation MDEA composite absorbers, which is characterized in that MDEA composite absorbers include MDEA,
Alcohol and water, the composite absorber due to MDEA hydrotropy effect, absorb sour gas before be homogeneous body, absorb sour gas after
Liquid-liquid two-phase is spontaneously formed, liquid phase is the lean solution phase of supported acidic gas, and lower liquid phase is the rich solution phase of supported acidic gas；
In MDEA composite absorbers, the mass percent of MDEA is 20%-40%, and the mass percent of alcohol is 20%-60%, water
Mass percent be 20%-60%；
React salt, the major part water, a part of unreacted of generation in above-mentioned rich solution phase with sour gas comprising major part MDEA
MDEA and alcohol；Lean solution includes mutually most of alcohol, a part of unreacted MDEA, fraction water and fraction MDEA and sour gas
React the salt generated；The alcohol is selected from n-butanol, isoamyl alcohol or tert-pentyl alcohol.
2. utilizing MDEA composite absorbers described in claim 1 for the method for sour gas separation, which is characterized in that including
Following steps：By sour gas and MDEA composite absorber haptoreactions, MDEA composite absorbers due to MDEA hydrotropy effect,
It is homogeneous body before absorption sour gas, spontaneously forms liquid-liquid two-phase after absorbing sour gas, liquid phase is supported acidic gas
Lean solution phase, lower liquid phase are the rich solution phase of supported acidic gas, detach rich solution phase, so that rich solution is mutually entered follow-up desorption unit and carry out
Sour gas desorbs, and completes to be reused for absorption process after absorbent and lean solution after desorption mix.
3. the method for being used for sour gas separation according to claim 2, which is characterized in that by adjusting the compound suctions of MDEA
Agent composition ratio is received, makes composite absorber absorb the volume ratio of liquid phase and lower liquid phase spontaneously formed after sour gas to be
(0.10-4.50):1。
4. the method for being used for sour gas separation according to claim 2, which is characterized in that composite absorber is made to absorb acid
Property gas after the volume ratio of the liquid phase that spontaneously forms and lower liquid phase be (0.50-4.00):1.
5. the method for being used for sour gas separation according to claim 2, which is characterized in that the composite absorber is used for
The absorption temperature for absorbing sour gas is 20-80 DEG C, absorption pressure 0.1-8MPa.
6. according to claim 2 be used for sour gas separation method, which is characterized in that the sour gas be comprising
CO2、H2S、SO2In one or more flue gases, natural gas, conversion gas or synthesis gas.
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| US7541011B2 (en) * | 2006-04-07 | 2009-06-02 | Liang Hu | Phase transitional absorption method |
| US8318116B2 (en) * | 2006-04-07 | 2012-11-27 | Liang Hu | Methods for deacidizing gaseous mixtures by phase enhanced absorption |
| CA2866090A1 (en) * | 2012-03-02 | 2013-09-06 | Basf Se | Removing acid gases from water vapour-containing fluid streams |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101362974A (en) * | 2007-08-06 | 2009-02-11 | 中国海洋石油总公司 | Absorbent for deeply removing carbon dioxide |
| CN102186559A (en) * | 2008-10-13 | 2011-09-14 | 胡亮 | Methods and systems for deacidizing gaseous mixtures |
| DE102012020141A1 (en) * | 2012-10-15 | 2014-04-17 | Hermann Büttner | Process for the synchronous absorption of carbon dioxide from flue gas and synthesis of dialkyl carbonates and alkylene carbonates |
| CN103143236A (en) * | 2013-03-06 | 2013-06-12 | 胜利油田胜利勘察设计研究院有限公司 | Decarburization solution for recovering and removing carbon dioxide gas from carbon dioxide flooding produced gas of oilfield |
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