CN107970743A - A kind of method for separating carbon dioxide - Google Patents
A kind of method for separating carbon dioxide Download PDFInfo
- Publication number
- CN107970743A CN107970743A CN201610918017.4A CN201610918017A CN107970743A CN 107970743 A CN107970743 A CN 107970743A CN 201610918017 A CN201610918017 A CN 201610918017A CN 107970743 A CN107970743 A CN 107970743A
- Authority
- CN
- China
- Prior art keywords
- carbon dioxide
- liquid
- tower
- absorbing liquid
- absorption tower
- 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.)
- Granted
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
- B01D53/14—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
-
- 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
- B01D53/1406—Multiple stage absorption
-
- 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
- B01D53/1418—Recovery of products
-
- 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
-
- 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
- B01D53/1468—Removing hydrogen sulfide
-
- 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
-
- 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
- B01D2252/30—Ionic liquids and zwitter-ions
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/50—Carbon oxides
- B01D2257/504—Carbon dioxide
-
- 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
Abstract
This disclosure relates to a kind of method for separating carbon dioxide, this method is absorbed using two tower multistages, desorption technique, easy to operate, is effectively increased the absorption efficiency and removal efficiency of carbon dioxide, is reduced absorbing liquid usage amount, improves the operating flexibility of device；Using heat transfer techniques, rich solution can be heated using low-grade heat source and obtain heat transfer rich solution, add the ability of flash tank carbon dioxide removal, the thermic load of desorber bottom reboiler is reduced at the same time, the ability of absorbing liquid absorbing carbon dioxide is improved, so as to improve the capacity usage ratio of whole decarbonization system；It can carry out the content of carbon dioxide in chain control purified gas by varying rich solution temperature and/or desorption bottom reboiler thermic load, control program is simply efficient；The condensate liquid that desorption tower top effluent obtains after cooling enters at the top of absorption tower, it is possible to reduce the loss amount of absorbent, so as to reduce the magnitude of recruitment of fresh absorbent and fresh water, further reduces the operating cost of device.
Description
Technical field
A kind of this disclosure relates to method for absorbing and separating of gas, and in particular, to method for separating carbon dioxide.
Background technology
Carbon dioxide is more and more closed as the final product aoxidized containing carbon species because of greenhouse gases effect
Note.Whether reduce CO2 emission from industrial production source, or to containing carbon dioxide gas mixture into advancing one
Step processing, the capture in carbon dioxide both at home and abroad, seal up for safekeeping, substantial amounts of research work has all been carried out in the field such as utilization and storage.
Known carbon dioxide capture, separation method are more, and existing physical separation (absorption, UF membrane, deep cooling), chemical absorbing, also have
The coefficient separate mode of physical chemistry.
At present, the method for being commercially used for carbon dioxide separation mainly has：Low-temp methanol washing process, Benfield method, activation
MDEA methods and mixed alkanalamine etc..Above method is all to use two tower process, and a tower absorbs, tower desorption, and carbon dioxide is inhaled
Receive with desorption alternately, achieve the purpose that to separate carbon dioxide.Although existing carbon dioxide separation technology part changes
Carbon dioxide separation performance, but also there are absorbing agent absorption capacity is small, absorption and regeneration high energy consumption, device Operational Figure Of Merit are low and dress
Put the problems such as investment is high.
The content of the invention
The purpose of the disclosure is to provide a kind of method for separating carbon dioxide, and this method is low with energy consumption, absorption rate height,
The advantages that uptake is big, device operation is flexible, easily controllable.
To achieve these goals, the disclosure provides a kind of method for separating carbon dioxide, and this method includes：
A, the mixed gas containing carbon dioxide is made to be absorbed into absorption tower with absorbing liquid counter current contacting, from the suction
Receive the tower top of tower and bottom of towe respectively obtains purified gas and rich carbonated rich solution；
B, make to obtain heat transfer rich solution after the rich solution is heated, the heat transfer rich solution is entered low pressure after decompression and dodge
Steaming pot carries out gas-liquid separation, obtains flashed vapour and flash distillation product；
C, enter the flash distillation product and regeneration of absorption solution is carried out at the top of desorber, from the tower top and bottom of towe of the desorber
Respectively obtain regeneration gas and be stripped of the lean solution of carbon dioxide；The lean solution is entered after cooling at the top of the absorption tower, make
Continue absorbing carbon dioxide for a part for the absorbing liquid；
D, the first semi lean solution for being stripped of partial CO 2 is extracted out in the middle part of the desorber；Make first semi lean solution
In a part after cooling enter the absorption tower at the top of, as the absorbing liquid a part continue absorbing carbon dioxide；
First semi lean solution of remainder is set to continue absorbing liquid again in the middle part of the desorber with being returned after lean solution heat exchange
It is raw.
Compared with the prior art, it is the advantages of the method for the separation carbon dioxide of the disclosure：
(1) using two tower multistages absorb, desorption technique, it is easy to operate, effectively increase carbon dioxide absorption efficiency and
Removal efficiency, reduces absorbing liquid usage amount, improves the operating flexibility of device；
(2) heat transfer techniques are used, rich solution can be heated using low-grade heat source and obtain heat transfer rich solution, are increased
The ability of flash tank carbon dioxide removal, while the thermic load of desorber bottom reboiler is reduced, improve absorbing liquid suction
The ability of carbon dioxide is received, so as to improve the capacity usage ratio of whole decarbonization system；
(3) can come by varying rich solution temperature and/or desorption bottom reboiler thermic load two in chain control purified gas
The content of carbonoxide, control program is simple, can realize the regulation and control to carbon dioxide content in purified gas in a short time；
(4) condensate liquid that desorption tower top effluent obtains after cooling enters at the top of absorption tower, it is possible to reduce absorbent
Loss amount, so as to reduce the magnitude of recruitment of fresh absorbent and fresh water, further reduces the operating cost of device；
(5) method of the separation carbon dioxide of the disclosure can be adjusted according to actual carbon dioxide treatment Capability Requirement
The composition of absorbent, can be adapted for the gaseous mixture of different carbon dioxide content scopes, meanwhile, this method not only can be adapted for
There was only the operating mode of carbon dioxide in mixed gas, be also applied for wrapping hydrogen sulfide containing operating mode in mixed gas.
Other feature and advantage of the disclosure will be described in detail in subsequent specific embodiment part.
Brief description of the drawings
Attached drawing is for providing further understanding of the disclosure, and a part for constitution instruction, with following tool
Body embodiment is used to explain the disclosure together, but does not form the limitation to the disclosure.In the accompanying drawings：
Fig. 1 is a kind of flow diagram of embodiment of the method for the separation carbon dioxide that the disclosure provides；
Fig. 2 is the flow diagram of another embodiment of the method for the separation carbon dioxide that the disclosure provides.
Description of reference numerals
1 purified gas liquid separation tank, 2 absorption tower
3 absorbing liquids supplement 4 desorber of tank
5 regeneration gas liquid separation tank, 6 flash tank
7 lean solution air cooler, 8 1# semi lean solution air coolers
9 regeneration 10 semi lean solution preheaters of Gas Cooler
11 rich solution heaters 12 purify Gas Cooler
13 lean solution feed pump, 14 1# semi lean solution feed pumps
15 semi lean solution regeneration pump, 16 pressure reducing valve
17 2# semi lean solutions air cooler, 18 2# semi lean solution feed pumps
19 electronic 20 rotary bodies of magnetic rotation rotation mechanism
21 absorbing liquid drawing pump, 22 refrigeration system
23 gas distribution grid, 24 liquid distributing board
Embodiment
The embodiment of the disclosure is described in detail below in conjunction with attached drawing.It should be appreciated that this place is retouched
The embodiment stated is only used for describing and explaining the disclosure, is not limited to the disclosure.
In the disclosure, in the case where not making conversely explanation, the noun of locality such as " upper and lower " used typically refers to the disclosure
In device or system it is upper and lower under normal operating condition, specifically, may be referred to the page of Fig. 1, " inside and outside " is
For the profile of device in itself.
The disclosure provides a kind of method for separating carbon dioxide, and this method includes：
A, the mixed gas containing carbon dioxide is made to be absorbed into absorption tower 2 with absorbing liquid counter current contacting, from described
The tower top and bottom of towe on absorption tower 2 respectively obtain purified gas and rich carbonated rich solution；
B, make to obtain heat transfer rich solution after the rich solution is heated, the heat transfer rich solution is entered low pressure after decompression and dodge
Steaming pot 6 carries out gas-liquid separation, obtains flashed vapour and flash distillation product；
C, the flash distillation product is entered the top of desorber 4 and carry out regeneration of absorption solution, from the tower top and tower of the desorber 4
Bottom respectively obtains regeneration gas and is stripped of the lean solution of carbon dioxide；The lean solution is set to enter the top of absorption tower 2 after cooling,
A part as the absorbing liquid continues absorbing carbon dioxide；
D, the first semi lean solution of partial CO 2 is stripped of from the middle part of desorber 4 extraction；Make described the first half poor
A part in liquid enters the top of absorption tower 2 after cooling, and the part as the absorbing liquid continues to absorb titanium dioxide
Carbon；Make first semi lean solution of remainder return to the middle part of desorber 4 after exchanging heat with the lean solution to continue to absorb
Liquid regenerates.
Compared with the prior art, it is the advantages of the method for the separation carbon dioxide of the disclosure：(1) inhaled using two tower multistages
Receive, desorption technique, it is easy to operate, the absorption efficiency and removal efficiency of carbon dioxide are effectively increased, reduces absorbing liquid use
Amount, improves the operating flexibility of device；(2) heat transfer techniques are used, low-grade heat source can be used to heat simultaneously rich solution
Heat transfer rich solution is obtained, adds the ability of flash tank carbon dioxide removal, while reduces the heat of desorber bottom reboiler
Load, improves the ability of absorbing liquid absorbing carbon dioxide, so as to improve the capacity usage ratio of whole decarbonization system；(3) may be used
To carry out the content of carbon dioxide in chain control purified gas by varying rich solution temperature and/or desorption bottom reboiler thermic load,
Control program is simple, can realize the regulation and control to carbon dioxide content in purified gas in a short time；(4) tower top effluent is desorbed
The condensate liquid obtained after cooling enters at the top of absorption tower, it is possible to reduce the loss amount of absorbent, so as to reduce fresh absorbent
With the operating cost of the magnitude of recruitment of fresh water, further reduction device；(5) method of the separation carbon dioxide of the disclosure can root
The factually carbon dioxide treatment Capability Requirement on border, adjusts the composition of absorbent, can be adapted for different carbon dioxide content scopes
Gaseous mixture, meanwhile, this method not only can be adapted in mixed gas only have carbon dioxide operating mode, be also applied for gaseous mixture
Hydrogen sulfide containing operating mode is wrapped in body.
According to the disclosure, as shown in Figure 1, the absorption tower 2 can be multistage absorption tower, it is preferable that tower diameter can be certainly
Increase step by step under above, i.e., enter per first grade absorption tower if any absorbing liquid, then corresponding tower diameter increases than upper level tower diameter, along tower
It can be non-isometric absorption on axial.Similarly, desorber 4 can also be multistage desorber, desorb CO2It is lucky with absorption process
On the contrary, therefore desorption tower diameter can be in be gradually reduced trend from top to bottom.Absorption tower 2 can be packed tower or plate column, absorption tower 2
Number of theoretical plate can be 5-15 blocks, preferably 7-12 blocks, further preferred 10 pieces；The desorber 4 can be packed tower or plate
Formula tower, the number of theoretical plate of desorber 4 can be 6-15 blocks, preferably 8-12 blocks, further preferred 10 pieces.Further, absorption tower
Preferably packed tower, filler can be one kind in structured packing, Pall ring and cascade ring；Desorber is preferably plate column, into
One kind in the preferred sieve-plate tower of one step, valve tower.The specific constructive form of packed tower and plate column, is those skilled in the art institute
Well known, the present invention repeats no more.
According to the disclosure, for the ease of further desorbing the carbon dioxide absorbed in absorbing liquid, this method can include：
The rich solution is entered the heating of heater 11 and obtain heat transfer rich solution, the heat transfer rich solution is entered after the decompression of pressure reducing valve 16
The low pressure flash chamber 6；Wherein, the temperature of the heat transfer rich solution can be 55-95 DEG C, be preferably 70-80 DEG C；The heat turns
The pressure moved after rich solution decompression can be 0.1-0.85MPa.Heater 11 can be shell-and-tube heater or shell-and-plate heater,
The disclosure is not done specifically limited.Can be in factory as long as the heat source of heater 11 can properly increase the temperature of rich solution
At least one of Low Temperature Thermal, underground heat, fume afterheat and solar energy, be preferably the low-temperature heat source in factory.
According to the disclosure, in order to further recycle the absorbing liquid in desorption tower top regeneration gas, this method can also include, make
Enter regeneration gas liquid separation tank 5 after the regeneration gas cooling and carry out gas-liquid separation, obtain rich carbonated regeneration gas and condensation
Liquid；The condensate liquid is set to return to the top of absorption tower 2, the part as the absorbing liquid continues absorbing carbon dioxide.
According to the disclosure, since flashed vapour and purified gas can carry a small amount of moisture and micro absorbent, while with
Absorption, desorption process constantly carry out, and partially absorb agent and understand quality decline in the process of running and influence decarburization effect, in order to supplement
The absorbing liquid consumed in cyclic process, ensures the internal circulating load of absorbing liquid in device, and under preferable case, this method can include, and make
The lean solution and the condensate liquid enter absorbing liquid supplement tank 3, are mixed with the supplement absorbing liquid for entering absorbing liquid supplement tank 3
After obtain blend absorbent, the blend absorbent is entered the top of the absorption tower 2 after cooling, as the absorbing liquid
A part continues absorbing carbon dioxide.Under above-mentioned preferable case, suitable absorbing liquid can be supplemented according to device operating condition,
Ensure the separative efficiency of carbon dioxide in gas mixture.
In order to further improve the absorption efficiency of carbon dioxide and removal efficiency, under preferable case, this method can also wrap
Include, the second semi lean solution of partial CO 2 is stripped of from the middle part of desorber 4 extraction, make second semi lean solution through supercooling
But the middle part of absorption tower 2 is entered afterwards, the part as the absorbing liquid continues absorbing carbon dioxide.In above-mentioned preferable case
Under, the absorbability of carbon dioxide in gas mixture can be effectively improved, while can be shown using two towers three sections of absorptions, desorption techniques
Writing reduces the thermic load of reboiler and rich solution heater.
According to the disclosure, in order to further improve the absorption efficiency of carbon dioxide, this method can also include, and make from described
The tower top for partially absorbing liquid and the absorption tower 2 being returned to after cooling of the middle part of absorption tower 2 extraction, continues absorbing carbon dioxide, drop
The temperature of the absorbing liquid after temperature can be 5-15 DEG C.
In order to further improve the absorption efficiency of carbon dioxide in absorption tower, in a kind of preferable specific embodiment party of the disclosure
Can be provided with formula, inside absorption tower 2 can rotating rotary body 20 around the shaft, the both ends of the shaft are individually fixed in described
Inside absorption tower 2；It can be provided with outside absorption tower 2 for driving the rotary body 20 electronic magnetic rotation favourable turn rotating around the shaft
Structure 19；The electronic magnetic rotation rotation mechanism 19 can be coaxial and non-contact setting with the rotary body 20.Above-mentioned preferable implementation
Mode can improve the speed of absorbing liquid absorbing carbon dioxide, in the case of equal treating capacity, can reduce the equipment on absorption tower
Size, reduces the dosage of absorbing liquid, further improves the economic performance of the technique.In addition, rotary body is arranged inside absorption tower,
It is in contact with absorbing liquid and mixed gas, and power intake of the electronic magnetic rotation rotation mechanism as rotary body, it is arranged at absorption tower
Outside, can efficiently reduce liquid phase leakage.
According to the disclosure, the content and temperature of carbon dioxide in gas mixture can change in very large range, it is preferable that
The temperature of mixed gas containing carbon dioxide can be 25 DEG C -75 DEG C, and pressure can be 0.1MPa-4.5MPa, carbon dioxide
Volume content be 3.0%-45%.The mixed gas can be power-plant flue gas, conversion gas, F- T synthesis circulating air, speed to put
At least one of gas and plant tail gas.
In order to further improve the absorption and desorption efficiency of carbon dioxide, it is preferable that the operation temperature on absorption tower 2 can be
5 DEG C -85 DEG C, pressure can be 0.1MPa-4.5MPa, and the operation temperature of desorber 4 can be 95 DEG C -126 DEG C, and pressure can be
0.1MPa-0.25MPa.Under the operating conditions described above, absorption tower 2 and desorber 4 can be with normal operations, and in absorbing liquid is ensured
Absorbent does not occur on the premise of high temperature degradation loses absorbability, to further improve absorption and desorption efficiency.
According to the disclosure, the absorbing liquid can contain hydramine and/or activator, with or without having water, defoamer, ion
Liquid or corrosion inhibiter.The hydramine, activator, water, defoamer, ionic liquid and corrosion inhibiter are ripe for those skilled in the art
Know, the disclosure does not limit specific species, for example, hydramine can be selected from monoethanolamine (MEA), diethanol amine (DEA), N-
One or more in methyl diethanolamine (MDEA) and diethylenetriamine (DETA)；Activator can be selected from piperazine, N- first
Base piperazine, n-ethylpiperazine, N- propylpiperazines, N- isopropyls piperazine, N- butyl piperazine and one kind in N- isobutyl piperazines or
Several, preferably activator is piperazine；The water is preferably demineralized water；Defoamer can be selected from silicone emulsion, polyoxyethylene
Polyoxypropylene pentaerythrite ether, the fatty acid ester compounded thing of higher alcohols, polypropylene glycerol aether and polyoxyethylene polyoxypropylene glycerine
One or more in ether, polyoxyethylene polyoxy propyl alcohol amidogen ether and dimethyl silicone polymer；Ionic liquid can be selected from 1- fourths
Base -3- methylimidazoles hexafluorophosphate ([bmim] [PF6]), 1- (3- Propylaminos) -3- butyl imidazole hexafluorophosphates
([apbim][PF6]), 1- butyl -2,3- methylimidazoles hexafluorophosphate ([bmmim] [PF6]), proline oxycholine salt
([Choline] [Pro]), 1- (3- Propylaminos) -3- butyl imidazoles tetrafluoroborates ([apbim] [BF4]), 1- butyl -3- first
Base tetrafluoroborate ([bmim] [BF4]), 1- butyl -2,3- methylimidazoles tetrafluoroborate ([bmmim] [BF4])、1-
Ethyl-3-methylimidazole bis trifluoromethyl sulfimide salt ([emim] [Tf2N]) and 1- ethyls -2,3- methylimidazole double three
Methyl fluoride sulfimide salt ([emmim] [Tf2N]), the double fluoroform sulphur inferior amine salts of 1- (3- Propylaminos) -3- butyl imidazoles
([apbim][Tf2N]) and 1- (1- aminopropyls) -3- methylimidazole bromides ([NH2P-mim] [Br]) in one or more；
Corrosion inhibiter can be selected from potassium metavanadate, potassium vanadate, vanadic anhydride, antimony pentaoxide, antimony oxide, four three antimony of oxidation, wine
One or more in stone acid oxygen antimony sodium and potassium antimonyl tartrate, are preferably vanadium compounds such as potassium metavanadate, potassium vanadate and five
One or more in V 2 O, are most preferably potassium metavanadate.
In order to reduce the material grade of equipment and pipeline, it is preferable that corrosion inhibiter can be contained in absorbing liquid；In order to effectively disappear
Tower Concerning Flooding Phenomenon in desorber is removed or reduced, defoamer can also be preferably contained in absorbing liquid.It is highly preferred that the absorbing liquid
Hydramine, activator, defoamer, ionic liquid, corrosion inhibiter and water can be contained, wherein, it is described relative to the water of 100 parts by weight
The content of hydramine can be 10-100 parts by weight, and the content of the activator can be 0.01-10 parts by weight, the defoamer
Content can be 0.001-1 parts by weight, and the content of the ionic liquid can be 0.01-100 parts by weight, and the corrosion inhibiter contains
Amount can be 0.001-1 parts by weight, it is highly preferred that relative to the water of 100 parts by weight, the content of the hydramine can be 20-80
Parts by weight, the content of the activator can be 1-7 parts by weight, and the content of the defoamer can be 0.001-0.2 parts by weight,
The content of the ionic liquid can be 1-50 parts by weight, and the content of the corrosion inhibiter can be 0.001-0.2 parts by weight.Upper
In the case of stating preferably, hydramine and ionic liquid in absorbent can be regulated and controled according to actual carbon dioxide treatment Capability Requirement
Both ratios so that this method can be adapted for the broader mixed gas of carbon dioxide content scope, and absorbing liquid hot recycling
Performance is good, improves the efficiency of absorption and desorption.
The disclosure is further illustrated by embodiment below in conjunction with attached drawing, but therefore the disclosure is not subject to any
Limitation.
Embodiment 1
In the present embodiment, absorption tower packing area size is (by tower top to bottom of towe, similarly hereinafter)： (body portion containing rotation), tower height
40000mm, absorption tower bottom are equipped withRotary body；Desorber window screen size is：Tower height 33000m
m.Absorption tower number of theoretical plate is 10 pieces, and desorber number of theoretical plate is 8 pieces.Mixed gas composition is shown in Table 1.Absorbing liquid forms：Desalination
100 parts by weight of water, 69.0 parts by weight of MDEA, 3.44 parts by weight of activator piperazine, 0.02 parts by weight of defoamer silicone emulsion, delay
Lose 0.01 parts by weight of agent potassium metavanadate.
1 mixed gas of table forms
As shown in Figure 1, the carbon dioxide separation method of the present embodiment is set using two towers three sections of absorptions, three sections of desorption techniques
Put：
A. 23.29% (volume fraction), the gaseous mixture that temperature is 60 DEG C, pressure is 2.55MPa (A) carbon dioxide will be contained
Body enters temperature as 72 DEG C of absorption towers 2 and absorbing liquid counter current contacting using the feed rate of 3985kmol/h, and bottom of towe obtains being rich in two
The rich solution of carbonoxide, tower overhead gas are cooled to 45 DEG C by purification Gas Cooler 12, and into purified gas liquid separation tank 1, tank bottom is isolated
Condensate liquid, tank deck are purified gas, and carbon dioxide volume fraction is 0.016% in gained purified gas；
2 lower part of absorption tower is provided with rotary body 20 and electronic magnetic rotation rotation mechanism 19, and 1200 turns of electromagnetic rotating mechanism rotating speed/
Point.The rotary body rotating speed identical with electromagnetic rotating mechanism holding and steering.Rotary body is filling metal screen net structure, and liquid phase is equal
Can be to pass through the screen net structure, there is provided the place of gas-liquid contact.
B. the heated device 11 of rich solution in step a is heated to 82 DEG C, pressure is reduced to by 0.7MPa by pressure reducing valve 16
(A), it is directly entered low pressure flash chamber 6 after, tank deck obtains flash distillation air carbon dioxide, its flow is 68.74kmol/h, volume fraction
Form as CO2：77.84%, H2：13.77%, N2：0.007%, CO：0.0388%, H2O：8.2%, CH4：0.15%；Tank bottom obtains
To flash distillation product；
Rich solution heater 11 uses 125 DEG C of steam condensates as heat source, heating absorption tower outlet rich solution.
C. flash distillation product step b obtained is sent into 116 DEG C of tops of desorber 4 and carries out regeneration of absorption solution, discharges absorption
Carbon dioxide in liquid.From desorber, away from extraction at 9000mm at tangent line on tower top, one releases the second of partial CO 2
Semi lean solution, successively by 2# semi lean solutions feed pump 18,2# semi lean solutions air cooler 17, the temperature 60 C of the second semi lean solution, pressure
3.35MPa (A), is sent directly into absorption tower lower absorbent section and continues absorbing carbon dioxide, feed entrance point is away from lower tangential length
10000mm.In addition, from desorber away from tangent line 18000mm, the first semi lean solution being completely drawn out, by it with 3 on tower top:1 volume ratio
It is divided into two strands, for the first big person of semi lean solution volume successively by 1# semi lean solutions feed pump 14,1# semi lean solutions air cooler 8, the first half poor
Temperature 60 C, the pressure 3.22MPa (A) of liquid, are sent directly into absorption tower central absorbent section and continue absorbing carbon dioxide, middle part charging
Position is 19000mm away from tangential length under bottom of towe；The small person of first semi lean solution preheats with 4 tower bottom product of desorber through semi lean solution
Device 10 returns to the middle part of desorber 4 after preheating continues to remove the carbon dioxide in absorbing liquid, and the lean solution after stripping is through more than half poor
After liquid preheater 10 cools down, successively by absorbing liquid supplement tank 3, lean solution feed pump 13, lean solution air cooler 7,60 DEG C, pressure are cooled to
Power enters the circular regeneration for away from upper tangent line 6000mm positions at the top of absorption tower, completing absorbing liquid for 2.93MPa (A).
One absorbing liquid is extracted out at away from the upper tangent line 9000mm positions in absorption tower top to be sent into by absorbing liquid drawing pump 21
Refrigeration system reduce temperature after, return absorption tower away from upper tangent line 1500mm locate, continue absorption gas phase in carbon dioxide, Extract
Flow 35000kg/h, it is 8.5 DEG C to return to tower top temperature.
D. desorber 4 pushes up effluent after regeneration Gas Cooler 9 cools down, and gas-liquid point is carried out into regeneration gas liquid separation tank 5
From condensate liquid returns to absorbing liquid supplement tank 3, and gas phase is rich carbonated regeneration gas.This technique recycles condensing liquid quantity
3636kg/h, the fresh absorption liquid measure that need to be supplemented are 1834kg/h, and fresh absorbing liquid composition is identical with absorbing liquid initial composition.
The technological parameter of performance indicator and carbon dioxide separation that gas is purified in the present embodiment is listed in table 2.
Embodiment 2
As shown in Fig. 2, the apparatus and method that the present embodiment uses embodiment 1, the difference is that using two towers, two sections of suctions
Receive, desorption technique, i.e., do not include in the method for the present embodiment from desorber away from extracting the second half at 9000mm at tangent line on tower top out
Lean solution is sent into the step of absorbing carbon dioxide is continued on absorption tower.Reach purified gas CO substantially the same manner as Example 1 in the present embodiment2
When removing performance, the various process parameters of carbon dioxide separation are listed in table 2.
The performance indicator of 2 purified gas of table and the technological parameter of carbon dioxide separation
* regeneration degree=mol CO2/mol MDEA
From Table 2, it can be seen that absorbed using two towers, three sections of absorptions, desorption technique absorbability compared with two sections, desorption techniques
It is stronger, while there is lower reboiler and rich solution heater thermic load.
Embodiment 3
In the present embodiment, absorption tower packing area size is (by tower top to bottom of towe, similarly hereinafter)： (body portion containing rotation), tower height 20000mm, absorption tower bottom is equipped withRotary body；Desorber window screen size is： Tower height 23000mm.Absorption tower number of theoretical plate is 8 pieces, and desorber number of theoretical plate is 7 pieces.
Mixed gas composition is shown in Table 3.Absorbing liquid composition is same as Example 1.
3 mixed gas of table forms
As shown in Fig. 2, the carbon dioxide separation method of the present embodiment is using two towers two sections of absorptions, two sections of desorption techniques：
A. 26.0% (volume fraction), the gaseous mixture that temperature is 60 DEG C, pressure is 2.41MPa (A) carbon dioxide will be contained
Body enters temperature as 76 DEG C of absorption towers 2 and absorbing liquid counter current contacting using the feed rate of 3500kmol/h, and bottom of towe obtains being rich in two
The rich solution of carbonoxide, tower overhead gas are cooled to 45 DEG C by purification Gas Cooler 12, and into purified gas liquid separation tank, tank bottom is isolated cold
Lime set, tank deck are purified gas, and carbon dioxide volume fraction is 0.023% in gained purified gas；
2 lower part of absorption tower is provided with rotary body 20 and electronic magnetic rotation rotation mechanism 19, and 1500 turns of electromagnetic rotating mechanism rotating speed/
Point.Rotation body structure is same as Example 1, and rotary body is filling metal screen net structure, and liquid phase can be to pass through the silk screen knot
Structure, there is provided the place of gas-liquid contact.
B. the heated device 11 of rich solution in step a is heated to 80 DEG C, pressure is reduced to by 0.7MPa by pressure reducing valve 16
(A), low pressure flash chamber 6 is directly entered after, tank deck flashes off carbon dioxide, its flow is 46.11kmol/h, and volume fraction forms
For CO2：74.87%, H2：14.11%, N2：2.44%, CO：0.67%, H2O：7.65%, CH4：0.27%；Tank bottom is flashed
Product；
Rich solution heater 11 uses 125 DEG C of steam condensates as heat source, heating absorption tower outlet rich solution；
C. flash distillation product step b obtained is sent into 112 DEG C of tops of desorber 4 and carries out regeneration of absorption solution, discharges absorption
Carbon dioxide in liquid.From desorber away from 9000mm at tangent line on tower top at, the first lean solution is completely drawn out, by it with 3:1 volume
Score is into two strands, and the big person of the first lean solution volume is by by 1# semi lean solutions feed pump 14,1# semi lean solutions air cooler 8, half is poor successively
Temperature 60 C, the pressure 3.44MPa (A) of liquid, are sent directly into absorption tower central absorbent section and continue absorbing carbon dioxide, middle part charging
Position is 9500mm away from tangential length under bottom of towe；The small person of first semi lean solution preheats with 4 tower bottom product of desorber through semi lean solution
Device 10 returns to the middle part of desorber 4 after preheating continues to remove the carbon dioxide in absorbing liquid, and the lean solution after stripping is through more than half poor
After liquid preheater 10 cools down, successively by absorbing liquid supplement tank 3, lean solution feed pump 13, lean solution air cooler 7,60 DEG C, pressure are cooled to
Power enters the circular regeneration for away from upper tangent line 5000mm positions at the top of absorption tower, completing absorbing liquid for 3.03MPa (A)；
D. desorber 4 pushes up effluent after regeneration Gas Cooler 9 cools down, and gas-liquid point is carried out into regeneration gas liquid separation tank 5
From condensate liquid returns to absorbing liquid supplement tank 3, and gas phase is rich carbonated regeneration gas.This technique recycles condensing liquid quantity
3402kg/h, the fresh absorption liquid measure that need to be supplemented are 1577kg/h, and fresh absorbing liquid composition is identical with absorbing liquid initial composition；
One absorbing liquid is extracted out at away from the upper tangent line 9000mm positions in absorption tower top to be sent into by absorbing liquid drawing pump 21
Refrigeration system reduce temperature after, return absorption tower away from upper tangent line 1500mm locate, continue absorption gas phase in carbon dioxide, Extract
Flow 30500kg/h, it is 8.5 DEG C to return to tower top temperature.
The technological parameter of performance indicator and carbon dioxide separation that gas is purified in the present embodiment is listed in table 4.
Comparative example 1
Using the apparatus and method of embodiment 3, the difference is that this comparative example is using two towers, two sections of absorptions, desorption and richness
The not heated technique for being directly entered flash distillation of liquid.Reach purified gas CO substantially the same manner as Example 3 in this comparative example2Remove performance
When, the various process parameters of carbon dioxide separation are listed in table 4.
The performance indicator of 4 purified gas of table and the technological parameter of carbon dioxide separation
* regeneration degree=mol CO2/mol MDEA
As can be seen from Table 4, heat transfer technology is added using two towers two sections of absorptions, desorption techniques, except absorbing energy
Power is absorbed compared with two sections, desorption is stronger outer without heat transfer technics, it is often more important that, after rich solution heater is set, it can significantly reduce
Bottom reboiler thermic load is desorbed, the amplitude that reduces is 27.6%.
In addition, by monitoring CO in purified gas in real time2Content, as found CO in purified gas2There are the feelings increased suddenly in concentration
Condition (volume content increases to 0.1% from 0.023%), in embodiment 3, by setting chain control with rich solution heater, only
Normal setting value can be reached within 100 second time by changing CO contents in gas；And comparative example 1 is without using two sections of suctions of rich solution heater
Receipts, regeneration technology (traditional handicraft) then need to get to normal setting value in 350 second time, illustrate to set rich solution heater energy
It is enough to realize in a short time to CO in purified gas2The regulation and control of content；Using heat transfer techniques, can be added using low-grade heat source
Hot rich solution, adds flash tank removing CO2Ability, while reduce desorber bottom of towe thermic load, improve absorbing liquid absorption
CO2Ability, improve the capacity usage ratio of whole decarbonization system.It can be seen that the present invention uses heat transfer technology, rich solution is set to add
Hot device Technical expression has gone out more excellent performance.
Embodiment 4
As shown in Fig. 2, the process conditions such as the technological process that the present embodiment uses, operating condition, mixed gas composition, flow
It is same as Example 3.Difference from Example 3 is that the absorbing liquid composition in the present embodiment is different, absorbing liquid composition：Remove
100 parts by weight of brine, MDEA27.27 parts by weight, [bmim] [PF6] 22.73 parts by weight, 1.52 parts by weight of activator piperazine, disappear
0.02 parts by weight of infusion silicone emulsion, 0.01 parts by weight of corrosion inhibiter potassium metavanadate.
The technological parameter of performance indicator and carbon dioxide separation that gas is purified in the present embodiment is listed in table 5.
Embodiment 5
Using the apparatus and method of embodiment 4, the difference is that by [bmim] [PF in absorbing liquid6] ionic liquid replaces
The MDEA of parts by weight such as it is changed to.Reach purified gas CO substantially the same manner as Example 4 in this comparative example2When removing performance, titanium dioxide
The separated various process parameters of carbon are listed in table 5.
5 performance indicator of table
* regeneration degree=mol CO2/mol MDEA
As can be seen from Table 5, due to the addition of [bmim] [PF6] ionic liquid, rich solution regeneration degree is from without ion
0.52 during liquid increases to 0.55, so as to improve the carbon dioxide absorption ability (Nm of absorbing liquid3CO2/m3, from 27.1 rises
To 30.5).The addition of ionic liquid, can be greatly lowered MDEA absorbent usage amounts, and reduce absorbing liquid usage amount, into
And reduce reboiler, the thermic load of rich solution heater, fundamentally realize the purpose for reducing plant investment and operating cost.
It was found from the data of embodiment 1-5 and comparative example 1, carbon dioxide separation method provided by the invention has energy consumption
Low, absorption rate is high, uptake is big, and device operates the advantages that flexible, easily controllable, can significantly reduce carbon dioxide separation list
The operating cost of member.
The preferred embodiment of the disclosure is described in detail above in association with attached drawing, still, the disclosure is not limited to above-mentioned reality
The detail in mode is applied, in the range of the technology design of the disclosure, a variety of letters can be carried out to the technical solution of the disclosure
Monotropic type, these simple variants belong to the protection domain of the disclosure.
It is further to note that each particular technique feature described in above-mentioned embodiment, in not lance
In the case of shield, it can be combined by any suitable means.In order to avoid unnecessary repetition, the disclosure to it is various can
The combination of energy no longer separately illustrates.
In addition, it can also be combined between a variety of embodiments of the disclosure, as long as it is without prejudice to originally
Disclosed thought, it should equally be considered as disclosure disclosure of that.
Claims (10)
- A kind of 1. method for separating carbon dioxide, it is characterised in that this method includes：A, the mixed gas containing carbon dioxide is made to be absorbed into absorption tower (2) with absorbing liquid counter current contacting, from the suction Receive the tower top of tower (2) and bottom of towe respectively obtains purified gas and rich carbonated rich solution；B, make to obtain heat transfer rich solution after the rich solution is heated, the heat transfer rich solution is entered low pressure flash chamber after decompression (6) gas-liquid separation is carried out, obtains flashed vapour and flash distillation product；C, enter the flash distillation product and regeneration of absorption solution is carried out at the top of desorber (4), from the tower top and tower of the desorber (4) Bottom respectively obtains regeneration gas and is stripped of the lean solution of carbon dioxide；Make the lean solution enter the absorption tower (2) after cooling to push up Portion, the part as the absorbing liquid continue absorbing carbon dioxide；D, the first semi lean solution for being stripped of partial CO 2 is extracted out in the middle part of the desorber (4)；Make first semi lean solution In a part after cooling enter the absorption tower (2) at the top of, the part as the absorbing liquid continue absorb titanium dioxide Carbon；Make first semi lean solution of remainder return after exchanging heat with the lean solution to continue to inhale in the middle part of the desorber (4) Receive liquid regeneration.
- 2. according to the method described in claim 1, it is characterized in that, this method includes：The rich solution is set to enter heater (11) Heating obtains heat transfer rich solution, the heat transfer rich solution is entered the low pressure flash chamber (6) after pressure reducing valve (16) decompression；Its In, the temperature of the heat transfer rich solution is 70-80 DEG C；Pressure after the heat transfer rich solution decompression is 0.1-0.85MPa.
- 3. according to the method described in claim 1, it is characterized in that, this method further includes, the regeneration gas is set to enter after cooling down Regeneration gas liquid separation tank (5) carries out gas-liquid separation, obtains rich carbonated regeneration gas and condensate liquid；Return to the condensate liquid At the top of the absorption tower (2), the part as the absorbing liquid continues absorbing carbon dioxide.
- 4. according to the method described in claim 3, it is characterized in that, this method includes, make the lean solution and the condensate liquid into Entering absorbing liquid supplement tank (3), the supplement absorbing liquid with entering absorbing liquid supplement tank (3) obtains blend absorbent after mixing, The blend absorbent is set to enter after cooling at the top of the absorption tower (2), the part as the absorbing liquid continues to absorb Carbon dioxide.
- 5. according to the method described in claim 1, it is characterized in that, this method further includes, from the extraction of the desorber (4) middle part The second semi lean solution of partial CO 2 is stripped of, second semi lean solution is entered after supercooling in the absorption tower (2) Portion, the part as the absorbing liquid continue absorbing carbon dioxide.
- 6. according to the method described in claim 1, it is characterized in that, this method further includes, make to take out in the middle part of the absorption tower (2) The tower top for partially absorbing liquid and the absorption tower (2) being returned to after cooling gone out, continues absorbing carbon dioxide, the suction after cooling The temperature for receiving liquid is 5-15 DEG C.
- 7. according to the method described in claim 1, it is characterized in that, the absorption tower (2) are internally provided with and can rotate around the shaft Rotary body (20), it is internal that the both ends of the shaft are individually fixed in the absorption tower (2)；It is provided with outside the absorption tower (2) for driving the rotary body (20) electronic magnetic rotation rotation mechanism rotating around the shaft (19)；The electronic magnetic rotation rotation mechanism (19) is coaxial with the rotary body (20) and non-contact setting.
- 8. according to the method described in any one in claim 1-7, it is characterised in that the gaseous mixture containing carbon dioxide The temperature of body is 25 DEG C -75 DEG C, pressure 0.1MPa-4.5MPa, and the volume content of carbon dioxide is 3.0%-45%；The suction It is 5 DEG C -85 DEG C to receive tower (2) operation temperature, pressure 0.1MPa-4.5MPa；The operation temperature of the desorber (4) for 95 DEG C- 126 DEG C, pressure 0.1MPa-0.25MPa.
- 9. according to the method described in any one in claim 1-7, it is characterised in that the absorbing liquid contain hydramine and/or Activator, with or without having water, defoamer, ionic liquid or corrosion inhibiter.
- 10. according to the method described in claim 9, it is characterized in that, the absorbing liquid contain hydramine, activator, defoamer, from Sub- liquid, corrosion inhibiter and water, wherein, relative to the water of 100 parts by weight, the content of the hydramine is 10-100 parts by weight, described The content of activator is 0.01-10 parts by weight, and the content of the defoamer is 0.001-1 parts by weight, and the ionic liquid contains Measure as 0.01-100 parts by weight, the content of the corrosion inhibiter is 0.001-1 parts by weight.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610918017.4A CN107970743B (en) | 2016-10-20 | 2016-10-20 | Method for separating carbon dioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610918017.4A CN107970743B (en) | 2016-10-20 | 2016-10-20 | Method for separating carbon dioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN107970743A true CN107970743A (en) | 2018-05-01 |
| CN107970743B CN107970743B (en) | 2020-01-03 |
Family
ID=62003720
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201610918017.4A Active CN107970743B (en) | 2016-10-20 | 2016-10-20 | Method for separating carbon dioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN107970743B (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854465A (en) * | 2018-07-11 | 2018-11-23 | 北京化工大学 | The method that amido ionic liquid and ethanol amine are blended in absorbing carbon dioxide in microchannel |
| CN109232161A (en) * | 2018-11-15 | 2019-01-18 | 中国华能集团清洁能源技术研究院有限公司 | In a kind of power-plant flue gas carbon dioxide recovery with utilize system and method |
| CN110256188A (en) * | 2019-07-16 | 2019-09-20 | 西安长庆科技工程有限责任公司 | One kind containing CO to height2Ethane gas carry out deep purifying process and device |
| CN111422872A (en) * | 2019-01-10 | 2020-07-17 | 国家能源投资集团有限责任公司 | System and method for capturing carbon dioxide from a carbon dioxide generating asset group |
| CN113620798A (en) * | 2021-09-10 | 2021-11-09 | 中国华能集团清洁能源技术研究院有限公司 | System and method for synthesizing formic acid by hydrogenation of carbon dioxide driven by renewable energy |
| WO2022008876A1 (en) | 2020-07-10 | 2022-01-13 | Carbon Clean Solutions Limited | A method and system for the removal of carbon dioxide from solvents using low-grade heat |
| CN114685236A (en) * | 2020-12-28 | 2022-07-01 | 中国石油化工股份有限公司 | Method and device for removing carbon dioxide and methanol from crude propylene gas |
| CN115138178A (en) * | 2022-07-07 | 2022-10-04 | 武汉工程大学 | Polyamine-based organic amine and ionic liquid composite CO 2 Absorbent, preparation method and application thereof |
| WO2024023509A1 (en) | 2022-07-29 | 2024-02-01 | Carbon Clean Solutions Limited | A method and system for the removal of carbon dioxide from carbon capture solvents using heat from a gas |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1088472A (en) * | 1992-12-24 | 1994-06-29 | 四川化工总厂 | From mist, remove the method for carbon dioxide |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| CN104918681A (en) * | 2012-11-14 | 2015-09-16 | 得克萨斯州大学系统董事会 | Apparatus for and method of removing acidic gas from a gaseous stream and regenerating an absorbent solution |
| CN105126576A (en) * | 2015-07-29 | 2015-12-09 | 中国石油集团工程设计有限责任公司 | High-efficiency composite desulphurization solvent and system and method for removing acidic gas and organic sulfur |
-
2016
- 2016-10-20 CN CN201610918017.4A patent/CN107970743B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1088472A (en) * | 1992-12-24 | 1994-06-29 | 四川化工总厂 | From mist, remove the method for carbon dioxide |
| CN103768895A (en) * | 2012-10-23 | 2014-05-07 | 中国石油化工股份有限公司 | Method for low-energy consumption removal of carbon dioxide by hot potash |
| CN104918681A (en) * | 2012-11-14 | 2015-09-16 | 得克萨斯州大学系统董事会 | Apparatus for and method of removing acidic gas from a gaseous stream and regenerating an absorbent solution |
| CN103977683A (en) * | 2014-04-30 | 2014-08-13 | 天津大学 | Method and device for reducing regeneration energy consumption of decarburization absorption liquid |
| CN105126576A (en) * | 2015-07-29 | 2015-12-09 | 中国石油集团工程设计有限责任公司 | High-efficiency composite desulphurization solvent and system and method for removing acidic gas and organic sulfur |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108854465A (en) * | 2018-07-11 | 2018-11-23 | 北京化工大学 | The method that amido ionic liquid and ethanol amine are blended in absorbing carbon dioxide in microchannel |
| CN108854465B (en) * | 2018-07-11 | 2021-04-02 | 北京化工大学 | Method for absorbing carbon dioxide in micro-channel by mixing amino ionic liquid and ethanolamine |
| CN109232161A (en) * | 2018-11-15 | 2019-01-18 | 中国华能集团清洁能源技术研究院有限公司 | In a kind of power-plant flue gas carbon dioxide recovery with utilize system and method |
| CN111422872A (en) * | 2019-01-10 | 2020-07-17 | 国家能源投资集团有限责任公司 | System and method for capturing carbon dioxide from a carbon dioxide generating asset group |
| CN111422872B (en) * | 2019-01-10 | 2022-01-25 | 国家能源投资集团有限责任公司 | System and method for capturing carbon dioxide from a carbon dioxide generating asset group |
| CN110256188A (en) * | 2019-07-16 | 2019-09-20 | 西安长庆科技工程有限责任公司 | One kind containing CO to height2Ethane gas carry out deep purifying process and device |
| WO2022008876A1 (en) | 2020-07-10 | 2022-01-13 | Carbon Clean Solutions Limited | A method and system for the removal of carbon dioxide from solvents using low-grade heat |
| CN114685236A (en) * | 2020-12-28 | 2022-07-01 | 中国石油化工股份有限公司 | Method and device for removing carbon dioxide and methanol from crude propylene gas |
| CN113620798A (en) * | 2021-09-10 | 2021-11-09 | 中国华能集团清洁能源技术研究院有限公司 | System and method for synthesizing formic acid by hydrogenation of carbon dioxide driven by renewable energy |
| CN115138178A (en) * | 2022-07-07 | 2022-10-04 | 武汉工程大学 | Polyamine-based organic amine and ionic liquid composite CO 2 Absorbent, preparation method and application thereof |
| WO2024023509A1 (en) | 2022-07-29 | 2024-02-01 | Carbon Clean Solutions Limited | A method and system for the removal of carbon dioxide from carbon capture solvents using heat from a gas |
Also Published As
| Publication number | Publication date |
|---|---|
| CN107970743B (en) | 2020-01-03 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN107970743A (en) | A kind of method for separating carbon dioxide | |
| CN101274204B (en) | Absorbing agent for removing and recovering sulfur dioxide from gaseous mixture | |
| CN104492226B (en) | A kind of non-aqueous decarbonizing solution for trapping carbon dioxide in gas mixture and application thereof | |
| CN101612509A (en) | Capture the composite decarbonizing solution of carbon dioxide in the mist | |
| CN105521696A (en) | Room-temperature liquid-phase Claus process taking ionic liquid as media | |
| CN105664671B (en) | A kind of zero carbon emission technique gas purifying method and device | |
| CN104208985B (en) | Fume desulphurization method and system | |
| CN109126392B (en) | Method for carrying out CO (carbon monoxide) in flue gas by adopting ionic liquid2Trapping device and process | |
| CN106311149B (en) | A kind of absorbent for natural gas decarbonization | |
| CN107261767A (en) | A kind of flue gas decarbonization agent and the method for flue gas decarbonization | |
| EP3078409B1 (en) | Acidic gas absorbing agent, method for removing acidic gas and apparatus for removing acidic gas | |
| CN102658000A (en) | Method and absorption solvent for removing sulfur dioxide from flue gas | |
| CN116139657A (en) | Amine nonaqueous absorbent for capturing carbon dioxide and application method thereof | |
| CN103170216A (en) | Alcohol amine type ion liquor-containing compound absorbent capable of capturing carbon dioxide | |
| CN105749728A (en) | Carbon dioxide trapping method and device thereof | |
| CN113318572A (en) | Carbon dioxide phase change absorbent organic alcohol regeneration regulation and control method and application thereof | |
| CN105214450A (en) | A kind of selective absorbing SO 2absorbent and absorb SO 2process | |
| CN1872679A (en) | Method for preparing liquid carbon dioxide in foodstuff level by using tail gas of cement kiln | |
| CN111672277A (en) | Physical and chemical composite CO2Absorbent system | |
| CN102675248B (en) | Method for removing carbon dioxide in recycle gas for synthesizing ethylene oxide/glycol | |
| CN204093274U (en) | Flue gas desulphurization system | |
| CN115999325A (en) | Ionic liquid phase change absorbent and application thereof | |
| CN106984152B (en) | It is a kind of for trapping the two-phase mixture of carbon dioxide | |
| CN107866133B (en) | Ammonia hydrocarbon silane series decarbonization solvent and decarbonization method | |
| CN109569242A (en) | Strengthen solution-air-liquid tri-phase system and absorbs CO2Method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |