CN1074040C - Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor - Google Patents
Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor Download PDFInfo
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- CN1074040C CN1074040C CN97117692A CN97117692A CN1074040C CN 1074040 C CN1074040 C CN 1074040C CN 97117692 A CN97117692 A CN 97117692A CN 97117692 A CN97117692 A CN 97117692A CN 1074040 C CN1074040 C CN 1074040C
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- carbonic acid
- acid gas
- gas
- absorption liquid
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 306
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 72
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 72
- 238000011084 recovery Methods 0.000 title claims description 77
- 238000000034 method Methods 0.000 title abstract description 16
- 239000007788 liquid Substances 0.000 claims abstract description 184
- 230000001172 regenerating effect Effects 0.000 claims abstract description 8
- 238000010521 absorption reaction Methods 0.000 claims description 260
- 235000011089 carbon dioxide Nutrition 0.000 claims description 158
- 230000008929 regeneration Effects 0.000 claims description 79
- 238000011069 regeneration method Methods 0.000 claims description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 37
- 238000005516 engineering process Methods 0.000 claims description 25
- 238000001816 cooling Methods 0.000 claims description 13
- 239000007864 aqueous solution Substances 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 2
- 239000002994 raw material Substances 0.000 abstract description 4
- 230000002745 absorbent Effects 0.000 abstract 2
- 239000002250 absorbent Substances 0.000 abstract 2
- 239000007789 gas Substances 0.000 description 76
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 48
- 239000003345 natural gas Substances 0.000 description 23
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 18
- 235000009508 confectionery Nutrition 0.000 description 15
- 230000015572 biosynthetic process Effects 0.000 description 12
- 238000003786 synthesis reaction Methods 0.000 description 12
- 238000007599 discharging Methods 0.000 description 11
- 150000001412 amines Chemical class 0.000 description 10
- 229910021529 ammonia Inorganic materials 0.000 description 9
- GLUUGHFHXGJENI-UHFFFAOYSA-N Piperazine Chemical compound C1CNCCN1 GLUUGHFHXGJENI-UHFFFAOYSA-N 0.000 description 8
- 241000196324 Embryophyta Species 0.000 description 6
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Chemical compound NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 6
- 239000004202 carbamide Substances 0.000 description 6
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- GSEJCLTVZPLZKY-UHFFFAOYSA-N Triethanolamine Chemical compound OCCN(CCO)CCO GSEJCLTVZPLZKY-UHFFFAOYSA-N 0.000 description 4
- -1 alkali metal salt Chemical class 0.000 description 4
- 238000006243 chemical reaction Methods 0.000 description 4
- 230000014509 gene expression Effects 0.000 description 4
- 150000002431 hydrogen Chemical class 0.000 description 4
- 239000003921 oil Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 229910002091 carbon monoxide Inorganic materials 0.000 description 3
- BVKZGUZCCUSVTD-UHFFFAOYSA-N carbonic acid Chemical compound OC(O)=O BVKZGUZCCUSVTD-UHFFFAOYSA-N 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 150000003512 tertiary amines Chemical class 0.000 description 3
- UXFQFBNBSPQBJW-UHFFFAOYSA-N 2-amino-2-methylpropane-1,3-diol Chemical compound OCC(N)(C)CO UXFQFBNBSPQBJW-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 229910052783 alkali metal Inorganic materials 0.000 description 2
- 150000001413 amino acids Chemical class 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000007701 flash-distillation Methods 0.000 description 2
- 239000008246 gaseous mixture Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 150000003053 piperidines Chemical class 0.000 description 2
- 150000003141 primary amines Chemical class 0.000 description 2
- 150000003335 secondary amines Chemical class 0.000 description 2
- 229960004418 trolamine Drugs 0.000 description 2
- LDXJRKWFNNFDSA-UHFFFAOYSA-N 2-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)-1-[4-[2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidin-5-yl]piperazin-1-yl]ethanone Chemical compound C1CN(CC2=NNN=C21)CC(=O)N3CCN(CC3)C4=CN=C(N=C4)NCC5=CC(=CC=C5)OC(F)(F)F LDXJRKWFNNFDSA-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000002202 Polyethylene glycol Substances 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 238000013459 approach Methods 0.000 description 1
- PPBAJDRXASKAGH-UHFFFAOYSA-N azane;urea Chemical compound N.NC(N)=O PPBAJDRXASKAGH-UHFFFAOYSA-N 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- JYYOBHFYCIDXHH-UHFFFAOYSA-N carbonic acid;hydrate Chemical compound O.OC(O)=O JYYOBHFYCIDXHH-UHFFFAOYSA-N 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- BWHMMNNQKKPAPP-UHFFFAOYSA-L potassium carbonate Substances [K+].[K+].[O-]C([O-])=O BWHMMNNQKKPAPP-UHFFFAOYSA-L 0.000 description 1
- 235000015320 potassium carbonate Nutrition 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- NQRYJNQNLNOLGT-UHFFFAOYSA-N tetrahydropyridine hydrochloride Natural products C1CCNCC1 NQRYJNQNLNOLGT-UHFFFAOYSA-N 0.000 description 1
- 239000004408 titanium dioxide Substances 0.000 description 1
Classifications
-
- 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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- Carbon And Carbon Compounds (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
To provide a method for removing carbon dioxide in a high-pressure raw material gas under a high pressure is removed A raw material gas l containing carbon dioxide is fed to a decarbonator column and brought into contact with a liquid of a partial regenerating absorbent in a lower absorbing section to partially absorb the carbon dioxide. The resultant gas is then brought into contact with a liquid of a regenerating absorbentin an upper absorbing section to absorb the carbon dioxide until a minor concentration thereof attains. The carbon dioxide is further recovered from the regenerating absorbent under a high pressure.Also claimed the device above.
Description
The present invention relates to handle technology and device, fully remove high-content carbonic acid gas (CO in the unstripped gas by this technology from the high pressure feedstock gas of high-pressure natural gas and various synthesis gass with carbon dioxide absorption liquid
2) and the acquisition carbon dioxide content is 10～10, the processed gas of 000ppm, in addition, this technology also can be used for reclaiming the high-pressure carbon dioxide in the absorption liquid.
Usually the carbonic acid gas that contains a large amount of (for example 10～20%) in the high-pressure natural gas.When this Sweet natural gas was transformed into natural gas liquids (calling LNG in the following text), carbonic acid gas can become dry ice owing to cooling, and this solid matter can cause problems such as for example device obstruction.Therefore, its carbon dioxide content must be reduced to 50ppm or still less.
And, under the situation of ammonia-urea synthesis, partial oxidation that will be by Sweet natural gas, raw gasline or similar substance or steam reformation obtain the gaseous mixture be made up of hydrogen, carbon monoxide, carbonic acid gas etc., this gaseous mixture will carry out the CO conversion reaction, make carbon monoxide be transformed into carbonic acid gas, after branch is left away carbonic acid gas, be used for the synthetic of ammonia then as unstripped gas.On the other hand, isolated carbonic acid gas is pressurized to 100～200 normal atmosphere, and reacts with ammonia and to make urea.Therefore, the content of carbonic acid gas that is used for the synthetic unstripped gas of ammonia generally must be reduced to the order of magnitude of 500ppm.
In addition, be used at hydrogen under the situation of chemosynthesis, its carbon dioxide content be reduced to tens to several thousand ppm according to the difference of purposes.
For the carbonic acid gas that will separate is used for third stage recovery of oil (EOR), liquid carbon dioxide production or urea synthesis or it is stored in underground reservoir (as the measure of taking precautions against global temperature rise), its pressure must be increased to tens to a hundreds of normal atmosphere.
Therefore, preferably from being to remove carbonic acid gas the highly compressed unstripped gas originally, till the content of carbonic acid gas is extremely low, and under high pressure conditions with the carbon dioxide recovery that removes.But, the methods availalbe that can achieve the above object is not arranged in the prior art as yet.
In the prior art, adopt following technology to remove carbonic acid gas, make it reach very low content (for example order of magnitude of 100ppm).At first, a kind of gas is sent into a kind of bottom of decarbonation tower, simultaneously a kind of carbon dioxide absorption liquid is sent on this decarbonation tower, like this, gas contacts with absorption liquid generation solution-air, carbonic acid gas is absorbed and removes.Then, the absorption liquid (calling the absorption liquid that has absorbed carbonic acid gas in the following text) that will contain the carbonic acid gas of suction is sent in the recovery tower, by steam stripping carbonic acid gas is discharged and to obtain the absorption liquid of regenerating, more this regeneration absorption liquid is delivered in the decarbonation tower.
Another example that removes carbonic acid gas and reclaim the method for the carbonic acid gas remove from high-pressure natural gas under high pressure conditions is the technology that removes carbonic acid gas in batches.
But ordinary process and device thereof that above-mentioned abundant removal and high pressure reclaim carbonic acid gas have following problem:
(1) in the technology of above-mentioned use carbon dioxide absorption liquid, can reduce regeneration in the absorption liquid carbon dioxide content and remove carbonic acid gas, reach very low degree up to carbon dioxide content.But,, therefore be difficult to reclaim carbonic acid gas with sufficiently high pressure because this absorption liquid is regenerated by step-down.So, must by pneumatic plant with the carbonic acid gas that reclaims once more supercharging can use.
(2) in the technology of above-mentioned batch de removing carbon dioxide, still contain 1～5% carbonic acid gas through handling in the Sweet natural gas of removing carbonic acid gas.
The present invention is that the situation according to above-mentioned prior art proposes, its purpose is, proposes a kind ofly to remove high-load carbonic acid gas until reaching very low carbon dioxide content and reclaim the technology of high-pressure carbon dioxide from absorption liquid from high-pressure natural gas and various synthesis gas by means of carbon dioxide absorption liquid.
The inventor is by deep discovering, by implementing series of steps, can from unstripped gas, fully remove carbonic acid gas, simultaneously, can under high pressure conditions, reclaim carbonic acid gas, described each work step is: handle unstripped gas with a kind of carbon dioxide absorption liquid, carbonic acid gas is absorbed by liquid absorption; The absorption liquid that has absorbed carbonic acid gas is heated, make its release of carbon dioxide under high pressure conditions, and absorption liquid is partly regenerated; The partial regeneration absorption liquid of a part is turned back in the absorption work step; Remaining partial regeneration absorption liquid is further regenerated, and the further regenerated absorption liquid that will draw turns back in the absorption work step.The present invention finishes according to above-mentioned discovery just.
In other words, the present invention proposes a kind of fully remove and high pressure reclaims the technology of carbonic acid gas from high pressure feedstock gas, and this technology comprises following work step: will contain 2～50% carbonic acid gas and its pressure (absolute pressure) is not less than 2kg/cm
2High pressure feed send into entirely and have a following absorption portion and one and go up in the decarbonation tower of absorption portion, this unstripped gas contacts with the absorption liquid generation solution-air of partial regeneration in above-mentioned following absorption portion, carbonic acid gas is partly absorbed, then, absorption portion contacts with regeneration absorption liquid generation solution-air on above-mentioned again, carbonic acid gas is absorbed and removes, up to reaching very low carbon dioxide content; The processed gas that will contain the carbonic acid gas of 10～10000ppm is discharged outside this device; To the absorption that in the decarbonation tower, produces the absorption liquid of carbonic acid gas heat, and enter in the high pressure recovery tower, be 2kg/cm at pressure
2(absolute pressure) discharges partial CO 2 to the situation of feedstock gas pressures, obtain a kind of absorption liquid of partial regeneration, and the part of this partial regeneration absorption liquid is admitted to above-mentioned following absorption portion; Remaining partial regeneration absorption liquid is sent in a kind of low pressure recovery tower, discharged carbonic acid gas and the absorption liquid that obtains regenerating, and this regeneration absorption liquid is sent into above-mentioned last absorption portion; By cooling, and it is separated with all moisture of carrying secretly and reclaim the high pressure titanium dioxide the carbonic acid gas that in the high pressure recovery tower, under pressure, discharges; By cooling, and it is separated with all moisture of carrying secretly and reclaim carbonic acid gas the carbonic acid gas that in the low pressure recovery tower, discharges; The present invention also proposes to implement the device of above-mentioned technology.
The present invention can remove the carbonic acid gas of its high density from high-pressure natural gas and various synthesis gas, be not higher than the low-level of 1000ppm until reaching carbon dioxide content, and can reclaim high-pressure carbon dioxide.As a result, compression power required when using carbonic acid gas subsequently can be saved, and the size of equipment can be reduced.
Describe the present invention in detail below in conjunction with accompanying drawing, in the accompanying drawing:
Fig. 1 is that explanation is fully removed according to the present invention and high pressure reclaims the schema of the technology of the carbonic acid gas in the high pressure feedstock gas;
Fig. 2 is the schema that abundant removal of explanation and high pressure reclaim the ordinary process of the carbonic acid gas in the high pressure feedstock gas.
The unstripped gas of handling according to the present invention be from have high pressure and contain the Sweet natural gas of carbonic acid gas and various synthesis gas select.This class gas for example have raw gasline, Sweet natural gas, heavy oil, coke etc. are carried out that steam transforms or partial oxidation obtains and be to make carbon monoxide change carbonic acid gas into through the CO conversion reaction and the gas that contains carbonic acid gas.These gases that the present invention uses are preferably handled through desulfurization and are made the concentration of its sulfide be not more than 100ppm.
Though the pressure to above-mentioned raw materials gas is not done special restriction, its pressure is to be not less than 2kg/cm
2Be advisable, preferably be not less than 10kg/cm
2, the upper limit of pressure value is not made special regulation, but is generally 200～300kg/cm
2In like manner, though the carbon dioxide content in the unstripped gas is not done special restriction, its content is advisable with 1～50% (volume), preferably 10-30% (volume).
The pressure of handling the purified gases that obtains behind the above-mentioned raw materials gas according to the present invention is identical with unstripped gas basically, and its carbon dioxide content is 1～10000ppm, is preferably 10～1000ppm.
The used carbon dioxide absorption liquid of the present invention is a kind of aqueous solution that contains the absorption agent of selecting from various basic cpds and composition thereof.
Therefore, preferably select absorption liquid for use with following receptivity.
Through contacting with the solution-air of unstripped gas and after the absorbing carbon dioxide, in a kind of high pressure recovery tower, this carbon dioxide absorption liquid being carried out partial regeneration,, and then be recycled to the absorption work step of next stage so that make it discharge some carbonic acid gas.Therefore, its receptivity must be such: when the pressure component of carbonic acid gas is 2kg/cm
2Or when higher, the difference of the saturated carbon dioxide absorption value between absorption temperature (for example 40 ℃) and the partial regeneration temperature (for example 120 ℃) is not less than a particular value and (for example, is not less than every m
3Absorption liquid 30Nm
3CO
2, preferably be not less than every m
3Absorption liquid 40Nm
3CO
2).
Usually, if stipulated the temperature and the pressure component of carbonic acid gas, then according to the saturated carbon dioxide absorption curve of above-mentioned absorption liquid, its saturated carbon dioxide absorption value is a fixed value, and is almost irrelevant with the kind of carbonated gas.
In the present invention, as shown in the following embodiment that will illustrate, carbonic acid gas is to be 30kg/cm from pressure
2Or in the higher Sweet natural gas by removing in the absorption liquid that its is sucked partial regeneration, the resulting absorption liquid that contains carbonic acid gas is sent to a partial regeneration work step, in this work step, under the situation that does not reduce pressure, this absorption liquid is heated, to discharge carbonic acid gas.Therefore, preferably adopt in absorbing work step and depress absorbing carbon dioxide at low temperature and low the branch easily, and in the regeneration work step absorption liquid of release of carbon dioxide under high temperature and high partial pressures easily.
Therefore, preferably adopt the good absorption liquid that contains amine of physical absorption liquid or physical absorption performance as above-mentioned carbon dioxide absorption liquid.
Above-mentioned physical absorption liquid comprises methyl alcohol and Polyethylene glycol dimethyl ether.
As for amine with strong physical absorption performance, an alkali metal salt of specifically available all kinds of amine, Amino acid and Amino acid.In case of necessity, can add amine with strong chemical absorption performance, alkaline carbonate etc. therein.
Representative instance with amine of strong physical absorption performance is a tertiary amine, and its principal reaction is as follows:
Therefore, tertiary amine can be by means of regeneration easily such as flicker methods.On the other hand, primary amine and secondary amine are the base substances with strong chemical absorption performance, and its principal reaction is as follows:
Above-mentioned regeneration requires decomposition heat.But, even under the situation of equation (2), have high sterically hindered amine and also form easily and a kind ofly have the characteristic key that more approaches ionic linkage than chemical bond, thereby further carry out following reaction:
So the amine with strong physical absorption performance not only is meant tertiary amine, and comprise primary amine and secondary amine.
Therefore, the preferred example of amine is a bulky amine, and best bulky amine has N methyldiethanol amine (MDEA), trolamine (TEA), dimethylamino-1, ammediol (DMAPD), diethylin-1, ammediol (DEAPD).
The available an alkali metal salt is a salt of wormwood.
In addition, can in above-mentioned carbon dioxide absorption liquid, for example add carbon dioxide absorption promotor: piperazine, substituted-piperazinyl, piperidines and substituted piperidine.
Different according to the kind of absorption agent and working conditions, carbon dioxide absorption liquid can be that to contain concentration of absorbing be 20～80% the aqueous solution.
In case of necessity, can in carbon dioxide absorption liquid, add a kind of solvent as N-crassitude or tetramethylene sulfone.
The pressure of the high-pressure carbon dioxide that reclaims from carbon dioxide absorption liquid is not less than 2kg/cm
2, this pressure preferably is in from 10kg/cm
2To the scope of the pressure that is substantially equal to unstripped gas, although the size of this pressure depends on the kind of unstripped gas and the purposes of carbonic acid gas.
Therefore, the high pressure recovery tower carries out operation under above-mentioned pressure, it will absorb liquid heat to 90 °～150 ℃ (being preferably 100 °～140 ℃) of carbonic acid gas, so that partly discharge water outlet and carbonic acid gas from aforesaid liquid, thereby carbon dioxide absorption liquid partly be regenerated.
The absorption liquid of partial regeneration for example is recirculated into that a reboiler heats it, makes it not to be higher than 2kg/cm in operating pressure
2For (being preferably 0.5～1.0kg/cm
2) and fluid temperature be further to regenerate under the condition of 100～150 ℃ (being preferably 110～140 ℃).
Send into the carbon dioxide content of regeneration level, the regeneration level of regeneration absorption liquid of sending into absorption portion on this tower and kind, the carbon dioxide content in the unstripped gas, pressure and other conditions that their ratio of sending into depends on absorption liquid, processed gas of absorption liquid of partial regeneration of following absorption portion on decarbonation absorption tower and flow velocity, concentration, pressure and other conditions of the high-pressure carbon dioxide that reclaims.For example, the degree of partial regeneration refers to that every mole of absorption liquid contains 0.05～0.3 mole CO
2, and regeneration level refers to that every mole of absorption liquid contains 0.01～0.1 mole CO
2, the shared ratio of partial regeneration absorption liquid of sending into the decarbonation absorption tower is 30～95%.
Specify method of the present invention referring to Fig. 1 below.
Unstripped gas 1 is sent into the bottom on decarbonation absorption tower 2.Following absorption portion 3 at this tower 2, solution-air takes place with partial regeneration absorption liquid 21 and contacts in unstripped gas 1, thereby making carbonic acid gas partly be absorbed liquid 21 absorbs, then, absorption portion 4 on tower 2, solution-airs take place with regeneration absorption liquid 22 and contact in unstripped gas 1, and carbonic acid gas further is absorbed, till reaching very low carbon dioxide content.Resulting gas is used as outside the processed gas 17 discharge systems.
In said process, regeneration absorption liquid 22 is downward through absorption portion 4, with unstripped gas 1 solution-air taking place simultaneously contacts, and mixing with partial regeneration absorption liquid 21 in the absorption portion 3 down, this blended absorption liquid is downward through down absorption portion 3, meanwhile with unstripped gas 1 solution-air taking place and contact, and discharges from the bottom on decarbonation absorption tower 2.
In case of necessity, the effusive absorption liquid 20 that has absorbed carbonic acid gas from the bottom on decarbonation absorption tower 2, by in heat exchanger 5, carrying out heat exchange or in heat exchanger 6 with partial regeneration absorption liquid 21, carry out heat exchange and heat with regeneration absorption liquid 22, and further be heated to preset temperature by well heater 7, send into high pressure recovery tower 8 then.
The absorption liquid 21 of resulting partial regeneration is discharged from the bottom of high pressure recovery tower 8, and with its part deliver to heat exchanger 5 internal cooling it, if necessary, heat exchanger 15 in, further cool off again, send into absorption portion 3 under the decarbonation absorption tower then.
The water of discharging on the high pressure recovery tower 8 and the mixture of carbonic acid gas enter gas-liquid separator 10 then at water cooler 9 internal cooling, and it is separated into water and high-pressure carbon dioxide 18.Water is back on the high pressure recovery tower 8 again.In case of necessity, a part of water can be delivered to the top on decarbonation absorption tower 2, perhaps be used to make regeneration of absorption solution, perhaps, send into low pressure recovery tower 11 as recirculated water.
The absorption liquid 21 of remaining partial regeneration enters low pressure recovery tower 11, and this recovery tower 11 is lower than 2kg/cm in absolute pressure
2Under the condition of the pressure that reduces, work in other words, and a reboiler 12 is housed in order to heat the liquid of its bottom.So, from the absorption liquid of partial regeneration, discharge water outlet and carbonic acid gas, thereby reach regeneration further.The regeneration level that has absorbed the absorption liquid of carbonic acid gas depends on Heating temperature, the residence time and the operating pressure when handling this absorption liquid in the low pressure recovery tower 11.
Regeneration absorption liquid 22 is from the discharge of the bottom of low pressure recovery tower 11, and wherein a part is delivered to heat exchanger 6 and cooled off, and in the time of if necessary, further cools off at heat exchanger 16 again, delivers to the last absorption portion 4 on decarbonation absorption tower then.
The water of discharging on the low pressure recovery tower 11 and the mixture of carbonic acid gas are at water cooler 13 internal cooling, and enter gas-liquid separator 14, it is separated into water and low pressure CO 2 19, wherein, water is back to the top of low pressure recovery tower 11, in case of necessity, a part of water can be delivered to the top on decarbonation absorption tower 2, perhaps be used for the regeneration of absorption liquid, perhaps enter in the high pressure recovery tower 8 as recirculated water.
Decarbonation absorption tower and several recovery tower can be tray column or packed tower, and solution-air contacts and the pressure-losses is little as long as they can carry out effectively.Therefore, can use for example material of wet wall type of any common compaction material.
If the ratio of the high-pressure carbon dioxide that reclaims according to the present invention increases, economic benefit is just bigger.The present invention can under high pressure reclaim and be no less than 50% carbonic acid gas, is more than 70% preferably, and best reaches more than 90%.
Therefore, the present invention can under high pressure reclaim carbonic acid gas, thus remarkable save compressed power, and reduce the size of equipment.
Further specify the present invention below by several examples, but should not regard these examples as limitation of the scope of the invention.
Example 1
This example relates to the application of technology shown in Fig. 1 schema, wherein, adopt the aqueous solution of the piperazine of the MDEA and 4% (weight) that contains 45% (weight) to handle the synthetic unstripped gas that is used for ammonia that obtains by gas renormalizing as the absorption liquid of absorbing carbonic acid gas.
Is 34kgG/cm with a kind of unstripped gas that contains the carbonic acid gas of hydrogen, nitrogen, hydrocarbons and 19% (volume) at pressure
2, temperature is that 45 ℃, flow velocity are 292000Nm
3Send into the bottom on decarbonation absorption tower under the condition of/h.
To following absorption portion and the 1716m of the unstripped gas that rises on above-mentioned absorption tower 2
3The absorption liquid generation solution-air contact of the partial regeneration of/h.So in following absorption portion, carbonic acid gas partly is removed from unstripped gas, the carbon dioxide content in unstripped gas is reduced to about 2% (volume).And, unstripped gas in last absorption portion with 163m
3The regeneration absorption liquid generation solution-air contact of/h.Then, discharging carbon dioxide content from the top of decarbonation tower is that 490ppm, temperature are that 39 ℃, pressure are 32kgG/cm
2Refining unstripped gas.
Absorbed the absorption liquid of carbonic acid gas, its temperature is 55 ℃, and its carbon dioxide content approximately is every m
3Absorption liquid is 78Nm
3This absorption liquid is heated to 120 ℃ through after the heat exchange, sends into the high pressure recovery tower then, here partly regenerates.Carbonic acid gas that discharges during partial regeneration and water enter water cooler with a spot of absorption liquid and cool off, and enter then in the gas-liquid separator, isolate carbonic acid gas.Through overcooling and isolating carbonic acid gas, about 40 ℃ of its temperature, pressure is 10kgG/cm
2, flow velocity is 49800Nm
3/ h.Above-mentioned carbonic acid gas is forced into 190kg/cm by the pneumatic plant (not shown)
2, can be used for urea synthesis.
On the other hand, the absorption liquid of the partial regeneration of discharging from high pressure recovery tower bottom, its temperature is 100 ℃, every m
3Contain carbonic acid gas (CO in the absorption liquid
2) about 43Nm
3Part in the absorption liquid of this partial regeneration is carried out heat exchange with the absorption liquid that has absorbed carbonic acid gas, further is cooled to 38 ℃, sends into the following absorption portion on absorption tower then.
Residue (163Nm
3/ h) partial regeneration absorption liquid is admitted to the low pressure recovery tower, here regenerate, and its pressure is reduced to 0.85kg/cm
2, simultaneously, carbonic acid gas and water are discharged from the top of recovery tower.Tower bottom liquid is heated to about 110 ℃ by the reboiler that is installed in low pressure recovery tower bottom, and is back in the low pressure recovery tower.So, obtained every m
3Absorption liquid only contains 1.2Nm
3Carbonic acid gas (CO
2) the regeneration absorption liquid.Carbonic acid gas that is discharged and water are cooled off in water cooler with a small amount of absorption liquid, enter gas-liquid separator then, and carbon dioxide separation is come out.Through overcooling and isolating carbonic acid gas, its temperature is about 40 ℃, and pressure is 0.35kgG/cm
2, flow velocity is 5700Nm
3/ h.
The temperature of the regeneration absorption liquid of discharging from low pressure recovery tower bottom is about 110 ℃, this liquid is sent to the last absorption portion on absorption tower, in this course, the absorption liquid of temperature is the lower absorption of 110 ℃ regeneration absorption liquid and temperature carbonic acid gas carries out heat exchange, makes its temperature further be reduced to 38 ℃.
In whole carbonic acid gas of Hui Shouing, have 90% in the high pressure recovery tower, to reclaim as stated above, 10% in the low pressure recovery tower, reclaim in addition.
Therefore, the carbon dioxide content that is used for the synthetic unstripped gas of ammonia can be reduced to and satisfy the desired level of ammonia synthesis technology.And the carbonic acid gas of recovery has high pressure, thus desired compression power can save urea synthesis the time, and can reduce the size of equipment.
Example 2
This example relates to the application of technology shown in Figure 1, it is characterized in that, adopt the aqueous solution of the piperazine of a kind of MDEA and 4% (weight) that contains 45% (weight) to handle the synthetic unstripped gas that obtains by the reformation Sweet natural gas as the absorption liquid of absorbing carbonic acid gas as ammonia.
The unstripped gas 1 that will contain hydrogen, nitrogen, hydrocarbon polymer and 19% (volume) carbonic acid gas is 34kgG/cm at pressure
2, temperature is that 45 ℃ and flow velocity are 292000Nm
3Send into the bottom of carbon dioxide absorption tower 2 under the condition of/h.
In the following absorption portion 3 on absorption tower 2, to the absorption liquid 21 (1716ms of the unstripped gas 1 that rises with partial regeneration
3/ h) the solution-air contact takes place, so in following absorption portion 3, the carbonic acid gas in the unstripped gas 1 is partly absorbed, and is reduced to about 2% (volume) up to its carbon dioxide content.And, in last absorption portion 4, unstripped gas 1 and regeneration absorption liquid 22 (200m
3/ h) solution-air taking place contacts.To discharge carbon dioxide content be that 50ppm, temperature are that 39 ℃, pressure are 33kg/cm at 2 top from the absorption tower
2Processed gas.
Absorbed the absorption liquid 20 of carbonic acid gas, every m
3Contain the 78Nm that has an appointment in the absorption liquid
3Carbonic acid gas (CO
2), this absorption liquid 20 is through heat exchange, temperature rises to 120 ℃, send into then in the high pressure recovery tower 8, here partly regenerated, carbonic acid gas that is discharged and water enter water cooler 9 internal cooling with a spot of absorption liquid, enter gas-liquid separator 10 then, and carbonic acid gas 18 is separated.Through overcooling and isolating carbonic acid gas 18, it is 33kgG/cm that its temperature is about 40 ℃, pressure
2, flow velocity is 49640Nm
3/ h.Above-mentioned carbonic acid gas 18 is pressurized to 150kgG/cm by the pneumatic plant (not shown)
2, be used further to urea synthesis.
On the other hand, the absorption liquid 21 of the partial regeneration of discharging from high pressure recovery tower 8 bottoms, its temperature is 100 ℃, carbon dioxide content is every m
3Absorption liquid contains 29.2Nm
3CO
2Part in the absorption liquid 21 of this partial regeneration is carried out heat exchange with the absorption liquid 20 that has absorbed carbonic acid gas, and its temperature further is reduced to 38 ℃, sends into the following absorption portion 3 on absorption tower 2 then.
All the other (200m
3/ h) the absorption liquid 21 of partial regeneration enters low pressure recovery tower 11, and here, its pressure is reduced to 0.85kgG/cm
2, and be reproduced, carbonic acid gas of being separated out and water are then discharged from the top of this tower.Reboiler 12 by being arranged on low pressure recovery tower 11 bottoms is heated to about 110 ℃ with the solution of tower 11 bottoms, is back in the low pressure recovery tower 11 again.So, obtained every m
3Contain 5Nm in the solution
3Carbonic acid gas (CO
2) regeneration absorption liquid 22.Carbonic acid gas that is discharged and water enter cooling in the water cooler 13 with a small amount of absorption liquid, and enter gas-liquid separator 14, isolate carbonic acid gas 19.Temperature through overcooling and isolating carbonic acid gas 19 is about 40 ℃, and pressure is 0.35kgG/cm
2, flow velocity is 5500Nm
3/ h.
The regenerated absorption liquid 22 of discharging from low pressure recovery tower 11 bottoms, its temperature is about 110 ℃, and it is admitted to the last absorption portion 4 on absorption tower 2.In this process, the absorption liquid 20 of temperature is the lower absorption of 110 ℃ regeneration absorption liquid 22 and temperature carbonic acid gas carries out heat exchange, makes its temperature be reduced to 38 ℃.
In whole carbonic acid gas of Hui Shouing, have 90% in high pressure recovery tower 8, to reclaim in a manner described, the 10%th, in low pressure recovery tower 11, reclaim.
Therefore, the carbon dioxide content that is used for the synthetic unstripped gas of ammonia has been reduced to the desired level of synthesis technique that can satisfy ammonia.And, the last carbon oxide pressure height that is reclaimed, thus the required compression power of urea synthesis can be saved, and equipment size is reduced.
Example 3
This example relates to the application of technology shown in Fig. 1 schema, it is characterized in that, handles Sweet natural gas with a kind of aqueous solution that contains the MDEA of 45% (weight) as the absorption liquid of absorbing carbonic acid gas.
The Sweet natural gas 1 that will contain 26% (volume) carbonic acid gas is 58kgG/cm at pressure
2And temperature is to send into the following absorption portion on absorption tower 2 under 25 ℃ the condition.
The following absorption portion 3 on absorption tower 2 is packed into for example a kind of wet wall type and directly fills material, can carry out effective solution-air with the absorption liquid 21 of partial regeneration to the Sweet natural gas 1 that rises and contact.So, in following absorption portion 3, can from Sweet natural gas 1, partly absorb carbonic acid gas, content up to its carbonic acid gas is reduced to about 3% (volume), in addition, have similar wet wall type packed bed in the absorption portion 4, the Sweet natural gas 1 of rising carries out effective solution-air with regenerated absorption liquid 22 again and contacts.Processed gas 17 is discharged at 2 top from the absorption tower, and the gas concentration lwevel of this processed gas 17 is 50ppm, and temperature is 50 ℃, and pressure is 58kgG/cm
2
The liquid 20 that has absorbed carbonic acid gas is heated to 130 ℃ through heat exchange, enters high pressure recovery tower 8 then, partly regenerates.
In high pressure recovery tower 8, the carbonic acid gas that discharges in above-mentioned heat-processed is separated from absorption liquid 20, obtains the absorption liquid 21 of partial regeneration.Therefore, needn't use for example reboiler 12 of well heater, still, also available in case of necessity this well heater.Carbonic acid gas that discharges and water cool off in water cooler 9 with a small amount of absorption liquid, then enter gas-liquid separator 10, isolate carbonic acid gas 18, are about 40 ℃ through the temperature of overcooling and isolating carbonic acid gas, and pressure is 55kgG/cm
2, almost the pressure with the Sweet natural gas 1 that is used as unstripped gas is suitable.Above-mentioned carbonic acid gas 18 can be forced into 150kgG/cm by the pneumatic plant (not shown)
2, be used for uncle's recovery of oil or be stored in underground.
On the other hand, the part of discharging from high pressure recovery tower 8 bottoms is received absorption liquid 21 again, its temperature is about 130 ℃, wherein there is a predetermined part to be admitted to the following absorption portion 3 on absorption tower 2, in this process, the absorption that partial regeneration absorption liquid 21 and temperature are lower the absorption liquid 20 of carbonic acid gas carry out heat exchange, further be cooled to temperature required.
Remaining partial regeneration absorption liquid 21 enters in the low pressure recovery tower 11, makes its pressure be reduced to 0.85kgG/cm
2, and obtaining regeneration, the carbonic acid gas 19 and the water of being separated out are discharged from the top of tower.The liquid of tower bottom is heated to about 130 ℃ by the reboiler 12 that is arranged on low pressure recovery tower 11 bottoms, and is recirculated in the low pressure recovery tower 11.So, obtained containing the regeneration absorption liquid of MDEA of 45% (weight) of having an appointment.Carbonic acid gas that discharges and water at water cooler 13 internal cooling, enter gas-liquid separator 14 with a small amount of absorption liquid then, isolate carbonic acid gas 19, are about 40 ℃ through the temperature of overcooling and isolating carbonic acid gas 19, and pressure is 0.35kgG/cm
2, as industrial gasses.
The temperature of the regeneration absorption liquid 22 that discharge 11 bottoms, many low pressure absorption towers is about 130 ℃, is admitted to the last absorption portion 4 on absorption tower 2.In this process, the absorption liquid 20 of temperature is the lower absorption of 130 ℃ regeneration absorption liquid 22 and temperature carbonic acid gas carries out heat exchange, further is cooled to temperature required.
In whole carbonic acid gas of Hui Shouing, have 85% in a manner described in 8 recovery of high pressure recovery tower, the 15%th, reclaim at the low pressure recovery tower.
Therefore, the carbon dioxide content in the processed gas 17 is lowered to the degree that can not produce solid-state dry ice in making natural gas liquids (LNG) process.And the pressure height of the carbonic acid gas of recovery is used for the required compression power of liquid carbon dioxide of uncle's recovery of oil so can save to produce, and can reduces the size of equipment.
Example 4
This example relates to the application of technology shown in Fig. 1 schema, it is characterized in that employing contains the trolamine (TEA) of 40% (weight) and the aqueous solution of 4% (weight) piperazine (reaction promotor) is handled the unstripped gas that is used for chemosynthesis that gas renormalizing obtains as the absorption liquid of removing carbonic acid gas.
At pressure is 33kgG/cm
2With temperature be the following absorption portion that the unstripped gas 1 that will contain the carbonic acid gas of methane, 19 (mole) % of hydrogen, 12 (mole) % of 68 (mole) % and other rare gas elementes under 60 ℃ the condition is sent into absorption tower 2.
In the following absorption portion 3 on absorption tower 2, with the absorption liquid 21 of partial regeneration solution-air taking place to the unstripped gas that rises contacts, so, in following absorption portion 3, partly remove carbonic acid gas from unstripped gas 1, be reduced to about 1% (volume) until its carbon dioxide content.And, with regeneration absorption liquid 22 solution-air taking place in last absorption portion 4 to the unstripped gas 1 that rises contacts.To discharge carbon dioxide content be 200ppm on 2 top from the absorption tower, and temperature is that 40 ℃, pressure are 32kgG/cm
2Processed gas 17.
The absorption liquid 20 that has absorbed carbonic acid gas is heated to 120 ℃ through heat exchanges, sends into then in the high pressure recovery tower 8,, about 60% of the carbonic acid gas that contains in the absorption liquid 20 that has absorbed carbonic acid gas is discharged here.Carbonic acid gas that discharges and water at water cooler 9 internal cooling, enter gas-liquid separator 10 with a small amount of absorption liquid then, isolate carbonic acid gas 18.Temperature through overcooling and isolating carbonic acid gas 18 is about 40 ℃, and pressure is 9kgG/cm
2This carbonic acid gas 18 is forced into 100kgG/cm by the pneumatic plant (not shown)
2, be used to produce liquid carbon dioxide.
On the other hand, the partial regeneration absorption liquid 21 of discharging from high pressure recovery tower 8 bottoms carries out heat exchange and further cooling, the following absorption portion 3 that enters absorption tower 2 then with the absorption liquid 20 that has absorbed carbonic acid gas.
The partial regeneration absorption liquid 21 of all the other (about 10%) enters low pressure recovery tower 11, and here, its pressure is reduced to 0.85kgG/cm
2, and obtaining regeneration, carbonic acid gas 19 of being separated out and water are discharged from the top of low pressure recovery tower 11.The liquid of tower bottom is heated to about 130 ℃ by being arranged on the reboiler 12 that low pressure reclaims 11 bottoms, and then to flowing into low pressure recovery tower 11.From resulting regeneration absorption liquid 22, the absorption of beginning contain carbonic acid gas existing about 98% in the absorption liquid 20 of carbonic acid gas and be released.Temperature by gas-liquid separator 14 isolated carbonic acid gas 19 is about 40 ℃, and pressure is 0.35kgG/cm
2This carbonic acid gas 19 is pressurized to 100kgG/cm by pneumatic plant again
2, be used to produce liquid carbonic acid gas then.
The temperature of the regeneration absorption liquid 22 of discharging from low pressure recovery tower 11 bottoms is about 130 ℃, is admitted to the last absorption portion 4 on absorption tower 2.In this process, the absorption that regeneration absorption liquid 22 and temperature are lower the absorption liquid 20 of carbonic acid gas carry out heat exchange, and with cold be that water further cools off it.
In whole carbonic acid gas of Hui Shouing, have 92% in high pressure recovery tower 8, to reclaim in a manner mentioned above, the 8%th, in low pressure recovery tower 11, reclaim.
So the carbon dioxide content that is used for the unstripped gas of chemosynthesis is lowered to is enough to supply with the degree of each work step subsequently.And the ratio height of the high-pressure carbon dioxide of recovery is produced the required compression power of liquid carbon dioxide so can save, and reduces the size of equipment.
Comparative example 1
Adopt high-pressure natural gas and the absorption liquid identical to handle Sweet natural gas, its carbon dioxide content is reduced to 50ppm by common technology (see figure 2) with embodiment 3, and the recovery carbonic acid gas.
The absorption liquid 120 that has absorbed carbonic acid gas is sent into first flash drum 123, at 3.8kgG/cm
2Pressure under carry out flash distillation, a part of carbonic acid gas in the absorption liquid 120 is discharged, and obtain the absorption liquid of partial regeneration, after the absorption liquid of this partial regeneration further heats in well heater 107, send into second flash drum 124, once more flash distillation and the absorption liquid 122 that obtains regenerating.
The pressure of the carbonic acid gas that obtains in first flash drum 123 is 3.8kgG/cm
2, the pressure (55kgG/cm of the carbonic acid gas that this pressure obtains far below above-mentioned example 3
2), therefore, in order to produce the liquid carbon dioxide that is used for uncle's recovery of oil, from compression power and equipment aspect, the technology of this comparative example 1 has more shortcoming than the technology of example 1.In this ordinary process, Sweet natural gas 101 is sent into absorption tower 102, and discharges processed gas 117 from this tower.Label 109 expressions are arranged on the groove top water cooler between second flash drum 124 and the separator tank 110.The carbonic acid gas that label 118 expression is discharged from separator tank 110, label 132 expressions from a flash drum 123 carbonic acid gas of discharging, a kind of water cooler of label 116 expressions.
Claims (4)
1. from high pressure feedstock gas, remove the also technology of high pressure recovery carbonic acid gas for one kind, the carbon dioxide absorption liquid that adopts contains the aqueous solution of the absorption agent of selecting from basic cpd and composition thereof, described technology comprises following steps: the absolute pressure that will contain carbonic acid gas is not less than 2kg/cm
2High pressure feedstock gas send in the decarbonation absorption tower with following absorption portion and last absorption portion, wherein, following absorption portion on this absorption tower, unstripped gas contacts with the absorption liquid generation solution-air of partial regeneration, and carbonic acid gas partly is absorbed by liquid absorption; Then, on the absorption tower, contact with regeneration absorption liquid generation solution-air in the absorption portion again, carbonic acid gas is absorbed by liquid absorption, and the carbon dioxide content in unstripped gas reaches very low level, outside not carbonated processed gas then is exhausted from system; The absorption that in the decarbonation absorption tower, produces with 90～150 ℃ of heating the absorption liquid of carbonic acid gas, and send in the high pressure recovery tower, make it at 2kg/cm
2Feedstock gas pressures under discharge some carbonic acid gas, draw the absorption liquid of partial regeneration, and the part of this partial regeneration absorption liquid sent into the following absorption portion on above-mentioned absorption tower; Remaining partial regeneration absorption liquid is sent in the low pressure recovery tower, make its in 100-150 ℃ temperature to be lower than 2kg/cm
2The absolute pressure release of carbon dioxide, obtain the absorption liquid of regenerating, and the absorption liquid of will regenerating is sent into above-mentioned last absorption portion; Reclaim the highly compressed carbonic acid gas by cooling off the carbonic acid gas that in the high pressure recovery tower, under pressure, discharges and it being separated with all moisture of being carried secretly; Reclaim carbonic acid gas by cooling off the carbonic acid gas that in the low pressure recovery tower, discharges and it being separated with all moisture of being carried secretly.
2. according to the removal from high pressure feedstock gas of claim 1 and the technology of high pressure recovery carbonic acid gas, it is characterized in that the carbon dioxide content in the above-mentioned high pressure feedstock gas is 2～50%.
3. according to the removal from high pressure feedstock gas of claim 1 and the technology of high pressure recovery carbonic acid gas, it is characterized in that the carbon dioxide content of above-mentioned processed gas is 10～10000ppm.
4. one kind is used for removing the also system of high pressure recovery carbonic acid gas from high pressure feedstock gas, and contain: one has the decarbonation absorption tower of inhaling part and last absorption portion down; A well heater that has been used for adding thermal absorption the absorption liquid of carbonic acid gas; The high pressure recovery tower of the absorption liquid that absorbed carbonic acid gas of being used to regenerate; Be arranged on a water cooler and a vapour-liquid separator at this high pressure recovery tower top; A low pressure recovery tower that is used for the regeneration section regenerated liquid; A well heater that is arranged on this low pressure recovery tower bottom; And a water cooler and a gas-liquid separator of being arranged on this low pressure recovery tower top.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP226543/1996 | 1996-08-28 | ||
| JP226543/96 | 1996-08-28 | ||
| JP22654396A JP3675980B2 (en) | 1996-08-28 | 1996-08-28 | Method and apparatus for advanced removal and high pressure recovery of carbon dioxide in high pressure source gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1176991A CN1176991A (en) | 1998-03-25 |
| CN1074040C true CN1074040C (en) | 2001-10-31 |
Family
ID=16846806
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN97117692A Expired - Lifetime CN1074040C (en) | 1996-08-28 | 1997-08-27 | Process for removal and high-pressure recovery of carbon dioxide from high-pressure raw gas and system therefor |
Country Status (5)
| Country | Link |
|---|---|
| JP (1) | JP3675980B2 (en) |
| CN (1) | CN1074040C (en) |
| AU (1) | AU728167B2 (en) |
| ID (1) | ID18130A (en) |
| MY (1) | MY118691A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101448272A (en) * | 2008-12-29 | 2009-06-03 | 深圳市同洲电子股份有限公司 | Mobile communication signal test system and method thereof |
| CN102899095A (en) * | 2012-08-29 | 2013-01-30 | 中国科学院过程工程研究所 | High-performance decarburization compound solvent for coke oven gas or natural gas, and preparation method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| NO990812L (en) | 1999-02-19 | 2000-08-21 | Norsk Hydro As | Method for removing and recovering CO2 from exhaust gas |
| KR100693949B1 (en) * | 1999-05-14 | 2007-03-12 | 텍사코 디벨롭먼트 코포레이션 | Hydrogen recycle and acid gas removal using a membrane |
| DE10028637A1 (en) * | 2000-06-09 | 2001-12-13 | Basf Ag | Process for deacidifying a hydrocarbon stream comprises contacting the stream with an absorbing liquid, separating the purified stream and the absorbing liquid |
| WO2005009592A1 (en) * | 2003-07-22 | 2005-02-03 | Dow Global Technologies Inc. | Regeneration of acid gas-containing treatment fluids |
| JP4585222B2 (en) * | 2004-04-12 | 2010-11-24 | 三菱重工業株式会社 | Impurity disposal system and method |
| JP4247204B2 (en) * | 2005-05-09 | 2009-04-02 | 株式会社ルネッサンス・エナジー・インベストメント | Decomposition method of low concentration methane |
| DE602006011899D1 (en) * | 2005-07-18 | 2010-03-11 | Union Engineering As | METHOD FOR RECOVERING HIGH - PURE CARBON DIOXIDE FROM A NITROGEN COMPOUND CONTAINING GASEOUS SOURCE |
| JP5112664B2 (en) * | 2006-09-05 | 2013-01-09 | 神戸市 | Methane recovery method and digestion gas purification device |
| WO2009112518A1 (en) * | 2008-03-13 | 2009-09-17 | Shell Internationale Research Maatschappij B.V. | Process for removal of carbon dioxide from a gas |
| JP5467394B2 (en) * | 2009-04-20 | 2014-04-09 | 独立行政法人産業技術総合研究所 | Carbon dioxide separation and recovery method by physical absorption method using ionic liquid |
| US8500868B2 (en) | 2009-05-01 | 2013-08-06 | Massachusetts Institute Of Technology | Systems and methods for the separation of carbon dioxide and water |
| WO2011121635A1 (en) * | 2010-03-29 | 2011-10-06 | 株式会社 東芝 | Acidic gas absorbent, acidic gas removal device, and acidic gas removal method |
| FR2960445A1 (en) * | 2010-06-01 | 2011-12-02 | Air Liquide | METHOD AND APPARATUS FOR SEPARATING AND PRODUCING CARBON DIOXIDE |
| US20150343369A1 (en) * | 2013-02-08 | 2015-12-03 | Toyo Engineering Corporation | Process for recovering carbon dioxide from construction exhaust gas |
| EP3156363A1 (en) | 2015-10-15 | 2017-04-19 | Casale SA | Process for making a synthesis gas by reforming of a hydrocarbon and including recovery of carbon dioxide at high pressure |
| CN110684574B (en) * | 2018-07-06 | 2021-06-01 | 中国石油化工股份有限公司 | Decarbonization method for preparing liquefied natural gas from high-carbon-content natural gas |
| CN109681158B (en) * | 2019-03-04 | 2020-11-24 | 中国石油大学(华东) | Device for carbon dioxide flooding technology |
| CN111717915B (en) * | 2019-03-19 | 2022-02-01 | 中石化石油工程技术服务有限公司 | Method and device capable of improving capture rate of carbon dioxide in carbon dioxide flooding produced gas of oil field |
| CN109999618B (en) * | 2019-04-25 | 2024-05-14 | 华能国际电力股份有限公司 | System and method for separating carbon dioxide from medium-high pressure gas source |
| CN113351172B (en) * | 2021-07-22 | 2023-01-06 | 安徽元琛环保科技股份有限公司 | Preparation method of denitration and CO2 adsorption material and prepared adsorption material |
| WO2024201895A1 (en) * | 2023-03-30 | 2024-10-03 | 三菱重工業株式会社 | Carbon dioxide recovery system |
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| US4705673A (en) * | 1984-10-10 | 1987-11-10 | Union Carbide Corporation | Mixed solvent system for treating acidic gas |
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| JP3626796B2 (en) * | 1995-10-03 | 2005-03-09 | 三菱重工業株式会社 | Method for removing high-concentration carbon dioxide from high-pressure natural gas |
-
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- 1996-08-28 JP JP22654396A patent/JP3675980B2/en not_active Expired - Lifetime
-
1997
- 1997-07-10 AU AU28540/97A patent/AU728167B2/en not_active Expired
- 1997-07-23 MY MYPI97003349A patent/MY118691A/en unknown
- 1997-08-25 ID IDP972948A patent/ID18130A/en unknown
- 1997-08-27 CN CN97117692A patent/CN1074040C/en not_active Expired - Lifetime
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|---|---|---|---|---|
| US4705673A (en) * | 1984-10-10 | 1987-11-10 | Union Carbide Corporation | Mixed solvent system for treating acidic gas |
| US4710362A (en) * | 1986-05-05 | 1987-12-01 | Texaco Inc. | Selective recovery of carbon dioxide |
| WO1994011090A1 (en) * | 1992-11-13 | 1994-05-26 | Norsk Hydro A.S | Pre-treatment of natural gas to be condensed to liquefied natural gas (lng) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101448272A (en) * | 2008-12-29 | 2009-06-03 | 深圳市同洲电子股份有限公司 | Mobile communication signal test system and method thereof |
| CN102899095A (en) * | 2012-08-29 | 2013-01-30 | 中国科学院过程工程研究所 | High-performance decarburization compound solvent for coke oven gas or natural gas, and preparation method thereof |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1176991A (en) | 1998-03-25 |
| JP3675980B2 (en) | 2005-07-27 |
| AU2854097A (en) | 1998-03-05 |
| MY118691A (en) | 2005-01-31 |
| AU728167B2 (en) | 2001-01-04 |
| ID18130A (en) | 1998-03-05 |
| JPH1067994A (en) | 1998-03-10 |
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