CN106731494A - The process of desorption air lift coupled and pressurizing absorption purification biogas - Google Patents
The process of desorption air lift coupled and pressurizing absorption purification biogas Download PDFInfo
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- CN106731494A CN106731494A CN201611095948.5A CN201611095948A CN106731494A CN 106731494 A CN106731494 A CN 106731494A CN 201611095948 A CN201611095948 A CN 201611095948A CN 106731494 A CN106731494 A CN 106731494A
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- stripping
- absorption tower
- absorbent
- biogas
- discharge
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 92
- 238000000034 method Methods 0.000 title claims abstract description 55
- 238000003795 desorption Methods 0.000 title claims abstract description 34
- 238000000746 purification Methods 0.000 title claims abstract description 34
- 230000008569 process Effects 0.000 title claims abstract description 23
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 124
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 85
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 61
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 239000002250 absorbent Substances 0.000 claims abstract description 52
- 230000002745 absorbent Effects 0.000 claims abstract description 52
- 238000007599 discharging Methods 0.000 claims abstract description 28
- 238000007789 sealing Methods 0.000 claims abstract description 25
- 238000001035 drying Methods 0.000 claims abstract description 17
- 238000002156 mixing Methods 0.000 claims abstract description 8
- 238000005406 washing Methods 0.000 claims abstract description 8
- 230000008929 regeneration Effects 0.000 claims abstract description 5
- 238000011069 regeneration method Methods 0.000 claims abstract description 5
- 238000001816 cooling Methods 0.000 claims abstract description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 81
- 238000007710 freezing Methods 0.000 claims description 23
- 230000008014 freezing Effects 0.000 claims description 23
- 239000003795 chemical substances by application Substances 0.000 claims description 21
- SBASXUCJHJRPEV-UHFFFAOYSA-N 2-(2-methoxyethoxy)ethanol Chemical compound COCCOCCO SBASXUCJHJRPEV-UHFFFAOYSA-N 0.000 claims description 16
- ZUHZGEOKBKGPSW-UHFFFAOYSA-N tetraglyme Chemical compound COCCOCCOCCOCCOC ZUHZGEOKBKGPSW-UHFFFAOYSA-N 0.000 claims description 16
- JLGLQAWTXXGVEM-UHFFFAOYSA-N triethylene glycol monomethyl ether Chemical compound COCCOCCOCCO JLGLQAWTXXGVEM-UHFFFAOYSA-N 0.000 claims description 14
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 13
- 210000001364 upper extremity Anatomy 0.000 claims description 10
- ZIBGPFATKBEMQZ-UHFFFAOYSA-N triethylene glycol Chemical compound OCCOCCOCCO ZIBGPFATKBEMQZ-UHFFFAOYSA-N 0.000 claims description 9
- SBZXBUIDTXKZTM-UHFFFAOYSA-N diglyme Chemical compound COCCOCCOC SBZXBUIDTXKZTM-UHFFFAOYSA-N 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 6
- YFNKIDBQEZZDLK-UHFFFAOYSA-N triglyme Chemical compound COCCOCCOCCOC YFNKIDBQEZZDLK-UHFFFAOYSA-N 0.000 claims description 6
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical class CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims description 5
- 238000003860 storage Methods 0.000 claims description 5
- 239000012530 fluid Substances 0.000 claims description 4
- 150000002170 ethers Chemical class 0.000 claims description 3
- 230000008878 coupling Effects 0.000 claims 1
- 238000010168 coupling process Methods 0.000 claims 1
- 238000005859 coupling reaction Methods 0.000 claims 1
- 239000008246 gaseous mixture Substances 0.000 claims 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 87
- 239000007789 gas Substances 0.000 description 72
- 239000000243 solution Substances 0.000 description 46
- 239000000047 product Substances 0.000 description 26
- 238000004448 titration Methods 0.000 description 17
- 238000007689 inspection Methods 0.000 description 16
- 229910052500 inorganic mineral Inorganic materials 0.000 description 14
- 239000011707 mineral Substances 0.000 description 14
- 239000003673 groundwater Substances 0.000 description 13
- 239000007864 aqueous solution Substances 0.000 description 12
- 230000006835 compression Effects 0.000 description 7
- 238000007906 compression Methods 0.000 description 7
- 238000005265 energy consumption Methods 0.000 description 7
- 238000005262 decarbonization Methods 0.000 description 6
- 239000000945 filler Substances 0.000 description 6
- 239000003345 natural gas Substances 0.000 description 6
- DGVSIBCCYUVRNA-UHFFFAOYSA-O [[5-(3-carbamoylpyridin-1-ium-1-yl)-3,4-dihydroxyoxolan-2-yl]methoxy-hydroxyphosphoryl] [3,4-dihydroxy-5-(6-oxo-3h-purin-9-yl)oxolan-2-yl]methyl hydrogen phosphate Chemical compound NC(=O)C1=CC=C[N+](C2C(C(O)C(COP(O)(=O)OP(O)(=O)OCC3C(C(O)C(O3)N3C4=C(C(N=CN4)=O)N=C3)O)O2)O)=C1 DGVSIBCCYUVRNA-UHFFFAOYSA-O 0.000 description 5
- 238000005261 decarburization Methods 0.000 description 5
- 229910001220 stainless steel Inorganic materials 0.000 description 5
- 239000010935 stainless steel Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 230000004907 flux Effects 0.000 description 4
- RGCLLPNLLBQHPF-HJWRWDBZSA-N phosphamidon Chemical group CCN(CC)C(=O)C(\Cl)=C(/C)OP(=O)(OC)OC RGCLLPNLLBQHPF-HJWRWDBZSA-N 0.000 description 4
- 230000009467 reduction Effects 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000012856 packing Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- 239000013589 supplement Substances 0.000 description 3
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-UHFFFAOYSA-N 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 2
- 238000009835 boiling Methods 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000006837 decompression Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 238000012423 maintenance Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- OAXIUZFXLOZILE-UHFFFAOYSA-N 2-(2-methoxyethoxy)propane Chemical class COCCOC(C)C OAXIUZFXLOZILE-UHFFFAOYSA-N 0.000 description 1
- ZNQVEEAIQZEUHB-UHFFFAOYSA-N 2-ethoxyethanol Chemical compound CCOCCO ZNQVEEAIQZEUHB-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 241000790917 Dioxys <bee> Species 0.000 description 1
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical class CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 1
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- -1 Physical Absorption Substances 0.000 description 1
- 239000002202 Polyethylene glycol Substances 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- GCNLQHANGFOQKY-UHFFFAOYSA-N [C+4].[O-2].[O-2].[Ti+4] Chemical compound [C+4].[O-2].[O-2].[Ti+4] GCNLQHANGFOQKY-UHFFFAOYSA-N 0.000 description 1
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- SIXOAUAWLZKQKX-UHFFFAOYSA-N carbonic acid;prop-1-ene Chemical compound CC=C.OC(O)=O SIXOAUAWLZKQKX-UHFFFAOYSA-N 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 125000004177 diethyl group Chemical group [H]C([H])([H])C([H])([H])* 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- DQYBDCGIPTYXML-UHFFFAOYSA-N ethoxyethane;hydrate Chemical compound O.CCOCC DQYBDCGIPTYXML-UHFFFAOYSA-N 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000011049 filling Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- JEIPFZHSYJVQDO-UHFFFAOYSA-N iron(III) oxide Inorganic materials O=[Fe]O[Fe]=O JEIPFZHSYJVQDO-UHFFFAOYSA-N 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 239000003960 organic solvent Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 229920001223 polyethylene glycol Polymers 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- XTUSEBKMEQERQV-UHFFFAOYSA-N propan-2-ol;hydrate Chemical compound O.CC(C)O XTUSEBKMEQERQV-UHFFFAOYSA-N 0.000 description 1
- 230000001172 regenerating effect Effects 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000002604 ultrasonography Methods 0.000 description 1
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
- B01D53/1425—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
- B01D53/1475—Removing carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L3/00—Gaseous fuels; Natural gas; Synthetic natural gas obtained by processes not covered by subclass C10G, C10K; Liquefied petroleum gas
- C10L3/06—Natural gas; Synthetic natural gas obtained by processes not covered by C10G, C10K3/02 or C10K3/04
- C10L3/10—Working-up natural gas or synthetic natural gas
- C10L3/101—Removal of contaminants
- C10L3/102—Removal of contaminants of acid contaminants
- C10L3/104—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/50—Combinations of absorbents
-
- 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
- B01D2252/60—Additives
Abstract
One kind desorption air lift coupled, it is characterized in that it is made up of two sections, epimere is stripping stage, hypomere is stripping section, dividing plate is provided between stripping stage and stripping section, the discharging tube of dividing plate is provided through on dividing plate, liquid sealing pipe is provided with outside discharging tube, dividing plate is fixed in the top seal bottom of liquid sealing pipe.The process of pressurizing absorption purification biogas, it is characterized in that it comprises the following steps：Absorption tower will be sent into after biogas pressurization and cooling, absorbent enters from absorption tower top, and biogas is inversely contacted with absorbent from bottom to top in absorption tower, rich CH4Gas is discharged from the top on absorption tower, is stored after drying；Enter the CH that flash column will dissolve from the solution for absorbing tower bottom discharge4With part CO2Discharge, this part mixed gas returns air accumulator, and participation washing is separated again with unstripped gas mixing again；Enter desorption air lift coupled from the solution of flash column discharge, the carbon dioxide for desorbing is discharged from the top of stripping stage；The solution from stripping stage discharge enters stripping section through discharging tube afterwards, and stripping regeneration is carried out using air, returns to absorption tower as absorbent afterwards.
Description
Technical field
The invention belongs to fields such as Chemical Engineering and Technology, regenerative resources, it is related to a kind of purification biogas technology, especially
It is related to a kind of process of pressurizing absorption purification biogas.
Background technology
Biogas is a kind of important clean reproducible energy, can not only substitute coal fired power generation and heat supply, and by net
Changing can be used as the substitute of natural gas after purifying.Marsh gas purifying purification relates generally to the operations such as desulfurization, decarburization, dehydration, dedusting,
Wherein Methane decarbonization is the committed step of marsh gas purifying purification.Decarbonization method mainly have pressure-variable adsorption, UF membrane, Physical Absorption,
Chemical absorbing, cryogenic separation and in-situ purification etc., wherein Physical Absorption method are to utilize CO2Dissolving with hydro carbons in physical solvent
The difference of degree completes decarburization task, and conventional physical solvent has water, methyl alcohol, NHD, propene carbonate, N- methyl
Pyrrolidones, many Ethylene Glycol Methyl isopropyl ethers and sulfolane etc..
In the absorbent that decarburization is used, NHD stable chemical performance, heat endurance are good, volatilization loss
It is small, have many advantages, such as that boiling point is high, freezing point is low, vapour pressure is low, it is a kind of excellent organic solvent, to CO2And H2S has excellent
Good selection absorbing and removing function, it is adaptable to the purification of producing synthesis gas from coal and natural gas, casing-head gas, refinery gas and town gas
The removing of middle sour gas, has the advantages that degree of purification is high, energy consumption is low, it is high to reclaim carbon dioxide purity, using polyethylene glycol two
General (such as 7MPa) operation under larger pressure of methyl ether decarburization, has water to aggravate equipment corrosion in absorbent, therefore using poly-
The water content of glycol dimethyl ether decarbonization process requirement NHD is controlled 5% or so, and maximum water content is no more than
10%, and the water content of biogas is very high, the water content of decarbonizing liquid is raised quickly if using NHD purifying biogas,
Needs frequently carry out dewater treatment to decarbonizing liquid.In addition, after the NHD decarbonization process operation regular period, decarbonizing liquid
The middle solia particle that adhesive force can be produced extremely strong, increase the viscosity of solution, and solution darkens, decarbonization system power consumption liter
High, solution internal circulating load is big, treatment tolerance declines, gas purifying effect is poor, and pipeline is frequently occluded, therefore needs periodically enter to decarbonizing liquid
Row purified treatment.
Pressurization washing process is that current industrialized European uses more Methane decarbonization method, and its principle is in pressurized conditions
Under, by CO2It is dissolved in the water and reduces its content in biogas, its process is usually：Absorption tower is sent into after biogas is pressurizeed,
Water enters as absorbent from top, and biogas is contacted with flow reversal from bottom to top in absorption tower, the most of CO in biogas2
With a small amount of CH4It is dissolved in water, rich CH4Gas is discharged from the top on absorption tower, and bio-natural gas are obtained after being further dried；From absorption
Tower bottom discharge water be dissolved in water into flash column in CH4With most of CO2Discharged from water, the mixing of this part
Gas participates in washing and separates again with unstripped gas mixing again；Enter desorber from the water of flash column discharge, using decompression or empty
Gas carries out stripping regeneration, returns to absorption tower as absorbent afterwards.
The advantage that pressure (hydraulic) water washes purifying biogas technique includes：The abundance of water, nontoxic, easily regeneration；CO2Removal efficiency
Height, methane losses are less；CO can simultaneously be removed2And H2S；Process is simple, operation temperature is low, and chemical reagent and steam, mistake are not consumed
Cheng Huanbao.But pressure (hydraulic) water washes purifying biogas technique also shortcoming, such as CO2Solubility in water it is relatively low, it is necessary to pressurize and
Reduce temperature and increase its solubility, energy consumption and device are larger；The specific heat of water is larger, and the energy consumption for needing of lowering the temperature is larger；The freezing point of water
It is zero degree, when applying in the northern area of China winter, is especially stopped production the maintenance period in device, has what is frozen in equipment and pipeline
May, bring security risk to equipment operation.
Pressure (hydraulic) water is washed in purifying biogas technical process, and the decompression desorption method for not using air lift is simple to operate, power consumption is small,
And the carbon dioxide of higher degree can be reclaimed, but the carbon dioxide after the completion of desorption of depressurizing in absorbing liquid is still in saturation shape
State, if desorption liquid returns to absorption tower and re-uses the efficiency that will influence to absorb；201110459278.1 disclose a kind of biogas
Purification method, by biogas by obtaining high methane content gas after supercharging, filtering, biological desulphurization, deoxidation, absorption process decarburization, dehydration
Body, during the liquid after flash distillation is desorbed, using air stripping can by absorbing liquid carbon dioxide eliminating completely,
But very big air mass flow is then needed using air stripping desorption completely, and the energy consumption of blower fan can be increased, and desorption outlet is
The relatively low carbon dioxide of concentration.CN101837227B discloses absorption liquid desorption method in a kind of methane purification system, absorbing liquid
By first order depressurization desorption, pressure (absolute pressure is in this patent) drops to 0.1 MPa from 0.6~1.6 MPa, and removing is big
Partial CO 2, is then desorbed by second level air stripping, and carbon dioxide has been removed substantially in absorbing liquid after the completion of desorption
Entirely, absorption tower is recycled to continue with.But, found in actual experiment in absorbing liquid after first order depressurization desorption process
Carbon dioxide is actually in hypersaturated state, it is necessary to desorption for a long time can be only achieved dissolution equilibrium state, is carrying out the
Secondary air stripping stills need larger air mass flow when desorbing；If can strengthen first order depressurization desorption process makes titanium dioxide
Carbon desorbs more thorough, then more carbon dioxide can not only be reclaimed in first order depressurization desorption, and in second level air
Stripping can just reach the purpose for desorbing completely when desorbing using less air mass flow, reduce the energy consumption of blower fan.
The content of the invention
The purpose of this programme is the deficiency for making up prior art, there is provided one kind desorbs air lift coupled and uses stripping gas
Carrying coupled carries out the process of pressurizing absorption purification biogas
One kind desorption air lift coupled, it is characterized in that it is made up of two sections, epimere is stripping stage, and hypomere is stripping section, solution
Inhale and be provided with dividing plate between section and stripping section, the discharging tube of dividing plate is provided through on dividing plate, liquid is provided with outside discharging tube
Dividing plate is fixed in tube sealing, the top seal bottom of liquid sealing pipe, and the lower end of liquid sealing pipe is provided with inlet opening；On stripping stage
Portion is provided with inlet and gas outlet, and stripping section top is provided with exhaust outlet bottom is provided with air inlet and leakage fluid dram.
The inlet opening upper limb of liquid sealing pipe is 0.5~3.0 meter with the distance on discharging tube top.
A kind of process that pressurizing absorption purification biogas is carried out using foregoing desorption air lift coupled, its
It is characterized in that it comprises the following steps：Absorption tower will be sent into after biogas pressurization and cooling, absorbent enters from absorption tower top, is inhaling
Receive biogas in tower inversely to be contacted with absorbent from bottom to top, rich CH4Gas is discharged from the top on absorption tower, is stored after drying；From
The solution for absorbing tower bottom discharge enters the CH that flash column will dissolve4With part CO2Discharge, this part mixed gas returns storage
Gas tank participates in washing and separates again with unstripped gas mixing again；Enter desorption air lift coupled, pressure from the solution of flash column discharge
Power drops to 0.1 MPa from flashing pressure, and the carbon dioxide for desorbing is discharged from the top of stripping stage；Discharged from stripping stage afterwards
Solution enter stripping section through discharging tube, carry out stripping regeneration using air, afterwards as absorbent return absorption tower.
The absorbent is made up of water and drop freezing point agent, and its reclaimed water is 9 with the mass ratio of drop freezing point agent:1~1:1；Selection
The index request of drop freezing point agent includes drop freezing point agent physical property stabilization, and volatility is low, and by the agent of drop freezing point and water group
Into absorbent in addition to low freezing point, drop freezing point agent also has higher boiling, CO high in itself2Solubility, CO high2/CH4Selectivity,
Low specific heat, low-corrosiveness, low viscosity, hypotoxicity；Drop freezing point agent is diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, four
Glycol monoethyl ether, diethylene glycol dimethyl ether, TRIGLYME, tetraethyleneglycol dimethyl ether, 1- (2- methoxyl group -1- methyl
Ethyoxyl) mixture of one or two or more in isopropanol and double (2- methoxy-propyls) ethers.
Preferably, drop freezing point agent is diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, TEG monomethyl ether, three
The mixture of one or two or more in glycol dimethyl ether and tetraethyleneglycol dimethyl ether.
Preferably, the absorbent is made up of water and drop freezing point agent, and its reclaimed water is 4 with the mass ratio of drop freezing point agent:1~3:
2。
The stripping stage of the desorption air lift coupled uses plate column, and is provided with ultrasonic wave on the bottom surface of column plate and shakes
Box, to strengthen desorption process.
The beneficial effect of this programme is：The desorption air lift coupled that this programme is used is set between stripping stage and stripping section
Dividing plate, discharging tube and liquid sealing pipe, can make liquid be directly entered stripping section through discharging tube from stripping stage, and due to the work of fluid-tight
With and cause the gas in stripping section from entering into stripping stage, it is to avoid use Valve controlling, it is simple to operate；This programme is used
Absorbent there is low freezing point, greatly reduce the possibility frozen in equipment and pipeline, increase the safety system of equipment operation
Number, therefore pressurizing absorption purification biogas technique can run at low temperature, and when temperature is higher CO2Used in this programme
Absorbent in solubility it is still larger, therefore pressurizing absorption purification biogas technique can run at relatively high temperatures,
So that pressurizing absorption purification biogas technique can be throughout the year in the case where control absorption tower inflow temperature is not used
All run；Compared with water, absorbent is to CO2Solubility increase, make CO2Increase to the mass transfer force in absorbent, absorb speed
Rate is big, and same absorption agent flux can purify more biogas；The specific heat reduction of absorbent, the energy consumption reduction for needing of lowering the temperature；
Using ultrasound-enhanced CO2Desorption, can not only reclaim more carbon dioxide, and can reduce the air mass flow of air lift, subtract
Small energy consumption.
Brief description of the drawings
Fig. 1 is desorption air lift coupled principle schematic diagram. of the invention.
Fig. 2 is the process flow diagram of pressurizing absorption purification biogas of the invention.
Fig. 3 is the process flow diagram of the pressurizing absorption purification biogas of prior art.
Fig. 4 is the process flow diagram of the pressurizing absorption purification biogas of prior art.
In figure：101- stripping stages；102- stripping sections；103- dividing plates；104- discharging tubes；105- liquid sealing pipes；106- inlet openings；
107- inlets；108- gas outlets；109- exhaust outlets；110- air inlets；111- leakage fluid drams；201- Marsh gas compression machines；202- is changed
Hot device；203- absorption towers；204- valves；205- driers；206- handpiece Water Chilling Units；207- booster pumps；208- valves；209- is flashed
Tower；210- valves；211- valves；212- desorbs air lift coupled；213- valves；214- valves；215- air blowers；216- valves
Door；217- liquid reserve tanks；218- valves；301- stripping towers；302- valves；303- air blowers；304- valves；401- desorbers；
402- valves；403- valves；404- feed pumps；405- stripping towers；406- valves；407- air blowers；408- valves；H- liquid sealing pipes
105 inlet opening upper limb and the distance on the top of discharging tube 104.
Specific embodiment
This programme is described in further detail below in conjunction with the accompanying drawings and by specific embodiment, following examples are descriptive
, it is not limited, it is impossible to the protection domain of this programme is limited with this.
Embodiment 1：
As shown in figure 1, a kind of desorption air lift coupled：It is made up of two sections, and epimere is stripping stage 101, and hypomere is gas
Section 102 is put forward, dividing plate 103 is provided between stripping stage 101 and stripping section 102, dividing plate 103 is provided through on dividing plate 103
Discharging tube 104, is provided with liquid sealing pipe 105 outside discharging tube 104, and dividing plate 103 is fixed in the top seal bottom of liquid sealing pipe 105
On, and the lower end of liquid sealing pipe 105 is provided with inlet opening 106；The top of stripping stage 101 is provided with inlet 107 and outlet
Mouth 108, exhaust outlet 109 is provided with the top of stripping section 102, and bottom is provided with leakage fluid dram 111, and bottom is provided with air inlet 110.
The inlet opening upper limb of liquid sealing pipe 105 is 1.0 meters, the internal diameter 0.07 of liquid sealing pipe 105 apart from H with the top of discharging tube 104
Rice, 0.03 meter of 104 internal diameter of discharging tube.Stripping stage 101 is plate column, and high 3.0 meters, 0.12 meter of tower internal diameter, the number of plates is 6 pieces, tower
0.2 meter of plate spacing；Stripping section 102 be packed tower, high 3.0 meters, 0.12 meter of tower internal diameter, filling diameter and height all for 10 mm not
Rust steel Dixon ring filler, packing section is high 1.5 meters.
As shown in Fig. 2 marsh gas purifying purification system includes Marsh gas compression machine 201, heat exchanger 202, absorption tower 203, valve
204th, 208,210,211,213,214,216,218, drier 205, handpiece Water Chilling Units 206, booster pump 207, flash column 209, solution
Air-breathing carries coupled 212, air blower 215, liquid reserve tank 217.
Wherein：
Absorption tower 203 is packed tower, and 0.1 meter of tower internal diameter loads the stainless steel Dixon ring filler that diameter and height are all 10 millimeters, fills out
Material section is high 2.0 meters；
Flash column 209 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces.
The absorbent that the present embodiment is used is the matter of the diethylene glycol monomethyl ether aqueous solution, its reclaimed water and diethylene glycol monomethyl ether
Amount is than being 4:1.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 20~10 DEG C.
A kind of process that pressurizing absorption purification biogas is carried out using foregoing desorption air lift coupled, natural pond
Gas is forced into 0.8 MPa, is cooled to 20 DEG C through heat exchanger 202 through Marsh gas compression machine 201, afterwards into absorption tower 203, biogas stream
It is 20 L/min to measure.
Absorbent is cooled to 10 DEG C, 0.8 MPa is forced into through booster pump 207, afterwards from absorption tower through handpiece Water Chilling Units 206
203 tops enter, and absorption agent flux is 2.5 L/min, and biogas is inversely contacted with absorbent from bottom to top in absorption tower 203,
Rich CH4Gas is discharged from the top on absorption tower 203 through valve 204, is stored as product gas after drier 205, determines its composition
For：Methane content is 97.50%（Percentage by volume）, carbon dioxide content is 2.49%（Percentage by volume）, water vapour content is
0.01%（Percentage by volume）.
Enter flash column 209, the Stress control in flash column 209 through valve 208 from the solution of the bottom of absorption tower 203 discharge
In 0.35 MPa, the CH that solution will dissolve in flash column 2094With part CO2Discharge, this part mixed gas is through valve
210 times air accumulators participate in washing and separate again with unstripped gas mixing again.
Enter desorption air lift coupled 212 through valve 211 from the solution of the bottom of flash column 209 discharge, pressure drops to 0.1
MPa（I.e. under atmospheric pressure）, the carbon dioxide desorbed in stripping stage 101 is from the top of stripping stage 101 through the row of valve 213
Go out；Solution after desorption is directly entered stripping section 102 from stripping stage 101 through discharging tube 104, and air blower 215 is from stripping section 102
Lower end blasts air with the wind speed of 20 L/min, air inversely contacted with solution from bottom to top after with the carbon dioxide for desorbing
Discharged through valve 214 from the top of stripping section 102 together.
Enter liquid reserve tank 217 through valve 216 from the solution of the bottom of stripping section 102 discharge, returned as absorbent inhale afterwards
Tower 203 is received, is controlled to supplement liquid level of the running water to maintain liquid reserve tank 217 in addition by valve 218.According to People's Republic of China (PRC) ground
Matter mineral products professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from
The CO2 contents of the solution of the bottom of stripping section 102 discharge are 10.20 mg/L.
The absorbent that the present embodiment is used is the diethylene glycol monomethyl ether aqueous solution, greatly reduces equipment with icing in pipeline
Possibility, can not only be run when ambient temperature is higher, and ambient temperature be 0~10 DEG C when also can safe operation,
Increase the safety coefficient of equipment operation；High-pureness carbon dioxide can be reclaimed；Desorption air lift coupled is in stripping stage and air lift
Dividing plate, discharging tube and liquid sealing pipe are set between section, liquid can be made to be directly entered stripping section through discharging tube from stripping stage, and by
Gas in the effect of fluid-tight causes stripping section is from entering into stripping stage, it is to avoid use Valve controlling, simple to operate；
With embodiment 2（Comparative example）Compare, carbon dioxide content is lower in the product gas obtained from absorption tower 203（Below 3%）, energy
Enough meet the requirement of compressed natural gas used as vehicle fuel technical standard.
Embodiment 2（Comparative example）：
As shown in figure 3, marsh gas purifying purification system include Marsh gas compression machine 201, heat exchanger 202, absorption tower 203, valve 204,
208th, 210,211,218,302,304, drier 205, handpiece Water Chilling Units 206, booster pump 207, flash column 209, liquid reserve tank 217,
Stripping tower 301, air blower 303.
Wherein：Absorption tower 203 is packed tower, and 0.1 meter of tower internal diameter loads the stainless steel θ nets that diameter and height are all 10 millimeters
Ring filler, packing section is high 2.0 meters；
Flash column 209 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Stripping tower 301 is packed tower, and 0.2 meter of tower internal diameter loads the stainless steel Dixon ring filler that diameter and height are all 10 millimeters, fills out
Material section is high 2.0 meters.
The absorbent that the present embodiment is used is running water.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 20~5 DEG C.
Marsh gas purifying purification process：Biogas is forced into 0.8 MPa, is cooled to 20 through heat exchanger 202 through Marsh gas compression machine 201
DEG C, afterwards into absorption tower 203, biogas flow is 20 L/min；
Absorbent is cooled to 10 DEG C, is forced into 0.8 MPa through booster pump 207 through handpiece Water Chilling Units 206, is pushed up from absorption tower 203 afterwards
Portion enters, and absorption agent flux is 2.5 L/min, and biogas is inversely contacted with absorbent from bottom to top in absorption tower 203, rich CH4
Gas is discharged from the top on absorption tower 203 through valve 204, after drier 205 as product gas store, determine consisting of：First
Alkane content is 93.60%（Percentage by volume）, carbon dioxide content is 6.39%（Percentage by volume）, water vapour content is 0.01%
（Percentage by volume）；
Enter flash column 209 through valve 208 from the solution of the bottom of absorption tower 203 discharge, the Stress control in flash column 209 exists
0.35 MPa, the CH that solution will dissolve in flash column 2094With part CO2Discharge, this part mixed gas is through valve 210
Participation washing is separated again with unstripped gas mixing again to return air accumulator；
Enter stripping tower 301 through valve 211 from the solution of the bottom of flash column 209 discharge, pressure drops to 0.1 MPa（I.e. in air
Pressure）, air blower 303 blasts air from the lower end of stripping tower 301 with the wind speed of 25 L/min, and air is reverse with solution from bottom to top
Discharged through valve 302 from the top of stripping tower 301 together with the carbon dioxide for desorbing after contact；
Enter liquid reserve tank 217 through valve 304 from the solution of the bottom of stripping tower 301 discharge, return to absorption tower as absorbent afterwards
203, controlled to supplement liquid level of the running water to maintain liquid reserve tank 217 in addition by valve 218.According to People's Republic of China's geology ore deposit
Produce professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from air lift
The CO of the solution of the bottom of tower 301 discharge2Content is 11.10 mg/L.
The absorbent that the present embodiment is used is running water, when ambient temperature is less than 0 DEG C in the strict control technique of needs
Absorbent temperature is higher than 0 DEG C, needs thoroughly to empty water in the device stopping production maintenance period, otherwise exists in equipment and pipeline and freezes
Possibility, to equipment operation bring security risk；Gas from stripping tower discharge is CO2With the mixture of air, it is impossible to enough to return
Receive the high-pureness carbon dioxide from the release of desorber top.
Embodiment 3（Comparative example）：
As shown in figure 4, marsh gas purifying purification system include Marsh gas compression machine 201, heat exchanger 202, absorption tower 203, valve 204,
208th, 210,211,218,402,403,406,408, drier 205, handpiece Water Chilling Units 206, booster pump 207, flash column 209, storage
Liquid case 217, desorber 401, feed pump 404；Stripping tower 405, air blower 407.
Wherein：Absorption tower 203 is packed tower, and 0.1 meter of tower internal diameter loads the stainless steel θ nets that diameter and height are all 10 millimeters
Ring filler, packing section is high 2.0 meters；
Flash column 209 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Desorber 401 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces；
Stripping tower 405 is packed tower, and 0.2 meter of tower internal diameter loads the stainless steel Dixon ring filler that diameter and height are all 10 millimeters, fills out
Material section is high 2.0 meters.
The absorbent that the present embodiment is used is running water.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 20~5 DEG C.
Marsh gas purifying purification process：
Biogas is forced into 0.8 MPa, is cooled to 20 DEG C through heat exchanger 202 through Marsh gas compression machine 201, afterwards into absorption tower 203,
Biogas flow is 20 L/min；
Absorbent is cooled to 10 DEG C, is forced into 0.8 MPa through booster pump 207 through handpiece Water Chilling Units 206, is pushed up from absorption tower 203 afterwards
Portion enters, and absorption agent flux is 2.5 L/min, and biogas is inversely contacted with absorbent from bottom to top in absorption tower 203, rich CH4
Gas is discharged from the top on absorption tower 203 through valve 204, after drier 205 as product gas store, determine consisting of：First
Alkane content is 95.50%（Percentage by volume）, carbon dioxide content is 4.49%（Percentage by volume）, water vapour content is 0.01%
（Percentage by volume）；
Enter flash column 209 through valve 208 from the solution of the bottom of absorption tower 203 discharge, the Stress control in flash column 209 exists
0.35 MPa, the CH that solution will dissolve in flash column 2094With part CO2Discharge, this part mixed gas is through valve 210
Participation washing is separated again with unstripped gas mixing again to return air accumulator；
Enter desorber 401 through valve 211 from the solution of the bottom of flash column 209 discharge, pressure drops to 0.1 MPa（I.e. in air
Pressure）, the carbon dioxide for desorbing discharges from the top of desorber 401 through valve 402；
Enter stripping tower 405 through valve 403 and feed pump 404 from the solution of the bottom of desorber 401 discharge, air blower 407 is from gas
The lower end of stripper 405 blasts air with the wind speed of 25 L/min, air inversely contacted with solution from bottom to top after with desorb
Carbon dioxide is discharged from the top of stripping tower 405 through valve 406 together；
Enter liquid reserve tank 217 through valve 408 from the solution of the bottom of stripping tower 405 discharge, return to absorption tower as absorbent afterwards
203, controlled to supplement liquid level of the running water to maintain liquid reserve tank 217 in addition by valve 218.According to People's Republic of China's geology ore deposit
Produce professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from air lift
The CO of the solution of the bottom of tower 405 discharge2Content is 11.05 mg/L.
The absorbent that the present embodiment is used is running water, and equipment is interior with pipeline to have the possibility for freezing, and runs band to equipment
Carry out security risk；CO can be reclaimed2, but feed pump is needed between desorber and stripping tower, control relatively complicated.
Embodiment 4：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the diethylene glycol monomethyl ether aqueous solution, its reclaimed water is 9 with the mass ratio of diethylene glycol monomethyl ether:
1, absorbent is cooled to 15 DEG C through handpiece Water Chilling Units 206, and the inlet opening upper limb of liquid sealing pipe 105 is apart from H with the top of discharging tube 104
0.5 meter, 101 high 2.7 meters of stripping stage is outer, the other the same as in Example 1, rich CH4Gas is made after drying from the Base top contact on absorption tower 203
Be product gas storage, determine consisting of：Methane content is 97.54%（Percentage by volume）, carbon dioxide content is 2.45%（Body
Product percentage）, water vapour content is 0.01%（Percentage by volume）；From the top of stripping stage 101 through the discharge gas of valve 213
Flow is 4.95 L/min, CO2Content is 97.05%（Percentage by volume）；According to People's Republic of China's geological and mineral industry mark
Quasi- DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from the bottom of stripping section 102
The CO of the solution of portion's discharge2Content is 12.08 mg/L.
The operation temperature on absorption tower 203 is 15~17 DEG C in the present embodiment, and carbon dioxide content exists in the product gas of acquisition
Less than 3%, disclosure satisfy that the requirement of compressed natural gas used as vehicle fuel technical standard.
Embodiment 5：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the triethylene glycol monomethyl ether aqueous solution, its reclaimed water is 7 with the mass ratio of triethylene glycol monomethyl ether:
3, absorbent is cooled to 20 DEG C through handpiece Water Chilling Units 206, and the inlet opening upper limb of liquid sealing pipe 105 is apart from H with the top of discharging tube 104
1.5 meters, 101 high 3.5 meters of stripping stage is outer, the other the same as in Example 1, rich CH4Gas is made after drying from the Base top contact on absorption tower 203
Be product gas storage, determine consisting of：Methane content is 97.42%（Percentage by volume）, carbon dioxide content is 2.57%（Body
Product percentage）, water vapour content is 0.01%（Percentage by volume）；From the top of stripping stage 101 through the discharge gas of valve 213
Flow is 5.10 L/min, CO2Content is 96.94%（Percentage by volume）；According to People's Republic of China's geological and mineral industry mark
Quasi- DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from the bottom of stripping section 102
The CO of the solution of portion's discharge2Content is 20.10 mg/L.
The operation temperature on absorption tower 203 is 20~22 DEG C in the present embodiment, and carbon dioxide content exists in the product gas of acquisition
Less than 3%, disclosure satisfy that the requirement of compressed natural gas used as vehicle fuel technical standard.
Embodiment 6：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the TEG monomethyl ether aqueous solution, its reclaimed water is 3 with the mass ratio of TEG monomethyl ether:
2, it is not provided with handpiece Water Chilling Units 206, ambient temperature is 25 DEG C, the inlet opening upper limb of liquid sealing pipe 105 and the distance on the top of discharging tube 104
H is 2.5 meters, and 101 high 4.4 meters of stripping stage is outer, the other the same as in Example 1, rich CH4Gas is from the Base top contact on absorption tower 203 through drying
Afterwards as product gas store, determine consisting of：Methane content is 96.95%（Percentage by volume）, carbon dioxide content is
3.04%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）；According to People's Republic of China's geological and mineral row
Industry standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from stripping section
The CO of the solution of 102 bottoms discharge2Content is 16.85 mg/L.
Embodiment 7：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the diethylene glycol dimethyl ether aqueous solution, its reclaimed water is 1 with the mass ratio of diethylene glycol dimethyl ether:
1, the inlet opening upper limb of liquid sealing pipe 105 is 3.0 meters apart from H with the top of discharging tube 104, and 101 high 5 meters of stripping stage is outer, and other are same
Embodiment 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, determine consisting of：Methane
Content is 98.46%（Percentage by volume）, carbon dioxide content is 1.53%（Percentage by volume）, water vapour content is 0.01%（Body
Product percentage）；From the top of stripping stage 101 through valve 213 discharge gas flow be 4.99 L/min, CO2Content is
97.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《Underground water
Matter method of inspection titration measuring free carbon dioxide》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Content is
28.40 mg/L。
Embodiment 8：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the TRIGLYME aqueous solution, its reclaimed water is 4 with the mass ratio of TRIGLYME:
Outside 1, the other the same as in Example 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, determines its group
Turn into：Methane content is 97.70%（Percentage by volume）, carbon dioxide content is 1.29%（Percentage by volume）, water vapour content
It is 0.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《Underground water
Matter method of inspection titration measuring free carbon dioxide》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Content is
15.41 mg/L。
Embodiment 9：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the tetraethyleneglycol dimethyl ether aqueous solution, its reclaimed water is 4 with the mass ratio of tetraethyleneglycol dimethyl ether:
Outside 1, the other the same as in Example 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, determines its group
Turn into：Methane content is 98.46%（Percentage by volume）, carbon dioxide content is 1.53%（Percentage by volume）, water vapour content
It is 0.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《Underground water
Matter method of inspection titration measuring free carbon dioxide》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Content is
16.05 mg/L。
Embodiment 10：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is 1- (2- methoxyl group -1- methyl ethoxies) isopropanol water solution, its reclaimed water and 1- (2- methoxies
Base -1- methyl ethoxies) isopropanol mass ratio be 4:Outside 1, the other the same as in Example 1, rich CH4Top of the gas from absorption tower 203
Draw after drying as product gas store, determine consisting of：Methane content is 98.12%（Percentage by volume）, carbon dioxide
Content is 1.87%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）；According to People's Republic of China's geology
Mineral products professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from gas
Carry the CO of the solution of the bottom of section 102 discharge2Content is 16.25 mg/L.
Embodiment 11：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is double (2- methoxy-propyls) ether aqueous solution, the matter of its reclaimed water and double (2- methoxy-propyls) ethers
Amount is than being 4:Outside 1, the other the same as in Example 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203,
Determine consisting of：Methane content is 98.05%（Percentage by volume）, carbon dioxide content is 1.94%（Percentage by volume）, water
Vapor content is 0.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-
1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from the solution of the bottom of stripping section 102 discharge
CO2Content is 13.66 mg/L.
Embodiment 12：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is the aqueous solution containing diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, its reclaimed water, diethyl two
Alcohol monomethyl ether, the mass ratio of triethylene glycol monomethyl ether are 8:1:1, inlet opening upper limb and the top of discharging tube 104 of liquid sealing pipe 105
It it is 1.5 meters apart from H, 101 high 3.4 meters of stripping stage is outer, the other the same as in Example 1, rich CH4Gas is passed through from the Base top contact on absorption tower 203
After drying as product gas store, determine consisting of：Methane content is 97.69%（Percentage by volume）, carbon dioxide content is
2.30%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）；According to People's Republic of China's geological and mineral row
Industry standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from stripping section
The CO of the solution of 102 bottoms discharge2Content is 12.71 mg/L.
Embodiment 13：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used for containing diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, TEG monomethyl ether it is water-soluble
Liquid, the mass ratio of its reclaimed water, diethylene glycol monomethyl ether, triethylene glycol monomethyl ether and TEG monomethyl ether is 7:1:1:1, it is extraneous
Temperature is 10~10 DEG C, and the inlet opening upper limb of liquid sealing pipe 105 is 1.5 meters, stripping stage 101 apart from H with the top of discharging tube 104
3.4 meters high outer, the other the same as in Example 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, is surveyed
It is fixed consisting of：Methane content is 98.30%（Percentage by volume）, carbon dioxide content is 1.69%（Percentage by volume）, water steaming
Gas content is 0.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993
《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Contain
It is 18.60 mg/L to measure.
Embodiment 14：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is to contain diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, diethylene glycol dimethyl ether, three second two
The aqueous solution of diethylene glycol dimethyl ether, its reclaimed water, diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, diethylene glycol dimethyl ether, triethylene glycol
The mass ratio of dimethyl ether is 6:1:1:1:1, ambient temperature is 5~15 DEG C outer, the other the same as in Example 1, rich CH4Gas is from absorption tower
203 Base top contact after drying as product gas store, determine consisting of：Methane content is 98.64%（Volume basis
Number）, carbon dioxide content is 1.35%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）；According to middle Chinese
People republic geological and mineral professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring dissociates dioxy
Change carbon》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Content is 22.53 mg/L.
Embodiment 15：The present embodiment part same as Example 1 is repeated no more, and difference is：
Except the absorbent for being used is to contain diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, TEG monomethyl ether, three second two
The aqueous solution of diethylene glycol dimethyl ether and tetraethyleneglycol dimethyl ether, its reclaimed water, diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, tetrem two
The mass ratio of alcohol monomethyl ether, TRIGLYME and tetraethyleneglycol dimethyl ether is 14:2:1:1:1:1, ambient temperature be 5~
15 DEG C outer, the other the same as in Example 1, rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, is determined
Consisting of：Methane content is 98.72%（Percentage by volume）, carbon dioxide content is 1.27%（Percentage by volume）, vapor
Content is 0.01%（Percentage by volume）；According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《Ground
Lower water examination method titration measuring free carbon dioxide》Determine the CO of the solution from the discharge of the bottom of stripping section 1022Content
It is 25.29 mg/L.
Two kinds of solvents are miscible, and to together, their molecular arrangement will change, and no longer be to be closely spaced mode, but
Every arrangement, so more difficult crystallization, i.e. freezing point reduction.In the pressurizing absorption purification biogas mistake described in embodiment 14~17
Cheng Zhong, drop freezing point agent effect a kind of than addition becomes apparent when adding two or more drop freezing point agent, reduces equipment and pipeline
The risk of interior icing.
Embodiment 16：The present embodiment part same as Example 1 is repeated no more, and difference is：
Ultrasonic vibration box is provided with the bottom surface of every block of column plate of stripping stage 101, the ultrasonic vibration box power is 10 watts, frequency
Rate is 40 kHz；Mounting means and CN201520937365.7 of the ultrasonic vibration box on column plate《Pure natural pond is eluted for pressure (hydraulic) water
The desorption apparatus of gas》In the ultrasonic vibration box mounting means mentioned it is identical.
The wind speed that air blower 215 blasts air from the lower end of stripping section 102 is 14 L/min.
Rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, determine consisting of：Methane
Content is 97.55%（Percentage by volume）, carbon dioxide content is 2.44%（Percentage by volume）, water vapour content is 0.01%（Body
Product percentage）；The carbon dioxide flow discharged from the top of stripping stage 101 is 5.40 L/min；According to the People's Republic of China (PRC)
Geological and mineral professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine
From the CO of the solution of the bottom of stripping section 102 discharge2Content is 9.60 mg/L.
In the pressurizing absorption purification process of methane described in the present embodiment, stripping stage 101 is accelerated using ultrasonic wave
Interior solution stripping CO2Process, make enter stripping section 102 solution in CO2Concentration reduction, therefore discharged from the bottom of stripping section 102
Solution stripping obtain more preferably, can not only reclaim more carbon dioxide, and the air mass flow of stripping section 102 can be reduced.
Embodiment 17：The present embodiment part same as Example 1 is repeated no more, and difference is：
In addition to only ultrasonic vibration box is provided with bottom two pieces of bottom surfaces of column plate of stripping stage 101, other same embodiments
16.Rich CH4Gas is stored as product gas after drying from the Base top contact on absorption tower 203, determine consisting of：Methane content is
97.35%（Percentage by volume）, carbon dioxide content is 2.64%（Percentage by volume）, water vapour content is 0.01%（Volume basis
Number）；The carbon dioxide flow discharged from the top of stripping stage 101 is 5.25 L/min；According to People's Republic of China's geology ore deposit
Produce professional standard DZT 0064.47-1993《Groundwater quality method of inspection titration measuring free carbon dioxide》Determine from air lift
The CO of the solution of 102 bottoms of section discharge2Content is 10.05 mg/L.
Claims (9)
1. a kind of to desorb air lift coupled, it is characterized in that it is made up of two sections, epimere is stripping stage, and hypomere is stripping section,
Dividing plate is provided between stripping stage and stripping section, the discharging tube of dividing plate is provided through on dividing plate, be provided with outside discharging tube
Dividing plate is fixed in liquid sealing pipe, the top seal bottom of liquid sealing pipe, and the lower end of liquid sealing pipe is provided with inlet opening；In stripping stage
Top is provided with inlet and gas outlet, and stripping section top is provided with exhaust outlet bottom is provided with air inlet and leakage fluid dram.
2. it is according to claim 1 to desorb air lift coupled, it is characterized in that the inlet opening upper limb of liquid sealing pipe and discharging tube top
The distance at end is 0.5~3.0 meter.
3. it is according to claim 1 to desorb air lift coupled, it is characterized in that the stripping stage uses plate column, and in column plate
Bottom surface on be provided with ultrasonic vibration box.
4. the technique side that the desorption air lift coupled described in a kind of usage right requirement 1 carries out pressurizing absorption purification biogas
Method, it is characterized in that it comprises the following steps：Absorption tower will be sent into after biogas pressurization and cooling, absorbent enters from absorption tower top
Enter, biogas is inversely contacted with absorbent from bottom to top in absorption tower, rich CH4Gas is discharged from the top on absorption tower, after drying
Storage；Enter the CH that flash column will dissolve from the solution for absorbing tower bottom discharge4With part CO2Discharge, this part gaseous mixture
Body returns air accumulator, and participation washing is separated again with unstripped gas mixing again；Enter desorption air lift coupling from the solution of flash column discharge
Tower, pressure drops to 0.1 MPa from flashing pressure, and the carbon dioxide for desorbing is discharged from the top of stripping stage；Afterwards from desorption
The solution of section discharge enters stripping section through discharging tube, and stripping regeneration is carried out using air, returns to absorption tower as absorbent afterwards；
The absorbent is made up of water and drop freezing point agent.
5. the process of pressurizing absorption purification biogas according to claim 4, it is characterized in that drop freezing point agent
For diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, TEG monomethyl ether, diethylene glycol dimethyl ether, TRIGLYME,
One kind or two in tetraethyleneglycol dimethyl ether, 1- (2- methoxyl group -1- methyl ethoxies) isopropanols and double (2- methoxy-propyls) ethers
Plant or various mixtures.
6. the process of pressurizing absorption purification biogas according to claim 5, it is characterized in that drop freezing point agent
It is diethylene glycol monomethyl ether, triethylene glycol monomethyl ether, TEG monomethyl ether, TRIGLYME and tetraethyleneglycol dimethyl ether
The mixture of middle one or two or more.
7. the process of pressurizing absorption purification biogas according to claim 4, it is characterized in that water and drop freezing point agent
Mass ratio be 9:1~1:1.
8. the process of pressurizing absorption purification biogas according to claim 7, it is characterized in that water and drop freezing point agent
Mass ratio be 4:1~3:2.
9. the process of pressurizing absorption purification biogas according to claim 4, it is characterized in that the desorption air lift
The stripping stage of coupled uses plate column, and is provided with ultrasonic vibration box on the bottom surface of column plate.
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