CN107019995A - The method and vacuum desorption discharge system of purifying biogas are washed for pressure (hydraulic) water - Google Patents
The method and vacuum desorption discharge system of purifying biogas are washed for pressure (hydraulic) water Download PDFInfo
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- CN107019995A CN107019995A CN201710427813.2A CN201710427813A CN107019995A CN 107019995 A CN107019995 A CN 107019995A CN 201710427813 A CN201710427813 A CN 201710427813A CN 107019995 A CN107019995 A CN 107019995A
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- desorber
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 193
- 238000003795 desorption Methods 0.000 title claims abstract description 64
- 238000000034 method Methods 0.000 title claims abstract description 43
- 238000010521 absorption reaction Methods 0.000 claims abstract description 87
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 87
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims abstract description 63
- 238000003860 storage Methods 0.000 claims abstract description 48
- 229910002092 carbon dioxide Inorganic materials 0.000 claims abstract description 46
- 239000001569 carbon dioxide Substances 0.000 claims abstract description 31
- 230000006837 decompression Effects 0.000 claims abstract description 30
- 230000006835 compression Effects 0.000 claims abstract description 21
- 238000007906 compression Methods 0.000 claims abstract description 21
- 238000005406 washing Methods 0.000 claims abstract description 16
- 238000007701 flash-distillation Methods 0.000 claims abstract description 12
- 238000010079 rubber tapping Methods 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 21
- 238000007599 discharging Methods 0.000 claims description 19
- 239000000047 product Substances 0.000 claims description 16
- 238000001816 cooling Methods 0.000 claims description 13
- 238000011049 filling Methods 0.000 claims description 12
- 229910001220 stainless steel Inorganic materials 0.000 claims description 12
- 239000010935 stainless steel Substances 0.000 claims description 12
- 239000000945 filler Substances 0.000 claims description 11
- RGCLLPNLLBQHPF-HJWRWDBZSA-N phosphamidon Chemical group CCN(CC)C(=O)C(\Cl)=C(/C)OP(=O)(OC)OC RGCLLPNLLBQHPF-HJWRWDBZSA-N 0.000 claims description 11
- 239000012530 fluid Substances 0.000 claims description 10
- 239000000463 material Substances 0.000 claims description 10
- 238000012856 packing Methods 0.000 claims description 7
- 238000000926 separation method Methods 0.000 claims description 6
- 239000013589 supplement Substances 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims 1
- 230000001737 promoting effect Effects 0.000 claims 1
- 238000002156 mixing Methods 0.000 abstract description 3
- 239000007789 gas Substances 0.000 description 41
- 229960004424 carbon dioxide Drugs 0.000 description 28
- 238000005265 energy consumption Methods 0.000 description 12
- 238000000746 purification Methods 0.000 description 10
- 239000003673 groundwater Substances 0.000 description 6
- 229910052500 inorganic mineral Inorganic materials 0.000 description 6
- 238000007689 inspection Methods 0.000 description 6
- 239000011707 mineral Substances 0.000 description 6
- 238000004448 titration Methods 0.000 description 6
- 238000010586 diagram Methods 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 238000005262 decarbonization Methods 0.000 description 3
- 238000005261 decarburization Methods 0.000 description 3
- 239000002904 solvent Substances 0.000 description 3
- -1 Physical Absorption Substances 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 230000000740 bleeding effect Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000003345 natural gas Substances 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 238000011069 regeneration method Methods 0.000 description 2
- OAXIUZFXLOZILE-UHFFFAOYSA-N 2-(2-methoxyethoxy)propane Chemical class COCCOC(C)C OAXIUZFXLOZILE-UHFFFAOYSA-N 0.000 description 1
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- XTHFKEDIFFGKHM-UHFFFAOYSA-N Dimethoxyethane Chemical compound COCCOC XTHFKEDIFFGKHM-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
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002090 carbon oxide 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
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- LYCAIKOWRPUZTN-UHFFFAOYSA-N ethylene glycol Natural products OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 239000012528 membrane Substances 0.000 description 1
- 239000002754 natural gas substitute Substances 0.000 description 1
- 231100000252 nontoxic Toxicity 0.000 description 1
- 230000003000 nontoxic effect Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 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
- B01D53/1456—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
- B01D53/1425—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
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Organic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Treating Waste Gases (AREA)
Abstract
A kind of method and vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine, and heat exchanger, drier, booster pump, flash column is depressured tower, desorber, storage tank, desorber vavuum pump, desorber Vacuum discharge pump；Absorption tower is sent into after biogas is cooled down through the pressurization of Marsh gas compression machine through heat exchanger；Water cools through handpiece Water Chilling Units, pressurizeed through booster pump after enter from absorption tower top, biogas is inversely contacted with water from bottom to top in absorption tower, rich CH4Gas is discharged from the top on absorption tower；Enter flash column from the water for absorbing tower bottom discharge, the CH discharged4And CO2Mixed gas returns air accumulator, and participation washing is separated again with unstripped gas mixing again；Enter decompression tower, top discharge of the carbon dioxide desorbed from decompression tower from the water of flash distillation tower bottom discharge；The water from decompression tower bottom discharge enters desorber afterwards, and the gas desorbed is discharged at the top of the desorber, enters storage tank from the water of desorption tower bottom discharge through desorber Vacuum discharge pump.
Description
Technical field
This programme is related to gas-liquid mass transfer technical field, more particularly to a kind of washes the method for purifying biogas and true for pressure (hydraulic) water
Sky desorption discharge system.
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
Change purification after can as natural gas substitute.Marsh gas purifying purification relates generally to the processes 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 CO2With dissolving of the hydro carbons in physical solvent
The difference of degree completes decarburization task, and conventional physical solvent has water, methanol, many glycol dimethyl ethers, propene carbonate, N- methyl
Pyrrolidones, many Ethylene Glycol Methyl isopropyl ethers and sulfolane etc., and the washing process that pressurizes be current industrialized European use compared with
Many Methane decarbonization methods, then several solvents be used for selexol process decarburization.
The principle that pressure (hydraulic) water washes purifying biogas is under an increased pressure, by CO2It is dissolved in the water and reduces it in biogas
Content, its process is usually：Absorption tower is sent into after biogas is pressurizeed, water enters as absorbent from top, in absorption tower
Biogas is contacted with flow reversal from bottom to top, most of CO in biogas2With a small amount of CH4It is dissolved in water, rich CH4Gas is from absorption tower
Upper end be brought out, obtain bio-natural gas after being further dried；Entering flash column from the water for absorbing tower bottom discharge will dissolve
CH in water4With most of CO2Discharged from water, this part mixed gas is mixed with unstripped gas again to be participated in washing again
Wash separation；The water discharged from flash column is desorbed into stripping tower, and stripping regeneration is carried out using decompression or air（Stripping is also referred to as
For air lift）, return 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 be removed simultaneously2And H2S；Technique is simple, and operation temperature is low, does not consume chemical reagent and steam, mistake
Cheng Huanbao.
In methane purification system, decompression desorption method is simple to operate, power consumption is small, and can reclaim the dioxy of higher degree
Change carbon, but the carbon dioxide after the completion of decompression desorption in absorbing liquid is still in saturation state, if desorption liquid returns to absorption tower
The efficiency of absorption will be influenceed by re-using；Air stripping can be complete by the carbon dioxide eliminating in absorbing liquid, but profit completely
Very big air mass flow is then needed with air stripping desorption, the energy consumption of blower fan can be increased.Therefore CN101837227A discloses one
Absorption liquid desorption method in methane purification system is planted, absorbing liquid is dropped by first order depressurization desorption, pressure from 0.6~1.6 MPa
To 0.1 MPa, then the most of carbon dioxide of removing is desorbed by second level air stripping, after the completion of desorption two in absorbing liquid
Carbonoxide is removed completely substantially, is recycled to absorption tower and is continued with.Although the technique can reclaim the carbon dioxide of higher degree,
But the method for also using air stripping desorption, introduces large quantity of air, and the amount of heat in air is transmitted into feedwater, these
Water needs to enter back into absorption tower after cooling, and temperature-fall period needs to consume big energy.
ZL201520937365.7 discloses a kind of desorption apparatus that purifying biogas is washed for pressure (hydraulic) water, is provided with ultrasonic wave
When Vibration Box washes purifying biogas to strengthen desorption process, for pressure (hydraulic) water and prepares bio-natural gas technique, desorption is thorough, can avoid
The stripping process used in old process.But, found in actual experiment due to being limited by vapor liquid equilibrium, even if employing
Still a small amount of CO is contained in intensified by ultrasonic wave desorption process, the water after desorption2, that is, desorb still not thorough.
The content of the invention
It is an object of the invention to the deficiency for making up prior art, there is provided a kind of method for washing purifying biogas for pressure (hydraulic) water
And vacuum desorption discharge system, to reduce due to caused by desorption process the problem of methane purification technology high energy consumption.
A kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine, and heat exchanger is done
Dry device, booster pump, flash column is depressured tower, desorber, storage tank, desorber vavuum pump, desorber Vacuum discharge pump.With biogas
The heat exchanger of compressor outlet connection, the absorption tower connected with heat exchanger exit passes through valve and drier at the top of absorption tower
Connection.Storage tank delivery port is connected by booster pump with absorption tower, is absorbed tower bottom and is passed through pipeline and valve and flash column top
Valve is provided with the top of connection, flash column to connect with air accumulator, the top that flash distillation tower bottom passes through pipeline and valve and decompression tower
Connection；Decompression top of tower is provided with valve and atmosphere, and decompression tower bottom is connected by pipeline with desorber top.In desorption
Top of tower is connected with desorber vavuum pump, desorber vavuum pump and atmosphere；Desorber bottom is provided with valve to send into
Air, desorption tower bottom is connected with desorber Vacuum discharge pump, and desorber Vacuum discharge pump is connected by pipeline with storage tank.
The specific feature of this programme also has, and also includes handpiece Water Chilling Units, and storage tank delivery port is connected with handpiece Water Chilling Units, cold water
Unit is connected by booster pump with absorption tower.
Water supply valve is provided with storage tank.
Desorber is packed tower, 0.2 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, is filled out
Expect that section is high 2.0 meters.
Absorption tower is packed tower, 0.1 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, is filled out
Expect that section is high 2.0 meters.
Flash column is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces.
Decompression tower is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces.
The present invention also provides a kind of method for washing purifying biogas for pressure (hydraulic) water, and it comprises the following steps：
Biogas is forced into 0.8 MPa through Marsh gas compression machine, 20 DEG C are cooled to through heat exchanger, absorption tower, biogas stream are sent into afterwards
Measure as 20 L/min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units, 0.8 MPa is forced into through booster pump, enters afterwards from absorption tower top, water-carrying capacity
For 2.5 L/min, biogas is inversely contacted with water from bottom to top in absorption tower, rich CH4Gas is arranged from the top on absorption tower through valve
Go out, stored after being dried through drier as product gas；
The Stress control that the water discharged from absorption tower bottom enters in flash column, flash column through valve is in 0.35 MPa, in flash distillation
In tower, water is by the CH of dissolving4With part CO2Discharge, it is again mixed with unstripped gas that this part mixed gas returns air accumulator through valve
Close and participate in washing separation again；Enter from the water of flash distillation tower bottom discharge through valve and be depressured tower, pressure drops to 0.1 MPa, desorbs
Discharged through valve at the top of carbon dioxide out from decompression tower；
The water from decompression tower bottom discharge through valve enters desorber afterwards, and the gas desorbed is at the top of desorber through valve
Discharge, after discharged through desorber vavuum pump, vacuum is maintained at 0.08 MPa in desorber, in addition through valve to desorber with
1.2 L/min wind speed blasts air, air inversely contacted with water from bottom to top after together with the carbon dioxide desorbed from
Discharged through valve at the top of desorber；
Through valve and desorber Vacuum discharge pump enter storage tank from the water of desorption tower bottom discharge, afterwards by through handpiece Water Chilling Units
Absorption tower is returned to after cooling and booster pump supercharging, supplements running water to maintain the liquid level of storage tank by Valve controlling in addition.
The present invention also provides a kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, and it includes Marsh gas compression
Machine, heat exchanger, drier, booster pump, flash column, be depressured tower, desorber, storage tank, desorber vavuum pump, the first discharge tank and
Second discharge tank.With the heat exchanger of Marsh gas compression machine outlet, the absorption tower connected with heat exchanger exit, at the top of absorption tower
Connected by valve with drier.Storage tank delivery port is connected by booster pump with absorption tower, absorb tower bottom by pipeline and
Valve is connected with flash column top, and be provided with valve at the top of flash column connects with air accumulator, and flash distillation tower bottom passes through pipeline and valve
Door is connected with being depressured the top of tower；Decompression top of tower is provided with valve and atmosphere, and decompression tower bottom passes through pipeline and desorption
Tower top is connected.Connected at the top of desorber with desorber vavuum pump, desorber vavuum pump and atmosphere.
The first discharge tank inlet is provided with the top of the first discharge tank, the top of the first discharge tank is provided with first
Discharge tank air inlet and the first discharge tank exhaust outlet, the first discharge tank leakage fluid dram is provided with the bottom of the first discharge tank.First
The first intake valve communicated with the external world, the pipe after the first discharge tank leakage fluid dram are set on the pipeline before discharge tank air inlet
The first tapping valve is provided with road, first row air valve is provided with the pipeline after the first discharge tank exhaust outlet.
The second discharge tank inlet is provided with the top of the second discharge tank, the top of the second discharge tank is provided with second
Discharge tank air inlet and the second discharge tank exhaust outlet, the second discharge tank leakage fluid dram is provided with the bottom of the second discharge tank.Second
The second intake valve communicated with the external world, the pipe after the second discharge tank leakage fluid dram are set on the pipeline before discharge tank air inlet
The second tapping valve is provided with road, second row air valve is provided with the pipeline after the second discharge tank exhaust outlet.
Desorber gas outlet is provided with the top of desorber, the top of desorber is provided with desorber charging aperture, in solution
The bottom for inhaling tower is provided with desorber bleed ports, and the bottom of desorber is provided with desorber discharging opening.
Pipeline after desorber discharging opening is divided into two-way, is connected all the way by the first outlet valve and the first discharge tank inlet
It is logical；Another road is connected by the second outlet valve with the second discharge tank inlet.
The discharging pipeline of first discharge tank and the second discharge tank is connected after converging with storage tank.
The pipeline after pipeline and the second discharge tank exhaust outlet after first discharge tank exhaust outlet converges rear and desorber
Bleed ports are connected.
Desorber material inlet valve, the pipeline after desorber gas outlet are set on the pipeline before desorber charging aperture
On set gradually desorber outlet valve and desorber vavuum pump.
The specific feature of this programme also has, and also includes handpiece Water Chilling Units, and storage tank delivery port is connected with handpiece Water Chilling Units, cold water
Unit is connected by booster pump with absorption tower.
The height of first discharge tank and the second discharge tank is 0.2 meter, and internal diameter is 0.15 meter.
Water supply valve is provided with storage tank.
Absorption tower is packed tower, 0.1 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, is filled out
Expect that section is high 2.0 meters；
Flash column is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Decompression tower is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces；
Desorber is packed tower, 0.2 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, packing section
It is high 2.0 meters.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 28~30 DEG C.
The present invention also provides a kind of method for washing purifying biogas for pressure (hydraulic) water, and it is using said system equipment and including such as
Lower step：
Biogas is forced into 0.8 MPa through Marsh gas compression machine, 20 DEG C are cooled to through heat exchanger, absorption tower, biogas stream are sent into afterwards
Measure as 20 L/min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units, 0.8 MPa is forced into through booster pump, enters afterwards from absorption tower top, water-carrying capacity
For 2.5 L/min, biogas is inversely contacted with water from bottom to top in absorption tower, rich CH4Gas is arranged from the top on absorption tower through valve
Go out, stored after being dried through drier as product gas；
The Stress control that the water discharged from absorption tower bottom enters in flash column, flash column through valve is in 0.35 MPa, in flash distillation
In tower, water is by the CH of dissolving4With part CO2Discharge, it is again mixed with unstripped gas that this part mixed gas returns air accumulator through valve
Close and participate in washing separation again；Enter from the water of flash distillation tower bottom discharge through valve and be depressured tower, pressure drops to 0.1 MPa, desorbs
Discharged through valve at the top of carbon dioxide out from decompression tower；
The water from decompression tower bottom discharge enters desorber afterwards, and the gas desorbed is at the top of desorber through desorber outlet
Valve is discharged, after discharged through desorber vavuum pump, vacuum is maintained at 0.08 MPa in desorber.
The first outlet valve, first row air valve, the second intake valve and the second tapping valve be open mode, the first intake valve,
When first tapping valve, the second outlet valve and second row air valve are closed mode, desorber discharging opening row of the water from desorption tower bottom
Go out the air entered in the first discharge tank, the first discharge tank through the first outlet valve to enter desorber through first row air valve and with water enter
Row gas-liquid mass transfer is to promote desorption, and the water in the second discharge tank is discharged through the second tapping valve, and extraneous air is through the second air inlet
Valve enters the second discharge tank；
It is closed mode, the first intake valve, first in the first outlet valve, first row air valve, the second intake valve and the second tapping valve
When tapping valve, the second outlet valve and second row air valve are open mode, water goes out from the discharging opening discharge of desorption tower bottom through second
Expect that the air that valve enters in the second discharge tank, the second discharge tank enters desorber through second row air valve and carries out gas-liquid mass transfer with water
To promote desorption, and the water in the first discharge tank is discharged through the first tapping valve, and extraneous air enters first through the first intake valve
Discharge tank；
Replace the on off state of switch valve successively, on off state is kept for 1 minute each time, realize that vacuum desorption discharges.
The water discharged afterwards from the first discharge tank and the second discharge tank enters storage tank, and water is delivered to cooling-water machine by storage tank
Absorption tower is returned to after group cooling and booster pump supercharging.
The beneficial effect of this programme is：This programme washes purifying biogas process using the pressure (hydraulic) water of vacuum desorption, desorbs
Thoroughly, and system introduce air capacity greatly reduce, the heat of introducing greatly reduces, and vacuum will also result in part water evaporation and reach
And absorption tower purifying biogas can be entered after need not cooling with the water in refrigeration, therefore system or cooling slightly,
Greatly reduce energy consumption for cooling；The method switched using switch valve carries out Vacuum discharge, it is to avoid use Vacuum discharge pump, energy
Consumption reduction；Air, which enters, to be entered desorber from desorber bottom again after discharge tank and carries out gas-liquid mass transfer with water to promote solution
Inhale, inhale hydrolysis thorough.
Brief description of the drawings
Fig. 1 is the vacuum desorption discharge system schematic diagram that purifying biogas is washed for pressure (hydraulic) water.
Fig. 2 is the process flow diagram of the pressurizing absorption purification biogas of prior art.
Fig. 3 is the vacuum desorption discharge system vacuum desorption partial schematic diagram that purifying biogas is washed for pressure (hydraulic) water.
Fig. 4 is the vacuum desorption discharge system schematic diagram that purifying biogas is washed for pressure (hydraulic) water.
In figure：101- Marsh gas compression machines；102- heat exchangers；103- absorption towers；104- valves；105- driers；106- is cold
Water dispenser group；107- booster pumps；108- valves；109- flash columns；110- valves；111- valves；112- is depressured tower；113- valves；
114- desorber material inlet valves；115- desorbers；116- desorber outlet valves；117- desorber vavuum pumps；118- valves；
119- valves；120- desorber Vacuum discharge pumps；121- storage tanks；122- water supply valves；201- feed pumps；202- air blowers；
The outlet valves of 301- first；The intake valves of 302- first；The discharge tanks of 303- first；The tapping valves of 304- first；305- first row air valves；
The outlet valves of 306- second；The intake valves of 307- second；The discharge tanks of 308- second；The tapping valves of 309- second；310- second row air valves.
Embodiment
This programme is described in further detail below in conjunction with the accompanying drawings and by specific embodiment.
Embodiment 1：
As shown in figure 1, a kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine 101,
Heat exchanger 102, drier 105, handpiece Water Chilling Units 106, booster pump 107, flash column 109 is depressured tower 112, desorber 115, water storage
Case 121, desorber vavuum pump 117, desorber Vacuum discharge pump 120.With the heat exchanger 102 of the outlet of Marsh gas compression machine 101,
With the absorption tower 103 of the outlet of heat exchanger 102, connected at the top of absorption tower 103 by valve 104 with drier 105.Water storage
The delivery port of case 121 is connected with handpiece Water Chilling Units 106, and handpiece Water Chilling Units 106 are connected by booster pump 107 with absorption tower 103, absorption tower
103 bottoms are connected by pipeline and valve 108 with the top of flash column 109, and the top of flash column 109 is provided with valve 110 and gas storage
Tank is connected, and the bottom of flash column 109 is connected by pipeline and valve 111 with being depressured the top of tower 112；The top of tower 112 is depressured to set
There are valve 113 and atmosphere, the decompression bottom of tower 112 is connected by pipeline and desorber material inlet valve 114 with the top of desorber 115
It is logical.Connected at the top of desorber 115 by desorber outlet valve 116 with desorber vavuum pump 117, desorber vavuum pump 117
With atmosphere；Desorber bottom is provided with valve 118 and passes through valve 119 and desorption to send into air, the bottom of desorber 115
Tower Vacuum discharge pump 120 is connected, and desorber Vacuum discharge pump 120 is connected by pipeline with storage tank 121.
Water supply valve 122 is provided with storage tank 121.
Wherein：Absorption tower 103 is packed tower, 0.1 meter of tower internal diameter, filling diameter and the high stainless steel θ nets all for 10 millimeters
Ring filler, packing section is high 2.0 meters；
Flash column 109 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Decompression tower 112 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces；
Desorber 115 is packed tower, 0.2 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, is filled out
Expect that section is high 2.0 meters.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 28~30 DEG C.
A kind of method for washing purifying biogas for pressure (hydraulic) water, it comprises the following steps：
Biogas is forced into 0.8 MPa through Marsh gas compression machine 101,20 DEG C are cooled to through heat exchanger 102, absorption tower is sent into afterwards
103, biogas flow is 20 L/min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units 106, is forced into 0.8 MPa through booster pump 107, enters afterwards from the top of absorption tower 103
Enter, water-carrying capacity is 2.5 L/min, and biogas is inversely contacted with water from bottom to top in absorption tower 103, rich CH4Gas is from absorption tower 103
Top discharged through valve 104, through drier 105 dry after stored as product gas；
The Stress control that the water discharged from the bottom of absorption tower 103 enters in flash column 109, flash column 109 through valve 108 is 0.35
MPa, in flash column 109, water is by the CH of dissolving4With part CO2Discharge, this part mixed gas is through 110 times gas storage of valve
Tank participates in washing with unstripped gas mixing again and separated again；The water discharged from the bottom of flash column 109 enters through valve 111 is depressured tower
112, pressure drops to 0.1 MPa, and the top of the carbon dioxide desorbed from decompression tower 112 is discharged through valve 113；
Afterwards from the water discharged the bottom of tower 112 is depressured through desorber material inlet valve 114 into desorber 115, the gas desorbed
Body is discharged from the top of desorber 115 through desorber outlet valve 116, after discharged through desorber vavuum pump 117, it is true in desorber
Sky is maintained at 0.08 MPa, blasts air to desorber 115 with 1.2 L/min wind speed through valve 118 in addition, air is under
And on inversely contacted with water after together with the carbon dioxide desorbed from the top of desorber 115 through desorber outlet valve
116 discharges；
The water discharged from the bottom of desorber 115 enters storage tank 121 through valve 119 and desorber Vacuum discharge pump 120, after pass through
Cross and absorption tower 103 is returned to after handpiece Water Chilling Units 106 cool and booster pump 107 is pressurized, supplement is controlled certainly by water supply valve 122 in addition
Water is to maintain the liquid level of storage tank 121.
The energy consumption of handpiece Water Chilling Units 106 is 0.1 kW/h；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 discharge of the bottom of desorber 115
Water in CO2Content is 11.05 mg/L；By Wuhan four directions Gasboard-3200 type biogas analysis-e/or determinings product gas, it is constituted
For：Methane content is 96.40%（Percentage by volume）, carbon dioxide content is 3.59%（Percentage by volume）, water vapour content is
0.01%（Percentage by volume）.
The present embodiment washes purifying biogas process using the pressure (hydraulic) water of vacuum desorption, is contrasted with embodiment 3, desorbs more thorough
Methane content is higher in bottom, product gas, and required energy consumption for cooling is lower.
Embodiment 2：
The present embodiment part same as Example 1 is repeated no more, and difference is：
Ambient temperature is 15~18 DEG C；Water from the discharge of the bottom of desorber 115 is through valve 119 and desorber Vacuum discharge pump 120
Into storage tank 121, cool afterwards without handpiece Water Chilling Units 106 and absorption tower 103 is only returned to after the supercharging of booster pump 107, water
Temperature maintains 9.5~10.5 DEG C.
According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《The groundwater quality method of inspection
Titration measuring free carbon dioxide》CO in determining the water discharged from the bottom of desorber 1152Content is 11.20 mg/L；By force
Chinese four directions Gasboard-3200 types biogas analysis-e/or determining product gas consisting of：Methane content is 96.35%（Volume basis
Number）, carbon dioxide content is 3.64%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）.
The present embodiment washes purifying biogas process using the pressure (hydraulic) water of vacuum desorption, is contrasted with embodiment 4, desorbs more thorough
Methane content is higher in bottom, product gas, not using handpiece Water Chilling Units, reduces energy consumption for cooling.
Embodiment 3（Comparative example）：
As shown in Fig. 2 the technological process of the pressurizing absorption purification biogas of prior art, including Marsh gas compression machine 101, heat exchange
Device 102, absorption tower 103, drier 105, handpiece Water Chilling Units 106, booster pump 107, flash column 109 is depressured tower 112, desorber
115, storage tank 121, feed pump 201；Air blower 202.
This implementation use Marsh gas compression machine 101, heat exchanger 102, absorption tower 103, drier 105, handpiece Water Chilling Units 106,
Booster pump 107, flash column 109, decompression tower 112, desorber 115, storage tank 121 are same as Example 1.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 28~30 DEG C.
Marsh gas purifying purification process part same as Example 1 is repeated no more, and difference is：
From the water discharged the bottom of tower 112 is depressured through desorber material inlet valve 114 and feed pump 201 into desorber 115, desorb
The gas come is discharged from the top of desorber 115 through desorber outlet valve 116, in addition through air blower 202 to desorber 115 with 25
L/min wind speed blasts air, air inversely contacted with water from bottom to top after together with the carbon dioxide desorbed from desorption
Discharged through desorber outlet valve 116 at the top of tower 115；The water discharged from the bottom of desorber 115 through valve 119 enters storage tank
121, return to absorption tower 103 after being pressurized through the cooling of handpiece Water Chilling Units 106 and booster pump 107 afterwards.
The energy consumption of handpiece Water Chilling Units 106 is 0.35 kW/h；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 discharge of the bottom of desorber 115
Water in CO2Content is 13.70 mg/L；By Wuhan four directions Gasboard-3200 type biogas analysis-e/or determinings product gas, it is constituted
For：Methane content is 96.00%（Percentage by volume）, carbon dioxide content is 3.99%（Percentage by volume）, water vapour content is
0.01%（Percentage by volume）.
Embodiment 4（Comparative example）：
The present embodiment part same as Example 3 is repeated no more, and difference is：Ambient temperature is 15~18 DEG C.
The energy consumption of handpiece Water Chilling Units 106 is 0.28 kW/h；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 discharge of the bottom of desorber 115
Water in CO2Content is 13.50 mg/L；By Wuhan four directions Gasboard-3200 type biogas analysis-e/or determinings product gas, it is constituted
For：Methane content is 96.05%（Percentage by volume）, carbon dioxide content is 3.89%（Percentage by volume）, water vapour content is
0.01%（Percentage by volume）.
Embodiment 5：
As shown in figure 4, a kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine 101,
Heat exchanger 102, drier 105, handpiece Water Chilling Units 106, booster pump 107, flash column 109 is depressured tower 112, desorber 115, water storage
Case 121, desorber vavuum pump 117, the first discharge tank 303 and the second discharge tank 308.With the outlet of Marsh gas compression machine 101
Heat exchanger 102, the absorption tower 103 with the outlet of heat exchanger 102 passes through valve 104 and drier at the top of absorption tower 103
105 connections.The delivery port of storage tank 121 is connected with handpiece Water Chilling Units 106, and handpiece Water Chilling Units 106 pass through booster pump 107 and absorption tower 103
Connection, the bottom of absorption tower 103 is connected by pipeline and valve 108 with the top of flash column 109, and the top of flash column 109 is provided with valve
Door 110 is connected with air accumulator, and the bottom of flash column 109 is connected by pipeline and valve 111 with being depressured the top of tower 112；It is depressured tower
112 tops are provided with valve 113 and atmosphere, and the decompression bottom of tower 112 passes through pipeline and desorber material inlet valve 114 and desorption
The top of tower 115 is connected.Connected, desorbed with desorber vavuum pump 117 by desorber outlet valve 116 at the top of desorber 115
Tower vavuum pump 117 and atmosphere.
Water supply valve 122 is provided with storage tank 121.
As shown in figure 3, the first discharge tank inlet is provided with the top of the first discharge tank 303, in the first discharge tank 303
Top be provided with the first discharge tank air inlet and the first discharge tank exhaust outlet, is provided with the bottom of the first discharge tank 303
One discharge tank leakage fluid dram.Set on pipeline before first discharge tank air inlet with extraneous the first intake valve 302 communicated, the
The first tapping valve 304 is provided with pipeline after one discharge tank leakage fluid dram, on the pipeline after the first discharge tank exhaust outlet
It is provided with first row air valve 305.
The top of second discharge tank 308 is provided with the second discharge tank inlet, set on the top of the second discharge tank 308
There are the second discharge tank air inlet and the second discharge tank exhaust outlet, the second discharge tank row is provided with the bottom of the second discharge tank 308
Liquid mouthful.The second intake valve 307 communicated with the external world is set on the pipeline before the second discharge tank air inlet, in the second discharge tank row
The second tapping valve 309 is provided with pipeline after liquid mouthful, second is provided with the pipeline after the second discharge tank exhaust outlet
Air bleeding valve 310.
The top of desorber 115 is provided with desorber gas outlet, the top of desorber is provided with desorber charging aperture,
The bottom of desorber is provided with desorber bleed ports, and the bottom of desorber is provided with desorber discharging opening.
Pipeline after desorber discharging opening is divided into two-way, passes through the first outlet valve 301 and the first discharge tank feed liquor all the way
Mouth connection；Another road is connected by the second outlet valve 306 with the second discharge tank inlet.
The discharging pipeline of first discharge tank 303 and the second discharge tank 308 is connected after converging with storage tank 121.
The pipeline after pipeline and the second discharge tank exhaust outlet after first discharge tank exhaust outlet converges rear and desorber
Bleed ports are connected.
Desorber material inlet valve 114 is set on the pipeline before desorber charging aperture, after desorber gas outlet
Desorber outlet valve 116 and desorber vavuum pump 117 are set gradually on pipeline.
The height of the discharge tank 308 of first discharge tank 303 and second is 0.2 meter, and internal diameter is 0.15 meter.
Absorption tower 103 is packed tower, and 0.1 meter of tower internal diameter, filling diameter and height are all filled out for 10 millimeters of stainless steel Dixon ring
Material, packing section is high 2.0 meters；
Flash column 109 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Decompression tower 112 is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces；
Desorber 115 is packed tower, 0.2 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, is filled out
Expect that section is high 2.0 meters.
Methane content of bilogas is 53%（Percentage by volume）, carbon dioxide content is 47%（Percentage by volume）.
Ambient temperature is 28~30 DEG C.
A kind of method for washing purifying biogas for pressure (hydraulic) water, it is using said system equipment and comprises the following steps：
Biogas is forced into 0.8 MPa through Marsh gas compression machine 101,20 DEG C are cooled to through heat exchanger 102, absorption tower is sent into afterwards
103, biogas flow is 20 L/min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units 106, is forced into 0.8 MPa through booster pump 107, enters afterwards from the top of absorption tower 103
Enter, water-carrying capacity is 2.5 L/min, and biogas is inversely contacted with water from bottom to top in absorption tower 103, rich CH4Gas is from absorption tower 103
Top discharged through valve 104, through drier 105 dry after stored as product gas；
The Stress control that the water discharged from the bottom of absorption tower 103 enters in flash column 109, flash column 109 through valve 108 is 0.35
MPa, in flash column 109, water is by the CH of dissolving4With part CO2Discharge, this part mixed gas is through 110 times gas storage of valve
Tank participates in washing with unstripped gas mixing again and separated again；The water discharged from the bottom of flash column 109 enters through valve 111 is depressured tower
112, pressure drops to 0.1 MPa, and the top of the carbon dioxide desorbed from decompression tower 112 is discharged through valve 113；
Afterwards from the water discharged the bottom of tower 112 is depressured through desorber material inlet valve 114 into desorber 115, the gas desorbed
Body is discharged from the top of desorber 115 through desorber outlet valve 116, after discharged through desorber vavuum pump 117, it is true in desorber
Sky is maintained at 0.08 MPa.
It is open mode in the first outlet valve 301, first row air valve 305, the second intake valve 307 and the second tapping valve 309,
When first intake valve 302, the first tapping valve 304, the second outlet valve 306 and second row air valve 310 are closed mode, water is from desorption
The desorber discharging opening discharge of the bottom of tower 115 enters in the first discharge tank 303, the first discharge tank 303 through the first outlet valve 301
Air enters desorber 115 through first row air valve 305 and carries out gas-liquid mass transfer with water to promote to desorb, and the second discharge tank 308
In water discharged through the second tapping valve 309, extraneous air enters the second discharge tank 308 through the second intake valve 307；
It is closed mode, first in the first outlet valve 301, first row air valve 305, the second intake valve 307 and the second tapping valve 309
When intake valve 302, the first tapping valve 304, the second outlet valve 306 and second row air valve 310 are open mode, water is from desorber
The discharging opening discharge of 115 bottoms enters the second discharge tank 308 through the second outlet valve 306, and the air in the second discharge tank 308 is through the
Two air bleeding valves 310 enter desorber 115 and carry out gas-liquid mass transfer with water to promote desorption, and the water in the first discharge tank 303 is passed through
First tapping valve 304 is discharged, and extraneous air enters the first discharge tank 303 through the first intake valve 302；
Replace the on off state of switch valve successively, on off state is kept for 1 minute each time, realize that vacuum desorption discharges.
The water discharged afterwards from the first discharge tank 303 and the second discharge tank 308 enters storage tank 121, and storage tank 121 is by water
Absorption tower 103 is returned to after being delivered to the cooling of handpiece Water Chilling Units 106 and the supercharging of booster pump 107, supplement is controlled by water supply valve 122 in addition
Running water is to maintain the liquid level of storage tank 121.
The energy consumption of handpiece Water Chilling Units 106 is 0.11 kW/h；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 discharge of the bottom of desorber 115
Water in CO2Content is 9.89 mg/L；By Wuhan four directions Gasboard-3200 type biogas analysis-e/or determinings product gas, it is constituted
For：Methane content is 96.60%（Percentage by volume）, carbon dioxide content is 3.39%（Percentage by volume）, water vapour content is
0.01%（Percentage by volume）.
The present embodiment washes purifying biogas process using the pressure (hydraulic) water of vacuum desorption, is contrasted with embodiment 3, desorbs more thorough
Methane content is higher in bottom, product gas, and required energy consumption for cooling is lower, and avoids using Vacuum discharge pump.
Embodiment 6：
The present embodiment part same as Example 5 is repeated no more, and difference is：
Ambient temperature is 15~18 DEG C；From the bottom of desorber 115 discharge water through valve 119 enter storage tank 121, afterwards without
Handpiece Water Chilling Units 106 cool and absorption tower 103 are only returned to after the supercharging of booster pump 107, and water temperature maintains 9.5~10.5 DEG C.
According to People's Republic of China (PRC) geological and mineral professional standard DZT 0064.47-1993《The groundwater quality method of inspection
Titration measuring free carbon dioxide》CO in determining the water discharged from the bottom of desorber 1152Content is 9.95 mg/L；By Wuhan
Cubic Gasboard-3200 types biogas analysis-e/or determining product gas consisting of：Methane content is 96.55%（Percentage by volume）,
Carbon dioxide content is 3.44%（Percentage by volume）, water vapour content is 0.01%（Percentage by volume）.
The present embodiment washes purifying biogas process using the pressure (hydraulic) water of vacuum desorption, is contrasted with embodiment 4, desorbs more thorough
Methane content is higher in bottom, product gas, not using handpiece Water Chilling Units, reduces energy consumption for cooling, and avoids to go out using vacuum
Expect pump.
Claims (10)
1. a kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine, and heat exchanger is dried
Device, booster pump, flash column is depressured tower, desorber, storage tank, desorber vavuum pump, desorber Vacuum discharge pump；With biogas pressure
The heat exchanger of contracting machine outlet, the absorption tower connected with heat exchanger exit is connected at the top of absorption tower with drier；Storage tank
Delivery port is connected by booster pump with absorption tower, absorb tower bottom connect by pipeline with flash column top, flash column top and
Air accumulator is connected, and flash distillation tower bottom is connected by pipeline with being depressured the top of tower；Top of tower and atmosphere are depressured, bottom of towe is depressured
Portion is connected by pipeline with desorber top；It is characterized in that being connected at the top of desorber with desorber vavuum pump, desorber vavuum pump
With atmosphere；Air is sent into desorber bottom, and desorption tower bottom is connected with desorber Vacuum discharge pump, desorber Vacuum discharge
Pump is connected by pipeline with storage tank.
2. the vacuum desorption discharge system according to claim 1 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that, also wrap
Handpiece Water Chilling Units are included, storage tank delivery port is connected with handpiece Water Chilling Units, and handpiece Water Chilling Units are connected by booster pump with absorption tower.
3. the vacuum desorption discharge system according to claim 1 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that desorption
Tower is packed tower, 0.2 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, and packing section is high 2.0 meters.
4. the vacuum desorption discharge system according to claim 1 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that absorbing
Tower is packed tower, 0.1 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, and packing section is high 2.0 meters；
Flash column is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；Decompression tower be plate column, 0.12 meter of tower internal diameter, the number of plates is 8
Block.
5. a kind of method for washing purifying biogas for pressure (hydraulic) water, it comprises the following steps：
Biogas is forced into 0.8 MPa through Marsh gas compression machine, 20 DEG C are cooled to through heat exchanger, absorption tower, biogas stream are sent into afterwards
Measure as 20 L/min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units, 0.8 MPa is forced into through booster pump, enters afterwards from absorption tower top, water-carrying capacity
For 2.5 L/min, biogas is inversely contacted with water from bottom to top in absorption tower, rich CH4Gas is arranged from the top on absorption tower through valve
Go out, stored after being dried through drier as product gas；
The Stress control that the water discharged from absorption tower bottom enters in flash column, flash column through valve is in 0.35 MPa, in flash distillation
In tower, water is by the CH of dissolving4With part CO2Discharge, it is again mixed with unstripped gas that this part mixed gas returns air accumulator through valve
Close and participate in washing separation again；Enter from the water of flash distillation tower bottom discharge through valve and be depressured tower, pressure drops to 0.1 MPa, desorbs
Discharged through valve at the top of carbon dioxide out from decompression tower；
The water from decompression tower bottom discharge through valve enters desorber afterwards, and the gas desorbed is at the top of desorber through valve
Discharge, after discharged through desorber vavuum pump, vacuum is maintained at 0.08 MPa in desorber, in addition through valve to desorber with
1.2 L/min wind speed blasts air, air inversely contacted with water from bottom to top after together with the carbon dioxide desorbed from
Discharged through valve at the top of desorber；
Through valve and desorber Vacuum discharge pump enter storage tank from the water of desorption tower bottom discharge, afterwards by through handpiece Water Chilling Units
Absorption tower is returned to after cooling and booster pump supercharging, supplements running water to maintain the liquid level of storage tank by Valve controlling in addition.
6. a kind of vacuum desorption discharge system that purifying biogas is washed for pressure (hydraulic) water, it includes Marsh gas compression machine, and heat exchanger is dried
Device, booster pump, flash column is depressured tower, desorber, storage tank, desorber vavuum pump, the first discharge tank and the second discharge tank；With
The heat exchanger of Marsh gas compression machine outlet, the absorption tower connected with heat exchanger exit is connected at the top of absorption tower with drier；
Storage tank delivery port is connected by booster pump with absorption tower, is absorbed tower bottom and is connected by pipeline with flash column top, flash column
Top is connected with air accumulator, and flash distillation tower bottom is connected by pipeline with being depressured the top of tower；It is depressured top of tower and atmosphere, drop
Pressure tower bottom is connected by pipeline with desorber top；Connected with desorber vavuum pump at the top of desorber, desorber vavuum pump and
Atmosphere；
The first discharge tank inlet is provided with the top of the first discharge tank, the top of the first discharge tank is provided with the first discharging
Canister incoming gas mouthful and the first discharge tank exhaust outlet, the first discharge tank leakage fluid dram is provided with the bottom of the first discharge tank；First discharging
The first intake valve communicated with the external world is set on the pipeline before canister incoming gas mouthful, on the pipeline after the first discharge tank leakage fluid dram
The first tapping valve is provided with, first row air valve is provided with the pipeline after the first discharge tank exhaust outlet；
The second discharge tank inlet is provided with the top of the second discharge tank, the top of the second discharge tank is provided with the second discharging
Canister incoming gas mouthful and the second discharge tank exhaust outlet, the second discharge tank leakage fluid dram is provided with the bottom of the second discharge tank；Second discharging
The second intake valve communicated with the external world is set on the pipeline before canister incoming gas mouthful, on the pipeline after the second discharge tank leakage fluid dram
The second tapping valve is provided with, second row air valve is provided with the pipeline after the second discharge tank exhaust outlet；
Desorber gas outlet is provided with the top of desorber, the top of desorber desorber charging aperture is provided with, in desorber
Bottom be provided with desorber bleed ports, the bottom of desorber is provided with desorber discharging opening；
Pipeline after desorber discharging opening is divided into two-way, is connected all the way by the first outlet valve with the first discharge tank inlet；
Another road is connected by the second outlet valve with the second discharge tank inlet；
The discharging pipeline of first discharge tank and the second discharge tank is connected after converging with storage tank；
The pipeline after pipeline and the second discharge tank exhaust outlet after first discharge tank exhaust outlet converges rear and desorber bleed
Mouth connection；
On the pipeline before desorber charging aperture set desorber material inlet valve, on the pipeline after desorber gas outlet according to
Secondary setting desorber outlet valve and desorber vavuum pump.
7. the vacuum desorption discharge system according to claim 6 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that, also wrap
Handpiece Water Chilling Units are included, storage tank delivery port is connected with handpiece Water Chilling Units, and handpiece Water Chilling Units are connected by booster pump with absorption tower.
8. the vacuum desorption discharge system according to claim 6 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that described
The height of first discharge tank and the second discharge tank is 0.2 meter, and internal diameter is 0.15 meter.
9. the vacuum desorption discharge system according to claim 6 that purifying biogas is washed for pressure (hydraulic) water, it is characterized in that absorbing
Tower is packed tower, 0.1 meter of tower internal diameter, filling diameter and the high stainless steel Dixon ring filler all for 10 millimeters, and packing section is high 2.0 meters；
Flash column is plate column, and 0.12 meter of tower internal diameter, the number of plates is 5 pieces；
Decompression tower is plate column, and 0.12 meter of tower internal diameter, the number of plates is 8 pieces；Desorber is packed tower, and 0.2 meter of tower internal diameter, filling is straight
Footpath and the high stainless steel Dixon ring filler all for 10 millimeters, packing section are high 2.0 meters.
10. a kind of method for washing purifying biogas for pressure (hydraulic) water, it is using said system equipment and comprises the following steps：By biogas
0.8 MPa is forced into through Marsh gas compression machine, 20 DEG C are cooled to through heat exchanger, absorption tower is sent into afterwards, and biogas flow is 20 L/
min；
Water is cooled to 10 DEG C through handpiece Water Chilling Units, 0.8 MPa is forced into through booster pump, enters afterwards from absorption tower top, water-carrying capacity
For 2.5 L/min, biogas is inversely contacted with water from bottom to top in absorption tower, rich CH4Gas is discharged from the top on absorption tower, through dry
Dry device is stored after drying as product gas；
The Stress control that the water discharged from absorption tower bottom enters in flash column, flash column is in 0.35 MPa, in flash column, water
By the CH of dissolving4With part CO2Discharge, this part mixed gas time air accumulator is mixed with unstripped gas again to be participated in washing again
Wash separation；Enter decompression tower from the water of flash distillation tower bottom discharge, pressure drops to 0.1 MPa, the carbon dioxide desorbed is from drop
Press the top discharge of tower；
The water from decompression tower bottom discharge enters desorber afterwards, and the gas desorbed is discharged at the top of the desorber, after pass through
Desorber vavuum pump is discharged, and vacuum is maintained at 0.08 MPa in desorber；
It is open mode, the first intake valve, first in the first outlet valve, first row air valve, the second intake valve and the second tapping valve
When tapping valve, the second outlet valve and second row air valve are closed mode, the desorber discharging opening of water from desorption tower bottom discharges warp
The air that first outlet valve enters in the first discharge tank, the first discharge tank enters desorber through first row air valve and enters promoting the circulation of qi with water
Liquid mass transfer is to promote desorption, and the water in the second discharge tank is discharged through the second tapping valve, and extraneous air enters through the second intake valve
Enter the second discharge tank；
It is closed mode, the first intake valve, first in the first outlet valve, first row air valve, the second intake valve and the second tapping valve
When tapping valve, the second outlet valve and second row air valve are open mode, water goes out from the discharging opening discharge of desorption tower bottom through second
Expect that the air that valve enters in the second discharge tank, the second discharge tank enters desorber through second row air valve and carries out gas-liquid mass transfer with water
To promote desorption, and the water in the first discharge tank is discharged through the first tapping valve, and extraneous air enters first through the first intake valve
Discharge tank；
Replace the on off state of switch valve successively, on off state is kept for 1 minute each time, realize that vacuum desorption discharges.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710427813.2A CN107019995B (en) | 2017-06-08 | 2017-06-08 | The method and vacuum desorption discharge system of purifying biogas are washed for pressure (hydraulic) water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201710427813.2A CN107019995B (en) | 2017-06-08 | 2017-06-08 | The method and vacuum desorption discharge system of purifying biogas are washed for pressure (hydraulic) water |
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| Publication Number | Publication Date |
|---|---|
| CN107019995A true CN107019995A (en) | 2017-08-08 |
| CN107019995B CN107019995B (en) | 2019-06-07 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107596871A (en) * | 2017-11-01 | 2018-01-19 | 安徽上造智能设备科技有限公司 | A kind of chemical workshop air cleaning unit |
| CN109852448A (en) * | 2019-04-01 | 2019-06-07 | 南京工业大学 | Device and method for pressurized water absorption decarburization of biogas by using micro-channel mixing device |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102861509A (en) * | 2012-09-26 | 2013-01-09 | 开封黄河空分集团有限公司 | Biogas decarburization and tertiary desorption process |
| CN103897760A (en) * | 2014-04-10 | 2014-07-02 | 开封黄河空分集团有限公司 | Marsh gas purification system |
| CN205223136U (en) * | 2015-11-23 | 2016-05-11 | 山东省科学院能源研究所 | A desorption device that is used for pure marsh gas of pressure water elution |
| CN106744956A (en) * | 2016-12-22 | 2017-05-31 | 乐陵胜利新能源有限责任公司 | A kind of high-pressure washing methane purification carbon dioxide in process recovery process |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102861509A (en) * | 2012-09-26 | 2013-01-09 | 开封黄河空分集团有限公司 | Biogas decarburization and tertiary desorption process |
| CN103897760A (en) * | 2014-04-10 | 2014-07-02 | 开封黄河空分集团有限公司 | Marsh gas purification system |
| CN205223136U (en) * | 2015-11-23 | 2016-05-11 | 山东省科学院能源研究所 | A desorption device that is used for pure marsh gas of pressure water elution |
| CN106744956A (en) * | 2016-12-22 | 2017-05-31 | 乐陵胜利新能源有限责任公司 | A kind of high-pressure washing methane purification carbon dioxide in process recovery process |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107596871A (en) * | 2017-11-01 | 2018-01-19 | 安徽上造智能设备科技有限公司 | A kind of chemical workshop air cleaning unit |
| CN109852448A (en) * | 2019-04-01 | 2019-06-07 | 南京工业大学 | Device and method for pressurized water absorption decarburization of biogas by using micro-channel mixing device |
| CN109852448B (en) * | 2019-04-01 | 2024-03-26 | 南京工业大学 | Device and method for absorbing and decarbonizing biogas by pressurized water by utilizing micro-channel mixing device |
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| CN107019995B (en) | 2019-06-07 |
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