CN109609223A - A kind of temperature and pressure collaboration gas absorption process for separation and purification - Google Patents
A kind of temperature and pressure collaboration gas absorption process for separation and purification Download PDFInfo
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- CN109609223A CN109609223A CN201811469616.8A CN201811469616A CN109609223A CN 109609223 A CN109609223 A CN 109609223A CN 201811469616 A CN201811469616 A CN 201811469616A CN 109609223 A CN109609223 A CN 109609223A
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- 238000010521 absorption reaction Methods 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 45
- 230000008569 process Effects 0.000 title claims abstract description 42
- 238000000926 separation method Methods 0.000 title claims abstract description 26
- 238000000746 purification Methods 0.000 title claims abstract description 16
- 238000001179 sorption measurement Methods 0.000 claims abstract description 178
- 239000003463 adsorbent Substances 0.000 claims description 26
- 230000000274 adsorptive effect Effects 0.000 claims description 15
- 238000003795 desorption Methods 0.000 claims description 15
- 238000001816 cooling Methods 0.000 claims description 14
- 239000002994 raw material Substances 0.000 claims description 11
- 230000008676 import Effects 0.000 claims description 8
- 239000012535 impurity Substances 0.000 claims description 5
- 239000000463 material Substances 0.000 claims description 5
- 238000010792 warming Methods 0.000 claims description 5
- 238000010926 purge Methods 0.000 claims description 4
- 239000012621 metal-organic framework Substances 0.000 claims description 3
- 239000002808 molecular sieve Substances 0.000 claims description 3
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000003610 charcoal Substances 0.000 claims description 2
- 239000007789 gas Substances 0.000 abstract description 91
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 52
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 26
- 239000003245 coal Substances 0.000 abstract description 13
- 229910052757 nitrogen Inorganic materials 0.000 abstract description 12
- 238000005265 energy consumption Methods 0.000 abstract description 5
- 238000000605 extraction Methods 0.000 abstract description 4
- 229920006395 saturated elastomer Polymers 0.000 description 5
- 230000006837 decompression Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 239000005431 greenhouse gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 239000002156 adsorbate Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000002075 main ingredient Substances 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000007420 reactivation Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000002594 sorbent Substances 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
Classifications
-
- 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
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0462—Temperature swing adsorption
-
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/047—Pressure swing adsorption
-
- 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
- C10L3/106—Removal of contaminants of water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
- B01D2257/7025—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40013—Pressurization
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40011—Methods relating to the process cycle in pressure or temperature swing adsorption
- B01D2259/40028—Depressurization
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/402—Further details for adsorption processes and devices using two beds
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/20—Capture or disposal of greenhouse gases of methane
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Analytical Chemistry (AREA)
- Solid-Sorbent Or Filter-Aiding Compositions (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention discloses a kind of temperature and pressure to cooperate with gas absorption process for separation and purification, by adsorbing point in different operating point high-temperature low-pressures, low-temp low-pressure adsorbs point, the temperature and pressure of various ways cooperate with circulation between cryogenic high pressure absorption point, high-temperature high-pressure adsorption point, improves traditional pressure-variable adsorption separation gas efficiency.The present invention, which solves, prepares that separation process energy consumption in gas process is higher, product yield is lower, system self-energy fails the problems such as making full use of for Pressure Swing Adsorption at present, the case where in particular for including the hardly possible separation component such as methane, nitrogen in mixed gas, the comprehensive utilization especially suitable for coal extraction low concentration gas and ventilating gas.
Description
Technical field
The present invention relates to gas purification technical fields, and in particular to a kind of temperature and pressure collaboration gas absorption process for separation and purification,
It is particularly suitable for the adsorbing separation purification of coal extraction low concentration gas and ventilating gas.
Background technique
Gas is the association product of coal, is a kind of non-renewable energy of preciousness, while being also a kind of strong greenhouse effects
Gas.For the discharge of coal mine gas, the discharge of ventilating gas accounts for about the 70% of coal mine gas total emission volumn.Due to ventilating tile
This concentration low (≤1%), flowed fluctuation are big, are difficult directly to utilize it.Therefore, how to realize coal extraction gas with
Ventilating gas effective use, for promoting the efficient production level of safety of coal mines, reducing greenhouse gas emission with particularly significant
Meaning.
For mixed gas such as similar coal mine gases, conventional pressure-variable adsorption is to pass through pressurized adsorbent under isothermal conditions, subtract
The mode of pressure desorption is combined into adsorbing separation operation circulation process, adsorbent to the adsorbance of adsorbate with the raising of pressure and
Increase, and is reduced with the reduction of pressure, while during decompression (be down to normal pressure or vacuumize), releasing the gas being adsorbed
Body makes adsorbent reactivation, obtains high purity product gas.
Main ingredient includes the components such as methane, nitrogen, oxygen in coal mine light concentration mash gas and ventilating gas, wherein methane
There is similar physicochemical structure characteristic with nitrogen, however conventional pressure swing adsorption means are difficult to be efficiently separated, at present still
Gas absorption process for separation and purification is cooperateed with without the temperature and pressure for difficult separation gas component.
Summary of the invention
The object of the present invention is to provide a kind of temperature and pressure to cooperate with gas absorption process for separation and purification, safe and efficient, low energy consumption.
To achieve the above object, The technical solution adopted by the invention is as follows: a kind of temperature and pressure cooperate with gas absorption separating-purifying
Method, using alternating temperature pressure swing adsorption system, which includes that air admission unit, exhaust unit and two in parallel are filled with absorption
The adsorption tower I and adsorption tower II of agent, adsorption tower I are internally provided with heat exchanger I, and adsorption tower II is internally provided with heat exchanger II, mentions
It is pure that steps are as follows:
1) mixed raw material gas initially enters cooling driers removing moisture through air admission unit after air compressor pressurizes, then
Into adsorption tower I, cooling boosting is carried out to adsorption tower I and completes foreign gas adsorption process, product gas is from adsorption tower I tower top stream
Out, it is discharged through exhaust unit；It opens vacuum pump simultaneously to purge adsorption tower II, adsorption tower II is made to keep evacuated state；
2) when impurity absorption is close to saturation in adsorption tower I, close the import of adsorption tower I, heat exchanger I and heat exchanger II into
The exchange of row heat carries out heating decompression to adsorption tower I after the equalized temperature between two towers and completes foreign gas desorption process, impurity
Gas passes through vacuum pump discharger from adsorption tower I tower bottom, while mixed raw material gas is added by air admission unit through air compressor
After pressure, cooling driers removing moisture is initially entered, adsorption tower II is entered back into, cooling boosting is carried out to adsorption tower II and completes foreign gas
Adsorption process, product gas are flowed out from adsorption tower II tower top, are discharged through exhaust unit；
3) when impurity absorption is close in adsorption tower II is saturated, the import of adsorption tower II is closed, while unstripped gas switches to
Adsorption tower I, and the exchange of the heat between two towers, adsorption tower I and the operation of adsorption tower II alternate cycles are carried out again.
Preferably, the concrete operations of foreign gas adsorption process are as follows: adsorption tower boosts to P1 under the conditions of temperature T2, reaches
High-temperature low-pressure adsorbs point A, then keeps adsorptive pressure constant and carries out being cooled to T1 to adsorption tower, reaches low-temp low-pressure absorption point
After B, adsorption tower keeps low temperature T1 constant and boosts to P2, reaches maximal absorptive capacity operating point cryogenic high pressure absorption point C, completes miscellaneous
Matter gas adsorption processes；
Foreign gas desorption process concrete operations are as follows: keeping the adsorptive pressure P2 of adsorption tower constant, carry out to adsorption tower
It is warming up to T2, after the High Pressure Absorption point D that reaches a high temperature, adsorption tower keeps high temperature T2 constant and is depressurized to P1, and the low pressure that reaches a high temperature is inhaled
Attachment A completes foreign gas desorption process.
Preferably, the concrete operations of foreign gas adsorption process are as follows: adsorption tower boosts to P1 under the conditions of temperature T2, reaches
High-temperature low-pressure adsorbs point A, then keeps temperature T2 constant and carries out boosting to P2 to adsorption tower, reach a high temperature High Pressure Absorption point D
Afterwards, adsorption tower keeps adsorptive pressure P2 constant and is cooled to T1, reaches maximal absorptive capacity operating point cryogenic high pressure absorption point C, complete
At foreign gas adsorption process；
Foreign gas desorption process concrete operations are as follows: keeping adsorption tower low temperature T1 constant, be depressurized to adsorption tower
P1, after reaching low-temp low-pressure absorption point B, adsorption tower keeps adsorptive pressure P1 constant and is warming up to T2, and reach a high temperature low pressure adsorbent
Point A completes foreign gas desorption.
Preferably, the adsorbent is charcoal adsorbent material, molecular sieve, metal-organic framework materials etc..
Preferably, the heat exchanger I, heat exchanger II are serpentine heat exchanger.
There are operating point high-temperature low-pressure absorption point A, low-temp low-pressure absorption point B, cryogenic high pressures to inhale for entire adsorption separation process
Attachment C, high-temperature high-pressure adsorption point D, corresponding adsorbance size order are QC> QB> QD> QA；The operating point temperature and
Pressure setting can be adjusted according to adsorbent species and mixing gas component to be separated, and mixed gas sorption separating-purifying is based on
Gas with various component adsorption equilibrium difference principle is realized；The high-temperature low-pressure absorption point A and high-temperature high-pressure adsorption point D is absorption
In tower adsorbent to mixed gas the operating point in same absorption isotherm under the conditions of high temperature T2；The low-temp low-pressure adsorbs point
B and cryogenic high pressure absorption point C for adsorbent in adsorption tower to mixed gas the work in same absorption isotherm under the conditions of low temperature T1
Condition point；The adsorption process can be alternately accomplished with separation process by two adsorption towers, between two towers can by heat exchanger or
Compressor carries out energy conduction, reduces system energy consumption.
Compared with prior art, the invention has the following beneficial effects:
The present invention utilizes Adsorption of the temperature change to gas with various on the sorbent, follows in identical absorption-desorption
During ring, while gas absorption amount increases, the adsorptive selectivity to specific gas is also improved, substantially increases transformation suction
Mixed gas sorption separative efficiency during attached under the conditions of identical adsorptive pressure, and multiple adsorption towers are used in parallel, absorption
Process and separation process alternately, can carry out energy conduction by heat exchanger or compressor between adsorption tower, improve and are
Temperature of uniting adjusts efficiency.This method is easy to operate, solves current prepare in gas process for Pressure Swing Adsorption and separated
Journey energy consumption is higher, product yield is lower, system self-energy fails the problems such as making full use of.
The present invention is especially suitable for the comprehensive utilizations of coal extraction low concentration gas and ventilating gas, are reducing greenhouse gases
Clean manufacturing utilization and the coal of coal mine gas are realized in the clean energy resource conversion that coal mine gas is obtained while gas (methane) discharges
The recycling economy development in mining area.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of alternating temperature pressure swing adsorption system of the invention.
Fig. 2 is the mixed gas sorption separation process schematic diagram of the embodiment of the present invention 1.
Fig. 3 is the mixed gas sorption separation process schematic diagram of the embodiment of the present invention 2.
In figure, 1, air admission unit, 2, air compressor, 3, cooling driers, 4, adsorption tower I, 5, heat exchanger I, 6, adsorption tower II,
7, heat exchanger II, 8, exhaust unit, 9, vacuum pump, 10, cold-heat-exchanging exchange system.
Specific embodiment
Invention is further described in detail in the following with reference to the drawings and specific embodiments.
Embodiment 1
In the present embodiment, gas to be separated is methane/nitrogen mixed raw material gas (methane concentration is lower than 30%).Using such as figure
Alternating temperature pressure swing adsorption system shown in 1, the system include air admission unit 1, exhaust unit 8 and two adsorption tower I4 in parallel and
Adsorption tower II6, adsorption tower I4 are internally provided with heat exchanger I5, and adsorption tower II6 is internally provided with heat exchanger II7, the heat exchanger
I5, heat exchanger II7 are serpentine heat exchanger.Adsorption tower I4 is filled with acticarbon, and adsorption tower II6 is filled with molecule
Sieve adsorbant.
Purification step is as follows:
(1) mixed raw material gas initially enters cooling driers 3 and removes water through air admission unit 1 after the pressurization of air compressor 2
Point, adsorption tower I4 is entered back into, adsorption tower I4 boosts to P1 (1MPa) under the conditions of temperature T2 (80 DEG C), and reach a high temperature low pressure adsorbent
Point A then keeps adsorptive pressure constant and carries out being cooled to T1 (0 DEG C) to adsorption tower I4, after reaching low-temp low-pressure absorption point B,
Adsorption tower I4 keeps low temperature T1 (0 DEG C) constant and boosts to P2 (5MPa), reaches the absorption of maximal absorptive capacity operating point cryogenic high pressure
Point C is completed methane gas adsorption process (as shown in Figure 2), and nitrogen is flowed out from adsorption tower I4 tower top, is discharged through exhaust unit 8；Together
Shi Kaiqi vacuum pump 9 purges adsorption tower II6, and adsorption tower II6 is made to keep evacuated state；
(2) when methane adsorption is close in adsorption tower I4 is saturated, the import of adsorption tower I4, heat exchanger I5 and heat exchanger are closed
II7 carries out heat exchange by cold-heat-exchanging exchange system 10, and the adsorptive pressure of adsorption tower I4 is kept after the equalized temperature between two towers
P2 (5MPa) is constant, carries out being warming up to T2 (80 DEG C) to adsorption tower I4, and after the High Pressure Absorption point D that reaches a high temperature, adsorption tower I4 is kept
High temperature T2 (80 DEG C) is constant and is depressurized to P1 (1MPa), and reach a high temperature low pressure adsorbent point A, completes methane desorption process (such as Fig. 2 institute
Show), methane gas passes through 9 discharger of vacuum pump from adsorption tower I4 tower bottom, while mixed raw material gas passes through air admission unit 1 through sky
After air compressor 2 pressurizes, initially enters cooling driers 3 and remove moisture, enter back into adsorption tower II6, adsorption tower II6 is in temperature T2 (80
DEG C) under the conditions of boost to P1 (1MPa), reach a high temperature low pressure adsorbent point A, then keeps adsorptive pressure constant and to adsorption tower II6
It carries out being cooled to T1 (0 DEG C), after reaching low-temp low-pressure absorption point B, adsorption tower II6 keeps low temperature T1 (0 DEG C) constant and boosts to
P2 (5MPa) reaches maximal absorptive capacity operating point cryogenic high pressure absorption point C, completes methane gas adsorption process (as shown in Figure 2),
Nitrogen is flowed out from adsorption tower II6 tower top, is discharged through exhaust unit 8；
(3) when methane adsorption is close in adsorption tower II6 is saturated, the import of adsorption tower II6 is closed, while unstripped gas switches
To adsorption tower I4, and the exchange of the heat between two towers, adsorption tower I4 and adsorption tower II6 alternating cycle work are carried out again, ensure that
The stability and continuity of system operation.
By multiple alternating temperature pressure swing adsorption cycles, nitrogen gas purity is exported up to 99%, it is reachable to collect methane gas purity
99%.
Embodiment 2
In the present embodiment, gas to be separated is methane/nitrogen mixed raw material gas (methane concentration is lower than 30%).Using such as figure
Alternating temperature pressure swing adsorption system shown in 1, the system include air admission unit 1, exhaust unit 8 and two adsorption tower I4 in parallel and
Adsorption tower II6, adsorption tower I4 are internally provided with heat exchanger I5, and adsorption tower II6 is internally provided with heat exchanger II7, the heat exchanger
I5, heat exchanger II7 are serpentine heat exchanger.Adsorption tower I4 is filled with adsorbent of molecular sieve, and adsorption tower II6 is filled with metal
Organic framework material adsorbent.
Purification step is as follows:
(1) mixed raw material gas initially enters cooling driers 3 and removes water through air admission unit 1 after the pressurization of air compressor 2
Point, adsorption tower I4 is entered back into, adsorption tower I4 is boosted to P1 (2MPa) under the conditions of temperature T2 (100 DEG C), and the low pressure that reaches a high temperature is inhaled
Attachment A then keeps temperature T2 (100 DEG C) constant and boost to P2 (6MPa) to adsorption tower I4, and the high pressure that reaches a high temperature is inhaled
After attachment D, adsorption tower I4 keeps adsorptive pressure P2 (6MPa) constant and is cooled to T1 (20 DEG C), reaches maximal absorptive capacity operating point
Cryogenic high pressure adsorbs point C, completes mixed gas sorption process (as shown in Figure 3), and product gas is flowed out from adsorption tower I4 tower top, through arranging
Gas unit 8 is discharged；It opens vacuum pump 9 simultaneously to purge adsorption tower II6, adsorption tower II6 is made to keep evacuated state；
(2) when methane adsorption is close in adsorption tower I4 is saturated, the import of adsorption tower I4, heat exchanger I5 and heat exchanger are closed
II7 carries out heat exchange by cold-heat-exchanging exchange system 10, and adsorption tower I4 low temperature T1 (20 is kept after the equalized temperature between two towers
DEG C) constant, adsorption tower I4 is carried out to be depressurized to P1 (2MPa), after reaching low-temp low-pressure absorption point B, adsorption tower I4 keeps adsorption pressure
Power P1 (2MPa) is constant and is warming up to T2 (100 DEG C), and reach a high temperature low pressure adsorbent point A, completes methane desorption (as shown in Figure 3),
Methane gas is by 9 discharger of vacuum pump, while mixed raw material gas passes through air admission unit 1 after the pressurization of air compressor 2, first
It is introduced into cooling driers 3 and removes moisture, enter back into adsorption tower II6, adsorption tower II6 boosts to P1 under the conditions of temperature T2 (100 DEG C)
(2MPa), reach a high temperature low pressure adsorbent point A, then keeps temperature T2 (100 DEG C) constant and carries out boosting to P2 to adsorption tower II6
(6MPa), after the High Pressure Absorption point D that reaches a high temperature, adsorption tower II6 keeps adsorptive pressure P2 (6MPa) constant and is cooled to T1 (20
DEG C), reach maximal absorptive capacity operating point cryogenic high pressure absorption point C, completion mixed gas sorption process (as shown in Figure 3) nitrogen from
The outflow of adsorption tower II6 tower top, is discharged through exhaust unit 8；
(3) when methane adsorption is close in adsorption tower II6 is saturated, the import of adsorption tower II6 is closed, while unstripped gas switches
To adsorption tower I4, and the exchange of the heat between two towers, adsorption tower I4 and adsorption tower II6 alternating cycle work are carried out again, ensure that
The stability and continuity of system operation.
By multiple alternating temperature pressure swing adsorption cycles, nitrogen gas purity is exported up to 99%, it is reachable to collect methane gas purity
99%.
Working principle:
By taking methane, nitrogen bi-component mixed gas to be separated as an example, under condition of different temperatures, methane and nitrogen are in adsorbent
On equilibrium adsorption otherness it is different, the selective absorption that cryogenic conditions both are conducive to, and hot conditions are conducive to gas
Body desorption, and it is similar to this difficult separation mixing gas component of methane, nitrogen, it is poor that adsorbing separation is mainly based upon adsorption equilibrium
What different principle was realized, the variation of adsorption temp can increase this otherness, be conducive to the adsorbing separation of mixing gas component.Cause
This mixed raw material gas initially enters cooling driers removing moisture, subsequently into two adsorption tower groups after air compressor compresses
At adsorption separation system, selectively adsorbed using the adsorbent loaded in tower and fall methane gas, nitrogen is then with high-purity gas
Form go out and utilize from adsorption tower top row, subsequent system decompression, the methane desorbing gas adsorbed in adsorbent comes out, and passes through tower
Bottom inverse put is discharged to obtain high-purity methane, and whole process is cryogenic absorption, desorption under high temperature, and two adsorption towers are used alternatingly, between two towers
Energy conduction can be carried out by heat exchanger or compressor, reduce system energy consumption, achieve the purpose that continuously to separate mixed gas.
Claims (5)
1. a kind of temperature and pressure cooperate with gas absorption process for separation and purification, which is characterized in that use alternating temperature pressure swing adsorption system, the system
Including air admission unit (1), exhaust unit (8) and two the adsorption tower I (4) for being filled with adsorbent and adsorption tower II in parallel
(6), adsorption tower I (4) is internally provided with heat exchanger I (5), and adsorption tower II (6) is internally provided with heat exchanger II (7), purification step
It is as follows:
1) mixed raw material gas initially enters cooling driers (3) removing water through air admission unit (1) after air compressor (2) pressurization
Point, adsorption tower I (4) are entered back into, cooling boosting is carried out to adsorption tower I (4) and completes foreign gas adsorption process, product gas is from absorption
The outflow of tower I (4) tower top, is discharged through exhaust unit (8)；It opens vacuum pump (9) simultaneously to purge adsorption tower II (6), makes to inhale
Attached tower II (6) keeps evacuated state；
2) when the close saturation of adsorption tower I (4) interior impurity absorption, the import of adsorption tower I (4), heat exchanger I (5) and heat exchange are closed
Device II (7) carries out heat exchange by cold-heat-exchanging exchange system 10, rises after the equalized temperature between two towers to adsorption tower I (4)
Temperature drop pressure completes foreign gas desorption process, and foreign gas passes through vacuum pump (9) discharger from adsorption tower I (4) tower bottom；Simultaneously
Mixed raw material gas by air admission unit (1) through air compressor (2) pressurization after, initially enter cooling driers (3) removing moisture, then into
Enter adsorption tower II (6), cooling boosting is carried out to adsorption tower II (6) and completes foreign gas adsorption process, product gas is from adsorption tower II
(6) tower top flows out, and is discharged through exhaust unit (8)；
3) when the close saturation of adsorption tower II (6) interior impurity absorption, the import of adsorption tower II (6) is closed, while unstripped gas switches
To adsorption tower I (4), and the exchange of the heat between two towers is carried out again, adsorption tower I (4) and adsorption tower II (6) alternate cycles are run.
2. a kind of temperature and pressure according to claim 1 cooperate with gas absorption process for separation and purification, which is characterized in that foreign gas
Adsorption process concrete operations are as follows: adsorption tower boosts to P1 under the conditions of temperature T2, and reach a high temperature low pressure adsorbent point A, then protects
It is constant and carry out being cooled to T1 to adsorption tower I to hold adsorptive pressure, after reaching low-temp low-pressure absorption point B, adsorption tower holding low temperature T1
It is constant and boost to P2, reach maximal absorptive capacity operating point cryogenic high pressure absorption point C, completion foreign gas adsorption process；
Foreign gas desorption process concrete operations are as follows: keeping the adsorptive pressure P2 of adsorption tower constant, heat up to adsorption tower I
To T2, after the High Pressure Absorption point D that reaches a high temperature, adsorption tower keeps high temperature T2 constant and is depressurized to P1, and reach a high temperature low pressure adsorbent point
A completes foreign gas desorption process.
3. a kind of temperature and pressure according to claim 1 cooperate with gas absorption process for separation and purification, which is characterized in that foreign gas
Adsorption process concrete operations are as follows: adsorption tower boosts to P1 under the conditions of temperature T2, and reach a high temperature low pressure adsorbent point A, then protects
It is constant and carry out boosting to P2 to adsorption tower to hold temperature T2, after the High Pressure Absorption point D that reaches a high temperature, adsorption tower keeps adsorptive pressure P2
It is constant and be cooled to T1, reach maximal absorptive capacity operating point cryogenic high pressure absorption point C, completion foreign gas adsorption process；
Foreign gas desorption process concrete operations are as follows: keeping adsorption tower low temperature T1 constant, carry out being depressurized to P1 to adsorption tower, reach
After adsorbing point B to low-temp low-pressure, adsorption tower keeps adsorptive pressure P1 constant and is warming up to T2, and reach a high temperature low pressure adsorbent point A, complete
It is desorbed at foreign gas.
4. a kind of temperature and pressure according to any one of claims 1 to 3 cooperate with gas absorption process for separation and purification, feature exists
In the adsorbent is one of charcoal adsorbent material, molecular sieve, metal-organic framework materials or a variety of.
5. a kind of temperature and pressure according to any one of claims 1 to 3 cooperate with gas absorption process for separation and purification, feature exists
In the heat exchanger I (5), heat exchanger II (7) are serpentine heat exchanger.
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| CN110252080A (en) * | 2019-07-05 | 2019-09-20 | 昆山澳纳森节能环保科技有限公司 | VOC organic waste gas treatment device |
| CN115779634A (en) * | 2022-12-12 | 2023-03-14 | 常州大学 | Pressure swing adsorption oxygen generation system and method for out-of-phase operation of parallel sleeve type adsorption towers |
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