CN112604453A - Decompression adsorption equipment gas recycle device among carbon disulfide production process - Google Patents
Decompression adsorption equipment gas recycle device among carbon disulfide production process Download PDFInfo
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- CN112604453A CN112604453A CN202011322872.1A CN202011322872A CN112604453A CN 112604453 A CN112604453 A CN 112604453A CN 202011322872 A CN202011322872 A CN 202011322872A CN 112604453 A CN112604453 A CN 112604453A
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- 238000001179 sorption measurement Methods 0.000 title claims abstract description 86
- QGJOPFRUJISHPQ-UHFFFAOYSA-N Carbon disulfide Chemical compound S=C=S QGJOPFRUJISHPQ-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 23
- 230000006837 decompression Effects 0.000 title description 3
- 239000007789 gas Substances 0.000 claims abstract description 170
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims abstract description 108
- 239000003345 natural gas Substances 0.000 claims abstract description 48
- 238000002156 mixing Methods 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims abstract description 18
- 238000004458 analytical method Methods 0.000 claims abstract description 17
- 238000004064 recycling Methods 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims abstract description 9
- 238000003795 desorption Methods 0.000 claims description 75
- 239000000047 product Substances 0.000 claims description 22
- 239000003463 adsorbent Substances 0.000 claims description 20
- 238000003786 synthesis reaction Methods 0.000 claims description 15
- 239000000446 fuel Substances 0.000 claims description 13
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 229910052717 sulfur Inorganic materials 0.000 claims description 12
- 239000011593 sulfur Substances 0.000 claims description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 10
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 10
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 9
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims description 9
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 9
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims description 9
- 238000006477 desulfuration reaction Methods 0.000 claims description 7
- 230000023556 desulfurization Effects 0.000 claims description 7
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- 230000003139 buffering effect Effects 0.000 claims description 4
- 229910052799 carbon Inorganic materials 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
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- 230000006835 compression Effects 0.000 claims description 3
- 238000007906 compression Methods 0.000 claims description 3
- 239000003365 glass fiber Substances 0.000 claims description 3
- 229930195733 hydrocarbon Natural products 0.000 claims description 3
- 150000002430 hydrocarbons Chemical class 0.000 claims description 3
- -1 polytetrafluoroethylene Polymers 0.000 claims description 3
- 239000013589 supplement Substances 0.000 claims description 3
- 229920001343 polytetrafluoroethylene Polymers 0.000 claims description 2
- 239000004810 polytetrafluoroethylene Substances 0.000 claims description 2
- 239000012528 membrane Substances 0.000 claims 3
- 230000006641 stabilisation Effects 0.000 claims 1
- 238000011105 stabilization Methods 0.000 claims 1
- 238000010521 absorption reaction Methods 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 239000002737 fuel gas Substances 0.000 description 8
- 239000012535 impurity Substances 0.000 description 6
- 238000009835 boiling Methods 0.000 description 5
- 238000010586 diagram Methods 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000005864 Sulphur Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- RBORURQQJIQWBS-QVRNUERCSA-N (4ar,6r,7r,7as)-6-(6-amino-8-bromopurin-9-yl)-2-hydroxy-2-sulfanylidene-4a,6,7,7a-tetrahydro-4h-furo[3,2-d][1,3,2]dioxaphosphinin-7-ol Chemical compound C([C@H]1O2)OP(O)(=S)O[C@H]1[C@@H](O)[C@@H]2N1C(N=CN=C2N)=C2N=C1Br RBORURQQJIQWBS-QVRNUERCSA-N 0.000 description 1
- 101100314150 Caenorhabditis elegans tank-1 gene Proteins 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- QGJOPFRUJISHPQ-NJFSPNSNSA-N carbon disulfide-14c Chemical compound S=[14C]=S QGJOPFRUJISHPQ-NJFSPNSNSA-N 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- 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
- B01D53/053—Pressure swing adsorption with storage or buffer vessel
-
- 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
- C10L3/103—Sulfur containing contaminants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/24—Hydrocarbons
- B01D2256/245—Methane
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/30—Sulfur compounds
- B01D2257/304—Hydrogen sulfide
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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)
- Separation Of Gases By Adsorption (AREA)
Abstract
The invention provides a device and a method for recycling analysis gas of a pressure swing adsorption device in a carbon disulfide production process, wherein the device comprises: the natural gas buffer tank, the absorption tower, there is analytic gas buffer tank the bottom of absorption tower through the pipe connection, there is the condenser bottom of absorption tower through vacuum pump connection, the export of analytic gas buffer tank collects the back with the export of condenser and the entry linkage of analytic gas blending tank, the export of analytic gas blending tank and the entry linkage of analytic gas compressor, the export of analytic gas compressor and the entry linkage of analytic gas condenser, the export of analytic gas condenser and the entry linkage of buffer tank behind the compressor, the export of buffer tank and another export of natural gas buffer tank are collected after letting in synthetic reaction system behind the compressor. The invention enables the utilization rate of natural gas to reach 100 percent, and reduces energy consumption and production cost.
Description
Technical Field
The invention relates to the technical field of chemical industry, in particular to a device and a method for recycling desorption gas of a pressure swing adsorption device in a carbon disulfide production process.
Background
Fig. 1 is a schematic diagram of a structure of a device for utilizing desorbed gas of a pressure swing adsorption device in the prior art, and as shown in fig. 1, the device comprises a natural gas buffer tank 1, an absorption tower 2, a finished gas buffer tank 3, a synthesis reaction furnace 4, a vacuum pump 5, a condenser 6, a desorbed gas buffer tank 7, a desorbed gas mixing tank 8 and an emergency flare 9 of the device. Wherein, synthesis reacting furnace 4 is the reacting furnace that natural gas and sulphur react and produce carbon disulfide, because this reaction needs the fuel gas that has certain pressure as the heat source of reacting furnace, and the gas that collects from analysis blending tank 8 is too low because of the pressure, can not be used for in the carbon disulfide production process who uses natural gas and sulphur as the raw materials, does not conform to the pressure parameter requirement of fuel gas in the production technology, so direct discharge to the emergent torch 9 of device and burn to waste a large amount of raw and other materials.
Disclosure of Invention
In order to solve the problems in the prior art, the invention provides a desorption gas recycling device of a pressure swing adsorption device in a carbon disulfide production process, which comprises the following steps: the system comprises a buffer tank (1), a first pressure swing adsorption tower (2), a second pressure swing adsorption tower (3), a finished gas buffer tank (4), a synthesis reaction furnace (5), a variable frequency vacuum pump (6), a condenser (7), a desorption gas buffer tank (8), a desorption gas mixing tank (9), a desorption gas compressor (10), a desorption gas condenser (11), a compressor rear buffer tank (12), a pressure gauge (13), a processor (14) and a one-way electromagnetic valve (15);
the outlet of the buffer tank (1) is connected with the inlet of a first pressure swing adsorption tower (2) through a pipeline, the outlet of the first pressure swing adsorption tower (2) is connected with the inlet of a second pressure swing adsorption tower (3) through a pipeline, the bottom of the second pressure swing adsorption tower (3) is connected with a desorption gas buffer tank (8) through a pipeline, the bottoms of the first pressure swing adsorption tower (2) and the second pressure swing adsorption tower (3) are connected with a condenser (7) through a variable frequency vacuum pump (6), the outlet of the desorption gas buffer tank (8) is converged with the outlet of the condenser (7) and then connected with the inlet of a desorption gas mixing tank (9), the outlet of the desorption gas mixing tank (9) is connected with the inlet of a desorption gas compressor (10), the outlet of the desorption gas compressor (10) is connected with the inlet of a gas-cooled desorption condenser (11), the outlet of the desorption gas-cooled condenser (11) is connected with the inlet of a buffer tank (12) behind the compressor, an outlet of the buffer tank (12) behind the compressor is communicated with a fuel device of the synthetic reaction system, a pressure gauge (13) and a processor (14) are further arranged at the outlet of the buffer tank (12) behind the compressor, and the pressure gauge (13) is electrically connected with the processor (14);
an outlet of the second pressure swing adsorption tower (3) is connected with an inlet of a finished product gas buffer tank (4), and an outlet of the finished product gas buffer tank (4) is connected with an inlet of a synthesis reaction furnace (5); when the gas quantity required by normal combustion which cannot be met by the gas in the buffer tank (12) behind the compressor is the gas quantity required by normal combustion, the outlet of the buffer tank (12) behind the compressor and the other outlet of the natural gas buffer tank (1) are converged and then are led into a fuel device of a synthetic reaction system, and a one-way electromagnetic valve (15) is further arranged at the other outlet of the natural gas buffer tank (1).
Furthermore, the buffer tank (1) adopts a glass fiber reinforced polytetrafluoroethylene diaphragm as a diaphragm material for buffering, and the buffering performance of the buffer tank is stable by mainly compressing air in one side of the diaphragm of the compression tank.
Furthermore, the adsorbent loaded in the first pressure swing adsorption tower (2) for adsorbing hydrogen sulfide is high-sulfur capacity special active carbon for desulfurization.
Furthermore, an adsorbent metal base for adsorbing carbon monoxide is loaded in the second pressure swing adsorption tower (3).
Furthermore, the finished product gas buffer tank (4) is a suction buffer tank, adopts a diaphragm type buffer mode, and has the functions of reducing the flow unevenness of a suction pipeline, reducing the inertia loss and improving the suction performance.
A method for recycling the gas desorbed from a pressure swing adsorption device is characterized by comprising the following steps:
step 1: the natural gas delivered by an external pipeline realizes stable pressure through a natural gas buffer tank (1), then is input into a first pressure swing adsorption tower (2), and hydrogen sulfide in the natural gas is absorbed by utilizing the high-pressure environment in the first pressure swing adsorption tower (2) and the special active carbon for high-sulfur capacity desulfurization;
step 2: then the gas is input into a second pressure swing adsorption tower (3), and the carbon monoxide in the natural gas is adsorbed by utilizing the high-pressure environment and the metal base of the second pressure swing adsorption tower (3);
and step 3: a higher natural gas finished product is obtained after passing through the second pressure swing adsorption tower (3) and is input into a finished product gas buffer tank (4), and the pressure of the finished product gas is stabilized through the finished product gas buffer tank (4);
and 4, step 4: meanwhile, natural gas components remained on the first pressure swing adsorption tower (2) and the second pressure swing adsorption tower (3) are extracted by a variable frequency vacuum pump (6), and are cooled by a condenser (7);
and 5: collecting hydrocarbons above C3+ and partial natural gas conveyed from a desorption gas buffer tank (8) and a condenser (7) by using a desorption gas mixing tank (9);
step 6: compressing the gas in the analysis gas mixing tank (9) by using an analysis gas compressor (10) to increase the pressure;
and 7: cooling the gas after the pressure increase by a desorption gas condenser (11);
and 8: collecting the condensed gas by using a compressor rear buffer tank (12);
and step 9: introducing gas collected in a buffer tank (12) behind a compressor into a fuel device of a synthesis reaction system to provide heat for the reaction of methane and sulfur; when a pressure gauge (13) detects the gas quantity required by normal combustion, which cannot be met by the gas in the buffer tank (12) behind the compressor, information is sent to a processor (14), the processor (14) opens a one-way electromagnetic valve (15), a part of gas is extracted from the natural gas buffer tank (1) to be used as supplement and is conveyed to a fuel device of a synthetic reaction system together with the gas in the buffer tank (12) behind the compressor, and heat is provided for the reaction of methane and sulfur.
The invention has the beneficial effects that: in order to save natural gas raw materials, desorption gas is compressed and pressurized by adding desorption gas compressor equipment to meet the pressure parameter requirement of fuel gas in the production process, and the cooled desorption gas is supplied to a device for combustion after being stabilized in pressure by passing through a compressor rear buffer tank, so that the utilization rate of natural gas reaches 100%, and the energy consumption and the production cost are reduced.
Drawings
FIG. 1 is a schematic diagram of a prior art apparatus for utilizing the desorbed gas from a pressure swing adsorption apparatus;
FIG. 2 is a schematic structural diagram of a device for recycling the desorbed gas from the pressure swing adsorption unit during the carbon disulfide production process of the present invention.
Wherein the reference numerals are: the system comprises a buffer tank-1, a first pressure swing adsorption tower-2, a second pressure swing adsorption tower-3, a finished gas buffer tank-4, a synthesis reaction furnace-5, a variable frequency vacuum pump-6, a condenser-7, a desorption gas buffer tank-8, a desorption gas mixing tank-9, a desorption gas compressor-10, a desorption gas condenser-11, a compressor rear buffer tank-12, a pressure gauge-13, a processor-14 and a one-way electromagnetic valve-15.
Detailed Description
The technical scheme of the invention is further described in detail by combining the drawings and the detailed implementation mode:
as shown in fig. 1, a desorption gas recycling device of a pressure swing adsorption device in a carbon disulfide production process comprises: the system comprises a buffer tank 1, a first pressure swing adsorption tower 2, a second pressure swing adsorption tower 3, a finished gas buffer 4, a synthesis reaction furnace 5, a variable frequency vacuum pump 6, a condenser 7, a desorption gas buffer tank 8, a desorption gas mixing tank 9, a desorption gas compressor 10, a desorption gas condenser 11, a compressor rear buffer tank 12, a pressure gauge 13, a processor 14 and a one-way electromagnetic valve 15;
the outlet of the buffer tank 1 is connected with the inlet of a first pressure swing adsorption tower 2 through a pipeline, the outlet of the first pressure swing adsorption tower 2 is connected with the inlet of a second pressure swing adsorption tower 3 through a pipeline, the bottom of the second pressure swing adsorption tower 3 is connected with a desorption gas buffer tank 8 through a pipeline, the bottoms of the first pressure swing adsorption tower 2 and the second pressure swing adsorption tower 3 are connected with a condenser 7 through a variable frequency vacuum pump 6, the outlet of the desorption gas buffer tank 8 is converged with the outlet of the condenser 7 and then connected with the inlet of a desorption gas mixing tank 9, the outlet of the desorption gas mixing tank 9 is connected with the inlet of a desorption gas compressor 10, the outlet of the desorption gas compressor 10 is connected with the inlet of a desorption gas condenser 11, the outlet of the desorption gas condenser 11 is connected with the inlet of a buffer tank 12 behind the compressor, and the outlet of the tank 12 behind the compressor is introduced into a fuel device of a synthesis reaction system, the outlet of the compressor rear buffer tank 12 is also provided with a pressure gauge 13 and a processor 14, and the pressure gauge 13 is electrically connected with the processor 14;
the outlet of the second pressure swing adsorption tower 3 is connected with the inlet of a finished product gas buffer 4, and the outlet of the finished product gas buffer 4 is connected with the inlet of a synthesis reaction furnace 5; when the gas quantity required by normal combustion which cannot be met by the gas in the buffer tank 12 behind the compressor is the gas quantity required by normal combustion, the outlet of the buffer tank 12 behind the compressor and the other outlet of the natural gas buffer tank 1 are converged and then are led into a fuel device of a synthetic reaction system, and a one-way electromagnetic valve 15 is further arranged at the other outlet of the natural gas buffer tank 1.
Furthermore, buffer tank 1 adopts glass fiber reinforcement poly tetrachloroethylene diaphragm as the diaphragm material and cushions, and its shock-absorbing capacity mainly realizes that pressure is steady through the compressed air in compression tank diaphragm one side.
Furthermore, the adsorbent loaded in the first pressure swing adsorption tower 2 for adsorbing hydrogen sulfide is high-sulfur capacity special activated carbon for desulfurization.
Further, an adsorbent metal base for adsorbing carbon monoxide is loaded in the second pressure swing adsorption tower 3.
Further, the finished product gas buffer 4 is a suction buffer tank, adopts a diaphragm type buffer mode, and has the functions of reducing the flow unevenness of a suction pipeline, reducing the inertia loss and improving the suction performance.
A method for recycling the gas desorbed from a pressure swing adsorption device is characterized by comprising the following steps:
step 1: the natural gas delivered by an external pipeline realizes stable pressure through a natural gas buffer tank 1, then is input into a first pressure swing adsorption tower 2, and hydrogen sulfide in the natural gas is absorbed by utilizing the high-pressure environment and the high-sulfur-capacity desulfurization special activated carbon in the first pressure swing adsorption tower 2;
step 2: then the gas is input into a second pressure swing adsorption tower 3, the carbon monoxide in the natural gas is adsorbed by utilizing the high-pressure environment and the metal base of the second pressure swing adsorption tower 3, the higher the relative molecular mass is, the higher the boiling point is, the pressure swing adsorption technology is based on the physical adsorption of molecules on the internal surface of an adsorbent (porous solid matter), the characteristic that the adsorbent is easy to adsorb high-boiling point components under the same pressure, the low-boiling point components are difficult to adsorb, the adsorption amount under the high pressure is increased, and the adsorption amount under the reduced pressure is reduced is utilized, the desorption gas (mainly comprising carbon monoxide, hydrogen sulfide and unreacted natural gas) generated in the carbon disulfide production process passes through an adsorbent bed under a certain pressure, and compared with the natural gas (molecular weight 16) with smaller molecular weight, namely lower boiling point, the carbon monoxide (molecular weight 28) with higher boiling point and the hydrogen sulfide (molecular weight 34) with larger molecular weight are selectively adsorbed on the adsorbent, and the less natural gas of molecular weight then is difficult for adsorbing and passes through the bed to realize the separation of natural gas and other impurity, then at the decompression in-process, because along with the reduction of pressure, the adsorbent also reduces the adsorption capacity of impurity gradually, consequently when high pressure, a large amount of impurity of adsorption will be analyzed out along with the reduction of pressure on the adsorbent, it is that the adsorbent bed realizes regeneration, can carry out the adsorbed process of stepping up of next time, this kind is adsorbed impurity when natural gas of impurity purification when high pressure step down and is analyzed impurity and make the regenerated circulation of adsorbent just be pressure swing adsorption process. The adsorbent for adsorbing hydrogen sulfide is special active carbon for high sulfur capacity desulfurization, and the adsorbent for adsorbing carbon monoxide is a metal base. According to the production work experience, the operation coefficient of the pressure swing adsorption time is 1.2-1.6 when the adjustment coefficient is 1.0. The pressure swing adsorption tower has a recommended time, which is a time given by the system according to the flow composition of raw materials and the condition of designing an adsorbent, a value is automatically given every adsorption period, and the pressure rising time T1 and the pressure reducing time T2 are increased or reduced according to the recommended time and multiplied by an operation coefficient when the pressure is increased or decreased;
and step 3: a higher natural gas finished product is obtained after passing through the second pressure swing adsorption tower 3, the natural gas finished product is input into a finished product gas buffer 4, and the pressure of the finished product gas is stabilized through the finished product gas buffer 4;
and 4, step 4: meanwhile, natural gas components remained on the first pressure swing adsorption tower 2 and the second pressure swing adsorption tower 3 are extracted by a variable frequency vacuum pump 6 and are cooled through a condenser 7, the variable frequency vacuum pump 6 is used for reducing the pressure of the tower to the pressure in the tower by the variable frequency vacuum pump 6 according to the internal pressure of the absorption tower, and when the reverse release of the absorption tower is finished (the pressure of the desorption gas in the tower is greater than the discharge pressure, the high-pressure desorption gas in the tower is discharged and enters a desorption gas buffer tank 8, the pressure in the tower is reduced along with the discharge of the high-pressure desorption gas until the pressure is lower than the discharge pressure, and the reverse release is finished), a part of natural gas components can remain on the adsorbent in the absorption tower to influence the next adsorption effect, so that the vacuum pump is required to pump vacuum, the adsorbent is better desorbed under the vacuum pressure, and the desorbed gas is low-pressure; the cooler (6) is used for cooling low-pressure analysis gas generated by residue on an adsorbent in the adsorption tower when the variable-frequency vacuum pump 6 is used for vacuumizing, and then reducing the temperature and the pressure of the low-pressure analysis gas simultaneously to enable the pressure and the temperature of the low-pressure analysis gas to accord with the suction pressure and the suction temperature of the analysis gas mixing tank 9;
and 5: the method comprises the following steps of collecting hydrocarbons above C3+ and partial natural gas conveyed from a desorption gas buffer tank 8 and a condenser 7 by using a desorption gas mixing tank 9, wherein the desorption gas mixing tank 9 is used for mixing high-pressure desorption gas from the desorption gas buffer tank 8 and low-pressure desorption gas passing through a cooler (6), and the desorption gas buffer tank 8 is used for enabling the pressure of the high-pressure desorption gas normally discharged from an adsorption tower to be stable through the desorption gas buffer tank 8, so that the next operation is facilitated;
step 6: the analysis gas compressor 10 is used for compressing the gas in the analysis gas mixing tank 9 to increase the pressure, and the analysis gas compressor 10 is used for increasing the analysis gas pressure from the analysis gas mixing tank 9 with too low pressure by using the compressor to meet the pressure parameter requirement of the fuel gas in the production process (providing the pressure parameter required by combustion according to the working pressure of a combustor);
and 7: cooling the gas after the pressure increase by using a desorption gas condenser 11; the condenser (11) is used for absorbing the heat of high-temperature analysis gas by utilizing circulating water under constant pressure and reducing the temperature of the analysis gas;
and 8: collecting the condensed gas by using a compressor rear buffer tank 12;
and step 9: introducing gas collected in a buffer tank 12 behind a compressor into a fuel device of a synthesis reaction system to provide heat for the reaction of methane and sulfur; when the pressure gauge 13 detects the gas amount required by the normal combustion which cannot be satisfied by the gas in the buffer tank 12 after the compressor, the information is sent to the processor 14, the processor 14 opens the one-way electromagnetic valve 15, and a part of the gas is extracted from the natural gas buffer tank 1 to be supplemented and is delivered to the fuel device of the synthetic reaction system together with the gas in the buffer tank 12 after the compressor. The compressor rear buffer tank 12 is used for stabilizing the pressure of the desorption gas passing through the compressor rear buffer tank 12, and then the desorption gas is used as most of the fuel gas to be mixed with a small part of natural gas supplemented by the natural gas buffer tank to form the fuel gas which enters the synthetic reaction production system for combustion; the condensed desorption gas passes through a compressor rear buffer tank 12 to enable the gas pressure in the compressor rear buffer tank to be stable, and then the desorption gas is used as supplementary fuel gas to enter a synthesis reaction production system to supply heat required by a synthesis reaction furnace 5; when the analytic gas pressure in the buffer tank 12 behind the compressor can not meet the pressure parameter requirement of the fuel gas in the production process, part of gas is extracted from the natural gas buffer tank 1 to be used as supplement and is conveyed to a fuel device of a synthetic reaction system together with the gas in the buffer tank 12 behind the compressor, and heat is provided for the reaction of methane and sulfur.
The above description is only an embodiment of the present invention, but the scope of the present invention is not limited thereto, and any changes or substitutions that are not thought of through the inventive work should be included in the scope of the present invention. Therefore, the protection scope of the present invention shall be subject to the protection scope defined by the claims.
Claims (6)
1. The utility model provides a desorption gas recycle device of pressure swing adsorption equipment in carbon disulfide production process which characterized in that includes: the system comprises a buffer tank (1), a first pressure swing adsorption tower (2), a second pressure swing adsorption tower (3), a finished gas buffer tank (4), a synthesis reaction furnace (5), a variable frequency vacuum pump (6), a condenser (7), a desorption gas buffer tank (8), a desorption gas mixing tank (9), a desorption gas compressor (10), a desorption gas condenser (11), a compressor rear buffer tank (12), a pressure gauge (13), a processor (14) and a one-way electromagnetic valve (15);
the outlet of the buffer tank (1) is connected with the inlet of a first pressure swing adsorption tower (2) through a pipeline, the outlet of the first pressure swing adsorption tower (2) is connected with the inlet of a second pressure swing adsorption tower (3) through a pipeline, the bottom of the second pressure swing adsorption tower (3) is connected with a desorption gas buffer tank (8) through a pipeline, the bottoms of the first pressure swing adsorption tower (2) and the second pressure swing adsorption tower (3) are connected with a condenser (7) through a variable frequency vacuum pump (6), the outlet of the desorption gas buffer tank (8) is converged with the outlet of the condenser (7) and then connected with the inlet of a desorption gas mixing tank (9), the outlet of the desorption gas mixing tank (9) is connected with the inlet of a desorption gas compressor (10), the outlet of the desorption gas compressor (10) is connected with the inlet of a gas-cooled desorption condenser (11), the outlet of the desorption gas-cooled condenser (11) is connected with the inlet of a buffer tank (12) behind the compressor, an outlet of the buffer tank (12) behind the compressor is communicated with a fuel device of the synthetic reaction system, a pressure gauge (13) and a processor (14) are further arranged at the outlet of the buffer tank (12) behind the compressor, and the pressure gauge (13) is electrically connected with the processor (14);
an outlet of the second pressure swing adsorption tower (3) is connected with an inlet of a finished product gas buffer tank (4), and an outlet of the finished product gas buffer tank (4) is connected with an inlet of a synthesis reaction furnace (5); when the gas quantity required by normal combustion which cannot be met by the gas in the buffer tank (12) behind the compressor is the gas quantity required by normal combustion, the outlet of the buffer tank (12) behind the compressor and the other outlet of the natural gas buffer tank (1) are converged and then are led into a fuel device of a synthetic reaction system, and a one-way electromagnetic valve (15) is further arranged at the other outlet of the natural gas buffer tank (1).
2. The device for recycling the desorption gas of the pressure swing adsorption device in the carbon disulfide production process according to claim 1, wherein the buffer tank (1) adopts a glass fiber reinforced polytetrafluoroethylene membrane as a membrane material for buffering, and the buffering performance of the buffer tank is mainly realized by compressed air in one side of the membrane of the compression tank to realize pressure stabilization.
3. The device for recycling desorbed gas from the pressure swing adsorption device in the carbon disulfide production process according to claim 1 or 2, wherein the adsorbent loaded in the first pressure swing adsorption tower (2) for adsorbing hydrogen sulfide is activated carbon special for high sulfur capacity desulfurization.
4. A desorption gas recycling device of a pressure swing adsorption device in a carbon disulfide production process according to any one of claims 1 to 3, characterized in that an adsorbent metal base for adsorbing carbon monoxide is loaded in the second pressure swing adsorption tower (3).
5. The device for recycling the desorption gas of the pressure swing adsorption device in the carbon disulfide production process according to any one of claims 1 to 4, wherein the product gas buffer tank (4) is a suction buffer tank, and a diaphragm type buffer mode is adopted, so that the flow unevenness of a suction pipeline is reduced, the inertia loss is reduced, and the suction performance is improved.
6. A method for recycling the gas desorbed from a pressure swing adsorption device is characterized by comprising the following steps:
step 1: the natural gas delivered by an external pipeline realizes stable pressure through a natural gas buffer tank (1), then is input into a first pressure swing adsorption tower (2), and hydrogen sulfide in the natural gas is absorbed by utilizing the high-pressure environment in the first pressure swing adsorption tower (2) and the special active carbon for high-sulfur capacity desulfurization;
step 2: then the gas is input into a second pressure swing adsorption tower (3), and the carbon monoxide in the natural gas is adsorbed by utilizing the high-pressure environment and the metal base of the second pressure swing adsorption tower (3);
and step 3: a higher natural gas finished product is obtained after passing through the second pressure swing adsorption tower (3) and is input into a finished product gas buffer tank (4), and the pressure of the finished product gas is stabilized through the finished product gas buffer tank (4);
and 4, step 4: meanwhile, natural gas components remained on the first pressure swing adsorption tower (2) and the second pressure swing adsorption tower (3) are extracted by a variable frequency vacuum pump (6), and are cooled by a condenser (7);
and 5: collecting hydrocarbons above C3+ and partial natural gas conveyed from a desorption gas buffer tank (8) and a condenser (7) by using a desorption gas mixing tank (9);
step 6: compressing the gas in the analysis gas mixing tank (9) by using an analysis gas compressor (10) to increase the pressure;
and 7: cooling the gas after the pressure increase by a desorption gas condenser (11);
and 8: collecting the condensed gas by using a compressor rear buffer tank (12);
and step 9: introducing gas collected in a buffer tank (12) behind a compressor into a fuel device of a synthesis reaction system to provide heat for the reaction of methane and sulfur; when a pressure gauge (13) detects the gas quantity required by normal combustion, which cannot be met by the gas in the buffer tank (12) behind the compressor, information is sent to a processor (14), the processor (14) opens a one-way electromagnetic valve (15), a part of gas is extracted from the natural gas buffer tank (1) to be used as supplement and is conveyed to a fuel device of a synthetic reaction system together with the gas in the buffer tank (12) behind the compressor, and heat is provided for the reaction of methane and sulfur.
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114015823A (en) * | 2021-10-27 | 2022-02-08 | 山西沃能化工科技有限公司 | Device and method for blast furnace hydrogen energy iron making by using pressure swing adsorption and hydrogen extraction gas separation |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4696680A (en) * | 1985-10-03 | 1987-09-29 | The United States Of America As Represented By The United States Department Of Energy | Method and apparatus for the selective separation of gaseous coal gasification products by pressure swing adsorption |
| CN102079999A (en) * | 2011-01-21 | 2011-06-01 | 成都赛普瑞兴科技有限公司 | Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material |
| CN105727687A (en) * | 2015-06-01 | 2016-07-06 | 代元军 | Desorption gas recycling apparatus and desorption gas recycling method for pressure swing adsorption apparatus |
-
2020
- 2020-11-23 CN CN202011322872.1A patent/CN112604453A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4696680A (en) * | 1985-10-03 | 1987-09-29 | The United States Of America As Represented By The United States Department Of Energy | Method and apparatus for the selective separation of gaseous coal gasification products by pressure swing adsorption |
| CN102079999A (en) * | 2011-01-21 | 2011-06-01 | 成都赛普瑞兴科技有限公司 | Method for producing liquefied natural gas and synthetic gas by taking coke oven gas as raw material |
| CN105727687A (en) * | 2015-06-01 | 2016-07-06 | 代元军 | Desorption gas recycling apparatus and desorption gas recycling method for pressure swing adsorption apparatus |
Non-Patent Citations (3)
| Title |
|---|
| 冯孝庭主编: "《吸附分离技术》", 30 November 2000, 北京：化学工业出版社 * |
| 化工部化工设备设计技术中心站机泵技术委员会编: "《工业泵选用手册》", 30 April 1998, 北京：化学工业出版社 * |
| 王驰著: "《典型有毒有害气体净化技术》", 31 March 2019, 北京：冶金工业出版社 * |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114015823A (en) * | 2021-10-27 | 2022-02-08 | 山西沃能化工科技有限公司 | Device and method for blast furnace hydrogen energy iron making by using pressure swing adsorption and hydrogen extraction gas separation |
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