CN110420536B - System and method for recycling VOCs (volatile organic compounds) on tank top and recycling nitrogen - Google Patents
System and method for recycling VOCs (volatile organic compounds) on tank top and recycling nitrogen Download PDFInfo
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- CN110420536B CN110420536B CN201910796896.1A CN201910796896A CN110420536B CN 110420536 B CN110420536 B CN 110420536B CN 201910796896 A CN201910796896 A CN 201910796896A CN 110420536 B CN110420536 B CN 110420536B
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 149
- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 97
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 71
- 238000004064 recycling Methods 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000001179 sorption measurement Methods 0.000 claims abstract description 114
- 239000007789 gas Substances 0.000 claims abstract description 110
- 238000001816 cooling Methods 0.000 claims abstract description 58
- 238000009833 condensation Methods 0.000 claims abstract description 44
- 230000005494 condensation Effects 0.000 claims abstract description 44
- 238000005057 refrigeration Methods 0.000 claims abstract description 44
- 238000011084 recovery Methods 0.000 claims abstract description 35
- 230000001172 regenerating effect Effects 0.000 claims abstract description 33
- 239000007788 liquid Substances 0.000 claims description 49
- 239000003463 adsorbent Substances 0.000 claims description 20
- 238000001704 evaporation Methods 0.000 claims description 16
- 238000003795 desorption Methods 0.000 claims description 13
- 230000008020 evaporation Effects 0.000 claims description 13
- 238000004458 analytical method Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 9
- 229910001873 dinitrogen Inorganic materials 0.000 claims description 8
- 230000001105 regulatory effect Effects 0.000 claims description 8
- 238000003860 storage Methods 0.000 claims description 6
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- 239000002912 waste gas Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 abstract description 2
- 239000003507 refrigerant Substances 0.000 description 10
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 8
- 239000000203 mixture Substances 0.000 description 6
- 239000002826 coolant Substances 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 239000013526 supercooled liquid Substances 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000007789 sealing Methods 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000002156 adsorbate Substances 0.000 description 1
- 230000003139 buffering effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000012544 monitoring process Methods 0.000 description 1
- 239000003348 petrochemical agent Substances 0.000 description 1
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000003892 spreading Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0003—Condensation of vapours; Recovering volatile solvents by condensation by using heat-exchange surfaces for indirect contact between gases or vapours and the cooling medium
-
- 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
- B01D53/002—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 condensation
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B21/00—Nitrogen; Compounds thereof
- C01B21/04—Purification or separation of nitrogen
- C01B21/0405—Purification or separation processes
- C01B21/0433—Physical processing only
- C01B21/045—Physical processing only by adsorption in solids
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- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Separation Of Gases By Adsorption (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a system and a method for recycling VOCs (volatile organic compounds) on the top of a tank and recycling nitrogen, wherein the system comprises a pressurizing subsystem, a condensing subsystem, a pressure swing adsorption subsystem and a nitrogen recycling subsystem, the pressurizing subsystem comprises a pressurizing air pump and a flame arrester, the condensing subsystem comprises a backheating heat exchanger, a precooling heat exchanger, a shallow cooling heat exchanger, a cryogenic heat exchanger, an explosion-proof refrigeration compressor, a condensing heat exchanger, an evaporative condensation heat exchanger, a throttling element and the like, the pressure swing adsorption subsystem comprises more than two groups of pressure swing adsorption devices which are arranged in parallel, and the nitrogen recycling subsystem comprises a nitrogen buffer tank and a one-way valve. According to the invention, the pressurizing regenerative heat exchanger, the precooling heat exchanger, the shallow cooling heat exchanger and the cryogenic heat exchanger are used for gradual cooling condensation, pressure swing adsorption recovery and purification of the gas of the VOCs on the top of the tank, the VOCs are finally recovered and utilized, the nitrogen on the top of the tank is purified and then is reused, and the unit has no secondary pollution during operation.
Description
Technical Field
The invention relates to a system and a method for recovering and recycling VOCs (volatile organic compounds) on the top of a tank and inert gas, in particular to a system and a method for recovering and recycling nitrogen-sealed tank top gas.
Background
In oil refining and petrochemical plants, various oils and petrochemicals are stored. Storage tanks are mostly built outdoors, and in order to prevent these materials from directly contacting with air, prevent the materials from volatilizing and being oxidized, and to ensure the safety of the container, nitrogen sealing devices are often used to keep the pressure of nitrogen gas at the top of the container constant, so that the nitrogen gas is isolated from the outside. In addition, in order to reduce the loss of material volatilization caused by small breath and large breath in the storage process of the storage tank, a nitrogen sealing device is also adopted.
And the treatment of the VOCs waste gas on the top of the tank is carried out comprehensively under the pressure of safe production and environmental protection. Chinese patent CN201721880896.2 discloses a device for recycling VOCs gas discharged from a fixed-roof storage tank, which solves the problem of up-to-standard discharge of VOCs but has large fuel gas loss through the treatment facility combining an alkaline washing unit, a recovery unit and a fuel gas pipe network. So far, no zero-emission system capable of recycling VOCs in VOCs gas at the top of the tank and recycling nitrogen sealed at the top of the tank exists in the market.
Disclosure of Invention
The purpose of the invention is as follows: in order to overcome the defects of the prior art, the first object of the invention is to provide a system which utilizes the technologies of pressurization, condensation, pressure swing adsorption and nitrogen recovery to realize the cooling recovery of VOCs on the top of a tank and purify and separate nitrogen for recycling; a second object is to provide a method for recovering VOCs using the above system, while the purified nitrogen can be reused.
The technical scheme is as follows: in order to solve the technical problem, the invention provides a system for recovering VOCs (volatile organic compounds) on the top of a tank and recycling nitrogen, which comprises a pressurization subsystem, a condensation subsystem, a pressure swing adsorption subsystem and a nitrogen recovery subsystem; the pressurizing subsystem is connected with an outlet of the gas inlet condensate tank and comprises a first flame arrester, a pressurizing air pump and a second flame arrester; the condensation subsystem comprises a regenerative heat exchanger, a gas-liquid separation tank, a first refrigeration subsystem and a second refrigeration subsystem, wherein the first refrigeration subsystem comprises a first explosion-proof refrigeration compressor, a condensation heat exchanger, a precooling throttling element, a precooling heat exchanger, a shallow cooling throttling element, a shallow cooling heat exchanger, an evaporation condensation throttling element, an evaporation condensation heat exchanger and a first gas-liquid separator; the second sub-refrigeration system comprises a second explosion-proof refrigeration compressor, an evaporative condensation heat exchanger, a cryogenic throttling element, a cryogenic heat exchanger and a second gas-liquid separator; the first refrigeration subsystem and the second refrigeration subsystem share an evaporative condensation heat exchanger;
the system comprises a regenerative heat exchanger, a pressurization subsystem, a pressure swing adsorption subsystem, a nitrogen recovery subsystem, a nitrogen buffer tank, a pressure swing adsorption subsystem, a nitrogen buffer tank, a control valve, a pressure swing adsorption subsystem and a control valve, wherein a hot side gas path inlet of the regenerative heat exchanger is connected with an outlet of the pressurization subsystem;
the first explosion-proof refrigeration compressor, the condensing heat exchanger, the three heat exchange branches connected in parallel and the first gas-liquid separator are sequentially connected to form a first refrigeration circulation loop; the first heat exchange branch comprises a precooling throttling element and a precooling heat exchanger, the second heat exchange branch comprises a shallow cooling throttling element and a shallow cooling heat exchanger, and the third heat exchange branch comprises an evaporation and condensation throttling element and an evaporation and condensation heat exchanger; the second explosion-proof refrigeration compressor, the evaporative condensation heat exchanger, the cryogenic throttling element, the cryogenic heat exchanger and the second gas-liquid separator are sequentially connected to form a second refrigeration circulation loop;
the pressure swing adsorption subsystem comprises more than two groups of pressure swing adsorption devices which are arranged in parallel; the outlet of the analysis valve of each group of pressure swing adsorption device is connected with the inlet of the gas inlet condensate tank.
Preferably, the pressure swing adsorption device comprises an adsorption tank, an air inlet valve, a desorption valve and an air outlet valve, wherein the adsorption tank comprises an adsorption tank body, an adsorbent arranged in the adsorption tank body and a desorption device for regenerating the adsorbent.
Preferably, the pressure swing adsorption devices are two groups, wherein one group is used for adsorbing the VOCs gas, and the other group is used for carrying out analysis treatment;
the two groups of pressure swing adsorption devices comprise an adsorption tank A, an adsorption tank B, an air inlet valve A, an air inlet valve B, a resolution valve A, a resolution valve B, an exhaust valve A and an exhaust valve B;
the gas-liquid separation tank is connected with a gas inlet at the bottom of the adsorption tank A through a gas inlet valve A; and the gas outlet at the top end of the adsorption tank A is connected with the nitrogen buffer tank through a gas outlet valve A.
Preferably, liquid outlets are formed in the bottoms of the heat recovery heat exchanger, the precooling heat exchanger, the shallow cooling heat exchanger and the cryogenic heat exchanger, and the condensed VOCs liquid is collected.
Preferably, the treatment temperature of the regenerative heat exchanger is 20 +/-3 ℃, the treatment temperature of the precooling heat exchanger is 4 +/-5 ℃, the treatment temperature of the shallow cooling heat exchanger is-25 +/-5 ℃, and the treatment temperature of the deep cooling heat exchanger is-60 +/-10 ℃.
The method for realizing VOCs recovery and nitrogen recycling by using the tank top VOCs recovery and nitrogen recycling system comprises the following steps:
a pressurizing step: discharging nitrogen-sealed VOCs gas on the tank top (101) to an inlet gas condensate tank (201) through a pressurizing air pump (203) for condensate and buffer storage;
a refrigeration step: the VOCs gas is introduced into a regenerative heat exchanger (205), a precooling heat exchanger (206), a shallow cooling heat exchanger (207) and a cryogenic heat exchanger (208) through a pressurizing air pump (203), and is cooled and liquefied through the circulating cooling of a refrigerating loop, more than 95 percent of the VOCs gas is cooled into liquid, and the liquid is recovered through liquid outlets at the bottoms of the regenerative heat exchanger (205), the precooling heat exchanger (206), the shallow cooling heat exchanger (207) and the cryogenic heat exchanger (208);
an adsorption treatment step: inputting the VOCs gas after condensation treatment into an adsorption tank of a pressure swing adsorption subsystem for adsorption treatment, and leading pure nitrogen obtained after adsorption to a nitrogen buffer tank (301) through a one-way valve (304); switching the VOCs gas after condensation treatment from the adsorption tank which is filled with the adsorption saturation to another adsorption tank for adsorption treatment through switching of a valve;
analyzing and regenerating steps: opening an adsorption tank desorption valve which is saturated in adsorption, desorbing the adsorbent, and desorbing VOCs gas adsorbed in the adsorbent; the desorbed VOCs gas is conveyed to the inlet of a gas inlet condensate tank (201) at the front end of the VOCs waste gas through pressure and enters the next recovery cycle;
a nitrogen recovery step; the adsorbed pure nitrogen is stored in a nitrogen buffer tank (301), and is recycled for the tank top (101) through a regulating valve A (102) or for a recycling device connected with the nitrogen buffer tank through a regulating valve B (103).
Has the advantages that: in the system for recycling the VOCs on the top of the tank and recycling the nitrogen, a condensing subsystem condenses high-temperature and high-pressure coolant gas generated by a first explosion-proof refrigerating compressor into high-pressure supercooled liquid through a condensing heat exchanger, and then conveys the high-pressure supercooled liquid into a precooling heat exchanger and a shallow cooling heat exchanger through a precooling throttling element and a shallow cooling throttling element, and the coolant evaporates and absorbs heat of the VOCs gas to vaporize, so that the VOCs gas is cooled and liquefied; high-temperature and high-pressure coolant gas generated by the second explosion-proof refrigeration compressor is condensed into high-pressure supercooled liquid by the evaporation and condensation heat exchanger and then is conveyed into the cryogenic heat exchanger by the cryogenic throttling element, and the coolant evaporates and absorbs heat of the VOCs gas to be vaporized, so that the VOCs gas is cooled and liquefied. In addition, the invention adopts a plurality of groups of pressure swing adsorption devices for alternate treatment, and the adsorption device is composed of two adsorption tanks for alternate adsorption and analysis. When one adsorption tank is in an adsorption state, the other adsorption tank is in a desorption state. When the amount of the VOCs gas adsorbed in the adsorption tank reaches a certain value (approaching saturation), the adsorption and desorption processes are switched. The analytic process adopts and reduces the interior pressure of adsorption tank, and along with the reduction of pressure, the saturated adsorption capacity reduces to deviate from the VOCs gas, the VOCs gas of deviating from passes through the entry of pressure transport device front end's the condensate tank that admits air, gets into the next recovery cycle. Compared with the prior art, the invention has the following advantages:
(1) the invention recovers VOCs gas through a pressurizing subsystem, a condensing subsystem, a pressure swing adsorption subsystem and a nitrogen recovery subsystem and recycles purified nitrogen through an adjusting valve; (2) the pressurizing air pump is an explosion-proof variable-frequency screw compressor, the pressure can be increased to 0.4-0.8 MPa, the condensation temperature of VOCs gas is increased, and the refrigeration efficiency is further improved; (3) the adsorption of the invention is more than two, the pressurized adsorption and the decompression analysis of VOCs gas can be simultaneously carried out, the working efficiency is improved, and the usage amount of the adsorbent is reduced; (4) VOCs gas adsorbed by the adsorbent in the adsorption tank is desorbed through pressure reduction, so that the adsorbent has activity again, extra power is not needed, and no secondary pollution is caused during the operation of the unit; (5) the oil gas desorbed from the adsorbent is introduced into the inlet of the gas inlet condensate tank at the front end of the condensation through pressure and then enters the next recovery cycle; (6) the VOCs gas on the tank top is gradually cooled sequentially through the regenerative heat exchanger, the precooling heat exchanger, the shallow cooling heat exchanger and the cryogenic heat exchanger, VOCs in the VOCs gas are effectively removed, and the condensed and separated VOCs are recycled; (7) the VOCs gas on the tank top is adsorbed to obtain high-purity nitrogen, and the high-purity nitrogen can be directly reused through the regulating valve.
Drawings
FIG. 1 is a schematic diagram of the configuration of a top VOCs recovery and nitrogen gas recycle system according to the present invention;
FIG. 2 is a schematic diagram of a condensing subsystem in the tank top VOCs recovery and nitrogen gas reuse system according to the present invention;
FIG. 3 is a schematic view of the VOCs gas flow of the top VOCs recovery and nitrogen reuse system of the present invention.
In FIG. 1, 101-tank top, 102-regulating valve A, 103-regulating valve B, 201-gas inlet condensate tank, 202-first flame arrester, 203-pressurized air pump, 204-second flame arrester, 205-regenerative heat exchanger, 206-precooling heat exchanger, 207-shallow cooling heat exchanger, 208-cryogenic heat exchanger, 209-gas-liquid separation tank, 301-nitrogen buffer tank, 302-adsorption tank A, 303-adsorption tank B, 304-check valve, 401-gas inlet valve A, 402-gas inlet valve B, 403-desorption valve A, 404-desorption valve B, 405-gas outlet valve A, 406-gas outlet valve B.
In FIG. 2, 501-a first explosion-proof refrigeration compressor, 502-a condensation heat exchanger, 503-a pre-cooling throttling element, 504-a shallow cooling throttling element, 505-an evaporation and condensation throttling element, 506-an evaporation and condensation heat exchanger, 601-a second explosion-proof refrigeration compressor, 602-a cryogenic throttling element and 603-a second gas-liquid separator.
In FIG. 3, 1-air inlet, 2-pressurized air pump outlet, 3-regenerative heat exchanger outlet, 4-precooling heat exchanger outlet, 5-shallow cooling heat exchanger outlet, 6-cryogenic heat exchanger outlet, and 7-adsorption outlet.
Detailed Description
The technical solution of the present invention is described in detail below with reference to the accompanying drawings, but the scope of the present invention is not limited to the embodiments.
As shown in fig. 1-2, a system for recovering VOCs and recycling nitrogen from a tank top disclosed in the embodiments of the present invention mainly includes a pressurization subsystem, a condensation subsystem, a pressure swing adsorption subsystem, and a nitrogen recovery subsystem; the pressurizing subsystem is connected with an outlet of the gas-intake condensate tank 201 and comprises a first flame arrester 202, a pressurizing air pump 203 and a second flame arrester 204; the condensing subsystem comprises a regenerative heat exchanger 205, a gas-liquid separation tank 209, a first refrigerating subsystem and a second refrigerating subsystem, wherein the first refrigerating subsystem comprises a first explosion-proof refrigerating compressor 501, a condensing heat exchanger 502, a precooling throttling element 503, a precooling heat exchanger 206, a shallow cooling throttling element 504, a shallow cooling heat exchanger 207, an evaporative condensation throttling element 505, an evaporative condensation heat exchanger 506 and a first gas-liquid separator 507; the second sub-refrigeration system comprises a second explosion-proof refrigeration compressor 601, an evaporative condensation heat exchanger 506, a cryogenic throttling element 602, a cryogenic heat exchanger 208 and a second gas-liquid separator 603; the first refrigeration subsystem and the second refrigeration subsystem share the evaporative condensing heat exchanger 506 to form a two-stage cascade refrigeration system.
A hot side gas path inlet of the regenerative heat exchanger 205 is connected with an outlet of a pressurization subsystem, a hot side gas path outlet of the regenerative heat exchanger 205 is connected with an inlet of a precooling heat exchanger 206, a gas path outlet of the precooling heat exchanger 206 is connected with an inlet of a shallow cooling heat exchanger 207, a gas path outlet of the shallow cooling heat exchanger 207 is connected with an inlet of a cryogenic heat exchanger 208, an outlet of the cryogenic heat exchanger 208 is connected with a cold side gas path inlet of the regenerative heat exchanger 205, a cold side gas path outlet of the regenerative heat exchanger 205 is connected with a gas inlet of a pressure swing adsorption subsystem through a gas-liquid separation tank 209, an exhaust port of the pressure swing adsorption subsystem is connected with a nitrogen recovery subsystem, the nitrogen recovery subsystem comprises a nitrogen buffer tank 301 and a one-way valve 304, the nitrogen buffer tank 301 is connected with an exhaust port;
the first explosion-proof refrigeration compressor 501, the condensing heat exchanger 502, the three heat exchange branches connected in parallel and the first gas-liquid separator 507 are connected in sequence to form a first refrigeration cycle loop; the first heat exchange branch comprises a pre-cooling throttling element 503 and a pre-cooling heat exchanger 206, the second heat exchange branch comprises a shallow cooling throttling element 504 and a shallow cooling heat exchanger 207, and the third heat exchange branch comprises an evaporation condensation throttling element 505 and an evaporation condensation heat exchanger 506; the second explosion-proof refrigeration compressor 601, the evaporative condensation heat exchanger 506, the cryogenic throttling element 602, the cryogenic heat exchanger 208 and the second gas-liquid separator 603 are sequentially connected to form a second refrigeration circulation loop;
the first flame arrester 202 and the second flame arrester 204 are respectively arranged at the front end and the rear end of the pressurizing air pump 203 and used for preventing flame from entering the next link or preventing flame from spreading between pipelines, the first flame arrester is of an explosion-proof type, and the second flame arrester is of an explosion-proof type. The pressurizing air pump 203 is an explosion-proof variable-frequency screw compressor, and the pressure can be increased to 0.4-0.8 MPa.
The pressure swing adsorption subsystem comprises more than two groups of pressure swing adsorption devices; each group of pressure swing adsorption devices comprises an adsorption tank, an air inlet valve, an analysis valve and an exhaust valve, wherein the adsorption tank comprises an adsorption tank body, an adsorbent arranged in the adsorption tank body and an analysis device for regenerating the adsorbent. In the embodiment, the voltage-changing absorption devices are arranged in two groups and are arranged in parallel; one group adsorbs VOCs gas while the other group is analyzed. The adsorbent in the adsorption tank body is coal-based activated carbon. The pressure swing adsorption apparatus includes an adsorption tank a 302, an adsorption tank B303, an intake valve a 401, an intake valve B402, a desorption valve a 403, a desorption valve B404, an exhaust valve a 405, and an exhaust valve B406.
The gas-liquid separation tank 203 is connected with a gas inlet at the bottom of the adsorption tank A302 through a gas inlet valve A401; the gas outlet at the top end of the adsorption tank A302 is connected with the nitrogen buffer tank 301 through a gas outlet valve A405; an inlet of an analysis valve A403 is connected between an air inlet at the bottom of the adsorption tank A302 and an outlet of the air inlet valve A401, and an outlet of the analysis valve A403 is connected with the air inlet condensate tank 201;
the regenerative heat exchanger 205, the precooling heat exchanger 206, the shallow cooling heat exchanger 207 and the cryogenic heat exchanger 208 are efficient shell-and-tube heat exchangers or efficient spiral tube heat exchangers, liquid outlets are formed in the bottoms of the heat exchangers, and condensed VOCs liquid is collected. The treatment temperature of the regenerative heat exchanger 205 is 20 +/-3 ℃, the treatment temperature of the precooling heat exchanger 206 is 4 +/-5 ℃, the treatment temperature of the shallow cooling heat exchanger 207 is-25 +/-5 ℃, the treatment temperature of the deep cooling heat exchanger 208 is-60 +/-10 ℃, and the treatment temperature of each heat exchanger can be properly adjusted for different VOCs materials and pressure increasing.
The main working principle of the system of the embodiment of the invention is as follows: when the refrigeration subsystem works, high-temperature and high-pressure refrigerant gas discharged by the first explosion-proof refrigeration compressor 501 enters the condensing heat exchanger 502 to be condensed into high-pressure supercooled refrigerant liquid, the high-temperature and high-pressure refrigerant gas is throttled and reduced into low-temperature and low-pressure vapor-liquid two-phase mixture by three paths through the precooling throttling element 503, the shallow-cooling throttling element 504 and the evaporating and condensing throttling element 505 to respectively enter the precooling heat exchanger 206, the shallow-cooling heat exchanger 207 and the evaporating and condensing heat exchanger 506, the low-temperature and low-pressure vapor-liquid two-phase mixture is evaporated in the precooling heat exchanger 206 and the shallow-cooling heat exchanger 207 and absorbs the heat of VOCs gas passing through the low-temperature and low-pressure vapor-liquid two-phase mixture, the high-temperature and high-pressure refrigerant gas discharged by the second explosion-proof refrigeration compressor 601 passing through the evaporating and condensing heat exchanger 506, so that, after the refrigerant is fully vaporized, the refrigerant is compressed by the first explosion-proof refrigeration compressor 501 through the first gas-liquid separator 507 and enters the next cycle. The high-temperature high-pressure refrigerant gas discharged by the second explosion-proof refrigeration compressor 601 enters the evaporative condensation heat exchanger 506 to be condensed into high-pressure supercooled refrigerant liquid, the high-temperature supercooled refrigerant liquid is throttled and reduced into low-temperature low-pressure gas-liquid two-phase mixture through the cryogenic throttling element 602 and enters the cryogenic heat exchanger 208, the low-temperature low-pressure gas-liquid two-phase mixture is evaporated in the cryogenic heat exchanger 208 and absorbs the heat of the VOCs gas passing through the low-temperature low-pressure gas-liquid two-phase mixture, the VOCs gas flowing through the cryogenic heat exchanger 208 is further cooled and liquefied, and the refrigerant is fully vaporized and then compressed by the second explosion-proof refrigeration compressor 601 to.
The method for realizing VOCs recovery and nitrogen recycling by using the tank top VOCs recovery and nitrogen recycling system mainly comprises the following steps:
(1) a pressurizing step: discharging nitrogen-sealed VOCs gas on the tank top 101 into an air inlet condensate tank 201 through a pressurizing air pump 203 for condensing and buffering;
(2) a refrigeration step: the VOCs gas is introduced into a regenerative heat exchanger 205, a precooling heat exchanger 206, a shallow cooling heat exchanger 207 and a cryogenic heat exchanger 208 through a pressurizing air pump 203, and is cooled and liquefied through the circulating cooling of a refrigerating loop, more than 95 percent of the VOCs gas is cooled into liquid, and is recovered through liquid outlets at the bottoms of the regenerative heat exchanger 205, the precooling heat exchanger 206, the shallow cooling heat exchanger 207 and the cryogenic heat exchanger 208;
(3) an adsorption treatment step: inputting the VOCs gas subjected to condensation treatment into an adsorption tank for adsorption treatment, and introducing pure nitrogen obtained after adsorption into a nitrogen buffer tank 301 through a one-way valve 304; switching the VOCs gas after condensation treatment from the adsorption tank which is filled with the adsorption saturation to another adsorption tank for adsorption treatment through switching of a valve;
(4) analyzing and regenerating steps: opening an adsorption tank desorption valve which is saturated in adsorption, desorbing the adsorbent, and desorbing VOCs gas adsorbed in the adsorbent; the desorbed VOCs gas is conveyed to the inlet of the gas inlet condensate tank 201 at the front end of the VOCs waste gas through pressure, and enters the next recovery cycle;
(5) a nitrogen recovery step; the adsorbed pure nitrogen is stored in a nitrogen buffer tank 301 and is recycled to the tank top 101 through a regulating valve A102 or a recycling device connected with the nitrogen buffer tank through a regulating valve B103.
TABLE 1 benzene tank head gas recycle Process parameters
This example illustrates the effectiveness of embodiments of the present invention by measuring process parameters when the VOCs component is benzene, table 1 for benzene drum top gas recovery process parameters, where the monitoring points are shown in fig. 3. The VOCs gas at the top of the tank is pressurized to 0.6MPa by the pressurizing air pump 203, and then is cooled in a grading manner by the heat regenerative heat exchanger 205, the precooling heat exchanger 206, the shallow cooling heat exchanger 207 and the cryogenic heat exchanger 208 in sequence, so that the VOCs gas is cooled to about minus 65 ℃ step by step, more than 99% of the VOCs gas is cooled to be liquid, and the liquid is recovered by a liquid outlet at the bottom of the corresponding heat exchanger. The treated tank top gas is nitrogen with purity over 99.99 percent and can be directly used.
Specifically, the treatment temperature of the regenerative heat exchanger 205 is 20 +/-3 ℃, the treatment temperature of the precooling heat exchanger 206 is 5 +/-3 ℃, the treatment temperature of the shallow cooling heat exchanger 207 is-25 +/-3 ℃, the treatment temperature of the deep cooling heat exchanger 208 is-65 +/-3 ℃, and the whole machine continuously circulates through the above processes, so that the purpose of continuously cooling the VOCs gas to-65 ℃ is achieved. At the moment, the gas content of VOCs is less than or equal to 30mg/m3The recovery rate of VOCs is more than or equal to 99 percent, and the content of nitrogen is more than or equal to 99.99 percent. Compared with a normal-pressure condensation system, the refrigeration efficiency is improved by about 8%, and the occupied area of the condensation prying block unit is reduced by about 5%. According to the specific components of the VOCs gas and the lifting pressure, the temperature field can be adjusted in time.
The condensed residual gas on the top of the tank enters an adsorption tank through an air inlet valve, and the nitrogen which is difficult to adsorb is separated from the VOCs which is easy to adsorb by utilizing the selectivity of the adsorbent in the adsorption tank to the adsorbate, namely the difference of the binding force between the VOCs gas and the nitrogen and the active carbon, wherein the content of the VOCs gas is less than or equal to 1mg/m3The purification rate of VOCs is more than or equal to 99.99 percent, and the nitrogen content is more than or equal to 99.999 percent; and opening a resolving valve connected with an air inlet at the bottom of the adsorption tank, reducing the pressure, conveying the gas to an inlet of the gas inlet condensate tank 102, and entering the next round of adsorption cycle to regenerate the adsorbent. Compared with a normal-pressure adsorption system with a condensation temperature subsystem, the system has the advantages that the filling amount of the adsorbent is reduced by 50%, the cost of the adsorption prying block unit is reduced by 45-55%, and the occupied area of the adsorption prying block unit is reduced by 20%. Pure nitrogen can be directly conveyed outwards through the regulating valve and directly utilized, so that the loss of the nitrogen seal at the top of the tank is reduced, and the income can be created.
As noted above, while the present invention has been shown and described with reference to certain preferred embodiments, it is not to be construed as limited thereto. Various changes in form and detail may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.
Claims (5)
1. Tank deck VOCs retrieves and nitrogen gas system of recycling, its characterized in that: comprises a pressurization subsystem, a condensation subsystem, a pressure swing adsorption subsystem and a nitrogen recovery subsystem; the pressurizing subsystem is connected with an outlet of the gas inlet condensate tank (201) and comprises a first flame arrester (202), a pressurizing air pump (203) and a second flame arrester (204); the pressurizing air pump (203) is an explosion-proof variable-frequency screw compressor, and the pressure is increased to 0.4-0.8 MPa; the condensing subsystem comprises a regenerative heat exchanger (205), a gas-liquid separation tank (209), a first refrigerating subsystem and a second refrigerating subsystem, wherein the first refrigerating subsystem comprises a first explosion-proof refrigerating compressor (501), a condensing heat exchanger (502), a precooling throttling element (503), a precooling heat exchanger (206), a shallow cooling throttling element (504), a shallow cooling heat exchanger (207), an evaporation and condensation throttling element (505), an evaporation and condensation heat exchanger (506) and a first gas-liquid separator (507); the second refrigeration subsystem comprises a second explosion-proof refrigeration compressor (601), an evaporative condensation heat exchanger (506), a cryogenic throttling element (602), a cryogenic heat exchanger (208) and a second gas-liquid separator (603); the first refrigeration subsystem and the second refrigeration subsystem share an evaporative condensation heat exchanger (506);
the hot side gas circuit inlet of the regenerative heat exchanger (205) is connected with the outlet of the pressurization subsystem, the hot side gas circuit outlet of the regenerative heat exchanger (205) is connected with the inlet of the precooling heat exchanger (206), the gas circuit outlet of the precooling heat exchanger (206) is connected with the inlet of the shallow cooling heat exchanger (207), the gas circuit outlet of the shallow cooling heat exchanger (207) is connected with the inlet of the deep cooling heat exchanger (208), the outlet of the deep cooling heat exchanger (208) is connected with the inlet of the cold side gas circuit of the regenerative heat exchanger (205), the outlet of the cold side gas circuit of the regenerative heat exchanger (205) is connected with the gas inlet of the pressure swing adsorption subsystem through the gas-liquid separation tank (209), the gas outlet of the pressure swing adsorption subsystem is connected with the nitrogen recovery subsystem, the nitrogen recovery subsystem comprises a nitrogen buffer tank (301) and a check valve (304), the nitrogen buffer tank (301, a control valve is connected between the nitrogen buffer tank (301) and the tank top (101);
the first explosion-proof refrigeration compressor (501), the condensing heat exchanger (502), the three heat exchange branches connected in parallel and the first gas-liquid separator (507) are sequentially connected to form a first refrigeration circulation loop; the first heat exchange branch comprises a pre-cooling throttling element (503) and a pre-cooling heat exchanger (206), the second heat exchange branch comprises a shallow cooling throttling element (504) and a shallow cooling heat exchanger (207), and the third heat exchange branch comprises an evaporation and condensation throttling element (505) and an evaporation and condensation heat exchanger (506); the second explosion-proof refrigeration compressor (601), the evaporative condensation heat exchanger (506), the cryogenic throttling element (602), the cryogenic heat exchanger (208) and the second gas-liquid separator (603) are sequentially connected to form a second refrigeration circulation loop; the treatment temperature of the regenerative heat exchanger (205) is 20 +/-3 ℃, the treatment temperature of the precooling heat exchanger (206) is 5 +/-3 ℃, the treatment temperature of the shallow cooling heat exchanger (207) is-25 +/-3 ℃, and the treatment temperature of the cryogenic heat exchanger (208) is-65 +/-3 ℃;
the pressure swing adsorption subsystem comprises more than two groups of pressure swing adsorption devices which are arranged in parallel; the outlet of the analysis valve of each group of pressure swing adsorption devices is connected with the inlet of the gas inlet condensate tank (201).
2. The system of claim 1 for recovery of top-tank VOCs and nitrogen gas reuse, wherein: the pressure swing adsorption device comprises an adsorption tank, an air inlet valve, a desorption valve and an air outlet valve, wherein the adsorption tank comprises an adsorption tank body, an adsorbent arranged in the adsorption tank body and a desorption device for regenerating the adsorbent.
3. The system of claim 1 for recovery of top-tank VOCs and nitrogen gas reuse, wherein: the pressure swing adsorption devices are divided into two groups, wherein one group is used for adsorbing VOCs gas, and the other group is used for carrying out analysis treatment;
the two groups of pressure swing adsorption devices comprise an adsorption tank A (302), an adsorption tank B (303), an air inlet valve A (401), an air inlet valve B (402), a resolution valve A (403), a resolution valve B (404), an exhaust valve A (405) and an exhaust valve B (406);
the gas-liquid separation tank (209) is connected with a gas inlet at the bottom of the adsorption tank A (302) through a gas inlet valve A (401); and the gas outlet at the top end of the adsorption tank A (302) is connected with the nitrogen buffer tank (301) through a gas outlet valve A (405).
4. The system of claim 1 for recovery of top-tank VOCs and nitrogen gas reuse, wherein: liquid outlets are formed in the bottoms of the heat recovery heat exchanger (205), the precooling heat exchanger (206), the shallow cooling heat exchanger (207) and the deep cooling heat exchanger (208), and the condensed VOCs liquid is collected.
5. A method for recovering VOCs and recycling nitrogen using the system for recovering VOCs and recycling nitrogen from the top of a tank of any one of claims 1 to 4, comprising the steps of:
a pressurizing step: discharging nitrogen-sealed VOCs gas on the tank top (101) to an inlet gas condensate tank (201) through a pressurizing air pump (203) for condensate and buffer storage;
a refrigeration step: the VOCs gas is introduced into a regenerative heat exchanger (205), a precooling heat exchanger (206), a shallow cooling heat exchanger (207) and a cryogenic heat exchanger (208) through a pressurizing air pump (203), and is cooled and liquefied through the circulating cooling of a refrigerating loop, more than 95 percent of the VOCs gas is cooled into liquid, and the liquid is recovered through liquid outlets at the bottoms of the regenerative heat exchanger (205), the precooling heat exchanger (206), the shallow cooling heat exchanger (207) and the cryogenic heat exchanger (208);
an adsorption treatment step: inputting the VOCs gas after condensation treatment into an adsorption tank of a pressure swing adsorption subsystem for adsorption treatment, and leading pure nitrogen obtained after adsorption to a nitrogen buffer tank (301) through a one-way valve (304); switching the VOCs gas after condensation treatment from the adsorption tank which is filled with the adsorption saturation to another adsorption tank for adsorption treatment through switching of a valve;
analyzing and regenerating steps: opening an adsorption tank desorption valve which is saturated in adsorption, desorbing the adsorbent, and desorbing VOCs gas adsorbed in the adsorbent; the desorbed VOCs gas is conveyed to the inlet of a gas inlet condensate tank (201) at the front end of the VOCs waste gas through pressure and enters the next recovery cycle;
a nitrogen recovery step; the adsorbed pure nitrogen is stored in a nitrogen buffer tank (301), and is recycled for the tank top (101) through a regulating valve A (102) or for a recycling device connected with the nitrogen buffer tank through a regulating valve B (103).
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| CN115089992B (en) * | 2022-07-07 | 2024-05-10 | 连云港市拓普科技发展有限公司 | Shallow cooling adsorption and desorption VOCs gas recovery method |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20140096184A (en) * | 2013-01-25 | 2014-08-04 | 삼성중공업 주식회사 | Voc recovery system |
| CN104888490A (en) * | 2015-05-29 | 2015-09-09 | 南京都乐制冷设备有限公司 | VOCs gas condensation recovery device and method |
| CN108211648A (en) * | 2018-02-08 | 2018-06-29 | 广东申菱环境系统股份有限公司 | Heat reclamation type condenses and alternating temperature pressure-variable adsorption group technology device for recovering oil and gas |
| CN207722586U (en) * | 2017-11-10 | 2018-08-14 | 南京天膜科技股份有限公司 | A kind of device realized VOCs zero-emissions and recycle nitrogen |
| CN209009342U (en) * | 2018-08-31 | 2019-06-21 | 江苏新久扬环保设备科技有限公司 | A kind of gas of oil storage tank recovery system of recyclable nitrogen |
| CN110143378A (en) * | 2018-02-13 | 2019-08-20 | 中国石油化工股份有限公司 | Storage tank VOCs safe collection Zero emission method |
| CN210728724U (en) * | 2019-08-27 | 2020-06-12 | 南京都乐制冷设备有限公司 | System for recycling VOCs (volatile organic compounds) on tank top and recycling nitrogen |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4867773A (en) * | 1988-10-06 | 1989-09-19 | Air Products And Chemicals, Inc. | Cryogenic process for nitrogen production with oxygen-enriched recycle |
-
2019
- 2019-08-27 CN CN201910796896.1A patent/CN110420536B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20140096184A (en) * | 2013-01-25 | 2014-08-04 | 삼성중공업 주식회사 | Voc recovery system |
| CN104888490A (en) * | 2015-05-29 | 2015-09-09 | 南京都乐制冷设备有限公司 | VOCs gas condensation recovery device and method |
| CN207722586U (en) * | 2017-11-10 | 2018-08-14 | 南京天膜科技股份有限公司 | A kind of device realized VOCs zero-emissions and recycle nitrogen |
| CN108211648A (en) * | 2018-02-08 | 2018-06-29 | 广东申菱环境系统股份有限公司 | Heat reclamation type condenses and alternating temperature pressure-variable adsorption group technology device for recovering oil and gas |
| CN110143378A (en) * | 2018-02-13 | 2019-08-20 | 中国石油化工股份有限公司 | Storage tank VOCs safe collection Zero emission method |
| CN209009342U (en) * | 2018-08-31 | 2019-06-21 | 江苏新久扬环保设备科技有限公司 | A kind of gas of oil storage tank recovery system of recyclable nitrogen |
| CN210728724U (en) * | 2019-08-27 | 2020-06-12 | 南京都乐制冷设备有限公司 | System for recycling VOCs (volatile organic compounds) on tank top and recycling nitrogen |
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Denomination of invention: System and method of VOCs recovery and nitrogen reuse on tank top Effective date of registration: 20221025 Granted publication date: 20210625 Pledgee: Jiangsu SINOSURE technology microfinance Co.,Ltd. Pledgor: NANJING ALL DELIGHT REFRIGERATION EQUIPMENT Co.,Ltd. Registration number: Y2022980019380 |
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