CN116603348A - Recycling treatment and recovery system and method for benzene-containing VOCs waste gas in chemical plant area - Google Patents
Recycling treatment and recovery system and method for benzene-containing VOCs waste gas in chemical plant area Download PDFInfo
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- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 title claims abstract description 363
- 239000012855 volatile organic compound Substances 0.000 title claims abstract description 67
- 239000002912 waste gas Substances 0.000 title claims abstract description 60
- 238000000034 method Methods 0.000 title claims abstract description 41
- 238000011084 recovery Methods 0.000 title claims abstract description 37
- 238000004064 recycling Methods 0.000 title claims abstract description 35
- 239000000126 substance Substances 0.000 title claims abstract description 24
- 239000002250 absorbent Substances 0.000 claims abstract description 148
- 230000002745 absorbent Effects 0.000 claims abstract description 148
- 230000008929 regeneration Effects 0.000 claims abstract description 76
- 238000011069 regeneration method Methods 0.000 claims abstract description 76
- 239000002904 solvent Substances 0.000 claims abstract description 45
- 238000003795 desorption Methods 0.000 claims abstract description 41
- 230000001502 supplementing effect Effects 0.000 claims abstract description 40
- 238000001816 cooling Methods 0.000 claims abstract description 37
- 238000002485 combustion reaction Methods 0.000 claims abstract description 33
- 238000003860 storage Methods 0.000 claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 claims abstract description 15
- 238000010521 absorption reaction Methods 0.000 claims description 89
- 239000007789 gas Substances 0.000 claims description 83
- 239000007788 liquid Substances 0.000 claims description 79
- 239000007791 liquid phase Substances 0.000 claims description 54
- 238000010992 reflux Methods 0.000 claims description 36
- 238000009833 condensation Methods 0.000 claims description 24
- 230000005494 condensation Effects 0.000 claims description 24
- 238000000605 extraction Methods 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 19
- 239000012071 phase Substances 0.000 claims description 16
- 238000000926 separation method Methods 0.000 claims description 14
- 150000001555 benzenes Chemical class 0.000 claims description 11
- 230000001172 regenerating effect Effects 0.000 claims description 6
- 230000006837 decompression Effects 0.000 claims description 5
- 230000007246 mechanism Effects 0.000 claims description 3
- 238000012544 monitoring process Methods 0.000 claims description 3
- 230000008901 benefit Effects 0.000 abstract description 9
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 15
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 12
- 230000008569 process Effects 0.000 description 10
- 230000000694 effects Effects 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 238000001179 sorption measurement Methods 0.000 description 7
- 239000002699 waste material Substances 0.000 description 7
- 239000010815 organic waste Substances 0.000 description 6
- PPASLZSBLFJQEF-RKJRWTFHSA-M sodium ascorbate Substances [Na+].OC[C@@H](O)[C@H]1OC(=O)C(O)=C1[O-] PPASLZSBLFJQEF-RKJRWTFHSA-M 0.000 description 6
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 5
- 239000004098 Tetracycline Substances 0.000 description 5
- 229910052799 carbon Inorganic materials 0.000 description 5
- 239000002351 wastewater Substances 0.000 description 5
- 239000004283 Sodium sorbate Substances 0.000 description 4
- 239000011692 calcium ascorbate Substances 0.000 description 4
- 239000002910 solid waste Substances 0.000 description 4
- SJRJJKPEHAURKC-UHFFFAOYSA-N N-Methylmorpholine Chemical compound CN1CCOCC1 SJRJJKPEHAURKC-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 239000002151 riboflavin Substances 0.000 description 3
- 239000000661 sodium alginate Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- KVZJLSYJROEPSQ-UHFFFAOYSA-N 1,2-dimethylcyclohexane Chemical compound CC1CCCCC1C KVZJLSYJROEPSQ-UHFFFAOYSA-N 0.000 description 2
- YJTKZCDBKVTVBY-UHFFFAOYSA-N 1,3-Diphenylbenzene Chemical group C1=CC=CC=C1C1=CC=CC(C=2C=CC=CC=2)=C1 YJTKZCDBKVTVBY-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000007084 catalytic combustion reaction Methods 0.000 description 2
- 238000009841 combustion method Methods 0.000 description 2
- 239000000110 cooling liquid Substances 0.000 description 2
- 238000007599 discharging Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000007654 immersion Methods 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000003507 refrigerant Substances 0.000 description 2
- 230000009469 supplementation Effects 0.000 description 2
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 description 1
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002920 hazardous waste Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- VUZPPFZMUPKLLV-UHFFFAOYSA-N methane;hydrate Chemical compound C.O VUZPPFZMUPKLLV-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910000510 noble metal Inorganic materials 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 230000008092 positive effect Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005057 refrigeration Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 238000012958 reprocessing Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- HXJUTPCZVOIRIF-UHFFFAOYSA-N sulfolane Chemical compound O=S1(=O)CCCC1 HXJUTPCZVOIRIF-UHFFFAOYSA-N 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
Classifications
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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
- B01D53/002—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
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0051—Regulation processes; Control systems, e.g. valves
-
- 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
- B01D5/0033—Other features
- B01D5/0054—General arrangements, e.g. flow sheets
-
- 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
- B01D5/0057—Condensation of vapours; Recovering volatile solvents by condensation in combination with other processes
-
- 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
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/009—Collecting, removing and/or treatment of the condensate
-
- 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
- B01D5/0078—Condensation of vapours; Recovering volatile solvents by condensation characterised by auxiliary systems or arrangements
- B01D5/0093—Removing and treatment of non condensable gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1431—Pretreatment by other processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D2257/7027—Aromatic hydrocarbons
-
- 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
- B01D2257/708—Volatile organic compounds V.O.C.'s
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- 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
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Automation & Control Theory (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a benzene-containing VOC in a chemical plant area S The waste gas recycling treatment recovery system and method, in particular to the technical field of benzene-containing VOCs waste gas recycling treatment recovery, which comprises a fan, wherein one end of the fan is connected with a pre-cooling condensing unit, the pre-cooling condensing unit is connected with a solvent absorbing unit, the upper part of the solvent absorbing unit is communicated with an inlet of an absorbent circulating supplementing unit and a factory combustion system, the lower part of the solvent absorbing unit is connected with a rectifying desorption unit, the upper part and the lower part of the rectifying desorption unit are respectively connected with a heat exchange condensing unit inlet and an absorbent regeneration unit, the upper part of the heat exchange condensing unit is respectively connected with a vacuum unit and a factory benzene storage tank, the vacuum unit is also communicated with the factory combustion system, and the absorbent regeneration unitAnd is also connected with the inlet of the absorbent circulation supplementing unit. The system has unique structure, improves the production efficiency of the system, has pure and recyclable absorbent components, small overall consumption, does not produce secondary pollution and VOC S The exhaust emission concentration is low and the recovery benefit is good.
Description
Technical Field
The invention belongs to the technical field of recycling treatment and recovery of benzene-containing VOCs (volatile organic compounds) waste gas, and particularly relates to a recycling treatment and recovery system and method of benzene-containing VOCs waste gas in a chemical plant area.
Background
With the high-speed development of the industry in China, benzene series are widely applied and common chemical raw materials in various industrial production and storage and transportation processes, and most benzene series (such as benzene, toluene, xylene and the like) have strong volatility, are easily volatilized into the air even under normal temperature conditions, and can form volatile organic gases (VOCs) in the production, storage and transportation processes and the use processes, thereby causing atmospheric pollution, not only damaging the environment, but also seriously threatening the human health, and therefore, the exhaust gas emission of the benzene-containing VOCs needs to be comprehensively treated;
according to different chemical production processes and exhaust emission modes, benzene-containing VOCs exhaust gas has different treatment technologies, and the main widely used technology at present is as follows: adsorption, combustion, absorption;
the adsorption method mainly uses active carbon adsorption, namely, after the benzene-containing VOCs waste gas passes through the active carbon, the special active carbon is used for adsorbing organic components such as triphenyl, and when the active carbon adsorption reaches saturation, the active carbon is desorbed and regenerated, so that the aim of recycling is fulfilled. After a certain period of use, the adsorption capacity of the activated carbon starts to decrease, and the activated carbon needs to be replaced. Therefore, the method is only suitable for treating the working conditions of low concentration and small amount of waste gas, if the amount of waste gas is large or the concentration is high, the activated carbon needs to be replaced frequently, a large amount of generated waste activated carbon is used as hazardous waste, secondary pollution is easy to cause, and in addition, the adsorption effect of the activated carbon on other linear alkanes is poor. Therefore, the adsorption method has better purification effect, but has larger initial investment, high operation cost, secondary pollution and higher treatment cost, and is difficult to keep long-term use in actual production.
The combustion method mainly comprises direct combustion and catalytic combustion, and is only suitable for organic waste gas with low concentration, large treatment capacity and low content of dangerous components in consideration of the limit value of emission standard; the catalytic combustion method can effectively treat the benzene-containing VOCs waste gas, but oxidizes organic pollutants in the waste gas into carbon dioxide and water at a lower temperature under the action of noble metal catalysts such as lead, palladium and the like, and the method is an organic waste gas treatment method without open fire under the catalysis condition, can treat various organic waste gases, has high cost, is only suitable for treating the organic waste gas with high concentration and low treatment capacity, and can easily explode due to strict temperature control of a catalyst bed layer, and has potential safety hazard. In addition, the combustion method mainly purifies the gas, and cannot effectively recover and recycle the economic components in the gas.
The absorption method mainly adopts an aqueous solution to absorb and treat the benzene-containing VOCs waste gas by a membrane contactor or a spraying mode. The absorption mode of the membrane contactor has high input cost and operation cost, and is difficult to implement for common enterprises. The spray absorption method is widely used, because the method adopts a spray mode to treat the waste gas containing benzene VOCs, and then adopts a rectification mode to recover the effective components. The absorption method can treat organic waste gas with high concentration and low treatment capacity, can treat organic waste gas with low concentration and high treatment capacity, has wide application range and small limit, but after the 'triphenyl' substance in the waste gas is dissolved and absorbed by the spray liquid, the generated waste water is required to be treated, and the method has the advantages of simpler structure, convenient implementation and relatively low input cost, but can generate dangerous waste such as benzene-containing waste liquid, and has higher requirement on the purity of the recovered effective components if the recovered effective components are utilized, so that the subsequent operation and maintenance cost is higher.
In conclusion, the benzene-containing VOCs waste gas treatment method commonly adopted in China at present has the advantages and limitations that: the system and the method for recycling the benzene-containing VOCs waste gas in the chemical plant area, which have the advantages of high input cost, high running cost, waste of a large amount of resources, secondary pollution, no meeting of increasingly strict emission limit values of the tail gas discharged after treatment, no consideration of resource saving and environmental friendliness in the treatment process, or no meeting of increasingly strong resource recycling requirements and material purity requirements even in consideration of the output of the treatment process of the terminal output, are needed, so that the waste gas is discharged up to the standard, pure benzene products are obtained, recycling and recycling of the absorbent are realized, and secondary pollution such as waste water, solid waste and the like is avoided.
Disclosure of Invention
The invention aims to overcome the defects of the prior art, and provides a recycling treatment and recovery system and method for benzene-containing VOCs waste gas in a chemical plant area, which can realize standard discharge of waste gas, obtain pure benzene products, realize recycling and utilization of absorbent, and can not generate secondary pollution such as waste water, solid waste and the like.
The invention solves the technical problems by adopting the following technical scheme:
benzene-containing VOC (volatile organic compound) in chemical plant area S The waste gas recycling treatment recovery system comprises a fan, a pre-cooling condensing unit, a solvent absorbing unit, a rectifying desorption unit, a heat exchange condensing unit, a vacuum unit, an absorbent circulation supplementing unit and an absorbent regeneration unit, wherein one end of the fan is connected with a benzene-containing VOC (volatile organic compound) S The waste gas inlet is connected, the other end is connected with the pre-cooling condensing unit through an air inlet pipe, the other end of the pre-cooling condensing unit is connected with the solvent absorbing unit through a pipeline, one end of the upper part of the solvent absorbing unit is connected with the inlet of the absorbent circulating supplementing unit through an absorbent supplementing liquid inlet pipe, and the other end of the upper part of the solvent absorbing unit is connected with the absorbent circulating supplementing unit through an absorbent supplementing liquid inlet pipeOne end is communicated with a factory combustion system through an exhaust pipe, the lower part of the solvent absorption unit is connected with the rectification desorption unit through a pipeline, the upper part of the rectification desorption unit is connected with an inlet of the heat exchange condensation unit through a pipeline, the lower part of the rectification desorption unit is connected with the absorbent regeneration unit, one end of the upper part of the heat exchange condensation unit is connected with the vacuum unit, the other end of the heat exchange condensation unit is connected with the factory benzene storage tank, the other end of the vacuum unit is communicated with the factory combustion system through the exhaust pipe, the other end of the absorbent regeneration unit is connected with an inlet of the absorbent circulation supplementing unit through an absorbent supplementing liquid inlet pipe, and liquid phase outlets of the precooling condensation unit, the rectification desorption unit and the heat exchange condensation unit are all connected with the factory benzene storage tank through extraction pipes.
Moreover, the pre-cooling condensing unit comprises a group of condensing components and a production pump which are connected in series, and the pre-cooling condenser and the gas-liquid separator; the top of the gas-liquid separator is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator is provided with a liquid phase outlet; the non-condensable gas outlet of the gas-liquid separator is connected with the solvent absorption unit; and a liquid phase outlet of the gas-liquid separator is connected with a factory benzene storage tank through a production pump and a production pipe.
Furthermore, the solvent absorption unit comprises an absorption tower, an absorption tower circulating heat exchanger and a circulating pump, wherein the bottom of the absorption tower is provided with benzene-containing VOC S The waste gas feed inlet is communicated with a top noncondensable gas outlet of the gas-liquid separator of the pre-cooling condensing unit, an absorbent supplementing liquid inlet is arranged on the upper portion of the absorption tower, the liquid inlet is connected with an outlet of the absorbent circulating supplementing unit, an absorption tower circulating heat exchanger is arranged in the absorption tower, the other end of the absorption tower circulating heat exchanger is connected with a circulating pump, and the other end of the circulating pump is connected with the rectifying desorption unit.
The rectification desorption unit comprises a rectification tower inlet heat exchanger, a rectification tower, a tower top condenser, a tower top reflux tank, a tower top reflux pump and a tower bottom reboiler, wherein a benzene-containing absorbent material feeding port is arranged in the middle of the rectification tower, the feeding port is connected with the rectification tower inlet heat exchanger, the other end of the rectification tower inlet heat exchanger is connected with a solvent absorption unit circulating pump outlet, the tower top condenser is connected with the tower top reflux tank, one end of the tower top reflux tank is connected with the tower top reflux pump, the other end of the tower top reflux pump is connected with a heat exchange condensing unit inlet, one end of the tower top reflux pump returns to the rectification tower, the other end outlet of the tower top reflux pump is led to a factory benzene storage tank, one end of the outlet of the tower bottom reboiler is connected with the rectification tower, and the other end of the outlet of the tower bottom reboiler is connected with an absorbent regeneration unit inlet.
Moreover, the heat exchange condensing unit comprises a heat exchange condenser and a gas-liquid separator; the top of the gas-liquid separator is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator is provided with a liquid phase outlet; the non-condensable gas outlet of the gas-liquid separator is connected with the vacuum unit; and a liquid phase outlet of the gas-liquid separator is connected with a factory benzene storage tank.
Moreover, the vacuum unit includes a vacuum pump; the cooling mechanism of the vacuum pump adopts a mode of cooling by an absorbent; the inlet of the vacuum pump is connected with the outlet of the heat exchange condensing unit, and the outlet of the vacuum pump is communicated with the factory combustion system through an exhaust pipe.
Moreover, the absorbent circulation supplementing unit comprises an absorbent supplementing pump, an absorbent heat exchanger and an absorbent circulation heat exchanger; the outlet of the absorbent replenishing pump is connected with the inlet of the absorbent heat exchanger through a pipeline, the other end of the absorbent heat exchanger is connected with the solvent absorption unit, one end of the absorbent circulating heat exchanger is connected with the inlet of the absorbent heat exchanger, and the other end of the absorbent circulating heat exchanger is connected with the inlet heat exchanger of the rectifying tower, so that the high efficiency and energy saving of cold and heat exchange of two logistics are realized.
And the absorbent regeneration unit comprises a regeneration extraction pump, a regeneration tank and a regeneration condenser, wherein the inlet of the regeneration extraction pump is connected with the outlet of the tower bottom reboiler of the rectification desorption unit, the outlet of the regeneration extraction pump is connected with the inlet heat exchanger of the rectification tower through a pipeline and is communicated with the inlet of the regeneration tank through a pipeline, the outlet of the regeneration tank is communicated with the inlet of the regeneration condenser, and the outlet of the regeneration condenser is communicated with the vacuum unit through a pipeline.
Moreover, an instrument for monitoring the benzene concentration is arranged on the exhaust pipe; the exhaust pipe is also provided with an exhaust branch pipe which is communicated with pipelines arranged on the pre-cooling condensing unit, the solvent absorbing unit, the rectifying desorption unit, the heat exchange condensing unit, the vacuum unit and the absorbent regeneration unit; the liquid discharge pipe is further provided with a liquid discharge branch pipe, and the liquid discharge branch pipe, the precooling condensing unit, the solvent absorbing unit, the rectifying desorption unit, the heat exchange condensing unit, the vacuum unit, the absorbent circulating supplementing unit and the absorbent regenerating unit form a circulating loop.
Benzene-containing VOC (volatile organic compound) in chemical plant area S The waste gas recycling treatment and recovery method is characterized in that: the method comprises the following steps:
(1) Benzene-containing VOCs S The waste gas is led to a recycling treatment recovery system by a fan, enters a precooling condenser after passing through a flame arrester, and contains benzene VOC S Pre-cooling and condensing the waste gas;
(2) Pre-cooling and condensing the benzene-containing VOC S After the waste gas is subjected to gas-liquid separation and part of benzene is recovered, condensed gas is introduced into an absorption tower, the top of the tower adopts a low-temperature pure organic absorbent similar to benzene series to absorb the inlet gas, the absorbed tail gas is condensed by a tower top condenser to prevent absorbent loss, the non-condensable gas and the non-condensable gas desorbed and condensed by a subsequent rectifying tower are combined and then are introduced into an external combustion device, namely a factory combustion system through a flame arrester, and clean gas generated after combustion reaches the standard and is discharged;
(3) The absorption rich liquid at the bottom of the absorption tower enters a rectifying tower for vacuum decompression desorption rectification after heat exchange, the gas phase at the top of the tower is enriched with 99.9 weight percent of benzene, and the benzene is sent into a benzene storage tank at a factory after being cooled, and finally, the product is continuously put into the factory for production; the bottom liquid phase obtains 99wt% of pure absorbent, and the recovered absorbent is cooled and returned to the absorption tower for continuous recycling.
The invention has the advantages and positive effects that:
the invention provides a recycling treatment and recovery system and method for benzene-containing VOCs waste gas in a chemical plant area, which adopts low-temperature pure organic absorbent similar to benzene series and compatible with the benzene-containing VOCs waste gas S Waste gas is absorbed, and separation of the absorbent and benzene series is realized through tower top condensation and vacuum decompression desorption rectification, so that the waste gas is discharged up to the standard, pure benzene products are obtained, and the separation of the benzene series is realizedThe absorbent is recycled and reused, and secondary pollution such as waste water, solid waste and the like can not be generated. The benzene series which is discharged from the outside and pollutes the air is recycled as resources, thereby generating economic benefit. The better the treatment effect of the method, the higher the purity of the benzene series product, the more the quantity and the greater the economic benefit.
The system and the method have unique, simple and controllable structure and easy operation, and improve the production efficiency of the system; the absorbent can be recycled, the absorption performance is stable, and the dissolution and absorption efficiency of benzene is high; the components of the absorbent are pure and liquid, so that secondary pollution such as waste water, solid waste and the like can not be generated; the cooling of the vacuum equipment adopts a cooling mode of an absorbent, so that the generation of dangerous wastes such as benzene pollution and the like by using water as cooling liquid is avoided, and the energy is saved and the environment is protected; the process flow is effectively optimized, the overall operation energy consumption of the system is reduced, the corrosion degree of the pipeline is reduced, and the investment and the operation cost are reduced; the tail gas discharged after treatment can meet the increasingly strict discharge limit, the treatment process considers the requirements of resource conservation and environmental friendliness, and the terminal output can also meet the increasingly strong requirements of resource recycling and material purity.
The system and the method combine the advantages of a condensation method, an absorption method and a rectification method, and the selection of the condensation temperature gives consideration to the requirements of refrigeration, absorption and rectification, so that the whole set of benzene-containing VOC S The waste gas recycling treatment recovery system and the waste gas recycling treatment recovery method have more compact structures; the exhaust gas directly enters the factory combustion system without reheating; the absorbed benzene series liquid phase is directly and completely recovered, the regenerated absorbent liquid phase is completely recycled, complex reprocessing is not needed, and the energy is fully recycled.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention.
Wherein, C101 is the fan, E101 is the precooling condenser, V101 is the gas-liquid separator, P101 is the extraction pump, T201 is the absorption tower, E201 is the absorption tower circulating heat exchanger, P201 is the circulating pump, E301 is the rectifying tower inlet heat exchanger, T301 is the rectifying tower, E302 is rectifying tower overhead condenser, V301 is rectifying tower overhead reflux drum, P301 is rectifying tower overhead reflux pump, E303 is rectifying tower bottom reboiler, E401 is the heat exchange condenser, V401 is the gas-liquid separator, XP501 is the vacuum pump, P601 is the absorbent make-up pump, E601 is the absorbent heat exchanger, E602 is the absorbent circulating heat exchanger, P701 is the regeneration extraction pump, V701 is the regeneration drum, E701 is the regeneration condenser.
Detailed Description
The invention will now be described in further detail by way of specific examples, which are given by way of illustration only and not by way of limitation, with reference to the accompanying drawings.
Benzene-containing VOC (volatile organic compound) in chemical plant area S The waste gas recycling treatment recovery system comprises a fan C101, a pre-cooling condensing unit 1, a solvent absorbing unit 2, a rectifying desorption unit 3, a heat exchange condensing unit 4, a vacuum unit 5, an absorbent circulating and supplementing unit 6, an absorbent regenerating unit 7, a factory combustion system and a factory benzene storage tank, wherein one end of the fan C101 is provided with a benzene-containing VOC S The other end of the pre-cooling condensing unit 1 is connected with a solvent absorbing unit 2 through a pipeline, one end of the upper part of the solvent absorbing unit 2 is connected with an inlet of an absorbent circulating supplementing unit 6 through an absorbent supplementing liquid inlet pipe, the other end of the solvent absorbing unit is communicated with a factory combustion system through an exhaust pipe, an instrument capable of monitoring benzene concentration is arranged on the exhaust pipe and used for discharging qualified gas, an exhaust branch pipe is further arranged on the exhaust pipe and is communicated with pipelines arranged on the pre-cooling condensing unit, the solvent absorbing unit, the rectifying desorption unit, the heat exchange condensing unit, the vacuum unit and the absorbent regeneration unit to form a circulating loop, and the circulating loop is used for detecting whether discharged gas reaches the standard or not, and the gas which does not reach the standard can flow back to the system inlet and is condensed, absorbed and rectified again; the lower part of the solvent absorption unit 2 is connected with the rectification desorption unit 3 through a pipeline, the upper part of the rectification desorption unit 3 is connected with the inlet of the heat exchange condensation unit 4 through a pipeline, the lower part of the rectification desorption unit 3 is connected with the absorbent regeneration unit 7, one end of the upper part of the heat exchange condensation unit 4 is connected with the vacuum unit 5, the other end of the upper part of the heat exchange condensation unit is connected with the benzene storage tank in a factory, and the other end of the vacuum unit 5 is connected with the benzene storage tank in the factory through an exhaust pipeThe system is communicated with a factory combustion system, the other end of the absorbent regeneration unit 7 is connected with an inlet of the absorbent circulation supplementing unit 6 through an absorbent supplementing liquid inlet pipe, and liquid phase outlets of the precooling condensing unit 1, the rectifying desorption unit 3 and the heat exchange condensing unit 4 are all connected with a factory benzene storage tank through extraction pipes; the fan drives the VOC containing benzene S The waste gas enters a pre-cooling condensing unit to be pre-cooled, condensed and separated from gas and liquid, and the pre-cooled, condensed and separated gas and liquid contain benzene VOC S The waste gas sequentially passes through a solvent absorption unit, a rectification desorption unit, a heat exchange condensation unit, a vacuum unit and an absorbent regeneration unit to finally form two phases, namely a gas phase and a liquid phase, and the treated VOC-containing waste gas S The clean gas generated after combustion reaches the standard and is discharged, and the condensed liquid phase with pure components enters a benzene storage tank in the factory to obtain qualified benzene products, thereby realizing the recycling of benzene. At the same time, the recycling regeneration of the absorbent is realized.
The pre-cooling condensing unit 1 comprises a pre-cooling condenser E101 and a gas-liquid separator V101; the precooling condenser E101 is provided with a condensate inlet, a condensate outlet and a condensate gas outlet; the top of the gas-liquid separator V101 is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator V101 is provided with a liquid phase outlet; the non-condensable gas outlet of the gas-liquid separator V101 is connected with the solvent absorption unit 2; the liquid phase outlet of the gas-liquid separator V101 is connected with a factory benzene storage tank through a extraction pump and an extraction pipe.
The solvent absorption unit 2 comprises an absorption tower T201, an absorption tower circulating heat exchanger E201 and a circulating pump P201; the bottom of the absorption tower T201 is provided with benzene-containing VOC S The waste gas feed inlet is communicated with a top noncondensable gas outlet of the gas-liquid separator V101 of the precooling condensing unit 1, an absorbent supplementing liquid inlet is arranged on the upper portion of the absorption tower T201 and is connected with an outlet of the absorbent circulating supplementing unit 6, an absorption tower circulating heat exchanger E201 is arranged in the absorption tower T201, the other end of the absorption tower circulating heat exchanger E201 is connected with a circulating pump P201, and the other end of the circulating pump P201 is connected with the rectifying desorption unit 3. The gas phase enriched and cleaned at the top of the absorption tower T201 is cooled at the top of the absorption tower and then sent into a factory combustion systemA system; and the bottom of the absorption tower T201 is enriched with a benzene-containing absorbent liquid phase, a small part of the benzene-containing absorbent liquid phase is circulated and refluxed, and a large part of the benzene-containing absorbent liquid phase enters the rectifying tower T301.
The rectification desorption unit 3 comprises a rectification tower inlet heat exchanger E301, a rectification tower T301, a tower top condenser E302, a tower top reflux tank V301, a tower top reflux pump P301 and a tower bottom reboiler E303; the middle part of the rectifying tower T301 is provided with a benzene-containing absorbent-containing liquid-phase material feeding hole, the feeding hole is connected with a rectifying tower inlet heat exchanger E301, the other end of the rectifying tower inlet heat exchanger E301 is connected with an outlet of a solvent absorption unit 2 circulating pump P201 in a liquid phase mode, a rectifying tower top condenser E302 is connected with a tower top reflux tank V301, one end of the tower top reflux tank V301 is connected with a tower top reflux pump P301, the other end of the tower top reflux pump P301 is connected with an inlet of a heat exchange condensing unit 4, one end of the tower top reflux pump P301 returns to the rectifying tower T301, an outlet of the other end of the tower top reflux pump P301 is led to a factory benzene storage tank, one end of an outlet of the tower bottom reboiler E303 is connected with the rectifying tower T301, and the other end of the outlet of the tower bottom reboiler E303 is connected with an inlet of an absorbent regeneration unit 7. The gas phase is enriched with a small amount of benzene, the gas phase is cooled by a rectifying tower top condenser E302 and then is sent to a tower top reflux tank V301, the gas phase of the tower top reflux tank V301 enters a heat exchange condensing unit 4, the liquid phase is refluxed to a tower top liquid phase production pipe, and the gas phase and the qualified benzene liquid phase product produced by the rectifying tower T301 are converged and sent to a factory benzene storage tank. The bottom of the rectifying tower T301 is provided with a liquid phase, the components are mainly absorbent, and after being treated by a tower bottom reboiler E303, a small part of the liquid phase flows back, and a large part of the liquid phase enters an absorbent regeneration unit 7 for subsequent treatment.
The heat exchange condensing unit 4 comprises a heat exchange condenser E401 and a gas-liquid separator V401; the heat exchanger E401 is provided with a condensate inlet, a condensate outlet and a condensate gas outlet; the top of the gas-liquid separator V401 is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator V401 is provided with a liquid phase outlet; the top noncondensable gas outlet of the gas-liquid separator V401 is connected with the inlet of the vacuum unit 5; the bottom liquid phase outlet of the gas-liquid separator V401 is connected with a liquid phase output pipe at the top of the rectifying tower T301, and is converged with qualified benzene liquid phase products produced at the top of the rectifying tower T301 and is sent to a factory benzene storage tank together.
The vacuum unit 5 comprises a vacuum pump XP501; the inlet of the vacuum pump XP501 is connected with the outlet of the heat exchange condensing unit 4, and the outlet of the vacuum pump XP501 is communicated with the factory combustion system through an exhaust pipe. The vacuum pump XP501 forms a vacuum environment for the rectifying tower T301 through vacuumizing effect, so that the normal operation of rectifying desorption of the rectifying tower T301 is ensured.
The absorbent circulation supplementing unit 6 comprises an absorbent supplementing pump P601, an absorbent heat exchanger E601 and an absorbent circulation heat exchanger E602; the outlet of the absorbent replenishing pump P601 is connected with the inlet of the absorbent heat exchanger E601 through a pipeline, the other end of the absorbent heat exchanger E601 is connected with the absorption tower T201 of the solvent absorption unit 2, one end of the absorbent circulating heat exchanger E602 is connected with the inlet of the absorbent heat exchanger E601, and the other end of the absorbent circulating heat exchanger E602 is connected with the inlet heat exchanger E301 of the rectifying tower, so that the high efficiency and energy saving of cold and heat exchange of two streams with different temperatures are realized under the condition that no refrigerant is adopted. The absorbent heat exchanger E601 and the absorbent circulating heat exchanger E602 are respectively provided with a condensate inlet, a condensate outlet and a condensate liquid phase outlet.
The absorbent regeneration unit 7 includes a regeneration extraction pump P701, a regeneration tank V701, and a regeneration condenser E701; the regeneration tank V701 is provided with a top gas phase outlet and a bottom liquid phase outlet, and the regeneration condenser E701 is provided with a condensate inlet, a condensate outlet and a condensate gas outlet; the inlet of the regeneration extraction pump P701 is connected with the outlet of a reboiler E303 at the bottom of the rectifying desorption unit 3, the outlet of the regeneration extraction pump P701 is connected with a heat exchanger E301 at the inlet of the rectifying tower through a pipeline, and the regenerated absorbent is conveyed to the absorbent circulation supplementing unit 6 and is communicated with the inlet of a regeneration tank V701 through a pipeline to carry out regeneration separation of the absorbent; the outlet of the regeneration tank V701 is communicated with the inlet of the regeneration condenser E701, and the outlet of the regeneration condenser E701 is communicated with the front end of the vacuum unit 5 through a pipeline.
Further, in order to enhance the condensation effect, other six units except the vacuum unit 5 are a pre-cooling condensation unit 1, a solvent absorption unit 2, a rectification desorption unit 3, a heat exchange condensation unit 4, an absorbent circulation supplementing unit 6 and an absorbent regeneration unit 7, which are all provided with a condenser and a heat exchanger, wherein the pre-cooling and gas-liquid separation are performedThe heat exchange, the regeneration, the product extraction and the recovery are all completed through a condenser and a heat exchanger, the heat exchanger comprises a shell-and-tube shell type, a plate type or an immersion type, two ends of the heat exchanger are respectively connected with a compressor and the condenser of a condensing unit, and the heat exchanger is used for condensing benzene-containing VOC entering the system through the condensing unit S And condensing and heat exchanging the waste gas.
Further, in order to enhance the absorption effect and the regeneration rate of the absorbent, the absorbent comprises methyl isobutyl ketone MIBK, N-methylpyrrolidone NMP, dimethyl sulfoxide DMSO, sulfolane, N-methylmorpholine, 1, 2-dimethylcyclohexane and other similar compatible organic matters with benzene series, and a single absorbent or a combination of a plurality of absorbents can be adopted.
Further, in order to avoid secondary pollution and dangerous waste, the cooling mechanism of the vacuum pump adopts an absorbent to cool, so that the dangerous waste such as benzene pollution and the like, which uses water as cooling liquid, is avoided, and the vacuum pump is more energy-saving and environment-friendly.
The invention also discloses a benzene-containing VOC in the chemical plant area S The waste gas recycling treatment and recovery method comprises the following steps:
(1) Benzene-containing VOCs S The waste gas is led to a recycling treatment recovery system by a fan, enters a precooling condenser after passing through a flame arrester, and contains benzene VOC S Pre-cooling and condensing the waste gas to 7 ℃;
(2) And then carrying out gas-liquid separation, recycling a part of benzene, introducing condensed gas into an absorption tower, absorbing the gas by using low-temperature N-methyl pyrrolidone (NMP) as an absorbent at the top of the absorption tower, condensing the absorbed tail gas through a tower top condenser to prevent NMP loss, merging non-condensable gas and non-condensable gas desorbed and condensed by a subsequent rectifying tower, introducing the non-condensable gas into an external combustion device, namely a factory combustion system, and generating clean gas to reach the standard after combustion and discharging.
(3) And (3) the absorption rich liquid at the bottom of the absorption tower enters a rectifying tower for vacuum decompression desorption rectification after heat exchange, 99.9wt% of benzene is enriched in the gas phase at the top of the tower, and the gas phase is sent to a benzene storage tank in a factory after being cooled, and finally, the product is continuously put into the factory for production. The bottom liquid phase is 99wt% pure NMP, and the recovered NMP is cooled and returned to the absorption tower to be used as absorbent for continuous recycling.
The comprehensive process comprises condensation recovery, solvent absorption, rectification desorption, skid-mounted equipment, space utilization to the maximum extent, land occupation saving, adoption of a DCS control system, unmanned automatic operation, qualified benzene products, recycling recovery of benzene and recycling regeneration of an absorbent.
The pre-cooling condensing unit comprises a pre-cooling condenser and a gas-liquid separator; benzene-containing VOCs S The waste gas enters a pre-cooling condenser after passing through an inlet flame arrester, is condensed to 7 ℃, enters a gas-liquid separator for gas-liquid separation, and the separated benzene-containing condensed liquid phase is sent to a factory benzene storage tank through a extraction pump, so that the recovery rate is improved, the emission standard is reached, and the condensed gas enters a subsequent solvent absorption unit for further separation and recovery.
The solvent absorption unit comprises an absorption tower, an absorption tower circulating heat exchanger and a circulating pump; the absorption tower is a cylindrical steel container, gas phase materials from the precooling condensing unit enter the bottom of the absorption tower, and low-temperature absorbent NMP enters the top of the absorption tower through a feed pump; the tower top pressure of the absorption tower is 0.115MPa (a), the tower top temperature is 0 ℃, the absorbed tail gas is cooled to 0 ℃ by chilled water through a condenser at the tower top of the absorption tower, NMP loss is prevented, noncondensable gas is led to a combustion system in a factory, and clean gas is generated after combustion and reaches the standard to be discharged; the pressure at the bottom of the absorption tower is 0.12MPa (a), the temperature at the bottom of the absorption tower is 11.5 ℃, the liquid phase containing benzene and absorbent is enriched at the bottom of the absorption tower, part of the absorption rich liquid is boosted by a circulating pump and then returns to the absorption tower as reflux liquid after being cooled to 7 ℃ by chilled water through a circulating heat exchanger of the absorption tower, and the rest of the absorption rich liquid is sent to a subsequent rectifying and desorbing unit for further separation and recovery.
The rectification desorption unit, the heat exchange condensation unit, the vacuum unit, the absorbent circulation supplementing unit and the absorbent regeneration unit complement each other, and the rectification desorption unit comprises a rectification tower inlet heat exchanger, a rectification tower, a tower top condenser, a tower top reflux tank, a tower top reflux pump and a tower bottom reboiler; the heat exchange condensing unit comprises a heat exchange condenser and a gas-liquid separator; the vacuum unit comprises a vacuum pump; the absorbent circulation supplementing unit comprises an absorbent supplementing pump, an absorbent heat exchanger and an absorbent circulation heat exchanger; the absorbent regeneration unit includes a regeneration extraction pump, a regeneration tank, and a regeneration condenser: the benzene-containing absorbent-containing liquid phase material from the solvent absorption unit enters the rectifying tower through the inlet heat exchanger of the rectifying tower, the top pressure of the rectifying tower is 0.04MPa (a), and the top temperature is 53.8 ℃. The gas phase material at the top of the tower passes through a tower top condenser, is cooled to 45 ℃ by circulating water, and enters a tower top reflux tank for gas-liquid separation to respectively produce gas phase and liquid phase materials. The bottom pressure of the rectifying tower is 0.042MPa (a), and the bottom temperature is 170.3 ℃. The liquid phase material components in the tower bottom of the rectifying tower are mainly absorbent, a small part of the liquid phase material components return to the tower bottom of the rectifying tower through a tower bottom reboiler for circulation, and the steam flow of the reboiler is timely adjusted according to the temperature of the tower bottom so as to ensure that enough rising steam exists in the tower; the rest is pressurized by a regeneration extraction pump of the absorbent regeneration unit, and then NMP regeneration is carried out.
Further, the gas phase material produced by the tower top reflux tank enters a heat exchange condenser of a heat exchange condensing unit, is cooled to 7 ℃ by chilled water, and enters a gas-liquid separator for gas-liquid separation: the produced small amount of non-condensable gas is converged by a vacuum pump of a vacuum unit and non-condensable gas at the top of the absorption tower and then is led to a factory combustion system, and clean gas is generated after combustion and is discharged after reaching standards; in addition, the vacuum pump forms a vacuum environment for the rectifying tower through vacuumizing effect, so that the normal operation of rectifying desorption of the rectifying tower is ensured; wherein the produced liquid phase outlet containing 99.9wt% of benzene is connected with a liquid phase output pipe at the top of the rectifying tower, and is converged with the qualified benzene liquid phase product produced at the top of the rectifying tower and is sent to a factory benzene storage tank together. After the whole liquid phase material output by the tower top reflux tank is boosted by the tower top reflux pump, a part of the whole liquid phase material returns to the rectifying tower to be used as reflux liquid, and the rest of the whole liquid phase material and benzene-containing liquid phase produced by other units are combined together to be sent to the factory benzene storage tank.
Further, a part of the liquid phase material which is boosted by the regenerative extraction pump of the absorbent regeneration unit enters the inlet heat exchanger of the rectifying tower to exchange heat with the inlet material of the rectifying tower, so that the high efficiency and energy saving of cold and heat exchange of two material flows with different temperatures are realized under the condition that no refrigerant is adopted, and then the liquid phase material enters the absorbent circulation heat exchanger of the absorbent circulation supplementing unit to be cooled, enters the front end of the absorbent heat exchanger and finally returns to the solvent absorption unit to be recycled; the rest of the non-condensable gas enters an NMP regeneration system main body, firstly enters a regeneration tank for decompression flash evaporation to generate NMP steam, then enters a regeneration condenser, is cooled to 45 ℃ by circulating water, and is subjected to gas-liquid separation, wherein the non-condensable gas is discharged into a factory combustion system through a vacuum pump, and the liquid phase flows back to the front end of a regeneration extraction pump for circulating regeneration. The regeneration system was operated once a year, each for 6 hours.
In order to enhance the condensation effect, other six units except the vacuum unit comprise a pre-cooling condensation unit, a solvent absorption unit, a rectification desorption unit, a heat exchange condensation unit, an absorbent circulation supplementing unit and an absorbent regeneration unit, wherein the pre-cooling, gas-liquid separation, heat exchange, regeneration, product extraction and recovery are all completed through the condenser and the heat exchanger, the heat exchanger comprises a shell-and-tube type, plate type or immersion type, two ends of the heat exchanger are respectively connected with a compressor and a condenser of a condensing unit, and the heat exchanger is used for introducing benzene-containing VOC (volatile organic compounds) into a system through the condensing unit S And condensing and heat exchanging the waste gas.
The invention adopts a system of precooling condensation, solvent absorption, rectification desorption, heat exchange condensation, absorbent supplementation and regeneration to the benzene-containing VOC S Waste gas is treated, a certain benzene product can be recovered by precooling and condensing, and the treated noncondensable gas contains VOC by solvent absorption S The components are very tiny and are communicated with a factory combustion system, clean gas generated after combustion reaches the standard and is discharged, the rectification desorption, heat exchange condensation, absorbent supplementation and regeneration can further realize the full recycling of benzene liquid phase and the cyclic regeneration of absorbent, the condensed liquid phase with purer components enters a factory benzene storage tank to realize the recycling recovery of benzene, the clean production of the whole process is fully realized, and the benzene-containing VOC is effectively recovered S The available components in the waste gas reduce the energy consumption and fully realize the comprehensive resource utilization of energy. The system of the invention has unique, simple, controllable and easy operation, improves the production efficiency of the system, and the absorbent component is pure, recyclable and regeneratedThe total dosage is small, no secondary pollution is generated, and VOC is generated S The exhaust emission concentration is low and the recovery benefit is good.
Although the embodiments of the present invention and the accompanying drawings have been disclosed for illustrative purposes, those skilled in the art will appreciate that: various substitutions, changes and modifications are possible without departing from the spirit and scope of the invention and the appended claims, and therefore the scope of the invention is not limited to the embodiments and the disclosure of the drawings.
Claims (10)
1. Benzene-containing VOC (volatile organic compound) in chemical plant area S Waste gas resourceful treatment recovery system, its characterized in that: comprises a fan, a precooling condensing unit, a solvent absorbing unit, a rectifying desorption unit, a heat exchange condensing unit, a vacuum unit, an absorbent circulating and supplementing unit and an absorbent regenerating unit, wherein one end of the fan is connected with a benzene-containing VOC (volatile organic compound) S The waste gas inlet is connected, the other end is connected with the precooling condensing unit through an air inlet pipe, the other end of the precooling condensing unit is connected with the solvent absorbing unit through a pipeline, one end of the upper part of the solvent absorbing unit is connected with the inlet of the absorbent circulating supplementing unit through an absorbent supplementing liquid inlet pipe, the other end of the solvent absorbing unit is communicated with the factory combustion system through an exhaust pipe, the lower part of the solvent absorbing unit is connected with the rectifying and desorbing unit through a pipeline, the upper part of the rectifying and desorbing unit is connected with the inlet of the heat exchanging condensing unit through a pipeline, the lower part of the rectifying and desorbing unit is connected with the absorbent regenerating unit, one end of the upper part of the heat exchanging condensing unit is connected with the vacuum unit, the other end of the heat exchanging condensing unit is connected with the factory benzene storage tank, the other end of the vacuum unit is communicated with the factory combustion system through an absorbent supplementing liquid inlet pipe and the absorbent circulating supplementing unit inlet, and the liquid outlets of the precooling condensing unit, the rectifying and the heat exchanging and condensing unit are all connected with the factory benzene storage tank through extraction pipes.
2. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the pre-cooling condensing unit comprises a group of condensing components and a extraction pump which are connected in series,the precooling condenser and the gas-liquid separator; the top of the gas-liquid separator is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator is provided with a liquid phase outlet; the non-condensable gas outlet of the gas-liquid separator is connected with the solvent absorption unit; and a liquid phase outlet of the gas-liquid separator is connected with a factory benzene storage tank through a production pump and a production pipe.
3. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the solvent absorption unit comprises an absorption tower, an absorption tower circulating heat exchanger and a circulating pump, and the bottom of the absorption tower is provided with benzene-containing VOC S The waste gas feed inlet is communicated with a top noncondensable gas outlet of the gas-liquid separator of the pre-cooling condensing unit, an absorbent supplementing liquid inlet is arranged on the upper portion of the absorption tower, the liquid inlet is connected with an outlet of the absorbent circulating supplementing unit, an absorption tower circulating heat exchanger is arranged in the absorption tower, the other end of the absorption tower circulating heat exchanger is connected with a circulating pump, and the other end of the circulating pump is connected with the rectifying desorption unit.
4. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the rectification desorption unit comprises a rectification tower inlet heat exchanger, a rectification tower, a tower top condenser, a tower top reflux tank, a tower top reflux pump and a tower bottom reboiler, wherein a benzene-containing absorbent material feeding port is arranged in the middle of the rectification tower, the feeding port is connected with the rectification tower inlet heat exchanger, the other end of the rectification tower inlet heat exchanger is connected with a solvent absorption unit circulating pump outlet, the tower top condenser is connected with the tower top reflux tank, one end of the tower top reflux tank is connected with the tower top reflux pump, the other end of the tower top reflux pump is connected with a heat exchange condensation unit inlet, one end of the tower top reflux pump returns to the rectification tower, the other end outlet of the tower top reflux pump is led to a factory benzene storage tank, one end of the outlet of the tower bottom reboiler is connected with the rectification tower, and the other end of the outlet of the tower bottom reboiler is connected with an absorbent regeneration unit inlet.
5. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceThe chemical treatment recovery system is characterized in that: the heat exchange condensing unit comprises a heat exchange condenser and a gas-liquid separator; the top of the gas-liquid separator is provided with a non-condensable gas outlet, and the bottom of the gas-liquid separator is provided with a liquid phase outlet; the non-condensable gas outlet of the gas-liquid separator is connected with the vacuum unit; and a liquid phase outlet of the gas-liquid separator is connected with a factory benzene storage tank.
6. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the vacuum unit comprises a vacuum pump; the cooling mechanism of the vacuum pump adopts a mode of cooling by an absorbent; the inlet of the vacuum pump is connected with the outlet of the heat exchange condensing unit, and the outlet of the vacuum pump is communicated with the factory combustion system through an exhaust pipe.
7. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the absorbent circulation supplementing unit comprises an absorbent supplementing pump, an absorbent heat exchanger and an absorbent circulation heat exchanger; the outlet of the absorbent replenishing pump is connected with the inlet of the absorbent heat exchanger through a pipeline, the other end of the absorbent heat exchanger is connected with the solvent absorption unit, one end of the absorbent circulating heat exchanger is connected with the inlet of the absorbent heat exchanger, and the other end of the absorbent circulating heat exchanger is connected with the inlet heat exchanger of the rectifying tower, so that the high efficiency and energy saving of cold and heat exchange of two logistics are realized.
8. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: the absorbent regeneration unit comprises a regeneration extraction pump, a regeneration tank and a regeneration condenser, wherein the inlet of the regeneration extraction pump is connected with the outlet of a reboiler at the bottom of the rectification desorption unit, the outlet of the regeneration extraction pump is connected with the inlet heat exchanger of the rectification tower through a pipeline and is communicated with the inlet of the regeneration tank through a pipeline, the outlet of the regeneration tank is communicated with the inlet of the regeneration condenser, and the outlet of the regeneration condenser is communicated with the vacuum unit through a pipeline.
9. The chemical plant area benzene-containing VOC of claim 1 S Waste gas resourceful treatment recovery system, its characterized in that: an instrument for monitoring the benzene concentration is arranged on the exhaust pipe; the exhaust pipe is also provided with an exhaust branch pipe which is communicated with pipelines arranged on the pre-cooling condensing unit, the solvent absorbing unit, the rectifying desorption unit, the heat exchange condensing unit, the vacuum unit and the absorbent regeneration unit; the liquid discharge pipe is further provided with a liquid discharge branch pipe, and the liquid discharge branch pipe, the precooling condensing unit, the solvent absorbing unit, the rectifying desorption unit, the heat exchange condensing unit, the vacuum unit, the absorbent circulating supplementing unit and the absorbent regenerating unit form a circulating loop.
10. Benzene-containing VOC (volatile organic compound) in chemical plant area S The waste gas recycling treatment and recovery method is characterized in that: the method comprises the following steps:
(1) Benzene-containing VOCs S The waste gas is led to a recycling treatment recovery system by a fan, enters a precooling condenser after passing through a flame arrester, and contains benzene VOC S Pre-cooling and condensing the waste gas;
(2) Pre-cooling and condensing the benzene-containing VOC S After the waste gas is subjected to gas-liquid separation and part of benzene is recovered, condensed gas is introduced into an absorption tower, the top of the tower adopts a low-temperature pure organic absorbent similar to benzene series to absorb the inlet gas, the absorbed tail gas is condensed by a tower top condenser to prevent absorbent loss, the non-condensable gas and the non-condensable gas desorbed and condensed by a subsequent rectifying tower are combined and then are introduced into an external combustion device, namely a factory combustion system through a flame arrester, and clean gas generated after combustion reaches the standard and is discharged;
(3) The absorption rich liquid at the bottom of the absorption tower enters a rectifying tower for vacuum decompression desorption rectification after heat exchange, the gas phase at the top of the tower is enriched with 99.9 weight percent of benzene, and the benzene is sent into a benzene storage tank at a factory after being cooled, and finally, the product is continuously put into the factory for production; the bottom liquid phase obtains 99wt% of pure absorbent, and the recovered absorbent is cooled and returned to the absorption tower for continuous recycling.
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| CN117619086A (en) * | 2023-12-02 | 2024-03-01 | 广州市帝东环保科技有限公司 | VOCs recovery device and recovery method thereof |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN117619086A (en) * | 2023-12-02 | 2024-03-01 | 广州市帝东环保科技有限公司 | VOCs recovery device and recovery method thereof |
| CN117619086B (en) * | 2023-12-02 | 2024-04-26 | 广州市帝东环保科技有限公司 | VOCs recovery device and recovery method thereof |
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