CN117582785A - UV light-cured monomer synthesis tail gas treatment and circulation system capable of realizing zero emission - Google Patents
UV light-cured monomer synthesis tail gas treatment and circulation system capable of realizing zero emission Download PDFInfo
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- CN117582785A CN117582785A CN202311754833.2A CN202311754833A CN117582785A CN 117582785 A CN117582785 A CN 117582785A CN 202311754833 A CN202311754833 A CN 202311754833A CN 117582785 A CN117582785 A CN 117582785A
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- 239000000178 monomer Substances 0.000 title claims abstract description 39
- 238000003786 synthesis reaction Methods 0.000 title claims description 24
- 230000015572 biosynthetic process Effects 0.000 title claims description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 122
- 238000010521 absorption reaction Methods 0.000 claims abstract description 104
- 238000005507 spraying Methods 0.000 claims abstract description 49
- 239000003960 organic solvent Substances 0.000 claims abstract description 38
- 238000006243 chemical reaction Methods 0.000 claims abstract description 34
- 239000000498 cooling water Substances 0.000 claims abstract description 20
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 19
- 238000003795 desorption Methods 0.000 claims abstract description 13
- 238000002076 thermal analysis method Methods 0.000 claims abstract description 10
- 230000007306 turnover Effects 0.000 claims abstract description 10
- 230000002194 synthesizing effect Effects 0.000 claims abstract description 7
- 238000007789 sealing Methods 0.000 claims abstract description 6
- 239000007788 liquid Substances 0.000 claims description 92
- 239000007921 spray Substances 0.000 claims description 56
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 51
- 238000003848 UV Light-Curing Methods 0.000 claims description 20
- 238000004064 recycling Methods 0.000 claims description 18
- 239000012855 volatile organic compound Substances 0.000 claims description 17
- 238000004458 analytical method Methods 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 14
- 239000012071 phase Substances 0.000 claims description 13
- 239000012074 organic phase Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 239000011259 mixed solution Substances 0.000 claims description 5
- 239000002994 raw material Substances 0.000 claims description 5
- 239000002274 desiccant Substances 0.000 claims description 4
- 229920006395 saturated elastomer Polymers 0.000 claims description 4
- MQIUGAXCHLFZKX-UHFFFAOYSA-N Di-n-octyl phthalate Natural products CCCCCCCCOC(=O)C1=CC=CC=C1C(=O)OCCCCCCCC MQIUGAXCHLFZKX-UHFFFAOYSA-N 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- BJQHLKABXJIVAM-UHFFFAOYSA-N bis(2-ethylhexyl) phthalate Chemical compound CCCCC(CC)COC(=O)C1=CC=CC=C1C(=O)OCC(CC)CCCC BJQHLKABXJIVAM-UHFFFAOYSA-N 0.000 claims description 3
- 238000000016 photochemical curing Methods 0.000 claims description 3
- 239000000741 silica gel Substances 0.000 claims description 3
- 229910002027 silica gel Inorganic materials 0.000 claims description 3
- 125000000113 cyclohexyl group Chemical group [H]C1([H])C([H])([H])C([H])([H])C([H])(*)C([H])([H])C1([H])[H] 0.000 claims description 2
- SNRUBQQJIBEYMU-UHFFFAOYSA-N dodecane Chemical compound CCCCCCCCCCCC SNRUBQQJIBEYMU-UHFFFAOYSA-N 0.000 claims description 2
- 229940094933 n-dodecane Drugs 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000011084 recovery Methods 0.000 abstract 1
- DAKWPKUUDNSNPN-UHFFFAOYSA-N Trimethylolpropane triacrylate Chemical compound C=CC(=O)OCC(CC)(COC(=O)C=C)COC(=O)C=C DAKWPKUUDNSNPN-UHFFFAOYSA-N 0.000 description 9
- 229940096522 trimethylolpropane triacrylate Drugs 0.000 description 9
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 6
- ZJCCRDAZUWHFQH-UHFFFAOYSA-N Trimethylolpropane Chemical compound CCC(CO)(CO)CO ZJCCRDAZUWHFQH-UHFFFAOYSA-N 0.000 description 5
- NIXOWILDQLNWCW-UHFFFAOYSA-N acrylic acid group Chemical group C(C=C)(=O)O NIXOWILDQLNWCW-UHFFFAOYSA-N 0.000 description 5
- SMZOUWXMTYCWNB-UHFFFAOYSA-N 2-(2-methoxy-5-methylphenyl)ethanamine Chemical compound COC1=CC=C(C)C=C1CCN SMZOUWXMTYCWNB-UHFFFAOYSA-N 0.000 description 4
- PEDCQBHIVMGVHV-UHFFFAOYSA-N Glycerine Chemical compound OCC(O)CO PEDCQBHIVMGVHV-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000005886 esterification reaction Methods 0.000 description 3
- 238000004880 explosion Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 238000003915 air pollution Methods 0.000 description 2
- 239000008346 aqueous phase Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 150000002148 esters Chemical class 0.000 description 2
- 239000000376 reactant Substances 0.000 description 2
- LCZVSXRMYJUNFX-UHFFFAOYSA-N 2-[2-(2-hydroxypropoxy)propoxy]propan-1-ol Chemical compound CC(O)COC(C)COC(C)CO LCZVSXRMYJUNFX-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- CERQOIWHTDAKMF-UHFFFAOYSA-N Methacrylic acid Chemical compound CC(=C)C(O)=O CERQOIWHTDAKMF-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000003377 acid catalyst Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 150000001732 carboxylic acid derivatives Chemical class 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
- 239000012295 chemical reaction liquid Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 230000032050 esterification Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 125000005395 methacrylic acid group Chemical group 0.000 description 1
- 239000003595 mist Substances 0.000 description 1
- WXZMFSXDPGVJKK-UHFFFAOYSA-N pentaerythritol Chemical compound OCC(CO)(CO)CO WXZMFSXDPGVJKK-UHFFFAOYSA-N 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229920005862 polyol Polymers 0.000 description 1
- 150000003077 polyols Chemical class 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 150000005846 sugar alcohols Polymers 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/1487—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
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a system for treating and circulating synthetic tail gas of a UV light-cured monomer, which can realize zero emission, and consists of a circulating tail gas turnover system, a cooling water spraying system and an organic solvent cold absorption-thermal analysis system, wherein the system and a reaction kettle for synthesizing the UV light-cured monomer form closed circulation of tail gas; the circulating tail gas turnover system comprises a spherical tank lined with a PVC bag-shaped sealing film; the cooling water spraying system comprises a water spraying tunnel, a hydrocyclone, a dryer, an induced draft fan, an oil-water separator and an organic solvent receiving tank; the organic solvent cold absorption-thermal desorption system comprises an absorption tower, a desorption kettle and a complete condenser. According to the invention, only one induced draft fan is required to drive air, and the air enters from the circulating tail gas turnover system and sequentially passes through the reaction kettle, the cooling water spraying system and the organic solvent cold absorption-thermal analysis system element, and finally returns to the circulating tail gas turnover system, so that the maximum recovery of the tail gas water-carrying agent can be realized, and the production without tail gas emission can be ensured.
Description
Technical Field
The invention belongs to the field of recycling of tail gas of organic synthesis reaction, and relates to a UV photocuring monomer synthesis tail gas treatment and recycling system capable of realizing zero emission.
Background
UV light curable monomers are known for their ability to polymerize and cure rapidly under UV light irradiation and generally refer to esters of polyols of acrylic (or methacrylic) acid (tripropylene glycol, pentaerythritol, trimethylol propane, glycerol, etc.), such as trimethylol propane triacrylate (TMPTA).
At present, the production of UV photo-curing monomers is mostly carried out by adopting the principle of 'acid catalyst catalyzed acrylic acid (or methacrylic acid) and polyalcohol (such as trimethylolpropane) to carry out esterification reaction', for example, the synthetic reaction process of TMPTA is as follows:
the esterification reaction of carboxylic acid and alcohol is reversible, and a water-carrying agent such as toluene, cyclohexane and the like is generally required to be added, so that the water generated by the reaction can be taken out of the reaction system, and the reaction can be moved towards the direction of generating ester, thereby realizing the maximum conversion rate.
During the esterification of UV light curing monomer, a certain amount of air is continuously introduced to prevent possible self-polymerization side reaction, so that tail gas saturated by water-carrying agent (toluene, cyclohexane, etc.) is inevitably produced, and the tail gas must be treated and discharged after reaching the standard.
The catalytic combustion method is the simplest tail gas treatment method, but the method does not consider recycling the water-carrying agent in the tail gas, and belongs to a method which has no benefit, pure money burning, production cost improvement for environmental protection and enterprise competitiveness reduction; the activated carbon adsorption method has complex equipment, high operation difficulty, high operation cost and serious resource waste. The inventor hopes to obtain a UV light curing monomer synthesis tail gas treatment and circulation system capable of realizing zero emission, and thoroughly eradicates the air pollution source of VOC while maximally realizing the recycling of the water carrying agent.
Disclosure of Invention
The invention aims to provide a system for treating and recycling the synthetic tail gas of a UV light curing monomer, which can realize zero emission, and the system comprises a cooling water spraying system, an organic solvent cold absorption-thermal analysis system and a circulating tail gas turnover system, and the system is a totally-enclosed tail gas recycling system formed by the system and a reaction kettle, so that the water-carrying agent (toluene, cyclohexane and the like) in the tail gas can be recycled to the maximum extent, and the production of the UV light curing monomer without tail gas emission can be ensured.
The invention aims at realizing the following technical scheme:
the treatment and circulation system comprises a circulation tail gas circulation system, a cooling water spraying system and an organic solvent cold absorption-thermal analysis system, wherein the treatment and circulation system and a reaction kettle for synthesizing the UV light curing monomers form closed circulation of tail gas;
the circulating tail gas turnover system comprises a spherical tank lined with a PVC bag-shaped sealing film; the air inlet of the spherical tank is connected with the air outlet of an absorption tower in the atmosphere or organic solvent cold absorption-thermal desorption system, and the air outlet of the spherical tank is connected with the air inlet of the reaction kettle;
the cooling water spraying system comprises a water spraying tunnel, a hydrocyclone, a dryer, an induced draft fan, an oil-water separator and an organic solvent receiving tank; the upper part of the water spraying tunnel is provided with a liquid inlet, one end of the water spraying tunnel is provided with an air inlet connected with the air outlet of the reaction kettle, the other end of the water spraying tunnel is provided with an air outlet connected with the inlet of the hydrocyclone, the air outlet of the hydrocyclone is connected with the inlet of the dryer, and the outlet of the dryer is connected with the air inlet of an absorption tower in the organic solvent cold absorption-thermal desorption system through a draught fan; an outlet at the bottom of the water spraying tunnel is connected with an inlet of the oil-water separator to enable the water-oil mixed solution to automatically flow into the oil-water separator, an oil phase outlet of the oil-water separator is connected with an organic solvent receiving tank, and an outlet of the organic solvent receiving tank is connected with a synthesis working section;
the organic solvent cold absorption-thermal desorption system comprises an absorption tower, a desorption kettle and a complete condenser; the upper part of the absorption tower is provided with a liquid inlet, the lower part of the absorption tower is provided with an air inlet connected with a draught fan in the cooling water spraying system, an air outlet at the top of the absorption tower is connected with an air inlet of the spherical tank, a liquid outlet at the bottom of the absorption tower is connected with an inlet of the analysis kettle, and an air outlet of the analysis kettle is connected with an inlet of the full condenser.
Preferably, the cooling water spraying system further comprises a spray water storage tank, a spray water delivery pump and a spray water cooler; the outlet of the spray water storage tank is connected with the liquid inlet of the water spray tunnel through a spray water delivery pump and a spray water cooler; the water phase outlet of the oil-water separator is connected with the spray water storage tank, so that the water phase obtained by oil-water separation automatically flows into the spray water storage tank for recycling.
Preferably, the water spray tunnel is provided with spray devices known in the art for spraying water downwardly to form a water curtain in the water spray tunnel.
Preferably, the cooling water spraying system further comprises an organic phase transfer pump; the organic phase transfer pump is arranged on an outlet pipeline of the organic solvent receiving tank.
Preferably, the dryer is filled with silica gel as a water removal desiccant.
Preferably, the organic solvent cold absorption-thermal analysis system comprises an absorption liquid storage tank, an absorption liquid delivery pump and an absorption liquid cooler; the outlet of the absorption liquid storage tank is connected with the liquid inlet at the upper part of the absorption tower through an absorption liquid delivery pump and an absorption liquid cooler; the liquid outlet of the analysis kettle is connected with the absorption liquid storage tank, so that the absorption liquid flows back to the absorption liquid storage tank.
The invention also aims to provide a method for treating and recycling the tail gas generated by synthesizing the UV light-cured monomer, which can realize zero emission, and comprises the following steps:
in the reaction process of the UV light curing monomer, a draught fan is started, air is introduced into a reaction kettle through a spherical tank of a circulating tail gas turnover system, and tail gas is discharged from an air outlet of the reaction kettle;
step (2), spray water enters a water spray tunnel from the upper part and is sprayed downwards to form a water curtain, tail gas is transversely introduced from the air inlet end of the water spray tunnel, partial Volatile Organic Compounds (VOC) in the tail gas are liquefied, water-oil mixed liquid is collected at the bottom of the water spray tunnel, the water-oil mixed liquid automatically flows into an oil-water separator for liquid separation, the obtained water phase is recycled as spray water, and an organic solvent returns to a synthesis section for reuse; the tail gas after spray treatment is sequentially separated by a hydrocyclone and dried by a dryer, and is sent into an absorption tower by an induced draft fan;
step (3), tail gas treated by a cooling water spraying system enters an absorption tower from the lower part, absorption liquid enters the absorption tower from the upper part, the absorption liquid and the tail gas are in countercurrent contact to absorb Volatile Organic Compounds (VOC) in the tail gas, the absorption liquid absorbing the volatile organic compounds flows out from the bottom of the absorption tower, the self-flowing absorption liquid enters an analysis kettle for heating analysis, the VOC is distilled out, and the absorption liquid enters a complete condenser for cooling to be liquid, and the liquid returns to a synthesis section for reuse; the treated tail gas is led out from the top of the absorption tower and is sent back to the tail gas circulation system for circulation.
In the step (1), the temperature of the tail gas is about 60 ℃; the volatile organic compounds in the tail gas are steam of a water-carrying agent, and a small amount of reaction raw materials of UV light-curing monomers and UV light-curing monomers; the contents of the tail gas water carrying agent, the reaction raw materials of the UV light curing monomer and the UV light curing monomer are all the contents corresponding to the saturated steam partial pressure of each component at normal pressure and 60 ℃.
The water-carrying agent is cyclohexane, toluene or other organic solvents used as the water-carrying agent.
Specifically, when the UV light-curable monomer is trimethylolpropane triacrylate (TMPTA), the reaction raw materials are trimethylolpropane and acrylic acid.
In the step (2), the working temperature of the spray water is 0-20 ℃, preferably 2-5 ℃.
Pumping spray water into a spray water cooler through a water spray pump, cooling to the working temperature, and then feeding into a water spray tunnel; the tail gas is sucked by a draught fan and enters a water spraying tunnel.
The volume ratio of the tail gas to the spray water is 10:1-500:1, and the residence time of the tail gas in the water spray tunnel is not less than 30 seconds.
The obtained water phase automatically flows back to the spray water storage tank and is used as spray water for recycling. The organic solvent is sent to the synthesis section for reuse through an organic phase transfer pump.
In the step (3), the volume ratio of the tail gas to the absorption liquid is 300:1-1000:1, and the residence time of the tail gas in the absorption tower is not less than 15 seconds.
The absorption liquid is n-dodecane or dioctyl phthalate.
The working temperature of the absorption liquid is-5 to 5 ℃ and the analysis working temperature is 110 to 130 ℃.
The absorption liquid after the heating analysis treatment automatically flows back to the absorption liquid storage tank.
When the air quantity of the induced draft fan introduced into the reaction kettle from the tail gas circulation system and the air quantity of the tail gas circulation system fed back to the circulation system reach balance, and the VOC content of the tail gas water-carrying agent (cyclohexane or toluene) and the like discharged by the absorption tower is stabilized at the level of 3000ppm, stable operation can be realized (the lower explosion limit of cyclohexane is 1.3%, and the lower explosion limit of toluene is 1.1%, which are far higher than the balance content level of the water-carrying agent in the circulation tail gas, so that the explosion risk is avoided).
The invention has the beneficial effects that:
the invention adopts a fully-closed tail gas circulation system which consists of an organic solvent cold absorption-thermal desorption system, a cooling water spray system and a circulating tail gas circulation system and can realize zero emission, the whole system only needs to be provided with an induced draft fan for driving air, and the air enters from the circulating tail gas circulation system and sequentially passes through a reaction kettle, the cooling water spray system and the organic solvent cold absorption-thermal desorption system, and finally returns to the circulating tail gas circulation system. The invention not only can realize the maximum recycling of the tail gas water-carrying agent (toluene, cyclohexane, etc.), but also can ensure the production of the UV light curing monomer without tail gas emission, thereby reaching the international advanced level.
The invention adopts the spherical tank lined with the PVC bag-shaped sealing film, and is used for collecting and recycling the air introduced into the reaction kettle, so that the air is not discharged into the atmosphere any more and the air pollution is thoroughly eradicated; the PVC bag-shaped sealing film is lined to ensure the air tightness of the spherical tank and prevent the leakage of the circulating air to the outside atmosphere.
Detailed Description
The technical scheme of the invention is further described below by referring to examples.
Example 1
The system comprises a tail gas circulation system, a cooling water spraying system and an organic solvent cold absorption-thermal analysis system, wherein the tail gas circulation system and the reaction kettle for synthesizing the UV light curing monomers form closed circulation of tail gas.
The tail gas circulation system for circulation consists of a spherical tank (with the specification of phi 15000, unit: mm) lined with a PVC bag-shaped sealing film and a one-way air inlet valve; the air inlet of the spherical tank is connected with the air outlet of an absorption tower in the air or organic solvent cold absorption-thermal desorption system, and the air outlet of the spherical tank is connected with the air inlet of a reaction kettle for synthesizing TMPTA;
the cooling water spraying system consists of a spray water storage tank, a spray water delivery pump, a spray water cooler, a water spraying tunnel (specification: 25000mm long by 3000mm high by 2500mm wide), a cyclone liquid separator, a group of 3 dryers (two are used and one is prepared, the dryer is filled with the drying agent, silica gel), a draught fan, an oil-water separator (5 m) 3 ) The organic solvent receiving tank and the organic phase transfer pump. The outlet of the spray water storage tank is connected with the liquid inlet of the water spray tunnel through a spray water delivery pump and a spray water cooler, one end of the water spray tunnel is provided with an air inlet connected with the air outlet of the reaction kettle, the other end of the water spray tunnel is provided with an air outlet connected with the inlet of the cyclone liquid separator, the air outlet of the cyclone liquid separator is connected with the inlet of the dryer, and the outlet of the dryer is connected with the air inlet of the absorption tower in the organic solvent cold absorption-thermal analysis system through a draught fan; an outlet at the bottom of the water spraying tunnel is connected with an inlet of the oil-water separator to enable water-oil mixed solution to automatically flow into the oil-water separator, and an aqueous phase outlet of the oil-water separator is connected with the spray water storage tank to enable an aqueous phase obtained by oil-water separation to automatically flow into the spray water storage tank for recycling; the oil phase outlet of the oil-water separator is connected with an organic solvent receiving tank, and the outlet of the organic solvent receiving tank is connected with a synthesis section through an organic phase transfer pump.
The organic solvent cold absorption-thermal analysis system consists of an absorption liquid storage tank, an absorption liquid delivery pump, an absorption liquid cooler, an absorption tower (the specification is that the diameter is 1500mm multiplied by 15000 mm), a group of four analysis kettles (the specification is that the diameter is 1200mm multiplied by 2500 mm) and a complete condenser; the outlet of the absorption liquid storage tank is connected with the liquid inlet at the upper part of the absorption tower through the absorption liquid delivery pump and the absorption liquid cooler, the air inlet at the lower part of the absorption tower is connected with the outlet of the induced draft fan in the cooling water spraying system, the air outlet at the top of the absorption tower is connected with the air inlet of the spherical tank in the tail gas circulation system, the liquid outlet at the bottom of the absorption tower is connected with the inlet of four parallel analytic kettles, the air outlet of the analytic kettles is connected with the inlet of the full condenser, and the liquid outlet of the analytic kettles is connected with the absorption liquid storage tank to enable absorption liquid to flow back to the absorption liquid storage tank.
In the process of synthesizing the UV light-cured monomer TMPTA, toluene is taken as a water carrying agent, and air is introduced into 2 reaction kettles (specification: 60 m) by utilizing the suction force of a draught fan through a one-way air inlet valve of a circulating tail gas turnover system 3 ) In the method, air escapes from the reaction kettle after passing through the reaction liquid to form tail gas (the temperature is 60 ℃), and the tail gas contains water-carrying agent toluene steam and a small amount of reactant trimethylolpropane, acrylic acid and reaction product trimethylolpropane triacrylate, wherein the contents of the reactant trimethylolpropane, the acrylic acid and the reaction product trimethylolpropane triacrylate are all the contents corresponding to the saturated steam partial pressure of each component under normal pressure and at 60 ℃.
The spraying water in the spraying water storage tank is conveyed to a spraying water cooler by a spraying water conveying pump, cooled to 4 ℃, then enters a water spraying tunnel from the upper part and is sprayed downwards to form a water curtain, the working temperature of the water spraying tunnel is 4 ℃, tail gas discharged from the reaction kettle enters the water spraying tunnel from the air inlet of the water spraying tunnel, the tail gas transversely passes through the water spraying tunnel, the volume ratio of the tail gas to the spraying water is 100:1, the residence time of the tail gas in the water spraying tunnel is 45 seconds, the tail gas is fully balanced in gas-liquid manner, VOC (volatile organic compounds) such as toluene and the like in the tail gas are liquefied to form a water-oil mixed solution, the water-oil mixed solution is collected at the bottom of the water spraying tunnel, the oil phase obtained by liquid separation automatically flows into an organic solvent receiving tank, the oil phase obtained by liquid separation is conveyed back to the synthesis section for multiplexing by an organic phase transfer pump, and the water phase obtained by liquid separation automatically flows back to the spraying water storage tank for recycling; and discharging tail gas from the outlet end of the other end of the water spray tunnel, separating and removing water mist by a hydrocyclone, then entering a dryer for drying treatment, and sending the tail gas into an absorption tower by an induced draft fan. The dryer is used alternately, and the drying agent in the dryer is regenerated periodically.
The method comprises the steps of taking dioctyl phthalate as an absorption liquid, conveying the absorption liquid in an absorption liquid storage tank to an absorption liquid cooler by an absorption liquid conveying pump, cooling to-5 ℃, then entering an absorption tower from the upper part, enabling tail gas (about 20 ℃) to enter the absorption tower from the lower part, enabling the volume ratio of the tail gas to the absorption liquid to be 1000:1, enabling the flow speed of the tail gas in the absorption tower to be 1m/s, enabling the residence time to be 30 seconds, enabling the tail gas to be in countercurrent contact with the absorption liquid in the absorption tower to perform sufficient gas-liquid exchange absorption, enabling toluene in the tail gas to be absorbed into the absorption liquid, enabling the absorption liquid with the toluene to flow out from the bottom of the absorption tower, enabling the absorption liquid to flow into an analysis kettle automatically, heating and analyzing at the temperature of 120 ℃, evaporating the toluene from the absorption liquid, enabling the absorption liquid to enter a complete condenser to be cooled into liquid, returning the absorption liquid with the toluene analyzed to a synthesis section for multiplexing. The tail gas discharged from the top of the absorption tower is returned to the tail gas circulation unit for circulation.
When the air quantity introduced by the induced draft fan and the air quantity sent back to the tail gas circulation system reach balance, stable operation can be realized, and the content of VOC (volatile organic compounds) such as toluene in the tail gas discharged by the absorption tower is stabilized at 3000ppm. Toluene with purity of more than 98% can be recovered by 1.5 tons per day.
Claims (10)
1. Can realize UV photocuring monomer synthesis tail gas treatment and circulation system of zero release, its characterized in that: the treatment and circulation system consists of a tail gas circulation system for circulation, a cooling water spraying system and an organic solvent cold absorption-thermal analysis system, wherein the treatment and circulation system and a reaction kettle for synthesizing UV light curing monomers form closed circulation of tail gas;
the circulating tail gas turnover system comprises a spherical tank lined with a PVC bag-shaped sealing film; the air inlet of the spherical tank is connected with the air outlet of an absorption tower in the atmosphere or organic solvent cold absorption-thermal desorption system, and the air outlet of the spherical tank is connected with the air inlet of the reaction kettle;
the cooling water spraying system comprises a water spraying tunnel, a hydrocyclone, a dryer, an induced draft fan, an oil-water separator and an organic solvent receiving tank; the upper part of the water spraying tunnel is provided with a liquid inlet, one end of the water spraying tunnel is provided with an air inlet connected with an air outlet of the reaction kettle, the other end of the water spraying tunnel is provided with an air outlet connected with an inlet of a hydrocyclone, the air outlet of the hydrocyclone is connected with an inlet of a dryer, and an outlet of the dryer is connected with an air inlet of an absorption tower in the organic solvent cold absorption-thermal desorption system through a draught fan; an outlet at the bottom of the water spraying tunnel is connected with an inlet of the oil-water separator to enable the water-oil mixed solution to automatically flow into the oil-water separator, an oil phase outlet of the oil-water separator is connected with an organic solvent receiving tank, and an outlet of the organic solvent receiving tank is connected with a synthesis working section;
the organic solvent cold absorption-thermal desorption system comprises an absorption tower, a desorption kettle and a complete condenser; the upper part of the absorption tower is provided with a liquid inlet, the lower part of the absorption tower is provided with an air inlet connected with an induced draft fan, an air outlet at the top of the absorption tower is connected with an air inlet of a spherical tank, a liquid outlet at the bottom of the absorption tower is connected with an inlet of an analysis kettle, and an air outlet of the analysis kettle is connected with an inlet of a full condenser.
2. The system for treating and recycling the synthesis tail gas of the UV light-cured monomer capable of realizing zero emission according to claim 1, which is characterized in that: the cooling water spraying system also comprises a spraying water storage tank, a spraying water delivery pump and a spraying water cooler; the outlet of the spray water storage tank is connected with the liquid inlet of the water spray tunnel through a spray water delivery pump and a spray water cooler; the water phase outlet of the oil-water separator is connected with the spray water storage tank, so that the water phase obtained by oil-water separation automatically flows into the spray water storage tank.
3. The system for treating and recycling the synthesis tail gas of the UV light-cured monomer capable of realizing zero emission according to claim 1, which is characterized in that: the cooling water spraying system also comprises an organic phase transfer pump; the organic phase transfer pump is arranged on an outlet pipeline of the organic solvent receiving tank.
4. The system for treating and recycling the synthesis tail gas of the UV light-cured monomer capable of realizing zero emission according to claim 1, which is characterized in that: the dryer is filled with silica gel as a dewatering and drying agent.
5. The system for treating and recycling the synthesis tail gas of the UV light-cured monomer capable of realizing zero emission according to claim 1, which is characterized in that: the organic solvent cold absorption-thermal analysis system comprises an absorption liquid storage tank, an absorption liquid conveying pump and an absorption liquid cooler; the outlet of the absorption liquid storage tank is connected with the liquid inlet at the upper part of the absorption tower through an absorption liquid delivery pump and an absorption liquid cooler; the liquid outlet of the analysis kettle is connected with the absorption liquid storage tank, so that the absorption liquid flows back to the absorption liquid storage tank.
6. A method for treating the tail gas synthesized by the UV light curing monomers by the aid of a zero-emission treatment and circulation system for the tail gas synthesized by the UV light curing monomers according to claim 1, which is characterized in that: comprising the following steps:
in the reaction process of the UV light curing monomer, a draught fan is started, air is introduced into a reaction kettle through a spherical tank of a circulating tail gas turnover system, and tail gas is discharged from an air outlet of the reaction kettle;
step (2), spray water enters a water spray tunnel from the upper part and is sprayed downwards to form a water curtain, tail gas is transversely introduced from the air inlet end of the water spray tunnel, water-oil mixed liquid is collected at the bottom of the water spray tunnel, the water-oil mixed liquid automatically flows into an oil-water separator for liquid separation, the obtained water phase is recycled as spray water, and an organic solvent returns to a synthesis section; the tail gas after spray treatment is separated by a hydrocyclone and dried by a dryer in sequence, and enters an absorption tower;
step (3), tail gas treated by a cooling water spraying system enters an absorption tower from the lower part, absorption liquid enters the absorption tower from the upper part, the absorption liquid and the tail gas are in countercurrent contact to absorb volatile organic compounds in the tail gas, the absorption liquid absorbing the volatile organic compounds flows out from the bottom of the absorption tower, the absorption liquid enters an analysis kettle from the self-flow to be heated and analyzed, the volatile organic compounds are distilled out, and the absorption liquid enters a total condenser to be cooled into liquid and returns to a synthesis working section for recycling; the treated tail gas is led out from the top of the absorption tower and is sent back to the tail gas circulation system for circulation.
7. The method of treating UV curable monomer synthesis tail gas according to claim 6, wherein: in the step (1), the temperature of the tail gas is 60 ℃; the volatile organic compounds in the tail gas are steam of a water-carrying agent, and a reaction raw material of a UV light-curing monomer and the UV light-curing monomer; the contents of the tail gas water carrying agent, the reaction raw materials of the UV light curing monomer and the UV light curing monomer are all the contents corresponding to the saturated steam partial pressure of each component at normal pressure and 60 ℃.
8. The method of treating UV curable monomer synthesis tail gas according to claim 6, wherein: in the step (1), the water-carrying agent is cyclohexane, toluene or other organic solvents used as the water-carrying agent.
9. The method of treating UV curable monomer synthesis tail gas according to claim 6, wherein: in the step (2), the working temperature of the spray water is 0-20 ℃, preferably 2-5 ℃;
the volume ratio of the tail gas to the spray water is 10:1-500:1, and the residence time of the tail gas in the water spray tunnel is not less than 30 seconds.
10. The method of treating UV curable monomer synthesis tail gas according to claim 6, wherein: in the step (3), the volume ratio of the tail gas to the absorption liquid is 300:1-1000:1, and the residence time of the tail gas in the absorption tower is not less than 15 seconds;
the absorption liquid is n-dodecane or dioctyl phthalate; the working temperature of the absorption liquid is-5 to 5 ℃ and the analysis working temperature is 110 to 130 ℃.
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| CN202311754833.2A CN117582785A (en) | 2023-12-20 | 2023-12-20 | UV light-cured monomer synthesis tail gas treatment and circulation system capable of realizing zero emission |
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| CN202311754833.2A CN117582785A (en) | 2023-12-20 | 2023-12-20 | UV light-cured monomer synthesis tail gas treatment and circulation system capable of realizing zero emission |
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