CN115138185B - Device and method for treating and recycling waste gas in epichlorohydrin production process - Google Patents
Device and method for treating and recycling waste gas in epichlorohydrin production process Download PDFInfo
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- CN115138185B CN115138185B CN202210912507.9A CN202210912507A CN115138185B CN 115138185 B CN115138185 B CN 115138185B CN 202210912507 A CN202210912507 A CN 202210912507A CN 115138185 B CN115138185 B CN 115138185B
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- 238000000034 method Methods 0.000 title claims abstract description 52
- 239000002912 waste gas Substances 0.000 title claims abstract description 49
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 22
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- BRLQWZUYTZBJKN-UHFFFAOYSA-N Epichlorohydrin Chemical compound ClCC1CO1 BRLQWZUYTZBJKN-UHFFFAOYSA-N 0.000 title claims description 17
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 claims abstract description 159
- 238000010521 absorption reaction Methods 0.000 claims abstract description 69
- 235000019445 benzyl alcohol Nutrition 0.000 claims abstract description 53
- 238000003795 desorption Methods 0.000 claims abstract description 38
- 239000007789 gas Substances 0.000 claims abstract description 36
- 238000005406 washing Methods 0.000 claims abstract description 30
- 230000002745 absorbent Effects 0.000 claims abstract description 22
- 239000002250 absorbent Substances 0.000 claims abstract description 22
- 239000007788 liquid Substances 0.000 claims abstract description 17
- LRWZZZWJMFNZIK-UHFFFAOYSA-N 2-chloro-3-methyloxirane Chemical compound CC1OC1Cl LRWZZZWJMFNZIK-UHFFFAOYSA-N 0.000 claims abstract description 6
- 238000010992 reflux Methods 0.000 claims abstract description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 9
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 claims description 8
- 239000004172 quinoline yellow Substances 0.000 claims description 8
- 239000004149 tartrazine Substances 0.000 claims description 7
- 239000002351 wastewater Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 5
- 239000002151 riboflavin Substances 0.000 claims description 5
- 239000010865 sewage Substances 0.000 claims description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims description 4
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 4
- 238000001816 cooling Methods 0.000 claims description 4
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 claims description 4
- 239000004229 Alkannin Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims 1
- 239000011780 sodium chloride Substances 0.000 claims 1
- SUKJFIGYRHOWBL-UHFFFAOYSA-N sodium hypochlorite Chemical compound [Na+].Cl[O-] SUKJFIGYRHOWBL-UHFFFAOYSA-N 0.000 claims 1
- 239000000243 solution Substances 0.000 description 18
- OWXJKYNZGFSVRC-NSCUHMNNSA-N (e)-1-chloroprop-1-ene Chemical compound C\C=C\Cl OWXJKYNZGFSVRC-NSCUHMNNSA-N 0.000 description 6
- ZAMOUSCENKQFHK-UHFFFAOYSA-N Chlorine atom Chemical compound [Cl] ZAMOUSCENKQFHK-UHFFFAOYSA-N 0.000 description 6
- 229910052801 chlorine Inorganic materials 0.000 description 6
- 239000000460 chlorine Substances 0.000 description 6
- 239000006096 absorbing agent Substances 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- AVGQTJUPLKNPQP-UHFFFAOYSA-N 1,1,1-trichloropropane Chemical compound CCC(Cl)(Cl)Cl AVGQTJUPLKNPQP-UHFFFAOYSA-N 0.000 description 1
- ZAIDIVBQUMFXEC-UHFFFAOYSA-N 1,1-dichloroprop-1-ene Chemical compound CC=C(Cl)Cl ZAIDIVBQUMFXEC-UHFFFAOYSA-N 0.000 description 1
- KNKRKFALVUDBJE-UHFFFAOYSA-N 1,2-dichloropropane Chemical compound CC(Cl)CCl KNKRKFALVUDBJE-UHFFFAOYSA-N 0.000 description 1
- IFDLXKQSUOWIBO-UHFFFAOYSA-N 1,3-dichloropropan-1-ol Chemical compound OC(Cl)CCCl IFDLXKQSUOWIBO-UHFFFAOYSA-N 0.000 description 1
- -1 1.2-dichloropropene Chemical compound 0.000 description 1
- ZXCYIJGIGSDJQQ-UHFFFAOYSA-N 2,3-dichloropropan-1-ol Chemical compound OCC(Cl)CCl ZXCYIJGIGSDJQQ-UHFFFAOYSA-N 0.000 description 1
- VRTNIWBNFSHDEB-UHFFFAOYSA-N 3,3-dichloroprop-1-ene Chemical compound ClC(Cl)C=C VRTNIWBNFSHDEB-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 239000012043 crude product Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- AEDZKIACDBYJLQ-UHFFFAOYSA-N ethane-1,2-diol;hydrate Chemical compound O.OCCO AEDZKIACDBYJLQ-UHFFFAOYSA-N 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 239000002440 industrial waste Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- WVDDGKGOMKODPV-ZQBYOMGUSA-N phenyl(114C)methanol Chemical compound O[14CH2]C1=CC=CC=C1 WVDDGKGOMKODPV-ZQBYOMGUSA-N 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000010977 unit operation Methods 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
- B01D53/1406—Multiple stage absorption
-
- 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
- B01D53/1425—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
- B01D53/1456—Removing acid components
-
- 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
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/202—Alcohols or their derivatives
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/202—Single element halogens
- B01D2257/2025—Chlorine
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/20—Halogens or halogen compounds
- B01D2257/206—Organic halogen compounds
- B01D2257/2064—Chlorine
Landscapes
- 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)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a device and a method for treating and recycling waste gas in an epoxy chloropropane production process, wherein the device comprises a first-stage absorption tower, a second-stage washing tower, a desorption tower, a first-stage deep cooler, a second-stage deep cooler, a heat exchanger, a first-stage condenser, a reflux tank, a heat exchanger, an absorption tower circulating pump, a desorption tower discharge pump, a washing tower discharge pump, a liquid ring vacuum pump, a gas-liquid separator and a tail gas fan; the process waste gas enters from the bottom of the first-stage absorption tower, and crude benzyl alcohol enters from the tower to countercurrent contact with the process waste gas for first-stage absorption after being cooled by the first-stage cryocooler; the secondary absorption benzyl alcohol is cooled by a secondary refrigerator and then is in countercurrent contact with the gas after primary absorption; the crude benzyl alcohol solution enters a desorption tower for negative pressure rectification, useful components carried in the process waste gas at the top of the tower are condensed by a condenser and then recycled, the purified benzyl alcohol solution at the bottom of the tower is pumped to a first-stage absorption tower, and the recycling of the absorbent is realized; and the washed gas reaching the standard is emptied after passing through a tail gas fan.
Description
Technical Field
The invention relates to the field of chemical equipment and chemical unit operation absorption and desorption units, in particular to a device and a method for treating and recycling waste gas in an epoxy chloropropane production process.
Background
Epichlorohydrin is an important chemical raw material. A certain amount of process off-gas is generated in the production of epichlorohydrin. The process waste gas is simultaneously entrained with a large amount of other gas impurities, wherein the main components are chlorine, chloropropene, epichlorohydrin, dichloropropene, 2.3-dichloropropene, 1.2-dichloropropene, dichloropropane, trichloropropane, 1,3 dichloropropanol, 2,3 dichloropropanol and the like; these process waste gases not only pollute the environment, but also cause waste of raw materials. Therefore, a proper method is sought to treat the process waste gas generated by the production of epichlorohydrin, and recycle the pollution and sustainable development of useful components to the environment, thereby having important practical significance and wide application prospect.
The selection of the process method and the absorbent flow rate is determined according to the properties of the process waste gas and the treatment requirements of the existing process waste gas in a workshop, outsourced finished benzyl alcohol solution, glycol chilled water at minus 16 ℃ and medium-pressure steam at 200 ℃.
At present, the epichlorohydrin is extremely widely applied, and the research and treatment of the process waste gas generated in the production of the epichlorohydrin are important for improving the ecological environment and continuous production and saving the production raw materials.
Disclosure of Invention
The invention aims to overcome the defects and the shortcomings of the prior art, and provides a device and a method for treating and recycling waste gas in an epoxy chloropropane production process, which have the advantages of simple operation in the whole absorption process, economy, environmental protection and easy large-scale application in industry.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
the device comprises a primary absorption tower, a desorption tower, a secondary washing tower body, a primary deep cooler, a secondary deep cooler, a desorption tower heat exchanger, a condenser, a reflux tank, a gas-liquid separator, an absorption tower circulating pump, a desorption tower discharge pump, a washing tower discharge pump, a liquid ring vacuum pump and a tail gas fan; the first-stage absorption tower and the second-stage washing tower are provided with a feed inlet at the bottom of the tower, and the middle of the desorption tower is provided with a bubble point feed inlet.
The invention also discloses a method based on the device for treating and recycling the waste gas in the epichlorohydrin production process, which comprises the following steps:
the process waste gas enters from the bottom of the first-stage absorption tower, the crude benzyl alcohol of the first-stage absorbent enters from the tower after being cooled by the first-stage cryocooler, and is in countercurrent contact with the process waste gas for first-stage absorption;
the secondary absorption absorbent is benzyl alcohol purified by a desorption tower, and enters from the top of the primary absorption tower to be in countercurrent contact with gas after primary absorption after being cooled by a secondary refrigerator;
the absorbed crude benzyl alcohol solution enters a desorption tower for negative pressure rectification, useful components carried in process waste gas are condensed at the tower top and then recycled through a condenser, the purified benzyl alcohol solution is pumped into a first-stage absorption tower in a circulating way by the absorption tower, and the recycling of the absorbent is realized;
and the washed gas reaching the standard is emptied after passing through a tail gas fan.
As a preferred embodiment of the invention, the crude benzyl alcohol with 96% of circulating absorbent content in the primary absorption tower is 30t/h in flow, and the temperature of the crude benzyl alcohol entering the tower after being cooled by the primary cryocooler is-10 ℃.
As a preferred embodiment of the invention, the content of the absorbent at the top of the primary absorption tower is 99.5% benzyl alcohol purified by a desorption tower, the flow is 10t/h, and the temperature of the tower entering after being cooled by the secondary cryocooler is-10 ℃.
As a preferred embodiment of the invention, the cooling mediums of the primary refrigerator and the secondary refrigerator are glycol water solutions, the water inlet temperature is minus 16 ℃, and the water return temperature is minus 10 ℃.
As a preferred embodiment of the invention, the crude benzyl alcohol solution circularly absorbed by the primary absorption tower is sent to the desorption tower for negative pressure rectification, the vacuum degree is-90 kpa, useful components carried in the process waste gas are arranged at the top of the tower, and the crude benzyl alcohol solution is condensed by the condenser E104 and then recycled, and the purified benzyl alcohol solution is arranged at the bottom of the tower.
As a preferred embodiment of the invention, the process waste gas absorbed by the primary absorption tower enters a secondary washing tower, and the washing liquid is 30% NAOH solution.
As a preferred embodiment of the invention, the main components of the wastewater washed by the secondary washing tower are NACL and NACLO, the discharged material of the washing tower is pumped to a sewage treatment plant for treatment, and the washed standard gas is exhausted after passing through a tail gas fan.
Compared with the prior art, the invention provides the device and the method for treating and recycling the waste gas in the epichlorohydrin production process, which have the following beneficial effects:
1. after primary absorption, the waste gas generated in the production of epoxy chloropropane only contains chlorine and trace chloropropene and benzyl alcohol carried by the chlorine, and after the waste gas passes through a secondary absorption tower, the chlorine and trace chloropropene carried by the waste gas can be completely removed; and the absorbed benzyl alcohol enters a desorption tower to carry out negative pressure rectification, the absorbent at the tower bottom is recycled, and useful components at the tower top are recycled. The scheme not only achieves the aim of standard emission of waste gas in the initial process of design, but also can recycle substances in the tail gas, and has important significance for improving economic benefit and protecting environment.
2. The absorber circularly absorbed and utilized by the primary absorption tower is crude benzyl alcohol (the content is 96 percent), and the flow is 30t/h; the absorbent used in the secondary absorption is benzyl alcohol purified by a desorption tower, and the flow is 10t/h. The crude benzyl alcohol is firstly used for preliminary absorption, and then the purified benzyl alcohol is used for thorough absorption. The two absorption modes are matched for use, so that the production energy consumption is greatly saved and the working efficiency is improved.
3. As can be seen from the ideal state equation pv=nrt, the temperature determines the partial pressure. According to the method for treating and recycling the waste gas of the epichlorohydrin production process, the crude benzyl alcohol of the absorbent and the purified benzyl alcohol are cooled to the temperature of minus 10 ℃ by the glycol aqueous solution at the temperature of minus 16 ℃ before entering the primary absorption tower, so that the aim of completely absorbing pollutants in the process waste gas as much as possible is fulfilled.
4. The crude benzyl alcohol absorbed by the first-stage absorption tower continuously enters the desorption tower for purification, so as to achieve the aim of repeated use.
Drawings
Fig. 1 is a schematic diagram of a method for treating and recycling exhaust gas in an epichlorohydrin production process according to an embodiment of the invention.
In the figure: t101, a primary absorption tower; t102, a desorption tower; t103, a secondary washing tower; e101, a primary refrigerator; e102, a secondary refrigerator; e103, a desorber heat exchanger; e104, a condenser; v101, a reflux drum; v102, a gas-liquid separator; p101, an absorption tower circulating pump; p102, a desorber discharge pump; p103, a discharging pump of the washing tower; p104, a liquid ring vacuum pump; p105, liquid ring vacuum pump.
Detailed Description
The following description of the embodiments of the present invention will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present invention, but not all embodiments.
In the description of the present invention, it should be understood that the terms "upper," "lower," "front," "rear," "left," "right," "top," "bottom," "inner," "outer," and the like indicate or are based on the orientation or positional relationship shown in the drawings, merely to facilitate description of the present invention and to simplify the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be configured and operated in a specific orientation, and thus should not be construed as limiting the present invention.
Referring to fig. 1, the device for treating and recycling waste gas in an epichlorohydrin production process of the present invention includes a primary absorption tower T101, a desorption tower T102, a secondary scrubber T103, a primary refrigerator E101, a secondary refrigerator E102, a desorption tower heat exchanger E103, a condenser E104, a reflux tank V101, a gas-liquid separator V102, an absorption tower circulation pump P101, a desorption tower discharge pump P102, a scrubber discharge pump P103, a liquid ring vacuum pump P104, and a tail gas fan P105;
the primary absorption tower T101 and the secondary washing tower T103 are fed from the bottom of the tower, and the desorption tower T102 is fed from the bubble point in the middle of the tower.
The invention relates to a method for a device for treating and recycling waste gas in an epoxy chloropropane production process, which comprises the following steps:
the process waste gas enters from the bottom of the first-stage absorption tower T101, the crude benzyl alcohol of the first-stage absorbent enters from the tower after being cooled by the first-stage cryogenic device E101, and is in countercurrent contact with the process waste gas for first-stage absorption;
the secondary absorption absorbent is benzyl alcohol purified by a desorption tower T102, and enters from the top of a primary absorption tower T101 to be in countercurrent contact with gas after primary absorption after being cooled by a secondary cryocooler E102;
the absorbed crude benzyl alcohol solution enters a desorption tower T102 for negative pressure rectification, useful components carried in process waste gas are condensed at the top of the tower by a condenser E104 and then recycled, the purified benzyl alcohol solution is at the bottom of the tower, and an absorption tower circulating pump P101 is sent to a primary absorption tower T101, so that the recycling of the absorbent is realized;
the washed gas reaching the standard is exhausted after passing through a tail gas fan P105.
The process waste gas feed inlet is arranged at the bottom of a packing layer close to the first-stage absorption tower T101, the crude product circulating benzyl alcohol feed inlet is arranged at the middle of the packing layer close to the first-stage absorption tower T101, the benzyl alcohol feed inlet after purification of the desorption tower T102 is arranged at the top of the first-stage absorption tower T101, and the top is provided with a liquid distributor and a demister. The absorbed crude benzyl alcohol is sent to a desorption tower T102 by an absorption tower circulating pump P101 for negative pressure rectification, useful components carried in process waste gas are condensed by a condenser E104 and recycled, purified benzyl alcohol solution is recycled in a tower kettle, the process waste gas absorbed by a first-stage absorption tower T101 is sent to the bottom of a second-stage washing tower T103 filler by a pipeline, alkali liquor is divided into two layers for spraying, a demister is arranged at the top, a washing tower discharging pump P103 after washing is sent to a sewage treatment plant for treatment, and the washed standard-reaching gas is discharged after passing through a tail gas fan P105.
In an alternative embodiment, as shown in FIG. 1, the crude benzyl alcohol with 96% circulating absorbent content in the first-stage absorber T101 in the present invention has a flow rate of 30T/h, and the temperature of the crude benzyl alcohol entering the first-stage absorber T101 after cooling is-10 ℃.
Wherein, the circulating crude benzyl alcohol used in the middle part of the first-stage absorption tower T101 is 30T/h, the temperature is-10 ℃, the lower the temperature is, the more favorable for the absorption of industrial waste gas, and the benzyl alcohol solution is used for absorbing the organic waste gas in the tail gas
In an alternative embodiment, as shown in fig. 1, the content of the absorbent at the top of the primary absorption tower T101 is 99.5% benzyl alcohol purified by the desorption tower T102, the flow is 10T/h, and the temperature of the tower entering after being cooled by the secondary cryogenic device E102 is-10 ℃.
Wherein, the content of the absorbent at the top of the primary absorption tower T101 is 99.5 percent of benzyl alcohol purified by the desorption tower T102, the flow is 10T/h, the temperature of the tower inlet is-10 ℃ after the benzyl alcohol is cooled by the secondary cryocooler E102, the purpose is to remove the chlorine which is not fully absorbed in the process waste gas,
in an alternative embodiment, as shown in fig. 1, the cooling mediums of the primary refrigerator and the secondary refrigerator are ethylene glycol water solutions, the water inlet temperature is minus 16 ℃, and the water return temperature is minus 10 ℃; and (3) delivering the crude benzyl alcohol solution circularly absorbed by the first-stage absorption tower T101 to the desorption tower T102 for negative pressure rectification, wherein the vacuum degree is-90 kpa, the tower top is the useful components carried in the process waste gas, the useful components are condensed by the condenser E104 and then recycled, and the purified benzyl alcohol solution is obtained at the tower bottom.
The desorption tower T102 is operated at negative pressure, the vacuum degree is-90 kpa, the energy consumption of medium-pressure steam is greatly reduced, the circulating liquid is benzyl alcohol purified by the desorption tower T102 so as to achieve the internal circulation of the benzyl alcohol, the benzyl alcohol is used as the circulating liquid, on one hand, the waste water emission can be reduced, on the other hand, the waste gas in the tail gas of the vacuum pump can be washed, the waste gas of the vacuum pump is merged into the main pipeline, and the emptying port is not independently arranged.
In an alternative embodiment, as shown in fig. 1, the process waste gas absorbed by the first-stage absorption tower T101 enters a second-stage washing tower T103, and the washing liquid is 30% NAOH solution, so as to completely remove chlorine and trace chloropropene entrained in the process waste gas.
Wherein, the chlorine gas which cannot be absorbed and a small amount of chloropropene and benzyl alcohol enter a second-stage washing tower T103 containing 30 percent of NAOH solution, so as to completely remove the chlorine gas and trace chloropropene carried in the process waste gas; the absorbed benzyl alcohol solution is purified in a desorption tower and returned to the first-stage absorption tower again, so that the purpose of recycling the absorbent is achieved.
In an alternative embodiment, as shown in fig. 1, the main components of the wastewater after being washed by the secondary washing tower T103 in the invention are NACL and NACLO, the discharge pump P103 of the washing tower is sent to a sewage treatment plant for treatment, and the washed standard-reaching gas is exhausted after passing through the exhaust fan P105.
The waste water generated after the washing of the second-stage washing tower T103 is sent to a sewage treatment plant for treatment through the washing tower discharge pump P103, and meanwhile, the washed standard gas is exhausted after passing through the tail gas fan P105.
The foregoing is only a preferred embodiment of the present invention, but the scope of the present invention is not limited thereto, and any person skilled in the art, who is within the scope of the present invention, should make equivalent substitutions or modifications according to the technical scheme of the present invention and the inventive concept thereof, and should be covered by the scope of the present invention.
Claims (4)
1. A method for treating and recycling waste gas in an epoxy chloropropane production process is characterized by comprising the following steps of: the treatment and recovery device comprises a primary absorption tower (T101), a desorption tower (T102), a secondary washing tower (T103), a primary deep cooler (E101), a secondary deep cooler (E102), a desorption tower heat exchanger (E103), a condenser (E104), a reflux tank (V101), a gas-liquid separator (V102), an absorption tower circulating pump (P101), a desorption tower discharging pump (P102), a washing tower discharging pump (P103), a liquid ring vacuum pump (P104) and a tail gas fan (P105); the primary absorption tower (T101) and the secondary washing tower (T103) are provided with feed inlets at the bottom of the tower, and the middle part of the desorption tower (T102) is provided with a bubble point feed inlet;
the method for treating and recycling the waste gas of the epichlorohydrin production process comprises the following steps:
the process waste gas enters from the bottom of a first-stage absorption tower (T101), the crude benzyl alcohol of the first-stage absorbent enters from the tower after being cooled by a first-stage deep cooler (E101), and is in countercurrent contact with the process waste gas for first-stage absorption;
the secondary absorbent is benzyl alcohol purified by a desorption tower (T102), and enters from the top of a primary absorption tower (T101) to be in countercurrent contact with gas after primary absorption after being cooled by a secondary cryocooler (E102);
the absorbed crude benzyl alcohol solution enters a desorption tower (T102) for negative pressure rectification, useful components carried in process waste gas are condensed at the tower top by a condenser (E104) and then recycled, the purified benzyl alcohol solution is at the tower bottom, and an absorption tower circulating pump (P101) is sent to a first-stage absorption tower (T101) to realize the recycling of the absorbent;
the washed gas reaching the standard is exhausted after passing through a tail gas fan (P105);
crude benzyl alcohol with 96% of circulating absorbent content in the primary absorption tower (T101) is cooled by the primary cryocooler (E101) and enters the tower at the temperature of-10 ℃ at the flow rate of 30T/h;
the content of the absorbent at the top of the primary absorption tower (T101) is 99.5 percent of benzyl alcohol purified by a desorption tower (T102), the flow is 10T/h, and the temperature of the tower inlet is-10 ℃ after being cooled by the secondary refrigerator (E102);
the process waste gas absorbed by the primary absorption tower (T101) enters a secondary washing tower (T103), and the washing liquid is 30% NAOH solution.
2. The method for treating and recycling the exhaust gas of the epichlorohydrin production process according to claim 1, which is characterized in that: the cooling mediums of the primary refrigerator and the secondary refrigerator are glycol water solutions, the water inlet temperature is minus 16 ℃, and the water return temperature is minus 10 ℃.
3. The method for treating and recycling the exhaust gas of the epichlorohydrin production process according to claim 1, which is characterized in that: and (3) delivering the crude benzyl alcohol solution circularly absorbed by the primary absorption tower (T101) to the desorption tower (T102) for negative pressure rectification, wherein the vacuum degree is-90 kpa, the tower top is the useful component carried in the process waste gas, and the useful component is condensed by the condenser (E104) and then recycled, and the purified benzyl alcohol solution is obtained at the tower bottom.
4. The method for treating and recycling the exhaust gas of the epichlorohydrin production process according to claim 1, which is characterized in that: the main components of the wastewater washed by the secondary washing tower (T103) are NaCl and NaClO, the wastewater is sent to a sewage treatment plant for treatment through a discharging pump (P103) of the washing tower, and the washed standard gas is exhausted after passing through a tail gas fan (P105).
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