CN211972183U - Acetic anhydride production system - Google Patents
Acetic anhydride production system Download PDFInfo
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- CN211972183U CN211972183U CN202020620112.8U CN202020620112U CN211972183U CN 211972183 U CN211972183 U CN 211972183U CN 202020620112 U CN202020620112 U CN 202020620112U CN 211972183 U CN211972183 U CN 211972183U
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- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 title claims abstract description 193
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 34
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 378
- 238000005336 cracking Methods 0.000 claims abstract description 48
- 238000010791 quenching Methods 0.000 claims abstract description 41
- 238000010521 absorption reaction Methods 0.000 claims abstract description 38
- 239000006200 vaporizer Substances 0.000 claims abstract description 34
- 230000000171 quenching effect Effects 0.000 claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 25
- 238000003860 storage Methods 0.000 claims abstract description 16
- 238000002360 preparation method Methods 0.000 claims abstract description 12
- 238000006243 chemical reaction Methods 0.000 claims abstract description 11
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 4
- 239000003054 catalyst Substances 0.000 claims description 28
- 238000011084 recovery Methods 0.000 claims description 10
- 230000018044 dehydration Effects 0.000 claims description 9
- 238000006297 dehydration reaction Methods 0.000 claims description 9
- 125000000218 acetic acid group Chemical group C(C)(=O)* 0.000 claims description 4
- 238000004939 coking Methods 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 22
- 239000007789 gas Substances 0.000 description 17
- 239000002994 raw material Substances 0.000 description 11
- CCGKOQOJPYTBIH-UHFFFAOYSA-N ethenone Chemical compound C=C=O CCGKOQOJPYTBIH-UHFFFAOYSA-N 0.000 description 5
- 239000000047 product Substances 0.000 description 5
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- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
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- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
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- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 2
- KGEKLUUHTZCSIP-HOSYDEDBSA-N [(1s,4s,6r)-1,7,7-trimethyl-6-bicyclo[2.2.1]heptanyl] acetate Chemical compound C1C[C@]2(C)[C@H](OC(=O)C)C[C@H]1C2(C)C KGEKLUUHTZCSIP-HOSYDEDBSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- RYYVLZVUVIJVGH-UHFFFAOYSA-N caffeine Chemical compound CN1C(=O)N(C)C(=O)C2=C1N=CN2C RYYVLZVUVIJVGH-UHFFFAOYSA-N 0.000 description 2
- HQKQRXZEXPXXIG-VJOHVRBBSA-N chembl2333940 Chemical compound C1[C@]23[C@H](C)CC[C@H]3C(C)(C)[C@H]1[C@@](OC(C)=O)(C)CC2 HQKQRXZEXPXXIG-VJOHVRBBSA-N 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- ZQMIGQNCOMNODD-UHFFFAOYSA-N diacetyl peroxide Chemical compound CC(=O)OOC(C)=O ZQMIGQNCOMNODD-UHFFFAOYSA-N 0.000 description 2
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- MDHYEMXUFSJLGV-UHFFFAOYSA-N phenethyl acetate Chemical compound CC(=O)OCCC1=CC=CC=C1 MDHYEMXUFSJLGV-UHFFFAOYSA-N 0.000 description 2
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- VGKYEIFFSOPYEW-UHFFFAOYSA-N 2-methyl-4-[(4-phenyldiazenylphenyl)diazenyl]phenol Chemical compound Cc1cc(ccc1O)N=Nc1ccc(cc1)N=Nc1ccccc1 VGKYEIFFSOPYEW-UHFFFAOYSA-N 0.000 description 1
- GOLORTLGFDVFDW-UHFFFAOYSA-N 3-(1h-benzimidazol-2-yl)-7-(diethylamino)chromen-2-one Chemical compound C1=CC=C2NC(C3=CC4=CC=C(C=C4OC3=O)N(CC)CC)=NC2=C1 GOLORTLGFDVFDW-UHFFFAOYSA-N 0.000 description 1
- RSWGJHLUYNHPMX-UHFFFAOYSA-N Abietic-Saeure Natural products C12CCC(C(C)C)=CC2=CCC2C1(C)CCCC2(C)C(O)=O RSWGJHLUYNHPMX-UHFFFAOYSA-N 0.000 description 1
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- BSYNRYMUTXBXSQ-UHFFFAOYSA-N Aspirin Chemical compound CC(=O)OC1=CC=CC=C1C(O)=O BSYNRYMUTXBXSQ-UHFFFAOYSA-N 0.000 description 1
- 241000402754 Erythranthe moschata Species 0.000 description 1
- LPHGQDQBBGAPDZ-UHFFFAOYSA-N Isocaffeine Natural products CN1C(=O)N(C)C(=O)C2=C1N(C)C=N2 LPHGQDQBBGAPDZ-UHFFFAOYSA-N 0.000 description 1
- KHPCPRHQVVSZAH-HUOMCSJISA-N Rosin Natural products O(C/C=C/c1ccccc1)[C@H]1[C@H](O)[C@@H](O)[C@@H](O)[C@@H](CO)O1 KHPCPRHQVVSZAH-HUOMCSJISA-N 0.000 description 1
- KXKVLQRXCPHEJC-UHFFFAOYSA-N acetic acid trimethyl ester Natural products COC(C)=O KXKVLQRXCPHEJC-UHFFFAOYSA-N 0.000 description 1
- 230000021736 acetylation Effects 0.000 description 1
- 238000006640 acetylation reaction Methods 0.000 description 1
- 229960001138 acetylsalicylic acid Drugs 0.000 description 1
- YTLQFZVCLXFFRK-UHFFFAOYSA-N bendazol Chemical compound N=1C2=CC=CC=C2NC=1CC1=CC=CC=C1 YTLQFZVCLXFFRK-UHFFFAOYSA-N 0.000 description 1
- 239000007844 bleaching agent Substances 0.000 description 1
- 229940115397 bornyl acetate Drugs 0.000 description 1
- 229960001948 caffeine Drugs 0.000 description 1
- VJEONQKOZGKCAK-UHFFFAOYSA-N caffeine Natural products CN1C(=O)N(C)C(=O)C2=C1C=CN2C VJEONQKOZGKCAK-UHFFFAOYSA-N 0.000 description 1
- 238000004523 catalytic cracking Methods 0.000 description 1
- 229920002301 cellulose acetate Polymers 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- PLHJDBGFXBMTGZ-WEVVVXLNSA-N furazolidone Chemical compound O1C([N+](=O)[O-])=CC=C1\C=N\N1C(=O)OCC1 PLHJDBGFXBMTGZ-WEVVVXLNSA-N 0.000 description 1
- 229960001625 furazolidone Drugs 0.000 description 1
- HIGQPQRQIQDZMP-UHFFFAOYSA-N geranil acetate Natural products CC(C)=CCCC(C)=CCOC(C)=O HIGQPQRQIQDZMP-UHFFFAOYSA-N 0.000 description 1
- HIGQPQRQIQDZMP-DHZHZOJOSA-N geranyl acetate Chemical compound CC(C)=CCC\C(C)=C\COC(C)=O HIGQPQRQIQDZMP-DHZHZOJOSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 239000003999 initiator Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 229940023569 palmate Drugs 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 229940124530 sulfonamide Drugs 0.000 description 1
- 150000003456 sulfonamides Chemical class 0.000 description 1
- 238000001308 synthesis method Methods 0.000 description 1
- KHPCPRHQVVSZAH-UHFFFAOYSA-N trans-cinnamyl beta-D-glucopyranoside Natural products OC1C(O)C(O)C(CO)OC1OCC=CC1=CC=CC=C1 KHPCPRHQVVSZAH-UHFFFAOYSA-N 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The utility model relates to an acetic anhydride production system belongs to acetic anhydride preparation technical field. The acetic anhydride production system comprises an acetic acid storage tank, an acetic acid vaporizer, a reboiler, a cracking furnace, a quenching heat exchanger, a condenser, an absorption tower, a dilute acetic acid tank, a gas-liquid separator and an absorption tower; the acetic acid storage tank is sequentially connected with the acetic acid vaporizer and the reboiler, acetic acid steam enters the cracking furnace to carry out cracking reaction, reaction products generated by the cracking furnace enter the quenching heat exchanger to be cooled, then enter the condenser to be condensed and enter the gas-liquid separator to be separated, gas enters the absorption tower, dilute acetic acid liquid enters the dilute acetic acid tank, part of the dilute acetic acid enters the acetic acid vaporizer, and the acetic acid vaporizer is connected with the absorption tower. The utility model effectively prolongs the production period of acetic anhydride by optimizing the flow, and avoids the shutdown of the production system caused by coking of the cracking reaction; meanwhile, the acetic acid is effectively recycled, so that the energy is effectively saved, and the production efficiency is improved.
Description
Technical Field
The utility model belongs to the technical field of the acetic anhydride preparation, concretely relates to acetic anhydride production system.
Background
The information in this background section is only for enhancement of understanding of the general background of the invention and is not necessarily to be construed as an admission or any form of suggestion that this information forms the prior art that is already known to a person of ordinary skill in the art.
Acetic anhydride (CAS: 108-24-7), also known as acetic anhydride, is a colorless, transparent liquid. Acetic anhydride is an important acetylation reagent, and is used for manufacturing cellulose acetate, acetic acid plastic and non-combustible film, and is used for manufacturing synomycin, furazolidone, dibazole, caffeine, aspirin, sulfonamide and the like in the medical industry, and is mainly used for producing disperse dark blue HCL, disperse scarlet S-SWEL, disperse yellow brown S-2REL and the like in the dye industry; in the perfume industry, the product can be used for producing coumarin, bornyl acetate, musk palmate, cedryl acetate, rosin acetate, phenethyl acetate, geranyl acetate, etc. Acetyl peroxide, made from acetic anhydride, is an initiator and a bleaching agent for polymerization reactions.
At present, the industrial production process of acetic anhydride mainly comprises an acetic acid cracking method, an acetaldehyde oxidation method and a methyl acetate carbonyl synthesis method. Among them, the acetic acid cracking method is still the most widely used and common method because of abundant raw material acetic acid and fuel resources. However, the adoption of the acetic acid cracking method has the problems of more waste gas and waste residue, easy environmental pollution, energy loss and the like. Meanwhile, the reaction for producing ketene by cracking acetic acid is a catalytic cracking reaction, and the reaction is easy to form carbon because the raw materials contain inevitable impurities, and the carbon is brought into the subsequent process, so that the equipment in the subsequent process is blocked and damaged, the production efficiency is influenced, and potential safety hazards are caused.
SUMMERY OF THE UTILITY MODEL
Aiming at the problems in the prior art, the utility model provides an acetic anhydride production system, which realizes the full recycling of acetic acid and reduces the pollution; meanwhile, the system obviously prolongs the cracking period and improves the production efficiency in a non-stop state through the parallel connection of the quenching heat exchangers.
In order to solve the technical problem, the technical scheme of the utility model is that:
an acetic anhydride production system comprises an acetic acid storage tank, an acetic acid vaporizer, a reboiler, a cracking furnace, a quenching heat exchanger, a condenser, an absorption tower, a dilute acetic acid tank, a gas-liquid separator and an absorption tower;
the acetic acid storage tank is sequentially connected with the acetic acid vaporizer and the reboiler, acetic acid steam enters the cracking furnace to carry out cracking reaction, reaction products generated by the cracking furnace enter the quenching heat exchanger to be cooled, then enter the condenser to be condensed and enter the gas-liquid separator to be separated, gas enters the absorption tower, liquid enters the dilute acetic acid tank, part of the dilute acetic acid enters the acetic acid vaporizer, and the acetic acid vaporizer is connected with the absorption tower.
Wherein the quench heat exchanger comprises a first quench heat exchanger and a second quench heat exchanger; the two are connected in parallel and are mutually standby quenching heat exchangers, when the pressure difference of the inlet and the outlet of the first quenching heat exchanger exceeds a preset value (such as 5KPa) in production, the second quenching heat exchanger is started for continuous use, the first quenching heat exchanger is closed at the same time, and the first quenching heat exchanger is cleaned for standby after being cooled to normal temperature; the said method can prolong the production period of the production system and reduce the shut-down accident caused by cleaning the heat exchanger.
The utility model discloses in, through set up the acetic acid vaporizer before the reboiler, effectively reduced acetic acid steam consumption, improved the life cycle of reboiler.
The utility model has the advantages that:
the production system of the acetic anhydride of the utility model effectively prolongs the production period of the acetic anhydride and avoids the shutdown of the production system caused by the coking of the cracking reaction by optimizing the flow, particularly by arranging the parallel quenching heat exchanger; meanwhile, the acetic acid is effectively recycled, so that the aim of fully recycling materials in the whole process is fulfilled, the energy is effectively saved, the production efficiency is improved, and the method has good practical application value.
Drawings
The accompanying drawings, which form a part hereof, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the disclosure and together with the description serve to explain the invention and not to limit the invention unduly.
FIG. 1 is a schematic view of a system for producing acetic anhydride according to examples 1 and 2 of the present invention;
the device comprises a catalyst preparation tank 1, a catalyst preparation tank 2, a catalyst pump 3, a catalyst mixer 4, an acetic acid storage tank 5, an acetic acid vaporizer 6, a reboiler 7, an acetic acid vaporizer 8, an acetic acid residue storage tank 9, a vertical cracking furnace 10, a condenser 11, a dilute acetic acid tank 12, a gas-liquid separator 13, an absorption tower 14, a crude acetic anhydride intermediate tank 15, an acetic anhydride rectifying tower 16, a recovery tower 17, a first quenching heat exchanger 18, a second quenching heat exchanger 19 and a dehydrating tower.
Detailed Description
It should be noted that the following detailed description is exemplary and is intended to provide further explanation of the invention. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this disclosure belongs.
It is noted that the terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of example embodiments according to the present disclosure. As used herein, the singular forms "a", "an" and "the" are intended to include the plural forms as well, and it should be understood that when the terms "comprises" and/or "comprising" are used in this specification, they specify the presence of stated features, steps, operations, devices, components, and/or combinations thereof, unless the context clearly indicates otherwise.
In a specific embodiment of the present invention, a acetic anhydride production system is provided, which includes an acetic acid storage tank, an acetic acid vaporizer, a reboiler, a cracking furnace, a quenching heat exchanger, a condenser, an absorption tower, a dilute acetic acid tank, a gas-liquid separator and an absorption tower;
the acetic acid storage tank is sequentially connected with the acetic acid vaporizer and the reboiler, acetic acid steam enters the cracking furnace to carry out cracking reaction, reaction products generated by the cracking furnace enter the quenching heat exchanger to be cooled, then enter the condenser to be condensed and enter the gas-liquid separator to be separated, gas enters the absorption tower, liquid enters the dilute acetic acid tank, part of the dilute acetic acid enters the acetic acid vaporizer, and the acetic acid vaporizer is connected with the absorption tower.
In yet another embodiment of the present invention, the quench heat exchanger comprises a first quench heat exchanger and a second quench heat exchanger; the two are connected in parallel and are mutually standby quench coolers, when the pressure difference of the inlet and the outlet of the first quench heat exchanger exceeds a preset value (such as 5KPa) in production, the second quench heat exchanger is started for continuous use, the first quench heat exchanger is closed at the same time, and the first quench heat exchanger is cleaned for standby after being cooled to normal temperature; the cracking furnace sends cracking reaction which is easy to form carbon and flows into the quenching heat exchanger to cause blockage, so the method effectively prolongs the production period of a production system and reduces the shutdown event caused by cleaning the quenching heat exchanger.
In another embodiment of the present invention, the cracking furnace is preferably a vertical cracking furnace, and the operation is more stable.
In another embodiment of the present invention, one or more, preferably 4, condensers are sequentially connected in series, so that the cracked product is cooled four times by four cooling and condensing processes, the temperature of the cracked gas at the outlet of the cracking furnace is increased (780-800 ℃), the temperature of the cracked gas is decreased step by step, and thus the materials are separated, the separated dilute acetic acid enters a dilute acetic acid tank after passing through a gas-liquid separator, and the ketene enters an absorption tower.
In another embodiment of the invention, the system comprises a dehydration tower, a part of the dilute acetic acid collected by the dilute acetic acid tank enters the dehydration tower for dehydration, and the dehydration tower is connected with an acetic acid vaporizer. The concentration of acetic acid in the dilute acetic acid is low, the concentration is improved after the dilute acetic acid passes through the dehydration tower, and the dilute acetic acid can be used as a cracking raw material and can also be used as acetic acid for recycling.
In yet another embodiment of the present invention, the system includes a recovery column, and the dehydration column is coupled to the recovery column. The recovery tower is used for recovering a part of acetic acid generated by the dehydration tower.
In another embodiment of the invention, the system comprises a catalyst preparation tank and a catalyst mixer, wherein the catalyst preparation tank is connected with the catalyst mixer, acetic acid in an acetic acid evaporator enters a preheating section of the cracking furnace and then is discharged into the catalyst mixer, and the catalyst mixer is connected with the cracking furnace.
In another embodiment of the invention, the slag discharged from the acetic acid evaporator enters the acetic acid slag storage tank.
In another embodiment of the invention, the system further comprises a crude acetic anhydride intermediate tank and an acetic anhydride rectifying tower, wherein the liquid discharged from the bottom of the absorption tower enters the crude acetic anhydride intermediate tank, the crude acetic anhydride intermediate tank is connected with the acetic anhydride rectifying tower, and the crude acetic acid is sent to the acetic anhydride rectifying tower for rectification treatment.
The utility model discloses a process of system production acetic anhydride does: the raw material acetic acid is pumped to an acetic acid vaporizer by a pump, and enters a cracking furnace after being vaporized. The reaction takes place in the cracking furnace to produce ketene and water. The cracked reactant is cooled by a quenching heat exchanger and enters a condenser for further condensation treatment, and unreacted acetic acid and water are separated. The collected dilute acetic acid is concentrated by a recovery process and then sent to an acetic acid vaporizer to be reused as a raw material. The uncondensed cracked gas enters an absorption process. Reacting with acetic acid in an absorption tower to generate crude acetic anhydride with a certain concentration. And rectifying the crude acetic anhydride by a rectifying tower to obtain a qualified acetic anhydride product.
Example 1 a system for producing an acetic anhydride product is operated as follows:
(1) cracking procedure
Firstly, the catalyst is loaded into a catalyst preparation tank 1 for standby after preparation, and is quantitatively pumped into a catalyst mixer 3 by a catalyst pump 2 during driving.
② the raw material acetic acid is pumped from an acetic acid storage tank 4 to an acetic acid vaporizer 5, then heated by a reboiler 6 and returned to an acetic acid evaporator 7, and the acetic acid evaporator 7 periodically discharges slag to an acetic acid residue storage tank 8. The acetic acid steam is preheated in the upper section of the cracking furnace 9, and is mixed with the catalyst sent by the metering pump in the catalyst mixer 3 after preheating, and then enters the vertical cracking furnace 9.
Thirdly, the cracked reactant enters a first quenching heat exchanger 17 (the second quenching heat exchanger 18 is a spare quenching heat exchanger at the moment) and then enters a condenser 10 for condensation treatment, and the uncondensed mixed gas enters an absorption process; the condensed acetic acid and water are mixed into dilute acetic acid, the dilute acetic acid enters a dilute acetic acid tank 11 from a gas-liquid separator 12, and the dilute acetic acid collected by the dilute acetic acid tank 11 is dehydrated by a dehydrating tower 19 and converted into concentrated acetic acid, and then is sent to an acetic acid vaporizer 5 to be used as a raw material again; a part of vaporized acetic acid generated in the acetic acid vaporizer 5 enters the absorption tower 13 as a raw material; meanwhile, the dehydrating tower 19 is connected with the recovery tower 16, and the dehydrated concentrated acetic acid can be contained in the recovery tower 16 for other purposes.
(2) Ketene absorption step
The cracked gas and the noncondensable gas from the gas-liquid separator 12 in the cracking step enter the bottom of the absorption tower 13, and the hot acetic acid from the bottom of the acetic acid vaporizer 5 is also fed to the bottom of the absorption tower 13. Crude acetic anhydride generated after the cracked gas is absorbed by acetic acid is extracted from the bottom of the absorption tower 13 and is sent to a crude acetic anhydride intermediate tank 14 of the rectification process through a circulating pump at the bottom of the absorption tower 13.
And secondly, pumping the acid gas-washed clean noncondensable gas to a gas-liquid separator 12 through a vacuum pump for separation again, discharging the separated dry tail gas to a cracking furnace 9 for incineration, and conveying the wastewater in the gas-liquid separator 12 to a wastewater collection tank for treatment in a wastewater treatment plant outside the plant area.
(3) Acetic anhydride rectification step
The crude acetic anhydride from the absorption process enters a crude acetic anhydride intermediate tank 14, is pumped into the lower part of an acetic anhydride rectifying tower 15, and is heated and distilled in the acetic anhydride rectifying tower 15 to obtain refined acetic anhydride.
Example 2 a system for producing an acetic anhydride product, operated as follows:
(1) cracking procedure
Firstly, the catalyst is loaded into a catalyst preparation tank 1 for standby after preparation, and is quantitatively pumped into a catalyst mixer 3 by a catalyst pump 2 during driving.
② the raw material acetic acid is pumped from an acetic acid storage tank 4 to an acetic acid vaporizer 5, then heated by a reboiler 6 and returned to an acetic acid evaporator 7, and the acetic acid evaporator 7 periodically discharges slag to an acetic acid residue storage tank 8. The acetic acid steam is preheated in the upper section of the cracking furnace 9, and is mixed with the catalyst sent by the metering pump in the catalyst mixer 3 after preheating, and then enters the vertical cracking furnace 9.
Thirdly, the cracked reactant enters a second quenching heat exchanger 18 (the first quenching heat exchanger 17 is a spare quenching heat exchanger at the moment) and then enters a condenser 10 for condensation treatment, and the uncondensed mixed gas enters an absorption process; the condensed acetic acid and water are mixed into dilute acetic acid, the dilute acetic acid enters a dilute acetic acid tank 11 from a gas-liquid separator 12, and the dilute acetic acid collected by the dilute acetic acid tank 11 is dehydrated by a dehydrating tower 19 and converted into concentrated acetic acid, and then is sent to an acetic acid vaporizer 5 to be used as a raw material again; a part of vaporized acetic acid generated in the acetic acid vaporizer 5 enters the absorption tower 13 as a raw material; meanwhile, the dehydrating tower 19 is connected with the recovery tower 16, and the dehydrated concentrated acetic acid can be contained in the recovery tower 16 for other purposes.
(2) Ketene absorption step
The cracked gas and the noncondensable gas from the gas-liquid separator 12 in the cracking step enter the bottom of the absorption tower 13, and the hot acetic acid from the bottom of the acetic acid vaporizer 5 is also fed to the bottom of the absorption tower 13. Crude acetic anhydride generated after the cracked gas is absorbed by acetic acid is extracted from the bottom of the absorption tower 13 and is sent to a crude acetic anhydride intermediate tank 14 of the rectification process through a circulating pump at the bottom of the absorption tower 13.
And secondly, pumping the acid gas-washed clean noncondensable gas to a gas-liquid separator 12 through a vacuum pump for separation again, discharging the separated dry tail gas to a cracking furnace 9 for incineration, and conveying the wastewater in the gas-liquid separator 12 to a wastewater collection tank for treatment in a wastewater treatment plant outside the plant area.
(3) Acetic anhydride rectification step
The crude acetic anhydride from the absorption process enters a crude acetic anhydride intermediate tank 14, is pumped into the lower part of an acetic anhydride rectifying tower 15, and is heated and distilled in the acetic anhydride rectifying tower 15 to obtain refined acetic anhydride.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention, and various modifications and changes may be made by those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (10)
1. The acetic anhydride production system is characterized by comprising an acetic acid storage tank, an acetic acid vaporizer, a reboiler, a cracking furnace, a quenching heat exchanger, a condenser, an absorption tower, a dilute acetic acid tank, a gas-liquid separator and the absorption tower;
wherein, the acetic acid storage tank is connected with an acetic acid vaporizer and a reboiler in sequence, acetic acid steam enters the cracking furnace to carry out cracking reaction, reaction products generated by the cracking furnace enter the quenching heat exchanger to be cooled, then enter the condenser to be condensed and enter the gas-liquid separator to be separated, gas enters the absorption tower, dilute acetic acid liquid enters the dilute acetic acid tank, part of the dilute acetic acid enters the acetic acid vaporizer, and the acetic acid vaporizer is connected with the absorption tower;
the quench heat exchanger comprises a first quench heat exchanger and a second quench heat exchanger; the two are connected in parallel and are mutually standby quench coolers.
2. The acetic anhydride production system according to claim 1, wherein the cracking furnace is a vertical cracking furnace.
3. The acetic anhydride production system according to claim 1, wherein the number of the condensers is one to a plurality.
4. The acetic anhydride production system according to claim 3, wherein the number of the condensers is 4.
5. The acetic anhydride production system according to claim 4, wherein 4 condensers are connected in series in this order.
6. The acetic anhydride producing system according to claim 1, further comprising a dehydration tower, one end of which is connected to the dilute acetic acid tank and the other end of which is connected to the acetic acid vaporizer, for feeding the dehydrated concentrated acetic acid to the acetic acid vaporizer.
7. The acetic anhydride production system according to claim 6, further comprising a recovery tower connected to the dehydration tower.
8. The acetic anhydride producing system according to claim 1, further comprising a catalyst preparation tank and a catalyst mixer, wherein the catalyst preparation tank is connected to the catalyst mixer, acetic acid fed into the acetic acid vaporizer through the reboiler enters a preheating section of the cracking furnace and then is discharged into the catalyst mixer, and the catalyst mixer is connected to the cracking furnace.
9. The acetic anhydride production system of claim 8, further comprising an acetic acid residue storage tank connected to the acetic acid vaporizer.
10. The acetic anhydride production system according to claim 1, wherein the system further comprises a crude acetic anhydride intermediate tank and an acetic anhydride rectifying tower, the liquid discharged from the bottom of the absorption tower enters the crude acetic anhydride intermediate tank, and the crude acetic anhydride intermediate tank is connected with the acetic anhydride rectifying tower.
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| CN115403463A (en) * | 2021-05-27 | 2022-11-29 | 湖州通宝精细化工有限公司 | Production process of high-purity acetic anhydride |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115403463A (en) * | 2021-05-27 | 2022-11-29 | 湖州通宝精细化工有限公司 | Production process of high-purity acetic anhydride |
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Address after: 277000 Xueneng 2nd Road, 10 billion yuan industrial park, Xuecheng District, Zaozhuang City, Shandong Province Patentee after: Shandong Jiachi New Materials Co.,Ltd. Address before: 277000 Xueneng 2nd Road, 10 billion yuan industrial park, Xuecheng District, Zaozhuang City, Shandong Province Patentee before: Shandong Jiachi New Chemical Co.,Ltd. |
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Denomination of utility model: A production system for acetic anhydride Effective date of registration: 20231222 Granted publication date: 20201120 Pledgee: Bank of Communications Co.,Ltd. Zaozhuang Branch Pledgor: Shandong Jiachi New Materials Co.,Ltd. Registration number: Y2023980074043 |