CN221230533U - Acetic acid cracking system for preparing ketene - Google Patents
Acetic acid cracking system for preparing ketene Download PDFInfo
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- CN221230533U CN221230533U CN202322520048.2U CN202322520048U CN221230533U CN 221230533 U CN221230533 U CN 221230533U CN 202322520048 U CN202322520048 U CN 202322520048U CN 221230533 U CN221230533 U CN 221230533U
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- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 555
- 238000005336 cracking Methods 0.000 title claims abstract description 124
- CCGKOQOJPYTBIH-UHFFFAOYSA-N ethenone Chemical compound C=C=O CCGKOQOJPYTBIH-UHFFFAOYSA-N 0.000 title claims abstract description 74
- 239000002253 acid Substances 0.000 claims abstract description 66
- 239000003054 catalyst Substances 0.000 claims abstract description 40
- 238000011084 recovery Methods 0.000 claims abstract description 16
- 238000010521 absorption reaction Methods 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 21
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 20
- 238000000197 pyrolysis Methods 0.000 claims description 17
- 238000003860 storage Methods 0.000 claims description 17
- 238000003776 cleavage reaction Methods 0.000 claims description 8
- 230000007017 scission Effects 0.000 claims description 8
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- 238000001816 cooling Methods 0.000 abstract description 27
- 238000000034 method Methods 0.000 abstract description 19
- 238000009833 condensation Methods 0.000 abstract description 9
- 230000005494 condensation Effects 0.000 abstract description 9
- 238000006243 chemical reaction Methods 0.000 abstract description 7
- 238000002360 preparation method Methods 0.000 abstract description 3
- 238000005516 engineering process Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 49
- 239000000463 material Substances 0.000 description 17
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 10
- 238000002156 mixing Methods 0.000 description 10
- DQWPFSLDHJDLRL-UHFFFAOYSA-N triethyl phosphate Chemical compound CCOP(=O)(OCC)OCC DQWPFSLDHJDLRL-UHFFFAOYSA-N 0.000 description 9
- 238000004064 recycling Methods 0.000 description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 8
- 239000003507 refrigerant Substances 0.000 description 6
- WFDIJRYMOXRFFG-UHFFFAOYSA-N Acetic anhydride Chemical compound CC(=O)OC(C)=O WFDIJRYMOXRFFG-UHFFFAOYSA-N 0.000 description 3
- VBBRYJMZLIYUJQ-UHFFFAOYSA-N cyclopropanone Chemical compound O=C1CC1 VBBRYJMZLIYUJQ-UHFFFAOYSA-N 0.000 description 3
- WASQWSOJHCZDFK-UHFFFAOYSA-N diketene Chemical compound C=C1CC(=O)O1 WASQWSOJHCZDFK-UHFFFAOYSA-N 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 239000002699 waste material Substances 0.000 description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- 239000006096 absorbing agent Substances 0.000 description 2
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 2
- 230000006978 adaptation Effects 0.000 description 1
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 1
- 239000003674 animal food additive Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 1
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 1
- 235000019838 diammonium phosphate Nutrition 0.000 description 1
- 239000000539 dimer Substances 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000000975 dye Substances 0.000 description 1
- BEFDCLMNVWHSGT-UHFFFAOYSA-N ethenylcyclopentane Chemical compound C=CC1CCCC1 BEFDCLMNVWHSGT-UHFFFAOYSA-N 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 239000002778 food additive Substances 0.000 description 1
- 239000005452 food preservative Substances 0.000 description 1
- 235000019249 food preservative Nutrition 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000004334 sorbic acid Substances 0.000 description 1
- 235000010199 sorbic acid Nutrition 0.000 description 1
- 229940075582 sorbic acid Drugs 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 239000002341 toxic gas Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a ketene preparation technology, and discloses an acetic acid cracking system for preparing ketene. When the method is used, acetic acid and a catalyst enter an inlet of an acetic acid cracking furnace for reaction, then enter a first-stage condenser for cooling, after the first-stage cooling, the separated dilute acetic acid is conveyed to a recovery device for treatment through a first-stage light acid conveying pump, ketene gas after the first-stage cooling enters a second-stage condenser for cracking, ketene gas after the second-stage condenser for condensing enters a third-stage condenser for cracking, ketene gas after the third-stage condenser for condensing enters a fourth-stage condenser for cracking, condensate after the second-stage condenser for cracking, the third-stage condenser for cracking and the fourth-stage condenser for cracking are conveyed to the recovery device for treatment through a light acid conveying pump respectively, ketene gas after the fourth-stage condensation cooling is obtained through a cracking outlet, and the ketene gas and tail gas enter the next ketene absorption process.
Description
Technical Field
The utility model relates to the technical field of ketene preparation, in particular to an acetic acid cracking system for preparing ketene.
Background
Ketene is the simplest ketene, and is a toxic gas at room temperature; the ketene is mainly used for synthesizing chemical basic raw materials and reagents, and is a main raw material for producing sorbic acid serving as a food preservative; ketene is unstable and difficult to store, and dimer diketene is extremely easy to form, and the diketene is a raw material of fine chemical dyes, medicines, pesticides, food and feed additives, auxiliaries and the like.
The current ketene preparation process comprises the following steps: acetic acid is cracked in a high temperature cracking furnace at 700-800 deg.c with triethyl phosphate, diammonium hydrogen phosphate, phosphoric acid, etc. as dewatering catalyst to produce ketene. In the process of producing ketene by the conventional process, the cracked ketene and dilute acetic acid are not thoroughly separated, so that the purity of the ketene is low, and the acetic acid cannot be fully recovered, thereby causing resource waste.
Disclosure of utility model
The application provides an acetic acid cracking system for preparing ketene, which solves the problems that the purity of the ketene is low, acetic acid cannot be fully recovered and resource waste is caused by incomplete separation of the cracked ketene and dilute acetic acid.
The application provides an acetic acid cracking system for preparing ketene, which comprises an acetic acid cracking furnace, a cracking condenser and a light acid delivery pump;
The cracking condenser consists of a first cracking condenser, a second cracking condenser, a third cracking condenser and a fourth cracking condenser;
The fade acid delivery pump consists of a first section fade acid delivery pump, a second section fade acid delivery pump, a third section fade acid delivery pump and a fourth section fade acid delivery pump;
The utility model provides a pyrolysis acid feed proportioning device and catalyst proportioning device are connected with respectively through the pipeline to the feed inlet of acetic acid pyrolysis stove, the discharge gate of acetic acid pyrolysis stove has ammonia buffer tank through the pipe connection, ammonia buffer tank has a schizolysis section condenser through pipe connection, schizolysis section condenser has gas-liquid separator through the pipe connection, gas-liquid separator's liquid outlet with recovery plant passes through the section of light acid delivery pump is connected, gas-liquid separator's gas outlet with the air inlet of schizolysis section condenser passes through the pipe connection, the gas outlet of schizolysis section condenser with the air inlet of schizolysis section condenser passes through the pipe connection, schizolysis section condenser with recovery plant passes through the section of light acid delivery pump respectively, three sections of light acid delivery pumps with four sections of light acid delivery pumps are connected.
Preferably, the catalyst dosing device consists of a catalyst storage tank and a catalyst mixer;
The catalyst storage tank is connected with the catalyst mixer through a catalyst pump, and the catalyst mixer is connected with the acetic acid cracking furnace through a metering pump.
Preferably, the pyrolysis acid batching equipment consists of an acetic acid raw material storage tank, an acetic acid intermediate tank, a batching tank, an acetic acid preheater and an acetic acid evaporator;
The acetic acid raw material storage tank with the acetic acid intermediate tank passes through the acetic acid raw material pump to be connected, the acetic acid intermediate tank with the batching groove passes through the acetic acid delivery pump to be connected, the batching groove with install schizolysis acid delivery pump and flowmeter on the pipeline between the acetic acid pre-heater, the acetic acid pre-heater with the acetic acid evaporator passes through the pipe connection, the acetic acid evaporator passes through the pipe connection the feed inlet of acetic acid pyrolysis furnace.
Preferably, the gas outlet of the cracking four-section condenser is connected with ketene absorption equipment through a pipeline.
Preferably, temperature sensors are arranged in the inner cavities of the acetic acid cracking furnace, the acetic acid preheater, the acetic acid evaporator, the first-stage cracking condenser, the gas-liquid separator, the second-stage cracking condenser, the third-stage cracking condenser and the fourth-stage cracking condenser.
Preferably, the acetic acid cracking furnace and the acetic acid evaporator are respectively provided with a pressure sensor in the inner cavity.
According to the technical scheme, when the acetic acid is used, acetic acid is pumped into an acetic acid intermediate tank by an acetic acid raw material pump from an acetic acid raw material storage tank, is conveyed to a material mixing tank by an acetic acid conveying pump, is mixed with 93-95% of the finished acid obtained after azeotropic concentration in the material mixing tank, is fed into an acetic acid cracking furnace for feeding, the prepared cracked acid acetic acid (93-95%) is metered into an acetic acid preheater by a flow meter by the cracked acid conveying pump to be preheated, the preheated acetic acid enters an acetic acid evaporator, acetic acid steam is vaporized in the evaporator and then enters an acetic acid cracking furnace inlet after being vaporized, simultaneously, catalyst triethyl phosphate pumped by metering is mixed and enters the acetic acid cracking furnace inlet, the feeding amount of the catalyst triethyl phosphate is 3 per mill of the feeding amount of the acetic acid, and the vaporized acetic acid and the catalyst simultaneously enter the acetic acid cracking furnace inlet.
After ammonia gas is added into the outlet of the acetic acid cracking furnace and mixed with about 3 per mill of acetic acid, the mixed gas (ketene) at the cracking outlet is cooled by a first-stage condenser, after the first-stage cooling, the separated dilute acetic acid is conveyed to a recovery device for treatment by a first-stage light acid conveying pump, the ketene gas after the first-stage cooling enters a second-stage condenser (the temperature is controlled to be 5-10 ℃), the ketene gas after the condensation of the second-stage condenser enters a third-stage condenser (the temperature is controlled to be 0 ℃), the ketene gas after the condensation of the third-stage condenser enters a fourth-stage condenser (the temperature is controlled to be-3 ℃), the condensate separated by the second-stage condenser, the third-stage condenser and the fourth-stage condenser is conveyed to the recovery device for treatment by a light acid conveying pump respectively, the ketene gas (the content is about 93%) is obtained after the fourth-stage condensation cooling of the cracking outlet, and the next ketene gas is absorbed by the next process.
Compared with the prior art, the utility model has the beneficial effects that:
1. The materials in the system are cooled and separated by the four-section condenser to obtain ketene gas and dilute acetic acid, so that the purity of the obtained ketene gas is high, the production efficiency is improved, and the energy is saved.
2. The method realizes the full recycling of the acetic acid, and the dilute acetic acid obtained after the liquid discharged from the cracking tower enters the gas-liquid separator for separation can be recycled and then used as a material for absorbing the tail gas of the absorption tower, so that the aim of fully recycling the material in the whole process is fulfilled.
3. Ammonia gas is added to the outlet of the acetic acid cracking furnace and is used as a reverse inhibitor to prevent ketene from being polymerized to generate diketene, so that raw materials are wasted and the normal operation of the reaction is influenced.
In summary, the acetic acid cracking system for preparing ketene not only ensures that the purity of the obtained ketene gas is high, the production efficiency is improved and the energy is saved, but also prevents raw materials from being wasted due to the fact that the ketene is polymerized to generate the ketene by adding ammonia gas at the outlet of the acetic acid cracking furnace, and dilute acetic acid can be recycled and then used as a material for absorbing tail gas of an absorption tower, so that the aim of fully recycling the material in the whole process is fulfilled.
Drawings
For a clearer description of the technical solutions of the present utility model, the drawings that are required to be used in the embodiments will be briefly described, and it will be obvious to those skilled in the art that other drawings can be obtained from these drawings without making any effort.
Fig. 1 is a schematic diagram of an acetic acid cleavage system for preparing ketene according to the present utility model.
Reference numerals in the specific embodiments are as follows:
1. An acetic acid cracking furnace; 2. a catalyst storage tank; 3. a material mixing tank; 4. a catalyst mixer; 5. a catalyst pump; 6. acetic acid raw material storage tank; 7. acetic acid intermediate tank; 8. acetic acid raw material pump; 9. an acetic acid delivery pump; 10. a cleavage acid delivery pump; 11. a flow meter; 12. an acetic acid preheater; 13. an acetic acid evaporator; 14. a metering pump; 15. an ammonia buffer tank; 16. cracking a first-stage condenser; 17. a gas-liquid separator; 18. a section of light acid delivery pump; 19. cracking the second-stage condenser; 20. a second stage of a light acid delivery pump; 21. cracking a three-section condenser; 22. a three-stage fade acid delivery pump; 23. cracking a four-section condenser; 24. a four-stage fade acid delivery pump; 25. recovery equipment; 26. a ketene absorber device; 27. a temperature sensor; 28. a pressure sensor.
Detailed Description
In order to enable those skilled in the art to better understand the technical solutions of the present utility model, the following description will make clear and complete descriptions of the technical solutions of the embodiments of the present utility model with reference to the accompanying drawings.
Referring to fig. 1, an acetic acid cracking system for preparing ketene is provided, in order to solve the problems that the purity of the ketene is low, acetic acid cannot be fully recovered and resource waste is caused due to incomplete separation of the cracked ketene and dilute acetic acid, the application provides an acetic acid cracking system for preparing the ketene, which not only ensures that the purity of the obtained ketene gas is high, improves the production efficiency and saves energy, but also prevents raw materials from being wasted due to the polymerization of the ketene into the ketene by adding ammonia gas at the outlet of an acetic acid cracking furnace, and the dilute acetic acid can be recovered and then used as a material for absorbing tail gas of an absorption tower, so that the purpose of fully recycling the material in the whole process is achieved. Concretely, an acetic acid cracking system for preparing ketene comprises an acetic acid cracking furnace 1, a cracking condenser and a light acid delivery pump; the cracking condenser consists of a first cracking condenser 16, a second cracking condenser 19, a third cracking condenser 21 and a fourth cracking condenser 23; the fade acid delivery pump is composed of a first section fade acid delivery pump 18, a second section fade acid delivery pump 20, a third section fade acid delivery pump 22 and a fourth section fade acid delivery pump 24; the feed inlet of the acetic acid cracking furnace 1 is respectively connected with a cracking acid batching device and a catalyst batching device through pipelines, and the cracking acid batching device consists of an acetic acid raw material storage tank 6, an acetic acid intermediate tank 7, a batching tank 3, an acetic acid preheater 12 and an acetic acid evaporator 13;
The acetic acid raw material storage tank 6 is connected with the acetic acid intermediate tank 7 through an acetic acid raw material pump 8, the acetic acid intermediate tank 7 is connected with the material mixing tank 3 through an acetic acid conveying pump 9, the acetic acid cracking furnace 1, the acetic acid preheater 12, the acetic acid evaporator 13, the cracking first-stage condenser 16, the gas-liquid separator 17, the cracking second-stage condenser 19, the cracking third-stage condenser 21 and the cracking fourth-stage condenser 23 are respectively provided with a temperature sensor 27 in the inner cavity, the acetic acid cracking furnace 1 and the acetic acid evaporator 13 are respectively provided with a pressure sensor 28 in the inner cavity, a cracking acid conveying pump 10 and a flowmeter 11 are arranged on a pipeline between the material mixing tank 3 and the acetic acid preheater 12, the acetic acid preheater 12 is connected with the acetic acid evaporator 13 through a pipeline, the acetic acid evaporator 13 is connected with a feed inlet of the acetic acid cracking furnace 1 through a pipeline, the catalyst material mixing equipment consists of a catalyst storage tank 2 and a catalyst mixer 4, the catalyst storage tank 2 is connected with the catalyst mixer 4 through the catalyst pump 5, and the catalyst mixer 4 is connected with the acetic acid cracking furnace 1 through a metering pump 14; acetic acid is pumped into an acetic acid intermediate tank 7 by an acetic acid raw material storage tank 6 through an acetic acid raw material pump 8, is conveyed to a material mixing tank 3 through an acetic acid conveying pump 9, and is mixed with finished acid (more than or equal to 85%) after azeotropic concentration in the material mixing tank 3 to 93-95% of pyrolysis acid for feeding by an acetic acid pyrolysis furnace 1; the catalyst pump 5 is used for sucking the catalyst triethyl phosphate into the catalyst mixer 4, and the process water is added to prepare 10% triethyl phosphate aqueous solution for the acetic acid cracking furnace 1, so that the acetic acid cracking speed and the reaction temperature can be accelerated and reduced; the prepared acetic acid (93-95%) of the pyrolysis acid is metered by a conveying pump 10 of the pyrolysis acid through a flowmeter 11 and enters an acetic acid preheater 12 for preheating, the preheating temperature reaches 80 ℃, the preheated acetic acid enters an acetic acid evaporator 13 (the temperature in the device reaches about 100-105 ℃ and the pressure is-0.03 Mpa), a jacket is pumped with steam for heating, the acetic acid steam is vaporized in the acetic acid evaporator 13 and then enters an acetic acid cracking furnace 1, meanwhile, the catalyst triethyl phosphate (10%) sent by a metering pump 14 is mixed and enters an inlet of the acetic acid cracking furnace 1, the feeding amount of the catalyst triethyl phosphate (10%) is 3 per mill of the feeding amount of the acetic acid, and the vaporized acetic acid and the catalyst simultaneously enter the inlet of the acetic acid cracking furnace 1.
The discharge port of the acetic acid cracking furnace 1 is connected with an ammonia buffer tank 15 through a pipeline, the ammonia buffer tank 15 is connected with a first-stage cracking condenser 16 through a pipeline, the first-stage cracking condenser 16 is connected with a gas-liquid separator 17 through a pipeline, the liquid outlet of the gas-liquid separator 17 is connected with a recovery device 25 through a first-stage pale acid delivery pump 18, the gas outlet of the gas-liquid separator 17 is connected with the gas inlet of a second-stage cracking condenser 19 through a pipeline, the gas outlet of the second-stage cracking condenser 19 is connected with the gas inlet of a third-stage cracking condenser 21 through a pipeline, the gas outlet of the third-stage cracking condenser 21 is connected with the gas inlet of a fourth-stage cracking condenser 23 through a pipeline, The second-stage condenser 19, the third-stage condenser 21 and the fourth-stage condenser 23 are respectively connected with a recovery device 25 through a second-stage pale acid delivery pump 20, a third-stage pale acid delivery pump 22 and a fourth-stage pale acid delivery pump 24, a small amount of uncleaved acetic acid and water generated by reaction are separated in the condensation process in the pyrolysis process, namely pale acid, are collected in a pale acid recovery tank through a gas-liquid separator, the gas outlet of the fourth-stage condenser 23 is connected with a ketene absorber 26 through a pipeline, ammonia gas is added at the outlet of the acetic acid pyrolysis furnace 1 (at the high temperature of 700-730 ℃ and the negative pressure of-0.06 to-0.08 MPa in the furnace), Because the temperature (550-600 ℃) of the mixed gas (ketene) at the cracking outlet is higher, the mixed gas firstly enters a first-stage condenser 16 for cooling, the refrigerant adopts circulating water (the temperature is less than 32 ℃), after the first-stage cooling, the mixed gas passes through a gas-liquid separator 17 (the temperature in the device is controlled at 60 ℃), the separated part is the incomplete cracking and the side reaction in the cooling process produces partial dilute acetic acid (about 30%), the separated dilute acetic acid is conveyed to a recovery device 25 for treatment by a first-stage dilute conveying pump 18, the ketene gas after the first-stage cooling enters a second-stage condenser 19 for cracking (the temperature is controlled at 5-10 ℃), the refrigerant adopts glycol chilled water (the temperature is less than-5 ℃), The method comprises the steps of simultaneously separating a small amount of acetic acid carried in ketene gas in a second-stage condensation cooling process, conveying the separated dilute acetic acid to recovery equipment 25 for treatment through a second-stage pale acid conveying pump 20, enabling the ketene gas condensed through a second-stage pyrolysis condenser 19 to enter a third-stage pyrolysis condenser 21 (the temperature is controlled to be 0 ℃), enabling a refrigerant to adopt ethylene glycol chilled water (the temperature is < -5 ℃), simultaneously separating a small amount of acetic acid carried in the ketene gas in the third-stage condensation cooling process, conveying the separated dilute acetic acid to the recovery equipment 25 for treatment through a third-stage pale acid conveying pump 22, enabling the ketene gas condensed through the third-stage pyrolysis condenser 21 to enter a fourth-stage pyrolysis condenser 23 (the temperature is controlled to be minus 3 ℃), enabling the refrigerant to adopt ethylene glycol chilled water (the temperature is < -5 ℃), simultaneously separating a small amount of acetic acid carried in the ketene gas and a small amount of acetic anhydride generated in a negative reaction process in the fourth-stage condensation cooling process, conveying the separated condensate to the recovery equipment 25 for treatment through a fourth-stage pale acid conveying pump 24, and obtaining the ketene gas (the left content is 93%) after fourth-stage condensation cooling through a pyrolysis outlet; Because the whole cracking reaction system is carried out under negative pressure, acetic acid is entrained in ketene gas, the acetic acid is heated at high temperature in an acetic acid cracking furnace 1 to react to generate waste gas, the selectivity of the acetic acid to crack the ketene is 90%, 4m 3 (standard) waste gas (the composition of which is CO213.9%, C2H422.7%, CO 46.9% and CH 416.5%) is generated every 100Kg raw material acetic acid is evaporated due to the waste gas generated by the negative reaction, and the ketene gas and tail gas enter the next ketene absorption process until the cracking process is finished.
According to the technical scheme, when the acetic acid is used, acetic acid is pumped into the acetic acid intermediate tank 7 by the acetic acid raw material pump 8 from the acetic acid raw material storage tank 6, is conveyed to the material mixing tank 3 by the acetic acid conveying pump 9, is mixed with 93-95% of the finished product acid (more than or equal to 85%) obtained after concentration by azeotropic concentration in the material mixing tank 3, is fed into the acetic acid cracking furnace 1, the prepared cracked acid acetic acid (93-95%) is metered into the acetic acid preheater 12 by the cracked acid conveying pump 10 through the flowmeter 11 to be preheated, the preheating temperature reaches 80 ℃, the preheated acetic acid enters the acetic acid evaporator 13 (the temperature in the acetic acid evaporator reaches about 100-105 ℃ and the pressure of-0.03 Mpa), the jacket is pumped into the steam to be heated, the acetic acid steam is gasified in the acetic acid evaporator 13 and then enters the acetic acid cracking furnace 1, the catalyst triethyl phosphate (10%) fed by the metering pump 14 is simultaneously mixed and then enters the inlet of the acetic acid cracking furnace 1, and the catalyst triethyl phosphate (10%) is fed into the acetic acid preheating furnace 1.
The ammonia gas is added into the outlet of the acetic acid cracking furnace 1 and is mixed with the acetic acid accounting for about 3 per mill, because the temperature (550-600 ℃) of the mixed gas (ketene) at the cracking outlet is higher, the mixed gas firstly enters a first-stage cracking condenser 16 for cooling, the refrigerant adopts circulating water (the temperature is lower than 32 ℃), after the first-stage cooling, the mixed gas passes through a gas-liquid separator 17 (the temperature in the separator is controlled at 60 ℃), the separated dilute acetic acid is conveyed to a recycling device 25 for treatment through a first-stage pale acid conveying pump 18, the ketene gas after the first-stage cooling enters a second-stage cracking condenser 19 (the temperature is controlled at 5-10 ℃), the refrigerant adopts glycol chilled water (the temperature is lower than-5 ℃), the separated dilute acetic acid enters a recycling device 25 through a second-stage pale acid conveying pump 20, the ketene gas after the separated gas enters a second-stage cooling device for treatment through the second-stage pale acid conveying pump 20, the ketene gas after the separated gas enters a third-stage cooling device for cooling, the ketene gas enters a third-stage cooling device 21 (the temperature is lower than 5 ℃), and the ethylene ketone gas after the separated gas enters a fourth-stage cooling device for recycling device for the cooling, and the ethylene ketone gas enters a fourth-stage cooling device for recycling device (the condensate is controlled at 3-3 ℃)), and the ethylene ketone gas after the temperature is cooled at the fourth-stage cooling device for the cooling is controlled at the temperature of 3).
Other embodiments of the utility model will be apparent to those skilled in the art from consideration of the specification and practice of the application disclosed herein. This application is intended to cover any variations, uses, or adaptations of the utility model following, in general, the principles of the utility model and including such departures from the present disclosure as come within known or customary practice within the art to which the utility model pertains. It is intended that the specification and examples be considered as exemplary only, with a true scope of the utility model being indicated by the following claims.
It is to be understood that the utility model is not limited to the precise arrangements and instrumentalities shown in the drawings, which have been described above, and that various modifications and changes may be effected without departing from the scope thereof. The embodiments of the present utility model described above do not limit the scope of the present utility model.
Claims (6)
1. An acetic acid cleavage system for preparing ketene, characterized by: comprises an acetic acid cracking furnace (1), a cracking condenser and a light acid delivery pump;
the cracking condenser consists of a first cracking section condenser (16), a second cracking section condenser (19), a third cracking section condenser (21) and a fourth cracking section condenser (23);
The fade acid delivery pump consists of a first section fade acid delivery pump (18), a second section fade acid delivery pump (20), a third section fade acid delivery pump (22) and a fourth section fade acid delivery pump (24);
The feed inlet of the acetic acid cracking furnace (1) is respectively connected with a cracking acid batching device and a catalyst batching device through pipelines, the discharge outlet of the acetic acid cracking furnace (1) is connected with an ammonia buffer tank (15) through a pipeline, the ammonia buffer tank (15) is connected with a first-stage cracking condenser (16) through a pipeline, the first-stage cracking condenser (16) is connected with a gas-liquid separator (17) through a pipeline, the liquid outlet of the gas-liquid separator (17) is connected with a recovery device (25) through a first-stage light acid conveying pump (18), the gas outlet of the gas-liquid separator (17) is connected with the gas inlet of a second-stage cracking condenser (19) through a pipeline, the gas outlet of the cracking second-section condenser (19) is connected with the gas inlet of the cracking third-section condenser (21) through a pipeline, the gas outlet of the cracking third-section condenser (21) is connected with the gas inlet of the cracking fourth-section condenser (23) through a pipeline, and the cracking second-section condenser (19), the cracking third-section condenser (21) and the cracking fourth-section condenser (23) are connected with the recovery equipment (25) through the second-section pale acid conveying pump (20), the third-section pale acid conveying pump (22) and the fourth-section pale acid conveying pump (24) respectively.
2. An acetic acid cleavage system for preparing ketene according to claim 1, wherein: the catalyst batching equipment consists of a catalyst storage tank (2) and a catalyst mixer (4);
The catalyst storage tank (2) is connected with the catalyst mixer (4) through a catalyst pump (5), and the catalyst mixer (4) is connected with the acetic acid cracking furnace (1) through a metering pump (14).
3. An acetic acid cleavage system for preparing ketene according to claim 1, wherein: the cracking acid batching equipment consists of an acetic acid raw material storage tank (6), an acetic acid intermediate tank (7), a batching tank (3), an acetic acid preheater (12) and an acetic acid evaporator (13);
Acetic acid raw materials storage tank (6) with acetic acid intermediate tank (7) are connected through acetic acid raw materials pump (8), acetic acid intermediate tank (7) with batching groove (3) are connected through acetic acid delivery pump (9), batching groove (3) with install schizolysis acid delivery pump (10) and flowmeter (11) on the pipeline between acetic acid pre-heater (12), acetic acid pre-heater (12) with acetic acid evaporator (13) are through pipe connection, acetic acid evaporator (13) are through pipe connection acetic acid pyrolysis furnace (1) feed inlet.
4. An acetic acid cleavage system for preparing ketene according to claim 1, wherein: the gas outlet of the cracking four-section condenser (23) is connected with a ketene absorption device (26) through a pipeline.
5. An acetic acid cleavage system for preparing ketene according to claim 1, wherein: the device is characterized in that temperature sensors (27) are arranged in inner cavities of the acetic acid cracking furnace (1), the acetic acid preheater (12), the acetic acid evaporator (13), the first-stage cracking condenser (16), the gas-liquid separator (17), the second-stage cracking condenser (19), the third-stage cracking condenser (21) and the fourth-stage cracking condenser (23).
6. An acetic acid cleavage system for preparing ketene according to claim 1, wherein: pressure sensors (28) are arranged in the inner cavities of the acetic acid cracking furnace (1) and the acetic acid evaporator (13).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322520048.2U CN221230533U (en) | 2023-09-15 | 2023-09-15 | Acetic acid cracking system for preparing ketene |
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| Application Number | Priority Date | Filing Date | Title |
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