CN108069852B - Acetic acid continuous recovery system and working method thereof - Google Patents
Acetic acid continuous recovery system and working method thereof Download PDFInfo
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- CN108069852B CN108069852B CN201810082773.7A CN201810082773A CN108069852B CN 108069852 B CN108069852 B CN 108069852B CN 201810082773 A CN201810082773 A CN 201810082773A CN 108069852 B CN108069852 B CN 108069852B
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- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 306
- 238000011084 recovery Methods 0.000 title claims abstract description 63
- 238000000034 method Methods 0.000 title claims abstract description 15
- 238000009833 condensation Methods 0.000 claims abstract description 75
- 230000005494 condensation Effects 0.000 claims abstract description 75
- 239000002904 solvent Substances 0.000 claims abstract description 26
- 238000002425 crystallisation Methods 0.000 claims abstract description 15
- 230000008025 crystallization Effects 0.000 claims abstract description 15
- 238000010438 heat treatment Methods 0.000 claims abstract description 12
- 238000002844 melting Methods 0.000 claims abstract description 12
- 230000008018 melting Effects 0.000 claims abstract description 12
- 239000007789 gas Substances 0.000 claims description 52
- 239000012267 brine Substances 0.000 claims description 41
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 41
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 33
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 32
- 238000001816 cooling Methods 0.000 claims description 20
- 229910052757 nitrogen Inorganic materials 0.000 claims description 16
- 239000007787 solid Substances 0.000 claims description 13
- 239000007788 liquid Substances 0.000 claims description 12
- 239000002826 coolant Substances 0.000 claims description 8
- 238000007710 freezing Methods 0.000 claims description 5
- 230000008014 freezing Effects 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- 239000000428 dust Substances 0.000 claims description 2
- 239000000052 vinegar Substances 0.000 description 5
- 235000021419 vinegar Nutrition 0.000 description 5
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 4
- 239000011780 sodium chloride Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000010924 continuous production Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003595 mist Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 239000004065 semiconductor Substances 0.000 description 2
- 238000009835 boiling Methods 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000796 flavoring agent Substances 0.000 description 1
- 235000019634 flavors Nutrition 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000010563 solid-state fermentation Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 238000013022 venting Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12J—VINEGAR; PREPARATION OR PURIFICATION THEREOF
- C12J1/00—Vinegar; Preparation or purification thereof
- C12J1/10—Apparatus
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D17/00—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces
- F25D17/02—Arrangements for circulating cooling fluids; Arrangements for circulating gas, e.g. air, within refrigerated spaces for circulating liquids, e.g. brine
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25D—REFRIGERATORS; COLD ROOMS; ICE-BOXES; COOLING OR FREEZING APPARATUS NOT OTHERWISE PROVIDED FOR
- F25D31/00—Other cooling or freezing apparatus
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- Physics & Mathematics (AREA)
- Combustion & Propulsion (AREA)
- Organic Chemistry (AREA)
- General Health & Medical Sciences (AREA)
- Genetics & Genomics (AREA)
- Bioinformatics & Cheminformatics (AREA)
- Wood Science & Technology (AREA)
- Zoology (AREA)
- Biochemistry (AREA)
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Abstract
The invention relates to a continuous acetic acid recovery system and a working method thereof, wherein the continuous acetic acid recovery system comprises a first cryogenic crystallizer, a second cryogenic crystallizer, a condensation cooler and a solvent recovery tank which can be alternately in a condensation state, fins are arranged in the first cryogenic crystallizer and the second cryogenic crystallizer, cold source media for condensation and heat source media for liquefaction can be introduced into the fins, and air inlets of the first cryogenic crystallizer and the second cryogenic crystallizer are respectively communicated with an air outlet of the condensation cooler; the first cryogenic crystallizer and the second cryogenic crystallizer which can be alternately in a condensation crystallization state and a heating melting state are arranged, when the first cryogenic crystallizer is in the condensation crystallization state, the second cryogenic crystallizer is in the heating melting state, and when the second cryogenic crystallizer is in the condensation crystallization state, the first cryogenic crystallizer is in the heating melting state, so that the continuous condensation solidification-heating liquefaction process of acetic acid can be realized, and the continuous recovery of acetic acid can be realized.
Description
Technical Field
The invention relates to the technical field of drying equipment, in particular to a continuous acetic acid recovery system and a working method thereof.
Background
In the prior art, the solid state fermentation method is one of the production processes of vinegar; the vinegar obtained by the method has good flavor, and is a traditional vinegar method in China; its advantages are long production period, high labor strength and low output rate of vinegar. This problem is caused by the low recovery rate of acetic acid in the material during production, and the lack of suitable acetic acid recovery equipment. The materials are usually subjected to vinegar residue treatment by adopting the process flows of boiling drying, solid-gas separation, particle material recovery and gaseous acetic acid recovery, and in the gaseous acetic acid recovery link, the existing gaseous acetic acid recovery device has low heat exchange efficiency, so that the energy consumption is high, or continuous production cannot be performed, so that the efficiency is low; in summary, designing an acetic acid continuous recovery system with high reliability suitable for automatic continuous production for recovering acetic acid with low flash point, strong volatility and pungent smell is a technical problem that needs to be solved urgently by those skilled in the art.
Disclosure of Invention
The invention aims to solve the technical problem of providing an acetic acid continuous recovery system which is simple in structure, efficient and energy-saving.
In order to solve the technical problems, the continuous acetic acid recovery system provided by the invention comprises a first cryogenic crystallizer, a second cryogenic crystallizer, a condensation cooler and a solvent recovery tank, wherein the first cryogenic crystallizer and the second cryogenic crystallizer can be alternately in a condensation state and a liquefaction state; the first cryogenic crystallizer and the second cryogenic crystallizer are internally provided with fins, cold source media for condensation and heat source media for liquefaction can be introduced into the fins, air inlets of the first cryogenic crystallizer and the second cryogenic crystallizer are respectively communicated with an air outlet of the condensation cooler, a first valve is arranged between the first cryogenic crystallizer and the condensation cooler, a second valve is arranged between the second cryogenic crystallizer and the condensation cooler, when the first valve is opened and the second valve is closed, gas mixed with gaseous acetic acid flowing out of the condensation cooler enters the first cryogenic crystallizer, the cold source media are introduced into the fins of the first cryogenic crystallizer, the gaseous acetic acid is condensed on the fins of the first cryogenic crystallizer, the heat source media are introduced into the fins of the second cryogenic crystallizer, and solid acetic acid on the fins of the second cryogenic crystallizer is heated and liquefied; when the first valve is closed and the second valve is opened, the gas mixed with gaseous acetic acid flowing out of the condensation cooler enters the second cryogenic crystallizer, a cold source medium is introduced into the fins of the second cryogenic crystallizer, the gaseous acetic acid is condensed on the fins of the second cryogenic crystallizer, a heat source medium is introduced into the fins of the first cryogenic crystallizer, and the solid acetic acid on the fins of the first cryogenic crystallizer is heated and liquefied; the first and second cryogenic crystallizers can be condensed and liquefied alternately, and the first and second cryogenic crystallizers are communicated with the solvent recovery tank, and the gaseous acetic acid can enter the solvent recovery tank after being condensed and liquefied.
Further, a primary water-cooling liquefying region and a secondary chilled water liquefying region are sequentially arranged in the condensation cooler, the cooling medium of the primary water-cooling liquefying region is room temperature water, the cooling medium of the secondary chilled water liquefying region is chilled brine at the temperature of minus 5 ℃, so that gas mixed with gaseous acetic acid is cooled, the gaseous acetic acid is converted into liquid acetic acid, and the liquid acetic acid is collected and enters a solvent recovery tank; the air outlet of the condensation cooler is provided with the water baffle device so as to reduce entrainment of acetic acid mist in the gas as much as possible, and the acetic acid content entering the cryogenic crystallizer can be effectively reduced; under normal conditions, the recovery rate of the solvent through primary water cooling and secondary freezing water cooling is about 85%, and the rest small amount of gaseous acetic acid enters a cryogenic crystallizer along with the gas to perform tertiary condensation, so that the solvent content in the circulating gas can be greatly reduced.
Further, cold source mediums introduced into the first cryogenic crystallizer and the second cryogenic crystallizer are chilled brine at the temperature of minus 18 ℃, heat source mediums introduced into the first cryogenic crystallizer and the second cryogenic crystallizer are hot nitrogen at the temperature of not lower than 120 ℃, liquefaction effect is ensured, the first cryogenic crystallizer and the second cryogenic crystallizer are in a condensation state when the cold source mediums are introduced into fins, a small amount of gas mixed with gaseous acetic acid passes through the fins, and the gaseous acetic acid is condensed and crystallized to be solid acetic acid which is attached to the surfaces of the fins; the first and second cryogenic crystallizers are in a melting state when heat source mediums are introduced into the first and second cryogenic crystallizers, solid acetic acid attached to the surfaces of the fins is heated and melted, and the obtained liquid acetic acid enters a solvent recovery tank.
Further, the acetic acid continuous recovery system further comprises a frozen brine recovery tank, wherein frozen brine in the fins of the first cryogenic crystallizer and the second cryogenic crystallizer can enter the frozen brine recovery tank, so that the frozen brine can be completely discharged before hot nitrogen is introduced into the fins of the first cryogenic crystallizer or the second cryogenic crystallizer.
The working method of the acetic acid continuous recovery system comprises the following steps:
A. the gas mixed with gaseous acetic acid obtained after solid-gas separation enters a condensation cooler through a bag-type dust collector, and is sequentially cooled through a primary water-cooling liquefaction zone and a secondary chilled water liquefaction zone of the condensation cooler, the temperature of the room temperature water of the primary water-cooling liquefaction zone and the temperature of chilled brine of the secondary chilled water liquefaction zone at minus 5 ℃ are respectively condensed and cooled, the obtained liquid acetic acid enters a solvent recovery tank, and the temperature of the gas mixed with a small amount of gaseous acetic acid is reduced to about 13 ℃ when the gas is discharged from the condensation cooler.
B. The first valve is opened, the second valve is closed, meanwhile, the fins of the first cryogenic crystallizer are filled with frozen brine at the temperature of minus 18 ℃, at this time, the first cryogenic crystallizer is in a condensation crystallization state, gas discharged from the condensation cooler enters the first cryogenic crystallizer, a small amount of gaseous acetic acid in the gas is condensed and crystallized to adhere to the surfaces of the fins, the temperature of the gas is reduced to about 0 ℃, and the gas is discharged out of the first cryogenic crystallizer.
C. After the first cryogenic crystallizer is in a condensation crystallization state for a preset time, the first valve is closed, the second valve is opened, meanwhile, freezing brine at the temperature of minus 18 ℃ is introduced into fins of the second cryogenic crystallizer, at the moment, the second cryogenic crystallizer is in the condensation crystallization state, gas discharged from the condensation cooler enters the second cryogenic crystallizer, a small amount of gaseous acetic acid in the gas is condensed and crystallized to be attached to the surfaces of the fins, the temperature of the gas is reduced to about 0 ℃ and is discharged out of the second cryogenic crystallizer; the fins of the first cryogenic crystallizer are filled with hot nitrogen with the temperature not lower than 120 ℃, the first cryogenic crystallizer is in a heating and melting state, solid acetic acid attached to the surfaces of the fins is heated and melted, and the obtained liquid acetic acid enters a solvent recovery tank.
D. The first cryogenic crystallizer and the second cryogenic crystallizer are alternately in a condensation crystallization state and a heating melting state, so that continuous recovery of acetic acid can be realized.
The invention has the technical effects that: (1) Compared with the prior art, the acetic acid continuous recovery system is provided with the first cryogenic crystallizer and the second cryogenic crystallizer which can be alternately in a condensation crystallization state and a heating melting state, wherein the first cryogenic crystallizer is in the condensation crystallization state, the second cryogenic crystallizer is in the heating melting state, and the second cryogenic crystallizer is in the condensation crystallization state, and the first cryogenic crystallizer is in the heating melting state, so that the continuous condensation solidification-heating liquefaction process of acetic acid can be realized, and the continuous recovery of acetic acid is realized; (2) The content of gaseous acetic acid in the gas can be reduced to below 15% by adopting water cooling in a condensation cooler and two-stage cooling of chilled brine cooling, and the content of acetic acid in the gas can be reduced to below 0.1% by adopting three-stage cooling recovery in combination with chilled brine condensation of a cryogenic crystallizer.
Drawings
The invention is described in further detail below with reference to the drawings of the specification:
FIG. 1 is a schematic diagram of the acetic acid continuous recovery system of the present invention.
In the figure: the device comprises a cryogenic crystallizer air outlet 40, a first cryogenic crystallizer 41, a second cryogenic crystallizer 42, a solvent recovery tank 43, a frozen brine recovery tank 44, a first valve 45, a second valve 46, a first frozen brine inlet 47, a second frozen brine inlet 48, a condensing cooler 5, an air inlet 50, a water deflector 51, a frozen brine inlet 52, a heater 61, a nitrogen inlet 62, a circulating fan 63, a third valve 64, a fourth valve 65 and a nitrogen air outlet 66.
Detailed Description
Embodiment 1 as shown in fig. 1, the acetic acid continuous recovery system of this embodiment includes a first cryocrystallizer 41, a second cryocrystallizer 42, a condensation cooler 5, a solvent recovery tank 43, and a chilled brine recovery tank 44; the gas mixed with the gaseous acetic acid enters the condensation cooler 5 through the gas inlet 50, the condensation cooler 5 condenses the gas mixed with the gaseous acetic acid, a primary water cooling liquefaction area and a secondary chilled water liquefaction area are sequentially arranged in the condensation cooler 5, the cooling medium of the primary water cooling liquefaction area is room temperature water, the cooling medium of the secondary chilled water liquefaction area is chilled brine at the temperature of minus 5 ℃, the chilled brine at the temperature of minus 5 ℃ enters the condensation cooler through the chilled brine inlet 52, the gas mixed with the gaseous acetic acid is cooled, the gaseous acetic acid is converted into liquid acetic acid, the condensation cooler 5 is communicated with the solvent recovery tank 43 through a pipeline, and the gaseous acetic acid is cooled and converted into the liquid acetic acid and then enters the solvent recovery tank 43. The air outlet of the condensation cooler 5 is provided with a water baffle 51 so as to reduce entrainment of acetic acid mist in the gas as much as possible, and the acetic acid content entering the cryogenic crystallizer can be effectively reduced; under normal conditions, the recovery rate of the solvent through primary water cooling and secondary freezing water cooling is about 85%, and the rest small amount of gaseous acetic acid enters a cryogenic crystallizer along with circulating gas to perform tertiary condensation.
Fins are arranged in the first cryogenic crystallizer 41 and the second cryogenic crystallizer 42, cold source media for condensation and heat source media for liquefaction can be introduced into the fins, the first cryogenic crystallizer 41 and the second cryogenic crystallizer 42 are in a condensation state when the cold source media are introduced into the fins, a small amount of gaseous acetic acid mixed gas passes through the fins, and the gaseous acetic acid is condensed and crystallized into solid acetic acid to be attached to the surfaces of the fins; the first and second cryogenic crystallizers 41 and 42 are in a melted state when a heat source medium is introduced therein, and the solid acetic acid adhering to the fin surfaces is heated and melted to obtain liquid acetic acid, which enters the solvent recovery tank 43.
The cold source mediums introduced into the first and second cryogenic crystallizers 41 and 42 are-18 ℃ frozen brine, the-18 ℃ frozen brine can enter the first cryogenic crystallizer 41 from the first frozen brine inlet 47, and the-18 ℃ frozen brine can enter the second cryogenic crystallizer 42 from the second frozen brine inlet 48; the air inlets of the first cryogenic crystallizer 41 and the second cryogenic crystallizer 42 are respectively communicated with the air outlet of the condensation cooler 5, a first valve 45 is arranged between the first cryogenic crystallizer 41 and the condensation cooler 5, a second valve 46 is arranged between the second cryogenic crystallizer 42 and the condensation cooler 5, a heat source medium introduced into the first cryogenic crystallizer 41 and the second cryogenic crystallizer 42 is hot nitrogen with the temperature not lower than 120 ℃, normal-temperature nitrogen enters the heater 61 through the nitrogen inlet 62, a third valve 64 is arranged between the heater 61 and the first cryogenic crystallizer 41, a fourth valve 65 is arranged between the heater 61 and the second cryogenic crystallizer 42, the first valve 45 is opened, the second valve 46 is closed, the third valve 64 is closed, and when the fourth valve 65 is opened, gas mixed with gaseous acetic acid flowing out of the condensation cooler 5 enters the first cryogenic crystallizer 41, the first brine inlet 47 is introduced into a cold source medium (-18 ℃ brine) in the fins of the first cryogenic crystallizer, the gaseous acetic acid is condensed on the first cryogenic crystallizer, and enters the fins of the second cryogenic crystallizer 41 through the solid state cooling medium, and enters the second cryogenic crystallizer 42 to be heated by the solid state cooling medium, and the solid acetic acid enters the second cryogenic crystallizer 42 after being circulated on the fins of the second cryogenic crystallizer 41; when the first valve 45 is closed, the second valve 46 is opened, the third valve 64 is opened, and the fourth valve 65 is closed, the gas mixed with gaseous acetic acid flowing out of the condensation cooler 5 enters the second cryogenic crystallizer 42, cold source medium (-18 ℃ of frozen saline water) is introduced into the fins of the second cryogenic crystallizer 42 through the second frozen saline water inlet 48, the gaseous acetic acid is condensed on the fins of the second cryogenic crystallizer 42, the nitrogen is heated by the heater 61 and enters the fins of the first cryogenic crystallizer 41 under the action of the circulating fan 63 to circulate, and the solid acetic acid on the fins of the first cryogenic crystallizer 41 is heated and liquefied; the first and second cryogenic crystallizers 41 and 42 can be condensed and liquefied alternately, the first and second cryogenic crystallizers 41 and 42 are communicated with the solvent recovery tank 43 through a pipeline, and the gaseous acetic acid can enter the solvent recovery tank 43 after being condensed and liquefied; the first and second cryogenic crystallizers 41 and 42 are further provided with a cryogenic crystallizer air outlet 40 for discharging the gas condensed by the cryogenic crystallizers.
To ensure system safety, the acetic acid continuous recovery system is also provided with a nitrogen vent 66 for venting nitrogen in emergency situations.
The frozen brine recovery tank 44 is communicated with the first cryogenic crystallizer 41, the second cryogenic crystallizer 42 and the condensation cooler 5, and frozen brine in the fins of the first cryogenic crystallizer 41 and the second cryogenic crystallizer 42 and the condensation cooler 5 can enter the frozen brine recovery tank 43, so that the frozen brine can be completely discharged before hot nitrogen is introduced into the fins of the first cryogenic crystallizer 41 or the second cryogenic crystallizer 42.
Preferably, the condensation cooler 5, the solvent recovery tank 43, the first cryocrystallizer 41 and the second cryocrystallizer 42 which are in direct contact with acetic acid are made of 316Ti stainless steel, so that the intergranular corrosion resistance of the semiconductor device can be improved, and the service life of the semiconductor device can be prolonged.
Example 2
The working method of the acetic acid continuous recovery system comprises the following steps:
A. the gas mixed with gaseous acetic acid discharged from the previous procedure enters the condensation cooler 5 through the gas inlet 50, is cooled by the primary water cooling liquefaction zone and the secondary chilled water liquefaction zone of the condensation cooler 5 in sequence, is respectively condensed and cooled by the room temperature water of the primary water cooling liquefaction zone and the chilled brine of the secondary chilled water liquefaction zone at the temperature of minus 5 ℃, the obtained liquid acetic acid enters the solvent recovery tank 43, and the temperature of the gas mixed with a small amount of gaseous acetic acid is reduced to about 13 ℃ when the gas mixed with the gaseous acetic acid is discharged from the condensation cooler 5.
B. When the first valve 45 is opened, the second valve 46 is closed, the third valve 64 is closed, and the fourth valve 65 is opened, the gas mixed with gaseous acetic acid flowing out of the condensation cooler 5 enters the first cryogenic crystallizer 41, cold source medium (-18 ℃ of frozen saline) is introduced into the fins of the first cryogenic crystallizer 41 through the first frozen saline inlet 47, nitrogen is heated by the heater 61 and enters the fins of the second cryogenic crystallizer 42 under the action of the circulating fan 63 for circulation, the first cryogenic crystallizer 41 is in a condensation state, and the second cryogenic crystallizer 42 is in a heated and melted state; the gaseous acetic acid condenses on the fins of the first cryogenically cooled crystallizer 41, the gas exits the first cryogenically cooled crystallizer 41 and the temperature drops to around 0 ℃.
C. After the first cryogenic crystallizer 41 is in a condensation crystallization state for a preset time, the first valve 45 is closed, the second valve 46 is opened, the third valve 64 is opened, the fourth valve 65 is closed, the gas mixed with gaseous acetic acid flowing out of the condensation cooler 5 enters the second cryogenic crystallizer 42, cold source medium (-18 ℃ frozen brine) is introduced into fins of the second cryogenic crystallizer 42 through a second frozen brine inlet 48, nitrogen enters the fins of the first cryogenic crystallizer 41 and circulates under the action of a circulating fan 63 after being heated by a heater 61, the first cryogenic crystallizer 41 is in a heated melting state, and solid acetic acid on the fins of the first cryogenic crystallizer 41 is melted and flows into a solvent recovery tank 43; the second cryogenically cooled crystallizer 42 is in a condensed state, gaseous acetic acid condenses on the fins of the second cryogenically cooled crystallizer 42, and the gas exits the second cryogenically cooled crystallizer 42 and falls to about 0 ℃.
D. The first and second cryogenic crystallizers 41 and 42 are alternately in a condensed and crystallized state and a heated and melted state, so that continuous recovery of acetic acid can be realized.
It is apparent that the above examples are merely illustrative of the present invention and are not limiting of the embodiments of the present invention. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. And obvious changes and modifications which come within the spirit of the invention are desired to be protected.
Claims (1)
1. The working method of the acetic acid continuous recovery system is characterized in that the acetic acid continuous recovery system comprises the following steps: the first cryogenic crystallizer, the second cryogenic crystallizer, the condensing cooler and the solvent recovery tank which can be alternately in a condensation state and a liquefaction state, wherein gas mixed with gaseous acetic acid enters the condensing cooler from an air inlet, the gas mixed with gaseous acetic acid is condensed by the condensing cooler, and the condensing cooler is communicated with the solvent recovery tank, so that liquid acetic acid obtained after the gaseous acetic acid is cooled enters the solvent recovery tank; fins are arranged in the first cryogenic crystallizer and the second cryogenic crystallizer, cold source media for condensation and heat source media for liquefaction can be introduced into the fins, air inlets of the first cryogenic crystallizer and the second cryogenic crystallizer are respectively communicated with an air outlet of the condensation cooler, a first valve is arranged between the first cryogenic crystallizer and the condensation cooler, and a second valve is arranged between the second cryogenic crystallizer and the condensation cooler;
a primary water-cooling liquefaction zone and a secondary chilled water liquefaction zone are sequentially arranged in the condensation cooler, the cooling medium of the primary water-cooling liquefaction zone is room temperature water, and the cooling medium of the secondary chilled water liquefaction zone is chilled brine at the temperature of minus 5 ℃; the air outlet of the condensing cooler is provided with a water baffle;
cold source mediums introduced into the first cryogenic crystallizer and the second cryogenic crystallizer are frozen brine at the temperature of minus 18 ℃, and heat source mediums introduced into the first cryogenic crystallizer and the second cryogenic crystallizer are hot nitrogen at the temperature of not lower than 120 ℃;
the acetic acid continuous recovery system also comprises a frozen brine recovery tank, wherein frozen brine in the fins of the first cryogenic crystallizer and the second cryogenic crystallizer can enter the frozen brine recovery tank;
the working method comprises the following steps:
A. the gas mixed with gaseous acetic acid obtained after solid-gas separation enters a condensation cooler through a bag-type dust collector, is sequentially cooled through a primary water-cooling liquefaction zone and a secondary chilled water liquefaction zone of the condensation cooler, is respectively condensed and cooled by room temperature water of the primary water-cooling liquefaction zone and chilled brine of the secondary chilled water liquefaction zone at the temperature of minus 5 ℃, and the obtained liquid acetic acid enters a solvent recovery tank, and the temperature of the gas mixed with a small amount of gaseous acetic acid is reduced to 13 ℃ when the gas is discharged from the condensation cooler;
B. the first valve is opened, the second valve is closed, meanwhile, freezing brine at the temperature of minus 18 ℃ is introduced into the fins of the first cryogenic crystallizer, at this time, the first cryogenic crystallizer is in a condensation crystallization state, gas discharged from the condensation cooler enters the first cryogenic crystallizer, a small amount of gaseous acetic acid in the gas is condensed and crystallized to adhere to the surfaces of the fins, the temperature of the gas is reduced to 0 ℃ and the gas is discharged out of the first cryogenic crystallizer;
C. after the first cryogenic crystallizer is in a condensation crystallization state for a preset time, the first valve is closed, the second valve is opened, meanwhile, freezing brine at the temperature of minus 18 ℃ is introduced into fins of the second cryogenic crystallizer, at the moment, the second cryogenic crystallizer is in the condensation crystallization state, gas discharged from the condensation cooler enters the second cryogenic crystallizer, a small amount of gaseous acetic acid in the gas is condensed and crystallized and is attached to the surfaces of the fins, the temperature of the gas is reduced to 0 ℃ and is discharged out of the second cryogenic crystallizer; the fins of the first cryogenic crystallizer are filled with hot nitrogen with the temperature not lower than 120 ℃, the first cryogenic crystallizer is in a heating and melting state, solid acetic acid attached to the surfaces of the fins is heated and melted, and the obtained liquid acetic acid enters a solvent recovery tank;
D. the first cryogenic crystallizer and the second cryogenic crystallizer are alternately in a condensation crystallization state and a heating melting state, so that continuous recovery of acetic acid can be realized.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810082773.7A CN108069852B (en) | 2018-01-29 | 2018-01-29 | Acetic acid continuous recovery system and working method thereof |
| CN202310753112.3A CN116574584A (en) | 2018-01-29 | 2018-01-29 | Efficient energy-saving acetic acid continuous recovery system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810082773.7A CN108069852B (en) | 2018-01-29 | 2018-01-29 | Acetic acid continuous recovery system and working method thereof |
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| CN202310753112.3A Division CN116574584A (en) | 2018-01-29 | 2018-01-29 | Efficient energy-saving acetic acid continuous recovery system |
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| CN108069852A CN108069852A (en) | 2018-05-25 |
| CN108069852B true CN108069852B (en) | 2023-07-18 |
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| CN202310753112.3A Pending CN116574584A (en) | 2018-01-29 | 2018-01-29 | Efficient energy-saving acetic acid continuous recovery system |
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| CN105209418A (en) * | 2013-05-13 | 2015-12-30 | 沙特基础工业公司 | Methods for preparing acetic acid via ethane oxidation |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105209418A (en) * | 2013-05-13 | 2015-12-30 | 沙特基础工业公司 | Methods for preparing acetic acid via ethane oxidation |
Non-Patent Citations (1)
| Title |
|---|
| 郑旭煦 等.《化工原理 下 第2版》.华中科技大学出版社,2016,第252页. * |
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| CN108069852A (en) | 2018-05-25 |
| CN116574584A (en) | 2023-08-11 |
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