CN213506667U - Enhanced reaction system for preparing acetic acid by methanol carbonylation - Google Patents
Enhanced reaction system for preparing acetic acid by methanol carbonylation Download PDFInfo
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- CN213506667U CN213506667U CN201921530090.XU CN201921530090U CN213506667U CN 213506667 U CN213506667 U CN 213506667U CN 201921530090 U CN201921530090 U CN 201921530090U CN 213506667 U CN213506667 U CN 213506667U
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 273
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 title claims abstract description 172
- 238000005810 carbonylation reaction Methods 0.000 title claims abstract description 82
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 71
- 230000006315 carbonylation Effects 0.000 title claims abstract description 31
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 76
- 229910002091 carbon monoxide Inorganic materials 0.000 claims abstract description 76
- 239000000047 product Substances 0.000 claims abstract description 17
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 14
- 230000008020 evaporation Effects 0.000 claims abstract description 12
- 238000001704 evaporation Methods 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims abstract description 6
- 239000007789 gas Substances 0.000 claims description 25
- 238000003860 storage Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 16
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 4
- 238000002360 preparation method Methods 0.000 abstract description 6
- 238000005728 strengthening Methods 0.000 abstract 1
- 229960000583 acetic acid Drugs 0.000 description 43
- 239000003054 catalyst Substances 0.000 description 16
- 238000004519 manufacturing process Methods 0.000 description 7
- 239000012071 phase Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 5
- 230000000052 comparative effect Effects 0.000 description 4
- 239000003795 chemical substances by application Substances 0.000 description 3
- 239000000796 flavoring agent Substances 0.000 description 3
- 235000013355 food flavoring agent Nutrition 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000012362 glacial acetic acid Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000000052 vinegar Substances 0.000 description 2
- 235000021419 vinegar Nutrition 0.000 description 2
- 239000004278 EU approved seasoning Substances 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 239000004599 antimicrobial Substances 0.000 description 1
- 239000007864 aqueous solution Substances 0.000 description 1
- 235000013351 cheese Nutrition 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000002740 effect on eyes Effects 0.000 description 1
- 235000011194 food seasoning agent Nutrition 0.000 description 1
- 230000007794 irritation Effects 0.000 description 1
- 235000015110 jellies Nutrition 0.000 description 1
- 239000008274 jelly Substances 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000002304 perfume Substances 0.000 description 1
- 238000005554 pickling Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000007711 solidification Methods 0.000 description 1
- 230000008023 solidification Effects 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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Abstract
The utility model provides an enhanced reaction system for preparing acetic acid by methanol carbonylation, which belongs to the technical field of acetic acid preparation, and comprises a feeding unit, a carbonylation reaction kettle, a micro-interface generator and a micro-interface generator, wherein the carbonylation reaction kettle is internally provided with the micro-interface generator, the micro-interface generator is connected with the feeding unit and is used as the place of the carbonylation reaction, and the micro-interface generator is used for crushing carbon monoxide bubbles into micro-bubbles with the diameter of micron level before the carbonylation reaction so as to increase the phase boundary mass transfer area between the carbon monoxide and the methanol in the carbonylation reaction process and enhance the efficiency of the carbonylation reaction; and the product treatment unit is connected with the reaction kettle and is used for carrying out flash evaporation and rectification treatment on the carbonylation reaction product to obtain the acetic acid. The utility model provides a strengthening reaction system of methyl alcohol carbonylation preparation acetic acid has reached and has solved among the prior art carbon monoxide and methyl alcohol and can't obtain the intensive mixing inside the carbonylation reation kettle, leads to the problem that system's reaction efficiency reduces.
Description
Technical Field
The utility model relates to a technical field of acetic acid preparation, in particular to an enhanced reaction system for preparing acetic acid by methanol carbonylation.
Background
Acetic acid, also called acetic acid or glacial acetic acid, is an organic monobasic acid, which is the main component of vinegar. Pure anhydrous acetic acid (glacial acetic acid) is colorless hygroscopic solid, is colorless crystals after solidification, is weakly acidic and strongly erodible in aqueous solution, and has irritation effect on eyes and nose due to steam.
Acetic acid is used as an acidity regulator, an acidulant, a pickling agent, a flavoring agent, a perfume, etc. It is also a good antimicrobial agent, mainly due to its ability to lower the pH below that required for optimal growth of microorganisms. Acetic acid is the most early and most used sour agent in China, and is mainly used for compound seasonings, wax preparation, cans, cheese, jelly and the like. When the flavoring agent is used for flavoring, acetic acid can be diluted to 4% -5% solution by adding water, and then the solution is added into various flavoring agents for application. The international third generation drink is made up by using vinegar as souring agent and adding pure natural nutrient health-care product. In the existing technology for preparing acetic acid, methanol liquid and carbon monoxide gas are directly introduced into a carbonylation reaction kettle, carbonylation reaction is carried out under the action of a catalyst at a specified temperature and pressure, and then a reaction product is distilled and separated to finally obtain the acetic acid.
However, when acetic acid is produced using the existing carbonylation reaction system, the methanol liquid and the carbon monoxide gas are directly introduced into the carbonylation reaction kettle, and the methanol liquid and the carbon monoxide gas are not sufficiently mixed inside the carbonylation reaction kettle, thereby reducing the reaction efficiency of the system.
Disclosure of Invention
In view of this, the utility model provides an intensive reaction system of methyl alcohol carbonylation preparation acetic acid to reach and solve among the prior art carbon monoxide and methyl alcohol and can't obtain intensive mixing in the carbonylation reation kettle is inside, lead to the problem that system reaction efficiency reduces.
The above technical purpose of the present invention can be achieved by the following technical solutions:
an enhanced reaction system for preparing acetic acid by methanol carbonylation comprises a feeding unit, a reaction unit and a control unit, wherein the feeding unit is used for storing and conveying carbon monoxide and methanol;
the micro-interface generator is used for crushing carbon monoxide bubbles into micro-bubbles with the diameter of micron level before the carbonylation reaction so as to increase the mass transfer area of the phase boundary between the carbon monoxide and the methanol in the carbonylation reaction process and enhance the carbonylation reaction efficiency;
and the product treatment unit is connected with the reaction kettle and is used for carrying out flash evaporation and rectification treatment on the carbonylation reaction product to obtain the acetic acid.
Further, in the above-mentioned enhanced reaction system for preparing acetic acid by carbonylation of methanol, the micro-interface generator converts the pressure energy of the gas and/or the kinetic energy of the liquid into the surface energy of the bubbles and transmits the surface energy to the hydrogen bubbles, so that the hydrogen is broken into micro-bubbles with a diameter of micron level.
Further, in the enhanced reaction system for preparing acetic acid by carbonylation of methanol, the micro-interface generator is selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator.
Furthermore, in the enhanced reaction system for preparing acetic acid by methanol carbonylation, the micro-bubbles with the micron scale are micro-bubbles with the diameter of more than or equal to 1 μm and less than 1 mm.
Further, in the above enhanced reaction system for preparing acetic acid by carbonylation of methanol, the feeding unit comprises:
the carbon monoxide feeding pipeline is connected with the micro-interface generator and is externally connected with a gas source and used for receiving carbon monoxide gas and conveying the carbon monoxide gas to the micro-interface generator;
and the methanol storage tank is connected with the reaction kettle and is used for storing methanol and conveying the methanol to the reaction kettle.
Further, in the above-mentioned enhanced reaction system for preparing acetic acid by methanol carbonylation, a first circulation pump is arranged between the methanol storage tank and the reaction kettle, and is used for conveying the methanol in the methanol storage tank to the reaction kettle.
Further, in the above enhanced reaction system for preparing acetic acid by carbonylation of methanol, the product processing unit comprises:
the flash tower is connected with the reaction kettle and is used for carrying out flash evaporation on the carbonylation reaction product;
and the rectifying device is connected with the flash tower and is used for rectifying the flash product.
Further, in the above-mentioned enhanced reaction system for preparing acetic acid by carbonylation of methanol, the rectification apparatus comprises:
the light component rectifying tower is connected with the flash tower and is used for rectifying and separating gas-phase components obtained by flash evaporation products;
and the heavy component rectifying tower is connected with the light component rectifying tower and is used for rectifying and separating the heavy component product separated from the light component rectifying tower to finally obtain the acetic acid.
To sum up, the beneficial effects of the utility model reside in that, the utility model provides a methanol carbonylation preparation acetic acid's intensive reaction system, the reation kettle among the prior art is replaced through the inside carbonylation reation kettle who is provided with micro interface generator for choose for use, make before carbon monoxide and methyl alcohol carry out the carbonylation reaction, micro interface generator breaks into the diameter with carbon monoxide and is more than or equal to 1 mu m, be less than 1 mm's microbubble, make carbon monoxide contact with the state and the methyl alcohol of microbubble, with the phase boundary mass transfer area between carbon monoxide and the methyl alcohol in the increase carbonylation reaction process, and carry out the carbonylation reaction again in the intensive mixing, thereby carbon monoxide and methyl alcohol can't obtain the intensive mixing in carbonylation reation kettle inside among the solution prior art, lead to the problem that system reaction efficiency reduces.
Especially, be provided with first circulating pump between methyl alcohol storage jar and the reation kettle during the system operation, first circulating pump can provide power for the transportation of methyl alcohol, makes methyl alcohol can carry to reation kettle with appointed speed, has improved the operating efficiency of system.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
fig. 1 is a schematic structural diagram of an enhanced reaction system for preparing acetic acid by methanol carbonylation according to an embodiment of the present invention.
Detailed Description
In order to make the objects and advantages of the present invention more apparent, the present invention will be further described with reference to the following embodiments; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meaning of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1, an enhanced reaction system for preparing acetic acid by methanol carbonylation according to an embodiment of the present invention includes: and a micro-interface generator 2 is arranged below the inside of the carbonylation reaction kettle 3, the inlet end of the micro-interface generator is connected with the feeding unit, and the outlet end of the micro-interface generator is connected with the product processing unit and used as a place for carbonylation reaction.
Preferably, the micro-interface generator converts pressure energy of gas and/or kinetic energy of liquid into surface energy of bubbles and transmits the surface energy to the bubbles, so that the bubbles are broken into micro-bubbles with the diameter of more than or equal to 1 mu m and less than 1mm, and the micro-bubbles are divided into a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator according to an energy input mode or a gas-liquid ratio, wherein the pneumatic micro-interface generator is driven by gas, and the input gas amount is far greater than the liquid amount; the hydraulic micro-interface generator is driven by liquid, and the input air quantity is generally smaller than the liquid quantity; the gas-liquid linkage type micro-interface generator is driven by gas and liquid at the same time, and the input gas amount is close to the liquid amount. The micro-interface generator 2 is a pneumatic micro-interface generator.
Referring to fig. 1, the feed unit includes: the carbon monoxide feeding pipeline 11 is in a slender round pipe shape, one end of the carbon monoxide feeding pipeline is externally connected with an air source, and the other end of the carbon monoxide feeding pipeline is connected with the micro-interface generator 2 and is used for receiving carbon monoxide and conveying the carbon monoxide to the micro-interface generator 2; methyl alcohol storage jar 12 is short thick round tank form, its with reation kettle 3 connects for save methyl alcohol, be provided with between methyl alcohol storage jar 12 and reation kettle 3, be used for carrying the inside methyl alcohol of methyl alcohol storage jar 12 to reation kettle 3 inside first circulating pump 13. When the system is used, methanol and corresponding catalysts are filled into a methanol storage tank 12, a carbon monoxide feeding pipeline 11 is connected with a gas source of carbon monoxide, the system is started, a first circulating pump 13 conveys the methanol and the catalysts to the inside of a reaction kettle 3, meanwhile, the carbon monoxide is conveyed to the inside of a micro-interface generator 2 through the carbon monoxide feeding pipeline 11, the micro-interface generator 2 breaks the carbon monoxide into micro bubbles with a micron scale and releases the micro bubbles to the inside of the reaction kettle 3, so that the phase boundary mass transfer area between the carbon monoxide and the methanol in a carbonylation reaction process is increased, the carbon monoxide is fully contacted with the methanol in a micro bubble state, the carbonylation reaction is carried out, waste gas generated in the carbonylation reaction is discharged from the top end of the reaction kettle 3, and a carbonylation reaction product is conveyed to a product processing unit.
Referring to fig. 1, the product processing unit includes: and the inlet end of the flash tower 4 is connected with the reaction kettle 3, the outlet end of the flash tower is connected with one end of a second circulating pump 6, the other end of the second circulating pump 6 is connected with the inlet end of a heat exchanger 7, and the outlet end of the heat exchanger 7 is connected with the reaction kettle 3. After the carbonylation reaction in the reaction kettle 3 is completed, the reaction kettle 3 conveys the carbonylation reaction product to the flash evaporation tower 4 for flash evaporation, and the liquid phase component containing the catalyst obtained by flash evaporation is conveyed to the heat exchanger 7 from the bottom of the flash evaporation tower 4 through the second circulating pump 6 for heat exchange and temperature reduction so as to remove reaction heat. The liquid phase component with the temperature reduced after heat exchange by the heat exchanger 7 flows back to the reaction kettle 3 to help control the constant of the carbonylation reaction temperature in the reaction kettle 3; and the rectifying device is connected with the flash tower 4 and is used for rectifying the flash product to finally obtain the acetic acid.
The rectifying device comprises: a light component rectifying tower 51, the inlet end of which is connected with the flash tower 4 and is used for rectifying the gas phase component obtained by flash evaporation; and the inlet end of the heavy component rectifying tower 52 is connected with the outlet end of the light component rectifying tower 51 and is used for rectifying the heavy component product separated by the light component rectifying tower 51. And the gas phase component obtained by flashing is sent into a light component rectifying tower 51 from the top of the flash tower 4 for rectification and separation, so that a light component and a heavy component are obtained by separation, the light component is discharged out of the system from the top of the light component rectifying tower 51, the heavy component is discharged out of the bottom of the light component rectifying tower 51 and enters a heavy component rectifying tower 52, and the acetic acid is obtained by rectification and separation in the heavy component rectifying tower 52.
The utility model provides an intensive carbonylation reaction system, through at 3 inside micro-interface generator 2 that link to each other with carbon monoxide charge-in pipeline that sets up of carbonylation reation kettle, make before carbon monoxide carries out the carbonylation reaction with methyl alcohol, micro-interface generator 2 breaks into the microbubble with carbon monoxide, make carbon monoxide contact with the state and the methyl alcohol of microbubble, with the phase boundary mass transfer area between carbon monoxide and the methyl alcohol in the increase carbonylation reaction process, and carry out the carbonylation reaction again of intensive mixing, thereby carbon monoxide and methyl alcohol can't obtain intensive mixing in carbonylation reation kettle 3 inside among the solution prior art, lead to the problem that system reaction efficiency reduces.
In order to further verify the processing method provided by the present invention, the beneficial effects of the present invention will be further explained by combining the examples and the comparative examples.
Example 1
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 170 ℃ and the pressure to be 2MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously conveying the carbon monoxide into a micro-interface generator 2 through the carbon monoxide feeding pipeline 11;
And (3) conveying the carbonylation reaction product to a flash tower 4, a light component rectifying tower 51 and a heavy component rectifying tower 52 in sequence, and finally obtaining acetic acid at the outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 89%.
Example 2
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 175 ℃ and the pressure to be 3MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously conveying the carbon monoxide into a micro-interface generator 2 through the carbon monoxide feeding pipeline 11;
And (3) conveying the carbonylation reaction product to a flash tower 4, a light component rectifying tower 51 and a heavy component rectifying tower 52 in sequence, and finally obtaining acetic acid at the outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 92%.
Example 3
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 180 ℃ and the pressure to be 4MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously conveying the carbon monoxide into a micro-interface generator 2 through the carbon monoxide feeding pipeline 11;
And (3) conveying the carbonylation reaction product to a flash tower 4, a light component rectifying tower 51 and a heavy component rectifying tower 52 in sequence, and finally obtaining acetic acid at the outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 95%.
Comparative example 1
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 170 ℃ and the pressure to be 2MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously introducing the carbon monoxide into the reaction kettle 3 to carry out carbonylation reaction;
and (3) sequentially conveying the carbonylation reaction product to a flash tower 4 and a rectifying device, and finally obtaining acetic acid at an outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 79%.
Comparative example 2
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 175 ℃ and the pressure to be 3MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously introducing the carbon monoxide into the reaction kettle 3 to carry out carbonylation reaction;
and (3) sequentially conveying the carbonylation reaction product to a flash tower 4 and a rectifying device, and finally obtaining acetic acid at the outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 83%.
Comparative example 3
Filling sufficient methanol and a catalyst in a corresponding proportion into a methanol storage tank 12, connecting a carbon monoxide feeding pipeline 11 with a gas source containing 200L of carbon monoxide, starting a system, setting the temperature of the system to be 180 ℃ and the pressure to be 4MPa, conveying the methanol and the catalyst into a reaction kettle 3, and simultaneously introducing the carbon monoxide into the reaction kettle 3 to carry out carbonylation reaction;
and (3) sequentially conveying the carbonylation reaction product to a flash tower 4 and a rectifying device, and finally obtaining acetic acid at the outlet of the heavy component rectifying tower 52. The acetic acid production was monitored and the carbon monoxide conversion was calculated to be 86%.
In view of this, the enhanced reaction system and process for preparing acetic acid by methanol carbonylation provided by the invention solve the problem that in the prior art, carbon monoxide and methanol cannot be fully mixed in the carbonylation reaction kettle 3, so that the reaction efficiency of the system is reduced.
The above-mentioned embodiments are merely illustrative and not restrictive, and those skilled in the art can modify the embodiments without inventive contribution as required after reading this specification, but only fall within the scope of the claims of the present invention.
Claims (8)
1. An enhanced reaction system for preparing acetic acid by carbonylation of methanol, comprising:
a feed unit to store and transport carbon monoxide and methanol;
the micro-interface generator is used for crushing carbon monoxide bubbles into micro-bubbles with the diameter of micron level before the carbonylation reaction so as to increase the mass transfer area of the phase boundary between the carbon monoxide and the methanol in the carbonylation reaction process and enhance the carbonylation reaction efficiency;
and the product treatment unit is connected with the reaction kettle and is used for carrying out flash evaporation and rectification treatment on the carbonylation reaction product to obtain the acetic acid.
2. The enhanced reaction system for preparing acetic acid by carbonylation of methanol according to claim 1, wherein the micro-interface generator breaks the hydrogen gas into micro-bubbles having a diameter of micrometer scale by converting pressure energy of the gas and/or kinetic energy of the liquid into surface energy of the bubbles and transferring the surface energy to the hydrogen gas bubbles.
3. The enhanced reaction system for preparing acetic acid by carbonylation of methanol according to claim 1, wherein the micro-interface generator is selected from one or more of a pneumatic micro-interface generator, a hydraulic micro-interface generator and a gas-liquid linkage micro-interface generator.
4. The enhanced reaction system for preparing acetic acid by carbonylation of methanol according to claim 1, wherein the micro-bubbles of micron scale are micro-bubbles with a diameter of 1 μm or more and less than 1 mm.
5. The enhanced reaction system for the carbonylation of methanol to produce acetic acid as recited in claim 1 wherein said feed unit comprises:
the carbon monoxide feeding pipeline is connected with the micro-interface generator and is externally connected with a gas source and used for receiving carbon monoxide gas and conveying the carbon monoxide gas to the micro-interface generator;
and the methanol storage tank is connected with the reaction kettle and is used for storing methanol and conveying the methanol to the reaction kettle.
6. The enhanced reaction system for preparing acetic acid by carbonylating methanol as claimed in claim 5, wherein a first circulation pump is disposed between the methanol storage tank and the reaction kettle for transferring the methanol in the methanol storage tank to the reaction kettle.
7. The enhanced reaction system for the carbonylation of methanol to produce acetic acid as recited in claim 1 wherein said product handling unit comprises:
the flash tower is connected with the reaction kettle and is used for carrying out flash evaporation on the carbonylation reaction product;
and the rectifying device is connected with the flash tower and is used for rectifying the flash product.
8. The enhanced reaction system for the carbonylation of methanol to produce acetic acid as recited in claim 7 wherein said rectification means comprises:
the light component rectifying tower is connected with the flash tower and is used for rectifying and separating gas-phase components obtained by flash evaporation products;
and the heavy component rectifying tower is connected with the light component rectifying tower and is used for rectifying and separating the heavy component product separated from the light component rectifying tower to finally obtain the acetic acid.
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