CN212595615U - Reaction unit and system for synthesizing acetic acid by methanol carbonyl - Google Patents
Reaction unit and system for synthesizing acetic acid by methanol carbonyl Download PDFInfo
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- CN212595615U CN212595615U CN202020145192.6U CN202020145192U CN212595615U CN 212595615 U CN212595615 U CN 212595615U CN 202020145192 U CN202020145192 U CN 202020145192U CN 212595615 U CN212595615 U CN 212595615U
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Abstract
The utility model provides a reaction unit and system of methyl alcohol oxo synthesis acetic acid, this reaction unit include reation kettle and fluid mixing part, and the fluid mixing part includes reaction raw materials distributor and return material pipe, and reation kettle includes the inlet pipe, and reation kettle is equipped with feed inlet, return material export and return material import, and in reaction raw materials distributor located reation kettle, the inlet pipe ran through the feed inlet and was connected with reaction raw materials distributor, and the return material pipe runs through the return material import, the return material export is connected with the return material pipe. The reaction device of the utility model is adopted to produce the acetic acid by the methanol oxo synthesis, the phenomenon that the shaft seal and the bottom fixed bearing are easy to damage in the operation process during the mechanical stirring is avoided, no dynamic sealing point exists in the whole reaction device, and the safe and stable operation of the reaction system is ensured; and meanwhile, the reactor is matched with a reaction raw material distributor, so that the raw materials in the reactor are distributed more uniformly, the gas-liquid two-phase mixing effect is improved, the reaction rate is increased, and the reaction state in the system is optimized.
Description
Technical Field
The utility model belongs to the chemical industry field relates to a reaction unit and system of methyl alcohol oxo synthesis acetic acid.
Background
Acetic acid is an important chemical intermediate and solvent for chemical reactions. The most common acetic acid synthesis process used at present is the methanol low-pressure carbonyl synthesis process, which is initiated in the 70 s by Monsanto company in America, and has made a major breakthrough in device productivity, product quality and production cost after decades of innovation and development. In the aspect of process technology improvement, companies continuously seek new schemes, and it is described in patent CN 201525813 of hualu-changsheng chemical corporation that a methyl iodide circulating tower and an evaporator are arranged in front of a rectifying device to circulate methyl iodide in a reaction system, so that the amount of methyl iodide impurities mixed in acetic acid is reduced, and energy consumption required for purifying acetic acid is saved. The patent CN 101665424 of Beijing Zehua chemical engineering Limited company describes that the functions executed by the existing lightness-removing tower and the existing dehydrating tower are combined in a rectifying tower to be completed, thereby simplifying the flow route of the preparation of acetic acid, reducing the equipment investment of the device, simultaneously reducing the difficulty of operation control, effectively reducing the energy consumption of the device and lowering the production cost.
At present, the technical improvement is mostly on a rectification system, the change of a reaction system is less, particularly, a reaction kettle unit still adopts a conventional mechanical stirring mode on gas-liquid stirring and mixing, and reaction equipment adopting mechanical stirring can effectively mix liquid-liquid and gas-liquid, but a shaft seal and a bearing required by mechanical transmission are extremely easy to damage in long-term operation, so that the shutdown maintenance is caused, and the continuous, stable and safe operation is difficult to realize. In recent years, gas-liquid stirring is an important direction for improving the technology of a methanol oxo acetic acid device, but the problems of poor gas-liquid mixing compared with the traditional mechanical stirring reaction device, reduced production capacity and the like exist.
SUMMERY OF THE UTILITY MODEL
To the technical problem who exists among the above-mentioned prior art, the utility model aims at providing a reaction unit and system of methyl alcohol oxo synthesis acetic acid, this reaction unit include fluid stirring part, replace mechanical stirring bearing seal and bottom fixing bearing the fragile condition in the operation process, will move the sealed point and eliminate, greatly improve security and stability. Meanwhile, the reactor is matched with a reaction raw material distributor, so that the distribution of reaction raw materials such as CO gas in the reactor is more uniform, the gas-liquid two-phase mixing effect is improved, the reaction rate is increased, and the reaction state is optimized.
The utility model discloses a realize through following technical scheme:
the utility model discloses a first aspect provides a reaction unit, including reation kettle and fluid mixing part, the fluid mixing part includes reaction raw material distributor and return material pipe, reation kettle includes the inlet pipe, reation kettle is equipped with feed inlet, return material export and return material import, reaction raw material distributor locates in the reation kettle, the inlet pipe runs through the feed inlet and with reaction raw material distributor connects, the return material pipe runs through the return material import, the return material export with the return material pipe is connected.
Preferably, the reaction kettle is further provided with a reaction liquid outlet for outputting the reaction liquid.
Preferably, a nozzle is arranged at the end part of the material returning pipe arranged in the reaction kettle.
More preferably, the spray head is positioned in the middle in the reaction kettle.
More preferably, the spray head is of a reducing structure.
More preferably, the spray head is located below the liquid level of the reaction device, and the distance between the spray head and the return inlet is 1/5-1/2 of the height of the reaction kettle barrel, such as 1/5-1/3 or 1/3-1/2.
Preferably, the feed inlet is arranged at the bottom of the reaction kettle.
Preferably, the return material outlet is arranged in the middle of the reaction kettle.
Preferably, the return material inlet is arranged at the top of the reaction kettle.
Preferably, the fluid stirring part further comprises a pump part and/or a cooling unit, and the return outlet is connected with the return pipe through the pump part and/or the cooling unit.
More preferably, the pump assembly comprises one or more pumps in parallel.
Preferably, the reaction raw material distributor is provided with air holes, the diameter of each air hole is 2-10 mm, and the distance between the air holes is 20-40 mm.
Preferably, the reaction raw material distributor is arranged at the bottom of the reaction kettle.
Preferably, the reaction raw material distributor is provided with an annular first distribution unit and a plurality of second distribution units, and the plurality of second distribution unit annular arrays are arranged on the annular first distribution unit.
The utility model discloses the second aspect provides a system for methyl alcohol oxo synthesis acetic acid, including above-mentioned reaction unit, flash separator and the refined unit that communicates in proper order.
Preferably, the flash separator is provided with a gas phase outlet and a liquid phase outlet, the gas phase outlet is communicated with the refining unit, and the liquid phase outlet is communicated with the reaction device.
The utility model discloses reaction unit includes fluid mixing part and reaction raw materials distributor, is used for in methyl alcohol oxo synthesis acetic acid production, avoids the easy phenomenon of destroying in mechanical stirring bearing seal and bottom fixing bearing in the operation process, does not have the dynamic seal point in the whole reaction unit, eliminates mechanical stirring probably because of the machine seals the parking hidden danger that leaks and the cauldron stirring part is inefficacy because of corroding and needs to be changed, ensures reaction system safety and stability operation, and practices thrift investment, operation, maintenance cost's expenditure; meanwhile, the reaction kettle is matched with a reaction raw material distributor, the distribution of reaction raw materials such as CO gas and the like and circulating mother liquor is improved, particularly the gas-liquid mixing effect at the position close to the wall is improved, the gas-liquid phase in the reaction kettle is fully mixed, the reaction speed is improved, the reaction state in the system is optimized, and therefore the productivity is improved.
Drawings
FIG. 1 is a schematic view of the structure of the upper part of a reaction apparatus.
FIG. 2 is a schematic view of the structure of the bottom of the reaction apparatus.
FIG. 3 is a schematic diagram of a reaction material distributor.
FIG. 4 is a schematic view of the overall structure of the reaction apparatus.
FIG. 5 shows a system for synthesizing acetic acid by methanol carbonylation.
Reference numerals
1 reaction apparatus
11 reaction kettle
1111 feed pipe
1112 feed inlet
1122 return outlet
1123 return material inlet
12 fluid agitating member
121 reaction raw material distributor
1211 air vent
1212 annular first distribution unit
1213 second distribution unit
122 return pipe
1221 spray head
123 pump component
1231 pump
124 cooling unit
2 flash separator
21 gas phase outlet
22 liquid phase outlet
3 refining unit
Detailed Description
The technical solution of the present invention is explained below by specific examples. It is to be understood that one or more method steps mentioned in the present application do not exclude the presence of other method steps before or after said combination step or that other method steps may be inserted between these explicitly mentioned steps; it should also be understood that these examples are for illustrative purposes only and are not intended to limit the scope of the present invention. Moreover, unless otherwise indicated, the numbering of the various method steps is merely a convenient tool for identifying the various method steps, and is not intended to limit the order in which the method steps may be arranged or the scope of the invention which may be practiced.
A reaction device, as shown in fig. 1, fig. 2 and fig. 4, comprising a reaction vessel 11 and a fluid stirring component 12, wherein the fluid stirring component 12 includes a reaction raw material distributor 121 and a return pipe 122, the reaction vessel 11 includes a feeding pipe 1111, the reaction vessel 11 is provided with a feeding port 1112, a return outlet 1122 and a return inlet 1123, the reaction raw material distributor 121 is disposed in the reaction vessel 11, the feeding pipe 1111 penetrates through the feeding port 1112 and is connected to the reaction raw material distributor 121, the return pipe 122 penetrates through the return inlet 1123, and the return outlet 1122 is connected to the return pipe 122.
The reaction device of the utility model is adopted to produce the acetic acid by the methanol oxo synthesis, the phenomenon that the shaft seal and the bottom fixed bearing are easy to damage in the operation process during the mechanical stirring is avoided, no dynamic sealing point exists in the whole reaction device, and the safe and stable operation of the reaction system is ensured; and meanwhile, the reactor is matched with a reaction raw material distributor, so that the raw materials in the reactor are distributed more uniformly, the gas-liquid two-phase mixing effect is improved, the reaction rate is increased, and the reaction state in the system is optimized.
In a preferred embodiment, the reaction vessel 11 is further provided with a reaction liquid outlet for outputting the reaction liquid.
In a preferred embodiment, the nozzle 1221 is preferably located in the middle of the inside of the reaction vessel 11.
In a preferred embodiment, a spray nozzle 1221 is disposed at the end of the return pipe 122 disposed in the reaction vessel 11. The nozzle 1221 is preferably of a reducing structure, so that the injection speed of the circulating reaction liquid can be obviously increased, and the degree of gas-liquid mixing can be improved.
In a preferred implementation, the spray nozzle 1221 is positioned below the liquid level of the reaction device, and the distance between the spray nozzle 1221 and the return material inlet 1123 is 1/5-1/2 of the height of the reaction kettle barrel.
In a preferred embodiment, the flow rate of the reaction material exiting the reaction material distributor may be 5 to 25 m/s.
In a preferred embodiment, the flow rate of the fluid sprayed from the spray head may be 5 to 20 m/s.
In a preferred embodiment, the feed port 1112 is preferably disposed at the bottom of the reaction vessel 11.
In a preferred embodiment, the return outlet 1122 is provided in the middle of the reaction vessel 11.
In a preferred embodiment, the return feed inlet 1123 is located at the top of the reaction vessel 11. The reaction liquid flows down from a high position, so that higher speed can be provided, and better stirring effect can be generated.
In a preferred embodiment, the fluid stirring unit 12 further includes a pump unit 123 and/or a cooling unit 124, and the return outlet 1122 is connected to the return pipe 122 via the pump unit 123 and/or the cooling unit 124. The reaction liquid is transported to the next unit under the power of the pump component. The cooling unit is used for cooling the reaction liquid.
The reaction liquid in the reaction device flows out from a return outlet 1122, the return outlet 1122 is arranged in the middle of the reaction kettle 11, and can be conveyed to the cooling unit 124 for cooling under the power action of the pump part 123 and then conveyed to the return inlet 1123, the reaction liquid flows downwards at a high speed along the return pipe 122 and is sprayed out by the spray head 1221, the peripheral liquid is driven to change the vector, and the reaction liquid is turned over from the kettle bottom of the reaction device to form different circulating flow states of a plurality of main flow layers.
In a preferred implementation, the pump assembly 123 includes one or more pumps 1231 in parallel. For example, the pump components may be two pumps connected in parallel, as shown in fig. 5, which can satisfy the requirement of sufficient gas-liquid two-phase mixing in a large-volume reaction device. The flow rate of the fluid provided by the pump can be 300-700 m3H, e.g. 300 to 530m3H or 530 to 700m3/h。
In a preferred embodiment, the reaction material distributor 121 is provided with air holes 1211, the diameter of the air holes 1211 is 2 to 10mm, and the distance between the air holes is 20 to 40 mm. No dead angle is left in the plane area of the reaction device, the whole reaction device presents the ascending trend of operation, and the reaction raw materials in the space of the whole reaction device are uniformly distributed along with the coalescence and separation of bubbles. The flow rate of the reaction raw material out of the reaction raw material distributor may be 5 to 25 m/s.
In a preferred embodiment, the reactant material distributor 121 is disposed at the bottom of the reaction vessel 11.
In a preferred embodiment, as shown in fig. 3, the reactant material distributor 121 is provided with an annular first distribution unit 1212 and a plurality of second distribution units 1213, the plurality of second distribution units 1213 being arranged in an annular array on the annular first distribution unit 1212. The reaction raw material distributor is convenient for the distribution of the reaction raw materials on the whole cross section of the reaction device, is suitable for a large-diameter reactor, simultaneously ensures the uniform distribution of the reaction raw materials in the vertical direction, especially ensures the full reaction of the upper reaction liquid under the condition of weakened stirring of the fluid, and improves the gas-liquid two-phase mixing reaction effect.
A system for synthesizing acetic acid by methanol carbonylation, as shown in figure 5, comprises the reaction device 1, a flash separator 2 and a refining unit 3 which are communicated in sequence.
In a preferred embodiment, the flash separator 2 is provided with a gas phase outlet 21 and a liquid phase outlet 22, the gas phase outlet 21 being in communication with the refining unit 3 and the liquid phase outlet 22 being in communication with the reaction device 1.
Comparative example
The industrial equipment for synthesizing acetic acid by using methyl alcohol carbonyl adopts mechanical stirring device and ring-type pipe body CO distributor before the reactor is reformed, and on the distributor there is no straight pipe section, and the material-returning mouth is positioned above the liquid level and has no reducing diameter. Under certain temperature and pressure and in the presence of catalyst, methanol and CO produce carbonylation reaction to produce acetic acid.
Example 1
Methyl alcohol oxo acetic acid industrial installation, the reactor is reformed transform the back, adopts the utility model discloses the fluid stirring part shown in fig. 1 and fig. 2 and the reaction raw materials distributor shown in fig. 3 (the first distribution unit of annular and 5 second distribution units, on 5 second distribution unit annular arrays locate the first distribution unit of annular), shower nozzle 1221 is located reaction unit liquid level below, shower nozzle 1221 with the distance between the returning charge import 1123 is the 1/3 of reation kettle barrel height. Under the conditions of certain temperature and pressure and the existence of a catalyst, methanol and CO are subjected to carbonylation reaction to generate acetic acid, and the outlet flow of a material returning circulating pump is 300m3The productivity was increased by 10% compared to the comparative example (as shown in FIG. 5).
Example 2
Methyl alcohol oxo acetic acid industrial installation, the reactor is reformed transform the back, adopts the utility model discloses the fluid stirring part shown in fig. 1 and fig. 2 and the reaction raw materials distributor shown in fig. 3 (the first distribution unit of annular and 8 second distribution units, on 8 second distribution unit annular arrays locate the first distribution unit of annular), shower nozzle 1221 is located reaction unit liquid level below, shower nozzle 1221 with the distance between the returning charge import 1123 is the 1/2 of reation kettle barrel height. Under the conditions of certain temperature and pressure and the existence of a catalyst, methanol and CO are subjected to carbonylation reaction to generate acetic acid, and the outlet flow of a material returning circulating pump is 700m3The productivity is improved by 20 percent compared with the comparative example
Example 3
The industrial device for synthesizing acetic acid by methanol carbonyl is adopted after the reactor is reformedThe novel fluid stirring component shown in fig. 1 and fig. 2 and the reaction raw material distributor shown in fig. 3 (an annular first distribution unit and 4 second distribution units, wherein 4 second distribution unit annular arrays are arranged on the annular first distribution unit), the spray head 1221 is positioned below the liquid level of the reaction device, and the distance between the spray head 1221 and the return material inlet 1123 is 1/5 of the height of the reaction kettle barrel. Under the conditions of certain temperature and pressure and the existence of a catalyst, methanol and CO are subjected to carbonylation reaction to generate acetic acid, and the outlet flow of a material returning circulating pump is 530m3And h, the productivity is improved by 15 percent compared with that of the comparative example.
The foregoing is merely a preferred embodiment of the present invention, and is not intended to limit the present invention in any way and in any way, and it should be understood that modifications and additions may be made by those skilled in the art without departing from the method of the present invention, and such modifications and additions are also considered to be within the scope of the present invention. Those skilled in the art can make various changes, modifications and evolutions equivalent to those made by the above-disclosed technical content without departing from the spirit and scope of the present invention, and all such changes, modifications and evolutions are equivalent embodiments of the present invention; meanwhile, any changes, modifications and evolutions of equivalent changes to the above embodiments according to the actual technology of the present invention are also within the scope of the technical solution of the present invention.
Claims (11)
1. The utility model provides a reaction unit, characterized in that, includes reation kettle (11) and fluid mixing part (12), fluid mixing part (12) are including reaction raw material distributor (121) and returning charge pipe (122), reation kettle (11) include inlet pipe (1111), reation kettle (11) are equipped with feed inlet (1112), returning charge export (1122) and returning charge import (1123), reaction raw material distributor (121) are located in reation kettle (11), inlet pipe (1111) run through feed inlet (1112) and with reaction raw material distributor (121) are connected, returning charge pipe (122) run through returning charge import (1123), returning charge export (1122) with returning charge pipe (122) are connected.
2. The reactor device according to claim 1, characterized in that it further comprises at least one of the following technical features:
1) the reaction kettle (11) is also provided with a reaction liquid outlet for outputting reaction liquid;
2) a spray head (1221) is arranged at the end part of the return pipe (122) arranged in the reaction kettle (11);
3) the feed inlet (1112) is arranged at the bottom of the reaction kettle (11);
4) the return outlet (1122) is arranged in the middle of the reaction kettle (11);
5) the material returning inlet (1123) is arranged at the top of the reaction kettle (11);
6) the reaction raw material distributor (121) is arranged at the bottom of the reaction kettle (11).
3. The reactor apparatus as claimed in claim 2, wherein in feature 2), the shower head (1221) is located in the middle inside the reaction vessel (11).
4. The reactor apparatus of claim 2, wherein in feature 2), the nozzles (1221) are of a reduced diameter configuration.
5. The reaction device according to claim 2, characterized in that in the characteristic 2), the spray nozzle (1221) is positioned below the liquid level of the reaction device, and the distance between the spray nozzle (1221) and the return material inlet (1123) is 1/5-1/2 of the height of the reaction kettle barrel.
6. A reactor device as claimed in claim 1, wherein the fluid stirring means (12) further comprises a pump means (123) and/or a cooling unit (124), and the return outlet (1122) is connected to the return pipe (122) via the pump means (123) and/or the cooling unit (124).
7. A reactor device as claimed in claim 6, wherein the pump means (123) comprises one or more pumps (1231) connected in parallel.
8. The reaction apparatus according to claim 1, wherein the reaction material distributor (121) is provided with air holes (1211), the diameter of the air holes (1211) is 2 to 10mm, and the distance between the air holes is 20 to 40 mm.
9. The reaction apparatus according to claim 1, wherein the reaction raw material distributor (121) is provided with an annular first distribution unit (1212) and a plurality of second distribution units (1213), the plurality of second distribution units (1213) being arranged in an annular array on the annular first distribution unit (1212).
10. A system for methanol oxo-synthesis of acetic acid, characterized by comprising a reaction apparatus (1) according to any one of claims 1 to 9, a flash separator (2) and a refining unit (3) in sequential communication.
11. A system for methanol oxo-acetic acid according to claim 10, wherein the flash separator (2) is provided with a gas phase outlet (21) and a liquid phase outlet (22), the gas phase outlet (21) being in communication with the refining unit (3) and the liquid phase outlet (22) being in communication with the reaction apparatus (1).
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| CN202020145192.6U CN212595615U (en) | 2020-01-22 | 2020-01-22 | Reaction unit and system for synthesizing acetic acid by methanol carbonyl |
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| CN202020145192.6U CN212595615U (en) | 2020-01-22 | 2020-01-22 | Reaction unit and system for synthesizing acetic acid by methanol carbonyl |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022148162A1 (en) * | 2021-01-06 | 2022-07-14 | 上海华谊能源化工有限公司 | Reaction device, and system and method for synthesizing acetic acid from carbonyl |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2022148162A1 (en) * | 2021-01-06 | 2022-07-14 | 上海华谊能源化工有限公司 | Reaction device, and system and method for synthesizing acetic acid from carbonyl |
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Effective date of registration: 20220810 Address after: 200241 No. 4280, Wu Long Road, Shanghai, Minhang District Patentee after: SHANGHAI HUAYI ENERGY CHEMICAL CO.,LTD. Patentee after: Guangxi Huayi Energy Chemical Co.,Ltd. Address before: 200241 No. 4280, Wu Long Road, Shanghai, Minhang District Patentee before: SHANGHAI HUAYI ENERGY CHEMICAL CO.,LTD. |