CN111111566A - Packed tower reactor for producing cyclic carbonate and production method - Google Patents
Packed tower reactor for producing cyclic carbonate and production method Download PDFInfo
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- CN111111566A CN111111566A CN201911382267.0A CN201911382267A CN111111566A CN 111111566 A CN111111566 A CN 111111566A CN 201911382267 A CN201911382267 A CN 201911382267A CN 111111566 A CN111111566 A CN 111111566A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/04—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D317/00—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms
- C07D317/08—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3
- C07D317/10—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings
- C07D317/32—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D317/34—Oxygen atoms
- C07D317/36—Alkylene carbonates; Substituted alkylene carbonates
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
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Abstract
The invention provides a filler tower reactor for producing cyclic carbonate and a production method thereof, wherein the filler tower reactor comprises a plurality of reaction tower sections, a carbon dioxide inlet, an alkylene oxide inlet, a catalyst inlet and at least one discharge hole, wherein the reaction tower sections are sequentially connected from bottom to top; the carbon dioxide inlet, the alkylene oxide inlet and the catalyst inlet are respectively arranged on the reaction tower section at the lowest part; at least one discharge port is arranged on the side wall of the reaction tower section; each reaction tower section is provided with a group of regular packing and a heat exchanger, and the heat exchanger is arranged above the regular packing. By adopting a plurality of reaction tower sections to be connected in series and utilizing the combination and alternate installation of a plurality of groups of regular packing and heat exchangers, the mass transfer efficiency and the heat exchange efficiency are fully improved, and the method has the advantages of uniform gas-liquid distribution, quick reaction heat removal and the like, and has good industrial application prospect.
Description
Technical Field
The disclosure relates to the field of chemical industry, in particular to a filler tower reactor for producing cyclic carbonate and a production method thereof.
Background
Cyclic carbonates are generally prepared by cycloaddition of carbon dioxide with alkylene oxides, and are one of the few ways to fix carbon dioxide for commercial use today. Taking the ethylene carbonate as an example, the ethylene carbonate is an excellent solvent for high polymers such as polyamide, polyacrylonitrile and the like, and can also be used as a concrete additive, a decarbonizer, a plastic foaming agent, and an intermediate for medicines, pesticides and organic synthesis. Because of its high dielectric constant, it can be used as electrolyte of lithium battery by compounding with dimethyl carbonate, ethyl methyl carbonate and diethyl carbonate.
At present, the domestic industrial production of ethylene carbonate basically adopts a single-kettle type batch reaction device and a continuous double-tower series reactor. The single-kettle intermittent reaction device is characterized in that part of products are added into a kettle, a catalyst is dissolved in the products, ethylene oxide and carbon dioxide are introduced, the reaction is maintained under stirring to control the conversion rate of the ethylene oxide, and the materials are discharged after flash evaporation. The reactor needs to adopt an external circulation heat exchange mode to cool a reaction system, so that reaction heat is not removed timely, the reaction speed is influenced, and certain potential safety hazards are caused. And the production efficiency of the reactor is low due to insufficient gas-liquid mixing.
The double-tower tandem reactor is generally characterized in that raw materials and a catalyst are added from the upper part of a first reactor, carbon dioxide is added from the middle lower part, the two raw materials are in reverse phase contact reaction, the bottom of the first reactor contains unreacted ethylene oxide and products which enter a second reactor to continue reaction, because the reaction is a strong exothermic reaction, in order to remove reaction heat, the bottom of the first reactor needs to be shunted, one part of the ethylene oxide and the products enter the second reactor to continue reaction, the conversion rate is improved by continuing reaction, and the other part of the ethylene oxide and the products are moved out of the reactors to perform external heat exchange and then return to the top of the first reactor to maintain the reaction temperature. The reactor needs to adopt an external circulation heat exchange mode to cool a reaction system, can cause reaction heat to move out untimely, influence reaction speed, and also can cause certain potential safety hazard, and the reactor can also produce the problem of insufficient gas-liquid mixing, thereby causing low production efficiency.
At present, there are reports of the prior art that improve systems and methods for producing ethylene (propylene) carbonate, for example, chinese patent application CN103980246A discloses a method for producing propylene (ethylene) carbonate by tubular reaction of carbon dioxide and propylene (ethylene) oxide, CN108484565A discloses a system for producing carbonic ester and a method for producing carbonic ester by using the same, CN106478583A discloses a synthesis method for directly producing ethylene carbonate from ethylene oxide and carbon dioxide, but these production systems and methods either have the problems of long reaction residence time and increased energy consumption due to poor gas-liquid contact; or poor mass transfer effect, which results in poor reaction effect.
Therefore, there is a need for a new apparatus and method for producing cyclic carbonates that solves the problems of the prior art.
It is noted that the information disclosed in the foregoing background section is only for enhancement of background understanding of the invention and therefore it may contain information that does not constitute prior art that is already known to a person of ordinary skill in the art.
Disclosure of Invention
The present disclosure is directed to overcoming at least one of the above-mentioned drawbacks of the prior art, and providing a packed tower reactor for producing cyclic carbonates and a production method thereof, so as to solve the problems of untimely removal of reaction heat, reaction speed influence, potential safety hazard, insufficient gas-liquid mixing, low production efficiency, etc. in the existing production system.
In order to achieve the purpose, the following technical scheme is adopted in the disclosure:
the present disclosure provides a packed column reactor for producing cyclic carbonates, comprising: the device comprises a plurality of reaction tower sections, a carbon dioxide inlet, an alkylene oxide inlet, a catalyst inlet and at least one discharge hole, wherein the plurality of reaction tower sections are sequentially connected from bottom to top; the carbon dioxide inlet, the alkylene oxide inlet and the catalyst inlet are respectively arranged on the reaction tower section at the lowest part; at least one discharge port is arranged on the side wall of the reaction tower section; each reaction tower section is provided with a group of regular packing and a heat exchanger, and the heat exchanger is arranged above the regular packing.
According to one embodiment of the present disclosure, the bottom of the lowermost reaction tower section is provided with a gas distributor and a liquid distributor, the liquid distributor is arranged above the gas distributor, and the structured packing is arranged above the liquid distributor.
According to one embodiment of the present disclosure, a gas distributor is provided at the bottom of each reaction tower section.
According to one embodiment of the present disclosure, the structured packing is selected from one or more of wire mesh corrugated packing, metal mesh corrugated packing, and metal orifice plate corrugated packing.
According to an embodiment of the present disclosure, the catalyst system further comprises a circulation pipeline, wherein one end of the circulation pipeline is connected to the at least one discharge hole, and the other end of the circulation pipeline is connected to the catalyst inlet.
According to one embodiment of the disclosure, each reaction tower section has a height of 100 mm-1200 mm, a diameter of 300 mm-3000 mm, the number of the reaction tower sections is 8-10, and the uppermost reaction tower section is provided with a discharge hole.
According to one embodiment of the disclosure, the number of the discharge ports is 1-3, and the discharge ports are sequentially and respectively arranged on the corresponding reaction tower sections from top to bottom.
According to one embodiment of the present disclosure, the heat exchanger is a heat conducting water coil heat exchanger.
The invention provides a method for producing cyclic carbonate, which adopts the packing tower reactor and comprises the following steps: introducing carbon dioxide, alkylene oxide and a catalyst into the reaction tower section at the lowest part through a carbon dioxide inlet, an alkylene oxide inlet and a catalyst inlet respectively; the alkylene oxide sequentially passes through the regular packing and the heat exchangers of a plurality of reaction tower sections from bottom to top, contacts and reacts with carbon dioxide under the action of a catalyst to obtain cyclic carbonate, and the reacted material is discharged through a discharge hole.
According to one embodiment of the present disclosure, the reacted material enters the reaction tower section through the catalyst inlet via the circulating pipeline to perform a circulating reaction.
According to the technical scheme, the beneficial effects of the disclosure are as follows:
according to the packing tower reactor for producing cyclic carbonate and the production method thereof, a plurality of reaction tower sections are connected in series, and a plurality of groups of regular packing and heat exchangers are combined and alternately installed, so that the mass transfer efficiency and the heat exchange efficiency are fully improved, the packing tower reactor has the advantages of uniform gas-liquid distribution, quick reaction heat removal and the like, and has a good industrial application prospect.
Drawings
In order that the embodiments of the disclosure may be more readily understood, a more particular description of the disclosure will be rendered by reference to the appended drawings. It should be noted that, in accordance with industry standard practice, various components are not necessarily drawn to scale and are provided for illustrative purposes only. In fact, the dimensions of the various elements may be arbitrarily expanded or reduced for clarity of discussion.
FIG. 1 is a schematic diagram of the structure of a packed column reactor for producing cyclic carbonates according to one embodiment of the present disclosure.
Wherein the reference numerals are as follows:
S1...Sn-1、Sn: reaction tower section
100: carbon dioxide inlet
102: gas distributor
200: alkylene oxide inlet
202: liquid distributor
300: catalyst inlet
400: discharge port
500: structured packing
600: heat exchanger
I: circulation pipeline
Detailed Description
Exemplary embodiments that embody features and advantages of the present disclosure are described in detail below in the specification. It is to be understood that the disclosure is capable of various modifications in various embodiments without departing from the scope of the disclosure, and that the description and drawings are to be regarded as illustrative in nature, and not as restrictive.
In the following description of various exemplary embodiments of the disclosure, reference is made to the accompanying drawings, which form a part hereof, and in which are shown by way of illustration various exemplary structures, systems, and steps in which aspects of the disclosure may be practiced. It is to be understood that other specific arrangements of parts, structures, example devices, systems, and steps may be utilized, and structural and functional modifications may be made without departing from the scope of the present disclosure. Moreover, although the terms "over," "between," "within," and the like may be used in this specification to describe various example features and elements of the disclosure, these terms are used herein for convenience only, e.g., in accordance with the orientation of the examples described in the figures. Nothing in this specification should be construed as requiring a specific three dimensional orientation of structures in order to fall within the scope of this disclosure.
Referring to fig. 1, a schematic diagram of the structure of a packed column reactor for producing cyclic carbonates according to an exemplary embodiment of the present disclosure is representatively illustrated. The packed tower reactor proposed in this disclosure is illustrated as applied to the production of cyclic carbonates. It will be readily appreciated by those skilled in the art that various modifications, additions, substitutions, deletions, or other changes may be made to the embodiments described below in order to adapt the design disclosed herein to the production of other chemical products, and still be within the scope of the principles of the packed column reactor for producing cyclic carbonates as set forth in the present disclosure.
As shown in FIG. 1, in the present embodiment, the packed column reactor proposed by the present disclosure mainly comprises a plurality of reaction tower sections (S)1...Sn-1、Sn) A carbon dioxide inlet 100, an alkylene oxide inlet 200, a catalyst inlet 300, and at least one outlet 400. It should be noted that fig. 1 shows only a schematic view of a main structural part of the cyclic carbonate production system, and does not show the entire structure. The production of the ring carbon proposed in the present disclosure will now be described with reference to the above-mentioned drawingsThe structure, connection and functional relationship of each main component of an exemplary embodiment of the packed column reactor for acid esters are explained in detail.
As shown in FIG. 1, in the present embodiment, the packed column reactor for producing cyclic carbonates mainly comprises a plurality of reaction tower sections (S)1...Sn-1、Sn) A carbon dioxide inlet 100, an alkylene oxide inlet 200, a catalyst inlet 300, and at least one outlet 400. In particular, the plurality of reaction tower sections (S)1...Sn-1、Sn) The reaction tower sections are sequentially connected from bottom to top, the height of each reaction tower section is 100-1200 mm, the diameter of each reaction tower section is 300-3000 mm, and the number of the reaction tower sections can be set to be 8-10. Each reaction tower section is provided with a group of structured packing 500 and a heat exchanger 600, and the heat exchanger 600 is arranged above the structured packing 500. Alternatively, the heat exchanger 600 may be a thermally conductive water coil heat exchanger or the like. The structured packing is selected from one or more of wire mesh corrugated packing, metal mesh corrugated packing and metal orifice plate corrugated packing.
According to the present disclosure, as mentioned above, the existing apparatus for producing cyclic carbonates has problems of untimely removal of reaction heat, affecting reaction speed and having potential safety hazard; or insufficient gas-liquid mixing, resulting in low production efficiency. The method adopts a mode of connecting a plurality of reaction tower sections in series, and can increase the contact area of the alkylene oxide and the carbon dioxide by adding the regular packing, thereby fully improving the gas-liquid reaction efficiency. Furthermore, the heat exchanger is arranged between every two layers of structured packing, so that the heat generated by the reaction can be discharged in time, and the heat can be removed in time. Compared with random packing, the structured packing adopted by the method can ensure that the packing tower reactor is provided with a relatively larger pipe diameter so as to meet the requirement of large-scale production.
At the lowermost reaction tower section S1A carbon dioxide inlet 100, an alkylene oxide inlet 200 and a catalyst inlet 300 are provided. Carbon dioxide inlet 100 is for carbon dioxide (CO)2) The gas, alkylene oxide inlet 200 is for the introduction of alkylene oxide liquid, typically the alkylene oxide may be selected from ethylene oxide or propylene oxide, and correspondingly the cyclic carbonate produced may beAs ethylene carbonate or propylene carbonate. Catalyst inlet 300 is for the introduction of catalyst. Alternatively, the catalyst may be generally an ionic liquid, potassium iodide, crown ether, or the like, but the present invention is not limited thereto.
The lowest reaction tower section S1Is also provided with a gas distributor 102 and a liquid distributor 202, the liquid distributor 202 being arranged above the gas distributor 102 and the structured packing 500 being arranged above the liquid distributor 202. The alkylene oxide and the catalyst enter the reaction tower section S through corresponding inlets1And then, uniform feeding is realized through the liquid distributor, and the mass transfer efficiency is improved. Simultaneously, carbon dioxide gas enters the reaction tower section S through the carbon dioxide inlet 1001The gas introduced is distributed uniformly over the entire cross-section by the gas distributor 102.
In some embodiments, as shown in FIG. 1, the bottom of each reactor section may be provided with a gas distributor 102. Through the design, the gas in each reaction tower section can be redistributed when entering the next reaction tower section, so that the mass transfer efficiency is further improved, and the reaction conversion rate is further improved.
At least one discharge port 400 is provided in the sidewall of the reaction tower section. As shown in fig. 1, a discharge hole 400 may be provided at each reaction tower section. In some embodiments, the discharge ports may be disposed in only upper several reaction tower sections to receive the products with higher reaction conversion rate. For example, 3 reaction tower sections S at the top part respectivelyn、Sn-1、Sn-2Set up 3 discharge gates respectively, these a little discharge gates are connected with row's material pipeline respectively and receive the result.
In some embodiments, a circulation line I may be further provided, and one end of the circulation line I is connected to the discharge port 400 and the other end is connected to the catalyst inlet 300. Using ethylene oxide as an example, it enters the reaction column section S1The concentration is not too high generally, part of the product is recycled through the circulating pipeline I, on one hand, the product which is not completely reacted can be converted for the second time, so that the product is fully reacted; on one hand, the water can also be diluted and enter a reaction tower section S1Concentration of ethylene oxide to improve conversion efficiency and avoid local problemsThe concentration of the partial ethylene oxide is too high; in addition, as the recycled material already contains part of the catalyst, the catalyst can be better blended, which is beneficial to further improving the reaction conversion rate and minimizing the energy consumption.
The present disclosure also provides a method for producing cyclic carbonate, which comprises the following steps:
respectively go through a carbon dioxide inlet 100, an alkylene oxide inlet 2020 and a catalyst inlet 300 to the lowest reaction tower section S1Introducing carbon dioxide, alkylene oxide and a catalyst; after entering through the carbon dioxide inlet 100, the carbon dioxide is uniformly distributed across the cross-section by the gas distributor 102 and enters the reactor section. With the addition of the alkylene oxide, the alkylene oxide sequentially passes through a plurality of reaction tower sections (S) from bottom to top1...Sn-1、Sn) The regular packing 500 and the heat exchanger 600 contact and react with carbon dioxide under the action of a catalyst to obtain cyclic carbonate, and the reacted materials are discharged through a discharge hole 400. In some embodiments, the reacted material enters the reaction tower section through the alkylene oxide inlet 100 via the circulation pipeline I to perform a circulation reaction, so as to further improve the reaction conversion rate.
In conclusion, the packing tower reactor and the method have the advantages that a plurality of reaction tower sections are connected in series, a plurality of groups of regular packing and heat exchangers are combined and alternately installed, mass transfer efficiency and heat exchange efficiency are fully improved, the packing tower reactor and the method have the advantages of uniform gas-liquid distribution, quick reaction heat removal and the like, the conversion rate of cyclic carbonate in the product obtained by the packing tower reactor and the method can reach more than 99%, and the packing tower reactor and the method are suitable for large-scale industrial production and have good application prospects.
The present disclosure will be further illustrated by the following specific examples, but the present disclosure is not limited thereto in any way.
Example 1
The production of ethylene carbonate was carried out using a packed column reactor as shown in FIG. 1. Wherein the diameter of each reaction tower section is 1000mm, the height of each section is 500mm, and the total number of the sections is 10. Three discharge ports are respectively arranged on the three reaction tower sections at the uppermost part of the reaction tower and are connected with a circulating pipeline.
Carbon dioxide enters from a carbon dioxide inlet and is fed by 2000Kg/h through a gas distributor, ethylene oxide enters from an ethylene oxide inlet and is fed by 2000Kg/h through a liquid distributor, catalyst is fed by 3Kg/h from a catalyst inlet and through a liquid distributor, and circulating material and the catalyst enter from one port. The temperature at the inlet of the packed tower reactor is 50 ℃, and the reaction pressure is 3.0 MPa. After the reaction materials are subjected to flash evaporation, tail gas is circulated to a carbon dioxide inlet, after 120min of reaction, three discharge ports are sampled, and the ethylene oxide content in the product is respectively measured by taking materials from the discharge ports from top to bottom as 0.33%, 0.08% and 0.03%. The reaction conversion rates were calculated to be 98%, 99.1%, 99.5%.
Example 2
The production of ethylene carbonate was carried out using a packed column reactor as shown in FIG. 1. Wherein the diameter of each reaction tower section is 1000mm, the height of each section is 500mm, and the total number of the sections is 10. Three discharge ports are respectively arranged on the three reaction tower sections at the uppermost part of the reaction tower and are connected with a circulating pipeline.
Carbon dioxide enters from a carbon dioxide inlet and is fed by 3000Kg/h through a gas distributor, ethylene oxide enters from an ethylene oxide inlet and is fed by 3000Kg/h through a liquid distributor, catalyst is fed by 3Kg/h from a catalyst inlet and is fed by the liquid distributor, and circulating material and the catalyst enter from one port. The temperature at the inlet of the packed tower reactor is 50 ℃, and the reaction pressure is 3.0 MPa. After the reaction materials are subjected to flash evaporation, tail gas is circulated to a carbon dioxide inlet, after reaction for 120min, three discharge ports are sampled, and the ethylene oxide content in the product is respectively measured by taking materials from the discharge ports from top to bottom as 0.93%, 0.12% and 0.06%. The reaction conversion rates were calculated to be 99%, 99.3%, 99.6%, respectively.
Therefore, the filler tower reactor disclosed by the invention is used for producing cyclic carbonate, the production efficiency is high, the product conversion rate is high and can basically reach more than 98-99%, and the industrial application prospect is good.
It should be noted by those skilled in the art that the described embodiments of the present invention are merely exemplary and that various other substitutions, alterations, and modifications may be made within the scope of the present invention. Accordingly, the present invention is not limited to the above-described embodiments, but is only limited by the claims.
Claims (10)
1. A packed column reactor for producing cyclic carbonates, comprising:
the reaction tower sections are sequentially connected from bottom to top;
a carbon dioxide inlet, an alkylene oxide inlet and a catalyst inlet which are respectively arranged at the lowest reaction tower section;
the at least one discharge hole is formed in the side wall of the reaction tower section;
each reaction tower section is provided with a group of regular packing and a heat exchanger, and the heat exchanger is arranged above the regular packing.
2. The packed tower reactor of claim 1, wherein the bottom of the lowermost reaction column section is provided with a gas distributor and a liquid distributor, the liquid distributor being disposed above the gas distributor and the structured packing being disposed above the liquid distributor.
3. The packed tower reactor of claim 2, wherein the gas distributor is disposed at the bottom of each of the reaction column sections.
4. The packed tower reactor of claim 1, wherein the structured packing is selected from one or more of wire mesh corrugated packing, metal mesh corrugated packing, and metal perforated plate corrugated packing.
5. The packed tower reactor of claim 1, further comprising a circulation conduit connected at one end to at least one of the feed ports and at another end to the catalyst inlet.
6. The packed tower reactor according to claim 1, wherein each of the reaction tower sections has a height of 100mm to 1200mm and a diameter of 300mm to 3000mm, the number of the reaction tower sections is 8 to 10, and the uppermost reaction tower section is provided with the discharge port.
7. The packed tower reactor according to claim 6, wherein the number of the discharge ports is 1-3, and the discharge ports are sequentially and respectively arranged on the corresponding reaction tower sections from top to bottom.
8. The packed tower reactor of claim 1, wherein the heat exchanger is a heat conducting water coil heat exchanger.
9. A method for producing a cyclic carbonate, characterized by using the packed column reactor according to any one of claims 1 to 8, comprising the steps of:
introducing carbon dioxide, alkylene oxide and a catalyst into the reaction tower section at the lowest part through the carbon dioxide inlet, the alkylene oxide inlet and the catalyst inlet respectively;
the alkylene oxide sequentially passes through the regular packing and the heat exchanger of the plurality of reaction tower sections from bottom to top, contacts and reacts with the carbon dioxide under the action of the catalyst to obtain the cyclic carbonate, and the reacted material is discharged through the discharge hole.
10. The production method of claim 9, wherein the reacted material enters the reaction tower section through the catalyst inlet through a circulating pipeline to perform circulating reaction.
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN114534640A (en) * | 2022-02-16 | 2022-05-27 | 安徽海华科技集团有限公司 | Methylation reaction system for o-cresol production |
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Application publication date: 20200508 |