CN115724743A - Application of catalyst in preparation of carbonic ester by decarbonylation of oxalate and process thereof - Google Patents
Application of catalyst in preparation of carbonic ester by decarbonylation of oxalate and process thereof Download PDFInfo
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Abstract
The invention relates to an application of a catalyst in preparation of carbonic ester by decarbonylation of oxalate and a process thereof. The gas after preheating, vaporization and overheating of oxalate is decomposed and reacted under the action of the catalyst to generate carbonic ester, the reaction gas is cooled and then subjected to gas-liquid separation, and the liquid is separated and purified to obtain the product carbonic ester, so that the problems of harsh reaction conditions, difficult product separation, low catalyst activity, easy inactivation and the like in the prior art are solved, the economy of the whole coal-based ethylene glycol process can be improved, and the industrial competitiveness is improved.
Description
Technical Field
The invention relates to the technical field of chemical industry, in particular to application of a catalyst in preparation of carbonic ester by decarbonylation of oxalate and a process thereof.
Background
Dimethyl carbonate (DMC), which is active in chemical properties, excellent in physical properties, non-toxic and easily biodegradable, is a new low-pollution and environment-friendly green basic chemical raw material, can be used as a solvent, a gasoline additive, a lithium ion battery electrolyte and a carbonylation, methylation and carbonylmethoxylation reagent, and is widely applied to the field of chemical engineering. At present, DMC production processes are various, mainly including phosgene method, alcohol oxidation carbon-based method, ester exchange method, urea alcoholysis method, direct synthesis method of carbon dioxide and alcohol and dimethyl oxalate decarbonylation method. Dimethyl oxalate comes from coal chemical industry and has wide raw material sources, so that the decarbonylation of dimethyl oxalate to prepare dimethyl carbonate becomes a method with great industrial prospects at present.
As early as 90 s in the last century, ube of Japan began to use alkali metal as a catalyst for the decarbonylation of dimethyl oxalate (DMO) to prepare DMC. Although the DMC yield is high in the initial stages of the reaction, the catalyst life is short. In recent years, research on DMC preparation by DMO decarbonylation, such as Hualu Hengsheng, china petrochemical industry, etc., mainly uses liquid-phase DMO decarbonylation, and the separation of a catalyst and a product is difficult in the liquid-phase decarbonylation technology, so that the service life of the catalyst needs to be improved.
Disclosure of Invention
The invention aims to solve the problems, and provides application of a catalyst in preparation of carbonic ester by decarbonylation of oxalate and a process thereof, so as to solve the problems of harsh reaction conditions, difficult product separation, low catalyst activity, easy inactivation and the like in the existing technology for preparing carbonic ester by decarbonylation of oxalate.
The purpose of the invention is realized by the following technical scheme:
an application of a catalyst in preparation of carbonic ester by decarbonylation of oxalate, wherein the catalyst consists of an active element M, a promoter N and a carrier;
the active element M is selected from one or more of Ru, rh, pd, ni, ag, re, ir, pt and Au, and is preferably Pd, ru and Ir;
the active auxiliary agent N is selected from one or more of Li, na, K, ca, mg, cu, zn, rb, ba, sr and Cs, and is preferably K, ba and Sr;
the carrier is selected from activated carbon, molecular sieve and Al 2 O 3 、SiO 2 Preferably activated carbon or molecular sieve;
the mass percentage of M is 0.01-3.0% based on the mass of the carrier; the mass percentage of N is 0.01-20%.
Preferably, the mass percentage of M is 0.01-1.0% of the mass of the carrier; the mass percentage of N is 0.5-20%.
The catalyst adopted by the invention is a bifunctional catalyst, so that the problem that the single alkali metal catalyst is easy to deposit carbon is solved, and the addition of the active component can inhibit the carbon deposition on the surface of the catalyst and prolong the service life of the catalyst; in addition, the addition of the alkali metal active assistant can lead the active component to obtain electrons from the alkali metal active assistant, and the proportion of the element with a zero valence state in the active component is increased, thereby increasing the activity and the selectivity of the catalyst.
Preferably, the catalyst is prepared by the following method:
(1) Weighing a precursor of M according to a ratio, and dissolving the precursor in a mixed solution of deionized water and ethanol to form a solution;
(2) Weighing N precursors according to a ratio, and dissolving the precursors into a mixed solution of deionized water and ethanol to form a solution;
(3) Weighing the carrier according to the proportion;
(4) And (3) co-impregnating the solutions in the steps (1) and (2) or impregnating the solutions on a carrier in a stepwise equal volume manner, drying and roasting to obtain the required catalyst.
Preferably, the mass percentage of the ethanol in the mixed solution in the step (1) and the step (2) is 5-25%; in the step (4), the drying temperature is 80-120 ℃, and the roasting temperature is 400-600 ℃.
A process for preparing carbonate by decarbonylating oxalate includes catalytic reaction of said catalyst, mixing oxalate-contained material with carrier gas, reaction of the resultant mixture in decarbonylating reactor containing said catalyst, and separation and refining of resultant.
In a most preferred embodiment, the process for preparing carbonate by decarbonylation of oxalate specifically comprises the following steps:
(1) The material S1 containing oxalate is pressurized by a pump and then mixed with a carrier gas S2, the formed mixed material S3 enters a decarbonylation reactor B2 for reaction, and a material flow S4 is obtained after the reaction;
(2) The material flow S4 and the material S1 containing oxalate exchange heat and enter a gas-liquid separation tank B3 for gas-liquid separation, a top gas-phase component S5 is mixed with a carrier gas S2, and a bottom liquid-phase component S6 enters a rectifying tower B4 for rectification;
(3) The tower bottom component S7 of the rectifying tower B4 is mixed with the material S1 containing oxalate, the tower top component S8 enters the rectifying tower B5 for rectification, the tower bottom component S10 of the rectifying tower B5 produces high-purity carbonate products, and the tower top component S9 of the rectifying tower B5 is further separated or circulated to the upstream to be mixed with the material S1 containing oxalate.
Preferably, a preheating mixer B1 is arranged at the upstream of the decarbonylation reactor B2, the mixed material S3 is preheated before entering the decarbonylation reactor B2, the preheating mixer B1 preheats the mixed material S3 to 150-300 ℃, and if the preheating temperature is too high, the decomposition reaction is easy to occur in advance to generate carbon deposition; if the temperature is too low, the material entering the decarbonylation reactor cannot be effectively preheated, resulting in uneven heating temperature.
When the material S1 containing oxalate does not contain dimethyl oxalate, the tower top component S9 of the rectifying tower B5 is mixed with the material S1 and then circulated to the preheating mixer B1;
when the oxalate-containing material S1 contains dimethyl oxalate, a rectifying tower B6 is also arranged behind the rectifying tower B5, a tower top component S9 of the rectifying tower B5 enters the rectifying tower B6 for rectification, a tower top component S11 (an azeotrope of dimethyl carbonate and methanol) of the rectifying tower B6 returns to the rectifying tower B5 for cyclic rectification, and a tower bottom component S12 (methanol) of the rectifying tower B6 is mixed with the material S1 and then circulated to the preheating mixer B1.
Preferably, the oxalate comprises one or more of dimethyl oxalate, diethyl oxalate and diphenyl oxalate, and the material S1 is a pure molten oxalate or a methanol solution containing oxalate; the carrier gas S2 comprises one or more of nitrogen, carbon monoxide and hydrogen.
Preferably, the decarbonylation reactor B2 has the temperature of 200-600 ℃, the pressure of 0.1-5MPa and the liquid hourly space velocity of 0.1-3.0h -1 The gas-liquid ratio is 200-25000, the S4 material flow obtained after the reaction mainly comprises carrier gas, carbon monoxide and carbonic ester,the temperature of the material S4 after heat exchange is more than or equal to 164 ℃.
Preferably, the temperature of the gas-liquid separation tank B3 is 5-10 ℃;
the pressure of the rectifying tower B4 is 0-0.5bar, and the temperature of a tower kettle is 50-120 ℃;
the pressure of the rectifying tower B5 is 1.0-2.0MPA, and the temperature of a tower kettle is 100-220 ℃;
the pressure of the rectifying tower B6 is 0-1.0MPA, and the temperature of the tower bottom is 50-150 ℃.
Preferably, the decarbonylation reactor B2 is a tubular reactor, and one or more decarbonylation reactors B2' are connected in series after the decarbonylation reactor B2.
Preferably, the pipe diameter of the decarbonylation reactor B2' is 0.2-0.8 of the pipe diameter of the decarbonylation reactor B2, the height of the decarbonylation reactor B2 is 0.1-0.25, the temperature of the decarbonylation reactor B2' is 170-200 ℃, and the pressure of the decarbonylation reactor B2' is 0.1-5MPa.
By adopting the method, dimethyl oxalate is decarbonylated to prepare dimethyl carbonate, the conversion rate of the dimethyl oxalate is 50-98%, and the selectivity of the carbonic ester is 60-95%. The catalyst life is tested for 200-4000h of stability, and the activity is not obviously reduced.
Compared with the prior art, the invention has the following advantages:
1) The invention adopts a fixed bed reactor, oxalate (such as DMO) is preheated and vaporized and then reacts on a special catalyst to generate carbonate (such as DMC), reaction gas is cooled and then subjected to gas-liquid separation, and liquid is separated and purified to obtain a product (such as DMC), thereby solving the problems of harsh reaction conditions, difficult product separation, low catalyst activity, easy inactivation and the like in the prior art.
2) The invention adopts the bifunctional catalyst, solves the problem that the single alkali metal catalyst is easy to deposit carbon, and the addition of the active component can inhibit the carbon deposition on the surface of the catalyst and prolong the service life of the catalyst; in addition, the addition of the alkali metal active auxiliary agent can lead the active component to obtain electrons from the alkali metal active auxiliary agent, and the proportion of elements with zero valence in the active component is increased, thereby increasing the activity and the selectivity of the catalyst.
Drawings
FIG. 1 is a flow chart of a process for preparing carbonate by decarbonylation of oxalate according to an embodiment of the present invention;
FIG. 2 is a flow chart of a process for preparing carbonate by decarbonylation of oxalate according to another embodiment of the present invention.
Detailed Description
The invention is described in detail below with reference to the figures and specific embodiments.
A process for preparing carbonic ester by decarbonylation of oxalic ester features that the following catalysts are used to make catalytic reaction,
the catalyst consists of an active element M, an active auxiliary N and a carrier, wherein the active element M is selected from one or more of Ru, rh, pd, ni, ag, re, ir, pt and Au; the active auxiliary agent N is selected from one or more of Li, na, K, ca, mg, cu, zn, rb, ba, sr and Cs; the carrier is selected from activated carbon, molecular sieve, al 2 O 3 、SiO 2 One or more of the above; based on the mass of the carrier, the mass percentage content of M is 0.01-3.0%; the mass percentage of N is 0.01-20%, preferably, the mass percentage of M is 0.01-1.0%; the mass percentage of N is 0.5-20%.
As a preferred embodiment, the active element M is selected from Pd, ru, ir; the active auxiliary agent N is selected from K, ba and Sr; the carrier is selected from activated carbon and molecular sieve.
The catalyst is prepared by the following method:
(1) Weighing a precursor of M according to a ratio, and dissolving the precursor in a mixed solution of deionized water and ethanol to form a solution;
(2) Weighing N precursors according to a ratio, and dissolving the precursors into a mixed solution of deionized water and ethanol to form a solution;
(3) Weighing the carrier according to the proportion;
(4) And (3) co-impregnating the solutions in the steps (1) and (2) or impregnating the solutions on a carrier in a stepwise equal volume manner, drying and roasting to obtain the required catalyst.
In the step (1) and the step (2), both the precursor of M and the precursor of N are soluble salts thereof, and the mass percentage of ethanol is 5-25%; in the step (4), the drying temperature is 80-120 ℃, and the roasting temperature is 400-600 ℃.
The specific steps of the process for preparing the carbonic ester by decarbonylation of the oxalate are as follows, and a process flow chart is shown in figure 1:
(1) The material S1 containing oxalate is pressurized by a pump and then mixed with a carrier gas S2, a mixed material S3 formed after preheating by a preheating mixer B1 enters a decarbonylation reactor B2 for reaction, and a material flow S4 is obtained after the reaction;
(2) The material S4 and the material S1 containing oxalate exchange heat and enter a gas-liquid separation tank B3 for gas-liquid separation, a top gas-phase material S5 and a carrier gas S2 are mixed and then enter a preheating mixer B1, and a bottom liquid-phase material S6 enters a rectifying tower B4 for rectification;
(3) The tower bottom component S7 of the rectifying tower B4 is mixed with the material S1 containing oxalate and returns to the preheating mixer B1, the tower top component S8 enters the rectifying tower B5 for rectification, the tower bottom component S10 of the rectifying tower B5 extracts high-purity carbonate and enters a product tank, and the tower top component S9 of the rectifying tower B5 is further separated or circulated to the preheating mixer B1.
When the material S1 containing oxalate does not contain dimethyl oxalate, the tower top component S9 of the rectifying tower B5 is mixed with the material S1 and then circulated to the preheating mixer B1;
when the oxalate-containing material S1 contains dimethyl oxalate, a rectifying tower B6 is also arranged behind the rectifying tower B5, a tower top component S9 of the rectifying tower B5 enters the rectifying tower B6 for rectification, a tower top material flow S11 (an azeotrope of dimethyl carbonate and methanol) of the rectifying tower B6 returns to the rectifying tower B5 for cyclic rectification, and a tower bottom material flow S12 (methanol) of the rectifying tower B6 is mixed with the material S1 and then circulated to the preheating mixer B1.
In the step (1), the oxalate comprises one or more of dimethyl oxalate, diethyl oxalate and diphenyl oxalate, and the material S1 is a pure molten oxalate or a methanol solution containing oxalate; the carrier gas S2 comprises one or more of nitrogen, carbon monoxide and hydrogen, and the preheating mixer B1 preheats the mixed material S3 to 150-300 ℃; the decarbonylation reactor B2 has the temperature of 200-600 ℃, the pressure of 0.1-5MPa and the liquid hourly space velocity of 0.1-3.0h -1 The gas-liquid ratio is 200-25000, the S4 material flow obtained after reaction mainly comprises carrier gas, carbon monoxide and carbonic ester, and the temperature of the material S4 after heat exchange is more than or equal to 164 ℃;
in the steps (2) and (3), the temperature of the gas-liquid separation tank B3 is 5-10 ℃; the pressure of the rectifying tower B4 is 0-0.5bar, and the temperature of a tower kettle is 50-120 ℃; the pressure of the rectifying tower B5 is 1.0-2.0MPA, and the temperature of the tower kettle is 100-220 ℃; the rectification pressure of the rectification tower B6 is 0-1.0MPA, and the temperature of the tower kettle is 50-150 ℃.
As a preferred embodiment, the decarbonylation reactor B2 is a tubular reactor, one or more small decarbonylation reactors B2' are connected in series after the decarbonylation reactor B2, as shown in FIG. 2, one or more small decarbonylation reactors B2' are connected in series after the decarbonylation reactor B2, and the tube diameter of the decarbonylation reactor B2' is 0.2-0.8 of the tube diameter of the decarbonylation reactor B2, the height is 0.1-0.25 of the height of the decarbonylation reactor B2, the temperature is 170-200 ℃, and the pressure is 0.1-5MPa.
It should be noted that, in the present invention, all the references to "pressure" refer to "absolute pressure".
The following are specific examples.
Preparation of catalyst for preparing carbonic ester by decarbonylation of oxalate
Examples A1 to A20
The catalyst was prepared by the following method,
(1) Weighing M precursor (such as Ni (NO) according to the proportion 3 ) 2 、AgNO 3 、Pd(NO 3 ) 2 Ruthenium nitrate) is dissolved in a mixed solution of deionized water and ethanol to form a solution, wherein the mass percentage of the ethanol in the mixed solution is 5-25%;
(2) Weighing N precursor (such as Ca (NO)) according to proportion 3 ) 2 、Mg(NO 3 ) 2 、KNO 3 、Ba(NO 3 ) 2 、Sr(NO 3 ) 2 ) Dissolving the mixture in a mixed solution of deionized water and ethanol to form a solution, wherein the mass percentage of the ethanol in the mixed solution is 5-25%;
(3) Weighing the carrier (e.g. SiO) proportionally 2 Activated carbon, molecular sieves);
(4) Mixing the solutions obtained in the steps (1) and (2), co-soaking or soaking the solutions onto a carrier in equal volume step by step, filtering and washing, drying at 80-120 ℃ for 2-10h, and then roasting at 400-600 ℃ for 1-6 h to obtain the catalyst.
The specific compositions and process parameters are detailed in table 1.
Comparative examples 1 to 3
Comparative example 1 compared to example a11, the same procedure was followed without the addition of the active element.
Comparative example 2 compared to example A2, the same procedure was followed without the addition of the active element.
Comparative example 3 compared to example A8, no active element was added and the remaining steps were the same.
The specific compositions and process parameters are detailed in table 1.
TABLE 1 concrete compositions of examples A1 to A18 and comparative examples 1 to 3
The catalyst prepared in the examples and the comparative examples is used for the process of preparing carbonic ester by decarbonylation of oxalate
Application example B1
The catalyst prepared in the example is used for the process for preparing dimethyl carbonate by decarbonylation of dimethyl oxalate, the process is shown as a figure 1, and the process parameters of all parts are detailed in a table 2. The DMO conversion, DMC selectivity and DMC stability of each example and comparative example were tested and the results are detailed in table 3.
TABLE 2 Process parameters for the parts of FIG. 1
TABLE 3 DMO conversion, DMC selectivity, and stability testing of each of the examples and comparative examples
| Name (R) | DMO conversion/% | DMC selectivity/%) | Stability test/h |
| Catalyst A1 | 90 | 85 | 3000 |
| Catalyst A2 | 70 | 95 | 500 |
| Catalyst A3 | 90 | 80 | 2500 |
| Catalyst A4 | 60 | 82 | 500 |
| Catalyst A5 | 50 | 61 | 200 |
| Catalyst A6 | 52 | 60 | 300 |
| Catalyst A7 | 50 | 60 | 400 |
| Catalyst A8 | 70 | 70 | 1500 |
| Catalyst A9 | 95 | 80 | 2500 |
| Catalyst A10 | 60 | 60 | 500 |
| Catalyst A11 | 95 | 90 | 4000 |
| Catalyst A12 | 98 | 85 | 4000 |
| Catalyst A13 | 90 | 60 | 1000 |
| Catalyst A14 | 80 | 83 | 3000 |
| Catalyst A15 | 80 | 90 | 1500 |
| Catalyst A16 | 85 | 70 | 1000 |
| Catalyst A17 | 85 | 80 | 2000 |
| Catalyst A18 | 70 | 74 | 1000 |
| Catalyst a | 40 | 40 | 30 |
| Catalyst b | 10 | 30 | 20 |
| Catalyst c | 30 | 37 | 40 |
The result shows that the catalyst of the embodiment of the invention has high activity and high selectivity, and compared with the comparative ratio, the DMO conversion rate and the DMC selectivity are obviously improved. In addition, the catalyst provided by the embodiment of the invention can effectively prolong the service life of the catalyst, and the service life can reach 4000h.
Application example B2
The catalyst prepared in the example is used for the process for preparing dimethyl carbonate by decarbonylation of dimethyl oxalate, the process shown in figure 2 is adopted, the process parameters of all parts are detailed in table 4, the conversion rates of DMO and DMC of each example and comparative example are tested, and the specific result is detailed in table 5.
Table 4 process parameters for each part of figure 2
TABLE 5 examples and comparative examples DMO, conversion and DMC selectivity
The embodiments described above are described to facilitate an understanding and use of the invention by those skilled in the art. It will be readily apparent to those skilled in the art that various modifications to these embodiments may be made, and the generic principles described herein may be applied to other embodiments without the use of the inventive faculty. Therefore, the present invention is not limited to the above embodiments, and those skilled in the art should make modifications and alterations without departing from the scope of the present invention.
Claims (10)
1. The application of the catalyst in preparation of carbonate by decarbonylation of oxalate is characterized in that the catalyst consists of an active element M, a promoter N and a carrier;
the active element M is selected from one or more of Ru, rh, pd, ni, ag, re, ir, pt and Au;
the active auxiliary agent N is selected from one or more of Li, na, K, ca, mg, cu, zn, rb, ba, sr and Cs;
the carrier is selected from activated carbon, molecular sieve and Al 2 O 3 、SiO 2 One or more of the above;
based on the mass of the carrier, the mass percentage content of M is 0.01-3.0%; the mass percentage of N is 0.01-20%.
2. The use of a catalyst according to claim 1 in the decarbonylation of an oxalate to produce a carbonate, wherein the catalyst is prepared by the following method:
(1) Weighing a precursor of M according to a ratio, and dissolving the precursor in a mixed solution of deionized water and ethanol to form a solution;
(2) Weighing N precursors according to a ratio, and dissolving the precursors into a mixed solution of deionized water and ethanol to form a solution;
(3) Weighing the carrier according to the proportion;
(4) And (3) co-impregnating the solutions in the steps (1) and (2) or impregnating the solutions on a carrier in a stepwise equal volume manner, drying and roasting to obtain the required catalyst.
3. The application of the catalyst in the decarbonylation of oxalate to produce carbonate according to claim 2, wherein the mass percent of ethanol in the mixed solution in the step (1) and the step (2) is 5% -25%; in the step (4), the drying temperature is 80-120 ℃, and the roasting temperature is 400-600 ℃.
4. A process for preparing carbonate by decarbonylation of oxalate features that the catalyst in any one of claims 1-3 is used to make catalytic reaction, the oxalate-containing material is mixed with carrier gas, the resultant mixture is fed into decarbonylation reactor containing said catalyst for reaction, and the resultant is separated and refined to obtain high-purity carbonate.
5. The process for preparing carbonate by decarbonylation of oxalate according to claim 4, comprising the steps of:
(1) The material S1 containing oxalate is pressurized by a pump and then mixed with a carrier gas S2, the formed mixed material S3 enters a decarbonylation reactor B2 for reaction, and a material flow S4 is obtained after the reaction;
(2) The material flow S4 and the material S1 containing oxalate exchange heat and enter a gas-liquid separation tank B3 for gas-liquid separation, a top gas-phase component S5 is mixed with a carrier gas S2, and a bottom liquid-phase component S6 enters a rectifying tower B4 for rectification;
(3) The tower bottom component S7 of the rectifying tower B4 is mixed with the material S1 containing oxalate, the tower top component S8 enters the rectifying tower B5 for rectification, the tower bottom component S10 of the rectifying tower B5 produces high-purity carbonate products, and the tower top component S9 of the rectifying tower B5 is further separated or circulated to the upstream to be mixed with the material S1 containing oxalate.
6. The process for preparing carbonate by decarbonylation of oxalate according to claim 5, wherein a preheating mixer B1 is arranged upstream of the decarbonylation reactor B2, the mixed material S3 is preheated before entering the decarbonylation reactor B2, and the preheating mixer B1 preheats the mixed material S3 to 150-300 ℃.
7. The process of claim 6, wherein the oxalate ester comprises one or more of dimethyl oxalate, diethyl oxalate, diphenyl oxalate;
when the material S1 containing oxalate does not contain dimethyl oxalate, the tower top component S9 of the rectifying tower B5 is mixed with the material S1 and then circulated to the preheating mixer B1;
when the oxalate-containing material S1 contains dimethyl oxalate, a rectifying tower B6 is also arranged behind the rectifying tower B5, a tower top component S9 of the rectifying tower B5 enters the rectifying tower B6 for rectification, a tower top component S11 of the rectifying tower B6 returns to the rectifying tower B5 for circular rectification, and a tower bottom component S12 of the rectifying tower B6 is mixed with the material S1 and then circulated to the preheating mixer B1.
8. The process for preparing carbonate by decarbonylation of oxalate according to claim 5, wherein the decarbonylation reactor B2 has a temperature of 200-600 ℃, a pressure of 0.1-5MPa, and a liquid hourly space velocity of 0.1-3.0h -1 The gas-liquid ratio is 200-25000.
9. The process for preparing carbonic ester by decarbonylation of oxalic ester according to claim 5, wherein the temperature of the gas-liquid separation tank B3 is 5-10 ℃;
the pressure of the rectifying tower B4 is 0-0.5bar, and the temperature of a tower kettle is 50-120 ℃;
the pressure of the rectifying tower B5 is 1.0-2.0MPA, and the temperature of a tower kettle is 100-220 ℃;
the pressure of the rectifying tower B6 is 0-1.0MPA, and the temperature of the tower bottom is 50-150 ℃.
10. The process for preparing carbonate by decarbonylation of oxalic ester according to any one of claims 5 to 9, wherein the decarbonylation reactor B2 is a tubular reactor, and one or more decarbonylation reactors B2' are connected in series after the decarbonylation reactor B2;
the pipe diameter of the decarbonylation reactor B2' is 0.2-0.8 of the pipe diameter of the decarbonylation reactor B2, and the height is 0.1-0.25 of the height of the decarbonylation reactor B2;
the temperature of the decarbonylation reactor B2' is 170-200 ℃, and the pressure is 0.1-5MPa.
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