CN110204444B

CN110204444B - Synthesis method of dimethyl carbonate

Info

Publication number: CN110204444B
Application number: CN201910590296.XA
Authority: CN
Inventors: 王计奎
Original assignee: Tengzhou Jingtengxinhui New Material Technology Co ltd
Current assignee: Tangshan Good Reputation Technology Development Co ltd
Priority date: 2019-07-02
Filing date: 2019-07-02
Publication date: 2022-04-22
Anticipated expiration: 2039-07-02
Also published as: CN110204444A

Abstract

The invention belongs to the field of production processes of chemical raw materials, and particularly relates to a production process for synthesizing dimethyl carbonate by using an ester exchange method. The catalyst used in the production process consists of 6-10wt% of active component and the balance of carrier, wherein the active component is Bi₂O₃And KOH, Bi₂O₃: KOH (weight ratio) 1: 2-4; the carrier is zinc-iron composite metal oxide. The production process for synthesizing the dimethyl carbonate has the advantages of mild reaction conditions, lower production cost and high yield of the dimethyl carbonate.

Description

Synthesis method of dimethyl carbonate

Technical Field

The invention belongs to the field of production processes of chemical raw materials, and particularly relates to a production process for synthesizing dimethyl carbonate by using an ester exchange method.

Background

Dimethyl carbonate (DMC) is an environmentally friendly organic chemical raw material which has a wide application and meets the requirement of modern 'cleaning process' and is known as a 'new base block' for organic synthesis, and is very important in recent years. Because the molecule of the compound contains methoxyl, carbonyl and carbonyl methyl, the compound has low toxicity, high solubility, excellent environmental protection performance and good reaction activity, can replace virulent phosgene and dimethyl sulfate, is widely applied to the rapid development industries of carbonylation and methylation reagents, gasoline additives, raw materials for synthesizing polycarbonate, coating solvents, lithium battery electrolyte and the like, has wide market, and is a popular green chemical in the chemical field at present.

The industrial production methods of dimethyl carbonate include a phosgenation method, a methanol liquid-phase oxidative carbonylation method and an ester exchange method. The transesterification method is increasingly emphasized due to mild reaction conditions, simple process flow, low equipment cost and coproduction of alkanediol, and becomes a method with great industrial application prospect at present. The catalysts used for synthesizing dialkyl carbonate by the transesterification method mainly include homogeneous base catalysts such as triethylamine, triphenylphosphine, etc., and solid base catalysts which are generally hydroxides, alkoxides or carbonates of alkali metals such as sodium hydroxide, potassium hydroxide, sodium methoxide and potassium carbonate. The homogeneous catalyst has high activity, but is not easy to separate, and is not beneficial to industrialization. Compared with homogeneous alkali catalyst, the solid alkali catalyst has the advantages of no corrosion to equipment, less environmental pollution, easy recovery, etc. and is the catalyst system with development foreground in the reaction of synthesizing dialkyl carbonate through ester exchange process.

Such as the one disclosed in Chinese patent CN 102471221A, which comprises a hydrogen ion (H) generating material⁺) And a catalyst selected from at least one of alkaline earth metal oxides, transition metal oxides, rare earth oxides and hydrotalcites, by reacting an alkyl alcohol with urea or an alkyl carbamate. Although this method can produce dialkyl carbonate in high yield and improve economic efficiency, the catalyst used is relatively complicated in production process and relatively high in production cost.

For example, chinese patent CN 107096540A discloses a process for synthesizing dimethyl carbonate by urea alcoholysis, wherein the metal elements in the composite metal oxide contained in the catalyst used in the process include the following four elements: mg (magnesium)²⁺、Sn²⁺、Ni²⁺And Al³⁺. The hydrotalcite-like compound is prepared by a coprecipitation method, and then is obtained by roasting. In the process, the yield of DMC can reach 55.3% at the reaction temperature of 200 ℃.

For example, chinese patent CN 105879892A discloses a process for synthesizing dimethyl carbonate by ester exchange method, wherein the solid base catalyst used in the process comprises Ca-Al-O-X, the molar content of Ca is 15-35%, the molar content of Al is 5-30%, the molar content of X is 0.1-10%, and the balance is the content of O. The reaction temperature of the process is lower, is 60 ℃, and the DMC yield can reach 55.7 percent at most.

For example, chinese patent CN 109772286A discloses a process for synthesizing alkyl carbonate by ester exchange method, wherein the solid base catalyst comprises a carrier and sodium aluminate as active component loaded on the carrier; the carrier is at least one composite metal oxide selected from zinc-aluminum composite metal oxide, nickel-aluminum composite metal oxide and cobalt-aluminum composite metal oxide. The preparation process comprises the following steps: firstly, preparing a hydrotalcite-like precursor of the composite metal oxide, then impregnating sodium aluminate, and roasting to obtain the solid base catalyst. The yield of DMC of the catalyst can reach 75.1% at 65 deg.C.

For example, US 4691041A discloses a process for the synthesis of dimethyl carbonate wherein the heterogeneous catalyst used is selected from the group consisting of ion exchange resins with quaternary ammonium functionalities, ion exchange resins with sulphonic functionalities, ion exchange resins with carboxylic functionalities, silica impregnated with alkali/alkaline earth metal silicates, ammonium exchanged molecular sieves. The DMC yield can reach 23.7% at 100 deg.C.

In general, the ester exchange method in the existing production process for synthesizing dimethyl carbonate is the most promising production process due to the advantages of mild reaction conditions and the like. However, the catalytic performance of the catalyst for synthesizing dimethyl carbonate by the ester exchange method still has various defects, so that the development of a new generation of catalyst with better performance is needed to provide more favorable support for the industrial production of dimethyl carbonate.

Disclosure of Invention

Therefore, the technical problem to be solved by the application is to provide a production process for synthesizing dimethyl carbonate, which has the advantages of high yield of dimethyl carbonate, mild reaction conditions and low production cost.

The present inventors have earnestly studied to solve the above-mentioned technical problems, and have found that the above-mentioned technical problems can be solved by using a high-performance catalyst. Firstly, producing a hydrotalcite precursor of a carrier by a coprecipitation method; then, the active component bismuth oxide (Bi) is directly loaded by wet impregnation without roasting₂O₃) And potassium hydroxide (KOH), and then drying and roasting under proper conditions to obtain the high-performance catalyst with the active component supported by the zinc-iron composite metal oxide. ZnO and ZnFe in the carrier of the catalyst₂O₄Has proper proportion and interaction force, the active components are uniformly distributed, and the interaction force between the active components and the carrier is moderate.

The technical scheme of the invention is as follows: the invention discloses a process for synthesizing dimethyl carbonate by ester exchange method, wherein the catalyst used in the process is prepared from6-10wt% of active component and the balance of carrier, wherein the active component is Bi₂O₃And KOH, Bi₂O₃: KOH (weight ratio) 1: 2-4; the carrier is zinc-iron composite metal oxide.

The content of the active component is preferably 6 to 8 wt.%, based on the total weight of the catalyst.

The carrier in the catalyst is prepared by roasting a hydrotalcite-like precursor, and the general formula of the carrier is as follows: [ Zn ]²⁺ _1-xFe³⁺ _x(OH)₂]^x+(CO₃ ^2-)_x/2·nH₂O, wherein x is more than or equal to 0.2 and less than or equal to 0.33, and n is more than or equal to 1 and less than or equal to 10.

X in the general formula is more preferably 0.25. ltoreq. x.ltoreq.0.33, and most preferably 0.25.

The inventors of the present application have found through research that, in the catalyst used in the present application, by selecting a zinc-iron hydrotalcite of a specific composition as a precursor of a carrier, loading an active component without calcination, and then controlling drying and calcination conditions, ZnO and ZnFe in the carrier can be combined₂O₄In a suitable ratio without causing ZnO or ZnFe₂O₄And if the amount of the catalyst is too large, the catalytic activity is remarkably reduced, proper interaction force can be generated between the two components in the carrier, and very moderate interaction force can be generated between the active component and the carrier, so that the low-temperature activity and stability of the catalyst are greatly improved, and the service life of the catalyst is prolonged.

On the contrary, if after the hydrotalcite-like precursor is prepared, firstly roasting (the roasting condition is the same as that after the active component is loaded in the application) to obtain the zinc-iron composite oxide, and then loading the active component by using the method in the application, the performance of the catalyst is tested under the same reaction condition, and the conversion rate of the ethylene carbonate of the catalyst is only 62.8%, and the catalytic activity of the catalyst is obviously reduced when the catalyst is reused for the 5 th time, so that the catalytic performance of the catalyst is far inferior to that of the catalyst in the application on the whole. For the reason, it is highly likely that the carrier is subjected to two times of calcination to cause the calcination thereinZnFe₂O₄The excess content is significantly increased and also greatly affects the force acting between the active ingredient and the carrier, resulting in easy inactivation of the active ingredient.

The research also finds that the carrier and the active component Bi₂O₃And KOH, and unexpected synergistic effect is generated among the three components, so that the catalyst has high low-temperature catalytic activity. Although it is known in the prior art that a composite metal oxide prepared from KOH or hydrotalcite can be directly used as a catalyst for synthesizing dimethyl carbonate, there is no report on the use of a composite metal oxide prepared from zinc-iron hydrotalcite as a catalyst or a carrier for synthesizing dimethyl carbonate, nor is there any report on the use of Bi₂O₃Can be used as an auxiliary agent for synthesizing a dimethyl carbonate catalyst based on KOH. The catalyst performance was tested under the same reaction conditions, with KOH, Bi alone₂O₃When the composite metal oxide is used as a catalyst, the catalyst activity is the highest KOH catalyst, but the conversion rate of the ethylene carbonate is only 41 percent, which is still far lower than that of the catalyst.

The invention also discloses a preparation method of the catalyst, which comprises the following steps:

1) firstly, preparing a hydrotalcite-like precursor according to the composition of a final carrier;

2) weighing KOH and soluble bismuth salt according to the composition of the final catalyst, and adding deionized water to prepare an impregnation liquid;

3) adding the hydrotalcite-like precursor obtained in the step 1) into the impregnation liquid prepared in the step 2), and performing wet impregnation (namely an excess solution impregnation method); then filtering or centrifugally separating to obtain a filter cake, and washing;

4) freeze-drying the filter cake, then roasting for 3-8h at 400-550 ℃ in an air atmosphere, and then cooling to room temperature to obtain the catalyst product.

The soluble bismuth salt in the step 2) is selected from one or more of bismuth nitrate, bismuth acetate, bismuth sulfate, bismuth chloride and the like, and is preferably bismuth nitrate.

The concentration of bismuth ions in the impregnation liquid in the step 2) is 0.1-1mol/L, and more preferably 0.3-0.7 mol/L; the KOH concentration is 0.5 to 2mol/L, more preferably 1 to 1.5 mol/L.

The freeze drying process of the step 3) comprises the following specific steps: the filter cake is frozen into solid in a freezing chamber, and then water vapor is sublimated under the condition of reduced pressure to obtain a dry product.

The roasting process of the step 4) is preferably as follows: heating the dried product from room temperature to 250 ℃ at the heating rate of 5-15 ℃/min, preserving the heat for 1-2h, then continuously heating to 550 ℃ at the heating rate of 5-15 ℃/min, more preferably 500 ℃ at the temperature of 400-. The rate of temperature rise is preferably 8 to 12 ℃/min, more preferably 10 ℃/min.

In a preferred embodiment, the hydrotalcite-like precursor in step 1) can be prepared by a co-precipitation method, which comprises the following steps:

a) firstly, weighing soluble zinc salt and soluble iron salt, and adding deionized water to prepare a mixed solution;

b) dropwise adding the mixed solution prepared in the step a) and a sodium carbonate solution into a reactor under continuous stirring; then adding a proper amount of sodium hydroxide solution to keep the pH value of the solution between 9.5 and 10.5 in the precipitation process;

c) after the precipitation is completed, aging the precipitate in mother liquor at 55-65 ℃ overnight;

d) and filtering and separating the precipitate, washing for a plurality of times with water, and drying to obtain the hydrotalcite-like precursor.

The soluble zinc salt or iron salt in the step a) is selected from one or more of nitrate, sulfate, acetate, hydrochloride and the like, and preferably is nitrate; the molar ratio of Zn ions to iron ions is 2-4, preferably 3.

The pH in step b) is preferably 10.

The ageing temperature in step c) is preferably 60 ℃.

In the preparation method of the catalyst, an optional forming step 5) can be introduced after the step 4) according to the requirements on the shape and mechanical strength of the catalyst in a specific use process, and a common forming mode, such as compression forming, extrusion forming, rotation forming and the like can be adopted, and a proper amount of common forming auxiliary agents, such as a binder such as methyl cellulose, a lubricant such as graphite and paraffin, an extrusion aid such as sesbania powder and the like can be introduced in the forming process according to the needs.

Through research, the inventor of the present application finds that, compared with other drying methods, such as drying, air drying and microwave drying, the freeze drying of the hydrotalcite-like precursor impregnated with the active component, which is selected in the present application, helps to make the distribution of the active component in the catalyst more uniform, increase the specific surface area of the catalyst, and greatly reduce the calcination temperature of the catalyst (for example, when the active component precursor is bismuth nitrate, the decomposition temperature is usually greater than 590 ℃, and through freeze drying, it is found that the calcination temperature can be reduced to 400 ℃, which greatly reduces the energy consumption), and helps to moderate the acting force of each component in the catalyst and the carrier, thereby improving the stability and the service life of the catalyst.

It has been found that the wet impregnation (i.e. excess solution impregnation) selected in the present application is more helpful to make the distribution of active components in the catalyst more uniform and to make the acting force between the catalyst and the carrier moderate, compared with other impregnation processes, such as dry impregnation (i.e. equivalent volume solution impregnation), multiple impregnation, solvent evaporation, precipitation in pores, etc., so as to improve the stability and service life of the catalyst. In other words, the particular choice of impregnation process made herein has a positive impact on the activity, stability and lifetime of the final catalyst.

Research also shows that the ZnO and ZnFe in the carrier can be subjected to sectional temperature rise through controlling the roasting conditions, particularly the sectional temperature rise and the temperature rise rate, compared with the sectional temperature rise to the calcining temperature in a one-step mode or at other temperature rise rates (namely the temperature rise rate is out of the range of 5-15 ℃/min)₂O₄In a more suitable ratio without causing ZnO or ZnFe₂O₄Too much and also contributes to moderate acting force of each component in the catalyst and the carrier, thereby improving the stability and the service life of the catalyst.

In sum, the selection of the impregnation process, the drying mode and the roasting condition in the application has positive influence on the improvement of the catalyst performance. Although the specific weight that the above factors take on the improvement in the final catalyst performance is not clear, if any of the above factors are not met during the preparation process, a significant reduction in the activity and stability of the catalyst will result. The inventors of the present application have thus reasonably thought that the above factors produce synergistic promoting effects with each other.

The production process for synthesizing dimethyl carbonate by the ester exchange method adopts the following reaction conditions: the reaction temperature is 55-100 ℃, the molar ratio of methanol to Ethylene Carbonate (EC) is 8-12, and the amount of the catalyst is 1-5% (relative to the weight of ethylene carbonate).

The reaction temperature is preferably 55-80 ℃, the molar ratio of methanol EC is preferably 8-10, and the amount of catalyst used is preferably 2-4.5% (relative to the weight of ethylene carbonate).

The inventor of the present application has found that, although the yield of DMC is slightly reduced in the catalyst of the present application at a low temperature, such as 55 ℃, and the amount of the catalyst is 4.5% (relative to the weight of ethylene carbonate), the economic efficiency of the production process is greatly improved as a whole due to the reduction of the reaction temperature and the amount of the catalyst.

Compared with the prior art, the beneficial effect that this application has is:

1. the carrier component and the active component Bi of the catalyst used in the production process of the catalyst₂O₃And KOH, and unexpected synergistic effect is generated among the three components, so that the catalyst has high low-temperature catalytic activity.

2. The catalyst used in the production process has long service life, can be repeatedly used for many times, still keeps good activity and selectivity, and has no obvious reduction in the performance, thereby greatly improving the economy of the production process.

3. The catalyst used in the production process can be recycled through filtration or centrifugal separation after reaction, the recycling process is simple to operate, and the use cost is greatly reduced.

4. The catalyst used in the production process has simple preparation process and is similar to water slipThe stone precursor can be used for loading active components without roasting after being prepared, thereby not only reducing the energy consumption, but also being beneficial to carriers ZnO and ZnFe₂O₄In proper proportion, it also helps to moderate the action force of each component in the catalyst and carrier.

5. In the preparation process of the catalyst used in the production process, the selection of the impregnation process, the drying mode and the roasting condition all have positive influence on the improvement of the catalyst performance, and the factors generate a synergistic promotion effect.

6. The production process has short reaction time and mild reaction conditions, thereby greatly reducing the production cost of synthesizing the dimethyl carbonate.

Additional advantages will be set forth in part in the description which follows and in part will be obvious from the description, or may be learned by practice of the invention. The following advantages are realized and attained, particularly in light of the chemical compositions, methods, and combinations particularly pointed out in the appended claims. It is to be understood that both the foregoing general description and the following detailed description are exemplary and explanatory only and are not restrictive.

Supplemental definition

The materials, compounds, compositions, and components described herein can be used in, or can be used in combination with, the methods and compositions described herein, or can be used in the practice of the methods and in the preparation of the compositions, or as products obtained by the methods. It is to be understood that when combinations, subsets, interactions, groups, etc. of these materials are disclosed that while specific reference of each and every combination and permutation of these compounds may not be explicitly made, each is specifically contemplated and described herein. For example, if an adjunct component is disclosed and discussed, and a number of alternative actual forms of the component are discussed, each and every combination and permutation of the adjunct component and the actual forms that are possible is specifically contemplated unless specifically indicated to the contrary. This concept applies to all aspects of this application, including but not limited to steps in methods of making and using the disclosed compositions. Thus, if there are a plurality of additional steps that can be performed it is understood that each of these additional steps can be performed by any specific embodiment or combination of embodiments of the disclosed methods, and that each such combination is specifically contemplated and should be considered disclosed.

In this specification and in the claims which follow, reference will be made to a number of terms which shall be defined to have the following meanings:

it must be noted that, as used in this specification and the appended claims, the singular forms "a," "an," and "the" include both one and more than one (i.e., two, including two) unless the context clearly dictates otherwise. Thus, for example, reference to "a pH adjuster as described" can include a single pH adjuster, or a mixture of two or more pH adjusters, and the like.

"optional" or "optionally" means that the subsequently described event or circumstance may or may not occur, and that the description includes instances where said event or circumstance occurs and instances where it does not. For example, the phrase "optional adjunct component" means that the adjunct component can or can not be present, and the description covers both situations where the adjunct component is included in the composition and where the adjunct component is not included in the composition.

Unless otherwise indicated, numerical ranges in this application are approximate and thus may include values outside of the ranges. Ranges of values can be expressed herein as from "about" one particular value, and/or to "about" another particular value. When such a range is expressed, it includes from the one particular value and/or to the other particular value. Similarly, when a particular value is expressed as an approximation by the use of the antecedent "about," it should be understood that it encompasses the particular value itself as well as the error ranges allowable in the art as a result of measurement or calculation. It will be further understood that the endpoints of each of the numerical ranges are significant both in relation to the other endpoint, and independently of the other endpoint.

Reference in the specification and concluding claims to parts by weight of a particular element or component in a composition or article refers to the weight relationship between that element or component and any other elements or components in the composition or article, expressed as parts by weight. Thus, in a composition comprising 2 parts by weight of component X and 5 parts by weight of component Y, X and Y are present in a weight ratio of 2:5 and are present in this ratio regardless of whether additional components are included in the composition.

Unless the context clearly dictates otherwise, or there is other meaning, or implicit based on the context or conventional manner in the art, all parts and percentages referred to herein are by weight and the weight percentages of a component are based on the total weight of the composition or product in which the component is included.

Reference throughout this application to "comprising," "including," "having," and similar language is not intended to exclude the presence of any optional components, steps or procedures, whether or not any optional components, steps or procedures are specifically disclosed. For the avoidance of any doubt, unless stated to the contrary, all methods claimed through use of the term "comprising" may include one or more additional steps, apparatus parts or components and/or materials. In contrast, the term "consisting of … …" excludes any component, step, or procedure not specifically recited or recited. Unless otherwise specified, the term "or" refers to the listed members individually as well as in any combination.

Furthermore, the contents of any referenced patent or non-patent document in this application are incorporated by reference in their entirety, especially with respect to definitions disclosed in the art (where not inconsistent with any definitions specifically provided herein) and general knowledge.

Detailed Description

The following examples are put forth so as to provide those of ordinary skill in the art with a complete disclosure and description of how the compounds, compositions, articles, devices, and/or methods described and claimed herein are made and evaluated, and are intended to be purely exemplary and are not intended to limit the scope of what applicants regard as their invention. Efforts have been made to ensure accuracy with respect to numbers (e.g., amounts, temperature, etc.) but some errors and deviations should be accounted for. Unless otherwise indicated, parts are parts by weight, temperatures are in degrees Celsius or at ambient temperature, and pressures are at or near atmospheric. There are many variations and combinations of reaction conditions (e.g., component concentrations, desired solvents, solvent mixtures, temperatures, pressures, and other reaction ranges) and conditions that can be used to optimize the purity and yield of the product obtained by the process. Only reasonable routine experimentation will be required to optimize such process conditions.

Example 1:

100mL of a mixed solution A of zinc nitrate and ferric nitrate was prepared with deionized water, wherein the molar ratio of zinc ions to iron ions was 2. Then 100mL of sodium carbonate solution B was prepared. Adding the solution A and the solution B into a reactor dropwise under continuous stirring; then adding a proper amount of sodium hydroxide solution with the concentration of 2mol/L to keep the pH value of the solution to be 9.5 in the precipitation process; after the precipitation is completed, the precipitate is aged in mother liquor at 55 ℃ overnight; and filtering and separating the precipitate, washing with water for several times, and drying at 100 ℃ for 12h to obtain the hydrotalcite-like precursor.

Bi in an amount of 6.5 wt% based on the weight of the catalyst as active component in the final catalyst₂O₃: KOH (weight ratio) 1: 2, preparing the impregnation liquid of bismuth nitrate and potassium hydroxide, wherein the concentration of bismuth ions is 0.2mol/L, and the concentration of KOH is 0.5 mol/L. Then adding zinc-aluminum hydrotalcite precursor and carrying out wet impregnation. The filter cake was then obtained by filtration and washed with water. Freeze-drying the filter cake, then placing the filter cake into a muffle furnace to be roasted under air atmosphere, firstly heating the dried product from room temperature to 200 ℃ at the heating rate of 8 ℃/min, preserving the heat for 2h, then continuously heating to 400 ℃ at the heating rate of 8 ℃/min, roasting at the temperature for 8h, and naturally cooling to room temperature after roasting is finished, thereby preparing the catalyst A.

Example 2

100mL of a mixed solution A of zinc nitrate and ferric nitrate was prepared with deionized water, wherein the molar ratio of zinc ions to iron ions was 4. Then 100mL of sodium carbonate solution B was prepared. Adding the solution A and the solution B into a reactor dropwise under continuous stirring; then adding a proper amount of sodium hydroxide solution with the concentration of 2mol/L to keep the pH value of the solution in the precipitation process at 10.5; after the precipitation is completed, the precipitate is aged in mother liquor at 65 ℃ overnight; and filtering and separating the precipitate, washing with water for several times, and drying at 100 ℃ for 12h to obtain the hydrotalcite-like precursor.

Bi in an amount of 9.5 wt% based on the weight of the catalyst as active component in the final catalyst₂O₃: KOH (weight ratio) 1: and 4, preparing an impregnation liquid of bismuth nitrate and potassium hydroxide, wherein the concentration of bismuth ions is 0.8mol/L, and the concentration of KOH is 1.8 mol/L. Then adding zinc-aluminum hydrotalcite precursor and carrying out wet impregnation. The filter cake was then obtained by filtration and washed with water. Freeze-drying the filter cake, then placing the filter cake into a muffle furnace to be roasted under air atmosphere, firstly heating the dried product from room temperature to 250 ℃ at the heating rate of 12 ℃/min, preserving the heat for 1h, then continuously heating to 550 ℃ at the heating rate of 12 ℃/min, roasting at the temperature for 3h, and naturally cooling to room temperature after roasting is finished, thereby preparing the catalyst B.

Example 3

100mL of a mixed solution A of zinc nitrate and ferric nitrate was prepared with deionized water, wherein the molar ratio of zinc ions to iron ions was 3. Then 100mL of sodium carbonate solution B was prepared. Adding the solution A and the solution B into a reactor dropwise under continuous stirring; then adding a proper amount of sodium hydroxide solution with the concentration of 2mol/L to keep the pH value of 10 in the precipitation process; after the precipitation is completed, the precipitate is aged in mother liquor at 60 ℃ overnight; and filtering and separating the precipitate, washing with water for several times, and drying at 100 ℃ for 12h to obtain the hydrotalcite-like precursor.

Bi in an amount of 7 wt% based on the weight of the active component in the final catalyst₂O₃: KOH (weight ratio) 1: 3 preparing the impregnation liquid of bismuth nitrate and potassium hydroxide, wherein the concentration of bismuth ions is 0.5mol/L, and the concentration of KOH is 1.2 mol/L. Then adding zinc-aluminum hydrotalcite precursor and carrying out wet impregnation. The filter cake was then obtained by filtration and washed with water. Freeze drying the filter cake, roasting in a muffle furnace under air atmosphere, heating the dried product from room temperature to 220 deg.C at a heating rate of 10 deg.C/min, maintaining the temperature for 1.5 hr, and heating at a heating rate of 10 deg.C/minAnd roasting at 450 ℃ for 4 hours, and naturally cooling to room temperature after roasting is finished, thereby preparing the catalyst C.

Comparative example 1

The preparation process is basically the same as that of example 3, except that: the active component is only KOH.

Comparative example 2

The preparation process is basically the same as that of example 3, except that: the active component is only Bi₂O₃。

Comparative example 3

The preparation process is basically the same as that of example 3, except that: after the hydrotalcite-like precursor is prepared, under the same roasting condition with the subsequent roasting condition, the hydrotalcite-like precursor is roasted to an oxide carrier and then loaded with an active component.

Comparative example 4

The preparation process is basically the same as that of example 3, except that: the filter cake after loading the active component is dried by a common drying mode (drying at 100 ℃ for 12 h).

Comparative example 5

The preparation process is basically the same as that of example 3, except that: the impregnation process was changed to dry impregnation (isovolumetric impregnation).

Comparative example 6

The preparation process is basically the same as that of example 3, except that: directly heating the dried product from room temperature to 450 ℃ at a heating rate of 10 ℃/min during roasting (the middle section heat preservation process is eliminated).

Test for catalytic Performance

The catalytic performance of the catalysts prepared in examples 1 to 3 and comparative examples 1 to 6, respectively, was tested under the reaction condition a, and the test results are shown in table 1, wherein the stability and lifetime were evaluated based on the number of times of reuse, which is the number of times that the catalyst can be recycled with its activity and selectivity substantially unchanged (the magnitude of the decrease in activity and selectivity is less than 10% compared to the initial activity and selectivity).

The reaction conditions a of the catalyst used for catalyzing the synthesis of dimethyl carbonate from Ethylene Carbonate (EC) and methanol ester through ester exchange reaction are as follows: the reaction temperature is 60 ℃, the reaction time is 4 hours, the molar ratio of the methanol to the ethylene carbonate is 10, and the dosage of the catalyst is 5 percent of the weight of the ethylene carbonate; the product was analyzed by a gas chromatography thermal conductivity cell detector.

In addition, the catalyst of example 3 was also tested for performance under reaction conditions b: the reaction temperature is 55 ℃, the reaction time is 4h, the molar ratio of the methanol to the ethylene carbonate is 10, and the dosage of the catalyst is 4.5 percent of the weight of the ethylene carbonate.

TABLE 1 catalyst Performance test results

As can be seen from the test results in table 1, in the production process of the present application, since the catalyst composed of the active component having a specific composition and the carrier is used, a high DMC yield can be achieved under mild reaction conditions, and since in the catalyst preparation process, the acting force of each component in the catalyst and the carrier is moderate by specific selection and control of the loading timing, impregnation process, drying manner and calcination condition of the active component, the catalyst has good stability and a long service life, thereby greatly reducing the production cost of the production process for synthesizing dimethyl carbonate and improving the economy thereof.

Throughout this application, various publications are referenced. The disclosures of these publications in their entireties are hereby incorporated by reference into this application in order to more fully describe the compounds, compositions, and methods described herein.

Various modifications and changes can be made to the compounds, compositions, and methods described herein. Other aspects of the compounds, compositions, and methods described herein will be apparent from consideration of the specification and practice of the compounds, compositions, and methods disclosed herein. It is intended that the specification and examples be considered as exemplary.

It should be understood that the above examples are only for clarity of illustration and are not intended to limit the embodiments. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. And obvious variations or modifications therefrom are within the scope of the invention.

Claims

1. A process for synthesizing dimethyl carbonate by ester exchange method features that the catalyst used is composed of 6-10wt% of active component and the rest of carrier, and the active component is Bi₂O₃And KOH, Bi₂O₃The weight ratio of KOH to KOH is 1: 2-4; the carrier is zinc-iron composite metal oxide.

2. The process according to claim 1, wherein the support is prepared by calcining a hydrotalcite-like precursor having the general formula: [ Zn ]²⁺ _1-xFe³⁺ _x(OH)₂]^x+(CO₃ ^2-)_x/2·nH₂O, wherein x is more than or equal to 0.2 and less than or equal to 0.33, and n is more than or equal to 1 and less than or equal to 10.

3. The production process according to claim 1 or 2, wherein the content of the active component is 6 to 8 wt% based on the total weight of the catalyst; in the general formula, x is more than or equal to 0.25 and less than or equal to 0.33.

4. The production process according to claim 1, wherein the catalyst is prepared by a method comprising the steps of:

3) adding the hydrotalcite-like precursor obtained in the step 1) into the impregnation liquid prepared in the step 2), and performing wet impregnation; then filtering or centrifugally separating to obtain a filter cake, and washing;

5. The production process according to claim 4, wherein the hydrotalcite-like precursor in step 1) is prepared by a co-precipitation method, comprising the following steps:

b) dropwise adding the mixed solution prepared in the step a) and a sodium carbonate solution into a reactor under continuous stirring; then adding sodium hydroxide solution to keep the pH value of the solution at 9.5-10.5 during the precipitation process;

d) and filtering, separating, washing and drying the precipitate to obtain the hydrotalcite-like precursor.

6. The production process according to claim 4, wherein the concentration of bismuth ions in the impregnation liquid in the step 2) is 0.1-1 mol/L; the KOH concentration is 0.5-2 mol/L.

7. The production process according to claim 4, wherein the roasting process in the step 4) is as follows: heating the dried product from room temperature to 200-250 ℃ at the heating rate of 5-15 ℃/min, preserving the heat for 1-2h, then continuously heating to 400-550 ℃ at the heating rate of 5-15 ℃/min, roasting at the temperature for 3-8h, and then cooling to room temperature.

8. The production process according to claim 4, wherein a shaping step is introduced after step 4).

9. The process according to claim 1, wherein the reaction conditions are: the reaction temperature is 55-100 ℃, the molar ratio of the methanol to the ethylene carbonate is 8-12, and the dosage of the catalyst is 1-5% of the weight of the ethylene carbonate.

10. The production process according to claim 9, wherein the reaction temperature is 55-80 ℃, the molar ratio of methanol to ethylene carbonate is 8-10, and the amount of the catalyst is 2-4.5% of the weight of the ethylene carbonate.