Ethylene carbonate and polyurethane chain extender joint production device

Abstract

The utility model discloses an ethylene carbonate and polyurethane chain extender joint production device which comprises a device main body, and the device main body comprises a first raw material transportation unit, an ethylene carbonate reactor, a film evaporator, a second raw material transportation unit, a polyurethane chain extender reactor and a crystallization kettle. According to the design of the joint production device, recycling of materials is fully considered, and the product structure can be flexibly adjusted when market conditions change by adjusting the production proportion of ethylene carbonate and the polyurethane chain extender, so that competitiveness is kept, and high economic benefits are achieved. In addition, due to the closed-loop characteristic of the joint production device, the influence on the environment is reduced, the utilization rate of raw materials is increased, and the double advantages of economy, high efficiency and environment friendliness are reflected.

Description

TECHNICAL FIELD

[0001] The utility model relates to chemical production device process technical field, concretely relates to a kind of ethylene carbonate, polyurethane chain extender combined production device. BACKGROUND

[0002] Ethylene carbonate (EC), melting point is 35 ℃~38 ℃, solid at room temperature, is an important organic solvent and chemical intermediate, mainly as solvent or synthetic VC and FEC additive is applied to lithium ion battery electrolyte industry, also can be used as synthetic DMC in polycarbonate industry.

[0003] The existing invention patent CN106478583A, CN106478586A etc. about ethylene carbonate synthesis all propose to solve the technical problems such as that reaction heat is not removed in time, epoxide conversion rate is not high, product purity cannot meet the requirements of electronic grade products etc.;Invention patent CN107915708A, CN107915710A etc. solve the problems of low activity of basic catalyst for ethylene carbonate production and easy deactivation from the angle of basic catalyst preparation.;The technical scheme proposed by invention patent CN110437201A mainly solves the problem of absorbing ethylene oxide not participating in the reaction process and converting coupling production of ethylene carbonate. The above technical schemes accelerate the technical upgrading process of equipment, process and basic catalyst in the reaction process, but do not make more optimization to the recovery of basic catalyst, and the technical upgrading increases the investment of single ethylene carbonate product, and the multiple influences of macroeconomic, industry competition pattern, market supply and demand relationship and raw material cost, the price of ethylene carbonate is lower than the production cost in a certain period, which leads to the reduction of production of enterprises, thereby affecting the operating rate. Therefore, it is urgent to develop new technology

[0004] Meanwhile, the research and development of cyclic carbonate as a raw material for synthesizing polymer materials has also attracted the attention of technical personnel due to the influence of the price of ethylene carbonate. For example, in the field of polyurethane chain extender materials, cyclic carbonate can provide a cheap and effective raw material for the synthesis of chain extenders, replacing ethylene oxide, which has high safety risks and high costs for environmental disposal. For example, invention patent CN113501933 A proposes mixing ethylene carbonate and hexanediamine and reacting under vacuum until no bubbles are generated to prepare polyurethane chain extender 1,6-di(2-hydroxy-ethoxycarbonyl amine)hexane (DHDU); invention patents CN115850032A and CN101244989A propose using ethylene oxide, hydroquinone, water, alkaline catalysts, and other reactions to prepare polyurethane chain extender hydroquinone dihydroxyethyl ether (HQEE). The above products can be used as cross-linking agents for mixing type, pouring type, and thermoplastic polyurethane elastomers, which can improve the stability of the products and improve various physical property indicators such as tear strength, heat resistance, hardness, elasticity, and compression deformation. However, the CO2 gas generated during the preparation process is not effectively used, or the use of high-risk ethylene oxide and alkaline catalysts also fails to recycle.

[0005] Therefore, there is an urgent need to develop a combined production device and process for ethylene carbonate and polyurethane chain extender to address the shortcomings of existing technology. Practical new type content

[0006] In view of the above problems, the present application discloses a combined production device for ethylene carbonate and polyurethane chain extender, which fully considers the recycling of materials and adjusts the production ratio of ethylene carbonate and polyurethane chain extender to flexibly adjust the product structure when market conditions change, thereby maintaining competitiveness and achieving high economic benefits. In addition, the closed-loop characteristics of the combined production device reduce the impact on the environment and improve the utilization rate of raw materials, embodying the dual advantages of economic efficiency and environmental friendliness.

[0007] In order to achieve the above object, the utility model provides a kind of ethylene carbonate, polyurethane chain extender combined production device, including device main body, device main body includes first raw material transport unit, ethylene carbonate reactor, film evaporator, second raw material transport unit, polyurethane chain extender reactor and crystallization kettle, the outlet end of first raw material transport unit is communicated with the inlet end of ethylene carbonate reactor, the outlet end of ethylene carbonate reactor is communicated with the inlet end of film evaporator, film evaporator includes first liquid phase outlet end and first gas phase outlet end, first liquid phase outlet end is communicated with the first inlet end of polyurethane chain extender reactor, and first gas phase outlet end is used to extract ethylene carbonate;The outlet end of second raw material transport unit is communicated with the second inlet end of polyurethane chain extender reactor, and polyurethane chain extender reactor includes second liquid phase outlet end and second gas phase outlet end, crystallization kettle includes third liquid phase outlet end and fourth liquid phase outlet end, second liquid phase outlet end is communicated with the inlet end of crystallization kettle, second gas phase outlet end and third liquid phase outlet end are all communicated with the inlet end of ethylene carbonate reactor, and fourth liquid phase outlet end is used to extract polyurethane chain extender.

[0008] Compared with prior art, the production device of the utility model can realize the combined production of ethylene carbonate and polyurethane chain extender in the same production device.The film evaporator of the utility model is provided with first liquid phase outlet end and first gas phase outlet end, and the first gas phase outlet end can extract part of ethylene carbonate to realize the production of ethylene carbonate product, and the first liquid phase outlet end is communicated with the first inlet end of polyurethane chain extender, so that the basic catalyst and the ethylene carbonate not extracted can enter the polyurethane chain extender reactor as production raw materials.The above-mentioned setting can realize the adjustment of the production ratio of ethylene carbonate and polyurethane chain extender by adjusting the extraction amount of ethylene carbonate, and then the product structure can be flexibly adjusted when market conditions change, to maintain competitiveness and achieve high economic efficiency.Meanwhile, the second gas phase outlet end in the polyurethane chain extender reactor and the third liquid phase outlet end in the crystallization kettle are both communicated with the inlet end of ethylene carbonate reactor, and such setting can realize the recycling of carbon dioxide, basic catalyst and unreacted ethylene carbonate.In summary, the combined production device of the utility model fully considers the recycling of materials, has closed-loop characteristics, reduces the impact on the environment, improves the utilization rate of raw materials, and embodies the dual advantages of economic efficiency and environmental friendliness.

[0009] As a preferred technical scheme, the first raw material transport unit of the utility model includes ethylene oxide conveying pipe, carbon dioxide conveying pipe and basic catalyst conveying pipe, and the ethylene oxide conveying pipe, carbon dioxide conveying pipe and basic catalyst conveying pipe are respectively communicated with the inlet end of ethylene carbonate reactor by pipeline.

[0010] As a preferred technical scheme, the second raw material conveying unit comprises a functional monomer conveying pipe, and the functional monomer conveying pipe is communicated with the second inlet end of the polyurethane chain extender reactor.

[0011] As a preferred technical scheme, the second gas phase outlet end and the inlet end of the ethylene carbonate reactor are further provided with a compression device, so that the carbon dioxide is pressurized and liquefied for recycling.

[0012] As a preferred technical scheme, the compression device is a carbon dioxide compressor.

[0013] As a preferred technical scheme, the first liquid phase outlet end and the polyurethane chain extender reactor are communicated by a pipeline.

[0014] As a preferred technical scheme, the first gas phase outlet end and the third liquid phase outlet end are both communicated with the inlet end of the ethylene carbonate reactor by a pipeline.

[0015] As a preferred technical scheme, the inlet end of the ethylene carbonate reactor is arranged at one side of the bottom of the ethylene carbonate reactor, and the outlet end of the ethylene carbonate reactor is arranged at one side of the top of the ethylene carbonate reactor.

[0016] As a preferred technical scheme, the first gas phase outlet end is arranged at the top of the thin film evaporator, and the first liquid phase outlet end is arranged at the bottom of the thin film evaporator.

[0017] As a preferred technical scheme, the second gas phase outlet end is arranged at one side of the top of the polyurethane chain extender reactor, and the second liquid phase outlet end is arranged at the bottom of the polyurethane chain extender reactor.

[0018] The utility model also provides a kind of ethylene carbonate, polyurethane chain extender combined production process, using the ethylene carbonate, polyurethane chain extender combined production device described above, comprising steps:

[0019] (1) ethylene oxide, carbon dioxide, basic catalyst enter ethylene carbonate reactor according to certain proportion and carry out reaction, and finished mixture enters thin film evaporator and is handled to extract part ethylene carbonate;

[0020] (2) remaining part ethylene carbonate, basic catalyst, functional monomer raw material enter polyurethane chain extender reactor and carry out reaction, and the carbon dioxide generated enters ethylene carbonate reactor and is recycled, and polyurethane chain extender, basic catalyst and unreacted ethylene carbonate enter crystallization kettle, first cooling treatment is carried out to make polyurethane chain extender crystallize, and basic catalyst and ethylene carbonate enter ethylene carbonate reactor and are recycled, and then heating treatment is carried out to extract polyurethane chain extender.

[0021] As a preferred technical solution, in step (1), the reaction temperature is 100-200℃, and the reaction pressure is 4-10 MPa.

[0022] As a preferred technical solution, in step (1), the processing temperature of the thin film evaporator is 100-200℃, and the processing pressure is 1-10 kPa.

[0023] As a preferred technical solution, in step (2), the reaction temperature is 100-200℃, and the reaction pressure is 100-101.325 kPa.

[0024] As a preferred technical solution, in step (2), the temperature of the cooling treatment is 40-95℃.

[0025] As a preferred technical solution, in step (2), the temperature of the heating treatment is 98-110℃.

[0026] As a preferred technical solution, the basic catalyst is selected from tetrabutylammonium bromide or ionic liquid,

[0027] As a preferred technical solution, the functional monomer raw material is selected from hydroquinone or hexanediamine.

[0028] As a preferred technical solution, the recovery amount of carbon dioxide accounts for 0-5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amounts.

[0029] As a preferred technical solution, the recovery amount of the basic catalyst accounts for 0-5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amounts. BRIEF DESCRIPTION OF DRAWINGS

[0030] Figure 1 The utility model discloses a combined production device for ethylene carbonate and polyurethane chain extender.

[0031] Element symbol explanation: 100 - device main body, 10 - first raw material transport unit, 11 - ethylene oxide conveying pipe, 12 carbon dioxide conveying pipe, 13 - basic catalyst conveying pipe, 20 - ethylene carbonate reactor, 30 - thin film evaporator, 31 - first liquid phase outlet end, 32 - first gas phase outlet end, 40 - second raw material transport unit, 41 - functional monomer conveying pipe, 50 - polyurethane chain extender reactor, 51 - second liquid phase outlet end, 52 - second gas phase outlet end, 60 - crystallization kettle, 61 - third liquid phase outlet end, 62 - fourth liquid phase outlet end, 70 - compression device. DETAILED DESCRIPTION

[0032] The utility model discloses a combined production device for ethylene carbonate and polyurethane chain extender, which comprisesFigure 1 As shown, the device body 100 includes a first raw material conveying unit 10, an ethylene carbonate reactor 20, a thin film evaporator 30, a second raw material conveying unit 40, a polyurethane chain extender reactor 50, and a crystallization kettle 60.

[0033] The first raw material conveying unit 10 is configured to convey reaction raw materials to the ethylene carbonate reactor. The outlet end (not shown in the figure) of the first raw material conveying unit 10 is in communication with the inlet end (not shown in the figure) of the ethylene carbonate reactor 20. In the present application, the first raw material conveying unit 10 includes an ethylene oxide conveying pipe 11, a carbon dioxide conveying pipe 12, and an alkaline catalyst conveying pipe 13. The ethylene oxide conveying pipe 11, the carbon dioxide conveying pipe 12, and the alkaline catalyst conveying pipe 13 are respectively in communication with the inlet end of the ethylene carbonate reactor 20 by means of pipes. In some embodiments, the output ends of the ethylene oxide conveying pipe 11, the carbon dioxide conveying pipe 12, and the alkaline catalyst conveying pipe 13 are respectively welded and connected to the inlet end of the ethylene carbonate reactor 20 by means of pipes.

[0034] The ethylene carbonate reactor 20 is a place where ethylene oxide, carbon dioxide, and alkaline catalysts react to synthesize ethylene carbonate. The ethylene carbonate reactor 20 can be a high-pressure reactor. The outlet end (not shown in the figure) of the ethylene carbonate reactor 20 is in communication with the inlet end (not shown in the figure) of the thin film evaporator 30 to convey the finished product mixture to the thin film evaporator 30 for processing. In some embodiments, the outlet end of the ethylene carbonate reactor 20 is in communication with the inlet end of the thin film evaporator 30 by means of pipes. In some embodiments, the inlet end of the ethylene carbonate reactor 20 is arranged at one side of the bottom of the ethylene carbonate reactor 20, and the outlet end of the ethylene carbonate reactor 20 is arranged at one side of the top of the ethylene carbonate reactor 20. Such an arrangement can increase the contact time of ethylene oxide, carbon dioxide, and alkaline catalysts in the reaction system, making the reaction more complete, effectively improving the conversion rate of the product, and facilitating the output of the finished product mixture, thereby effectively improving the production efficiency.

[0035] The thin film evaporator 30 is used to evaporate the product mixture output from the ethylene carbonate reactor 20 to extract part of the product ethylene carbonate, and to deliver the catalyst and the remaining part of the ethylene carbonate as a reaction raw material to the polyurethane chain extender reactor for reaction. The thin film evaporator 30 comprises a first liquid phase outlet end 31 and a first gas phase outlet end 32, the first liquid phase outlet end 31 is in communication with the first inlet end (not marked in the figure) of the polyurethane chain extender reactor 50, and the first gas phase outlet end 32 is used to extract ethylene carbonate, which can be refined in a rectification device (not shown in the figure) to obtain electronic-grade ethylene carbonate or industrial-grade ethylene carbonate. In some embodiments, the first liquid phase outlet end 31 is in communication with the first inlet end of the polyurethane chain extender reactor 50 by a pipeline. In some embodiments, the inlet end of the thin film evaporator 30 is arranged at the top of the thin film evaporator, the first gas phase outlet end 32 is arranged at one side of the top of the thin film evaporator 30, and the first liquid phase outlet end 31 is arranged at the bottom of the thin film evaporator 30.

[0036] The second raw material transportation unit 40 is used to deliver the functional monomer raw material to the polyurethane chain extender reactor. The outlet end (not marked in the figure) of the second raw material transportation unit 40 is in communication with the second inlet end (not marked in the figure) of the polyurethane chain extender reactor 50. In the present application, the second raw material transportation unit 40 comprises a functional monomer delivery pipe 41, which is in communication with the second inlet end of the polyurethane chain extender reactor 50, and in some embodiments, the functional monomer delivery pipe 41 is welded to the second inlet end of the polyurethane chain extender reactor 50.

[0037] The polyurethane chain extender reactor 50 is a place for the functional monomer raw material, the alkaline catalyst and the ethylene carbonate to react and synthesize the polyurethane chain extender, the alkaline catalyst and the ethylene carbonate are output from the first liquid phase outlet end 31 of the thin film evaporator 30 and enter the polyurethane chain extender reactor 50 through the first inlet end of the polyurethane chain extender reactor 50, the functional monomer raw material is output through the functional monomer conveying pipe 41 and enters the polyurethane chain extender reactor 50 through the second inlet end of the polyurethane chain extender reactor 50, after the above-mentioned raw materials enter the polyurethane chain extender reactor 50, carbon dioxide and the polyurethane chain extender are generated by reaction. The polyurethane chain extender reactor 50 comprises a second liquid phase outlet end 51 and a second gas phase outlet end 52, the second gas phase outlet end 52 is communicated with the inlet end of the ethylene carbonate reactor 20, so that the carbon dioxide is transported into the ethylene carbonate reactor 20 for recycling. The second gas phase outlet end 52 and the inlet end of the ethylene carbonate reactor 20 are also provided with a compression device 70, so that the carbon dioxide is first pressurized and liquefied and then transported to the inlet end of the ethylene carbonate reactor for recycling. In the utility model, the compression device can be a carbon dioxide compressor. The second liquid phase outlet end 51 of the utility model is communicated with the inlet end (not marked in the figure) of the crystallization kettle 60, so that the polyurethane chain extender product, the alkaline catalyst and the unreacted ethylene carbonate are transported into the crystallization kettle 60 for treatment. In some embodiments, the first inlet end and the second inlet end of the polyurethane chain extender reactor 50 are arranged at the top of the polyurethane chain extender reactor 50, the second gas phase outlet end 52 is arranged at the top of the polyurethane chain extender reactor 50, and the second liquid phase outlet end 51 is arranged at the bottom of the polyurethane chain extender reactor 50. In some embodiments, the second gas phase outlet end 52 and the inlet end of the ethylene carbonate reactor 20 are communicated by a pipeline, and the second liquid phase outlet end 51 and the inlet end of the crystallization kettle 60 are communicated by a pipeline.

[0038] The crystallization kettle 60 is used for separating the polyurethane chain extender product, the alkaline catalyst and the unreacted ethylene carbonate input from the polyurethane chain extender reactor. The crystallization kettle 60 comprises a third liquid phase outlet end 61 and a fourth liquid phase outlet end 62, the third liquid phase outlet end 61 is communicated with the inlet end of the ethylene carbonate reactor 20, so that the alkaline catalyst and the ethylene carbonate are transported into the ethylene carbonate reactor 20 for recycling. The fourth liquid phase outlet end 62 is used for extracting the polyurethane chain extender, and the extracted polyurethane chain extender can be further refined to obtain a polyurethane chain extender product with higher purity. In some embodiments, the inlet end of the crystallization kettle 60 is arranged at the top of the crystallization kettle 60, and the third liquid phase outlet end 61 and the fourth liquid phase outlet end 62 are arranged at the bottom of the crystallization kettle. In some embodiments, the third liquid phase outlet end 61 and the inlet end of the ethylene carbonate reactor 20 are communicated by a pipeline.

[0039] The utility model discloses still provide a kind of ethylene carbonate, polyurethane chain extender combined production process, using the ethylene carbonate, polyurethane chain extender combined production device described above, including steps:

[0040] (1) ethylene oxide, carbon dioxide, basic catalyst enters ethylene carbonate reactor according to certain proportion and carries out reaction, product mixture enters film evaporator and is handled to extract part ethylene carbonate;

[0041] (2) remaining part ethylene carbonate, basic catalyst, functional monomer raw material enter polyurethane chain extender reactor and carry out reaction, generated carbon dioxide enters ethylene carbonate reactor and is recycled, polyurethane chain extender, basic catalyst and unreacted ethylene carbonate enter crystallization kettle, first cooling treatment is carried out to make polyurethane chain extender crystallize, basic catalyst and ethylene carbonate enter ethylene carbonate reactor and are recycled, then heating treatment is carried out to extract polyurethane chain extender.

[0042] Basic catalyst is selected from ionic liquid, and the ionic liquid can be imidazole ionic liquid, pyridine ionic liquid, quaternary ammonium ionic liquid and quaternary phosphonium ionic liquid, preferably, basic catalyst is selected from quaternary ammonium ionic liquid, more preferably, basic catalyst is tetrabutylammonium bromide. The temperature of reaction is 100 DEG C to 200 DEG C, in some embodiments, the temperature of reaction is 150 DEG C to 200 DEG C, in some embodiments, the temperature of reaction is 200 DEG C. As an example, the temperature of reaction can be but not limited to 100 DEG C, 110 DEG C, 120 DEG C, 130 DEG C, 140 DEG C, 150 DEG C, 160 DEG C, 170 DEG C, 180 DEG C, 190 DEG C, 200 DEG C. The pressure of reaction is 4MPa to 10MPa, as an example, the pressure of reaction can be but not limited to 4MPa, 5MPa, 6MPa, 7MPa, 8MPa, 9MPa, 10MPa.

[0043] The processing temperature of film evaporator is 100 DEG C to 200 DEG C, as an example, the processing temperature can be but not limited to 100 DEG C, 110 DEG C, 120 DEG C, 130 DEG C, 140 DEG C, 150 DEG C, 160 DEG C, 170 DEG C, 180 DEG C, 190 DEG C, 200 DEG C. Processing pressure is 1kPa to 10kpa, as an example, the processing pressure can be but not limited to 1kpa, 2kpa, 3kpa, 4kpa, 5kpa, 6kpa, 7kpa, 8kpa, 9kpa, 10kpa.

[0044] The extraction amount of the partial ethylene carbonate accounts for 0% to 100% of the total amount of the ethylene carbonate, for example, the extraction amount of the partial ethylene carbonate accounts for 0%, 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, 100% of the total amount of the ethylene carbonate, but is not limited thereto, and other values not listed in the range of the utility model are also applicable.

[0045] The functional monomer raw material is selected from hydroquinone or hexanediamine. The reaction temperature is 100-200 DEG C, in some embodiments, the reaction temperature is 150-200 DEG C, in some embodiments, the reaction temperature is 200 DEG C. For example, the reaction temperature can be but is not limited to 100 DEG C, 110 DEG C, 120 DEG C, 130 DEG C, 140 DEG C, 150 DEG C, 160 DEG C, 170 DEG C, 180 DEG C, 190 DEG C, 200 DEG C. The reaction pressure is 100-101.325 kpa.

[0046] The temperature of the cooling treatment is 40-95 DEG C, for example, the temperature of the cooling treatment can be but is not limited to 40 DEG C, 50 DEG C, 60 DEG C, 70 DEG C, 80 DEG C, 90 DEG C, 95 DEG C. The temperature of the heating treatment is 98-110 DEG C, for example, the temperature of the heating treatment can be but is not limited to 98 DEG C, 99 DEG C, 100 DEG C, 101 DEG C, 102 DEG C, 103 DEG C, 104 DEG C, 105 DEG C, 106 DEG C, 107 DEG C, 108 DEG C, 109 DEG C, 110 DEG C.

[0047] The recovery amount of the carbon dioxide accounts for 0-5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amount, for example, the recovery amount of the carbon dioxide accounts for 0%, 1%, 2%, 3%, 4%, 5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amount, but is not limited thereto, and other values not listed in the range of the utility model are also applicable. The recovery amount of the basic catalyst accounts for 0-5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amount, for example, the recovery amount of the basic catalyst accounts for 0%, 1%, 2%, 3%, 4%, 5% of the sum of the ethylene oxide, carbon dioxide and basic catalyst feed amount, but is not limited thereto, and other values not listed in the range of the utility model are also applicable.

[0048] In order to better illustrate the purpose, technical scheme and beneficial effects of the utility model, the following will be further described with specific examples. It should be noted that the following examples are further explanations of the utility model and should not be regarded as limitations of the utility model.

[0049] Example 1

[0050] The embodiment provides a combined production process of ethylene carbonate and polyurethane chain extender, and comprises the following steps:

[0051] 2756 kg / h of ethylene oxide, 3380 kg / h of carbon dioxide and 26 kg / h of tetrabutylammonium bromide are respectively introduced into the ethylene carbonate reactor from the inlet end of the ethylene carbonate reactor, and the reaction is carried out under the conditions that the temperature is 200 DEG C and the pressure is 10 Mpa; the finished mixture is introduced into the thin film evaporator from the outlet end of the ethylene carbonate reactor, and the treatment is carried out under the conditions that the temperature is 130 DEG C and the pressure is 2 kpa; 99.8% of ethylene carbonate (the flow rate is 5541 kg / h) is obtained from the first gas phase outlet end, and further rectification is carried out to obtain electronic-grade ethylene carbonate product or industrial-grade ethylene carbonate product;

[0052] The tetrabutylammonium bromide and the remaining ethylene carbonate (the flow rate of tetrabutylammonium bromide is 26 kg / h, and the flow rate of ethylene carbonate is 174 kg / h) are introduced into the polyurethane chain extender reactor from the first liquid phase outlet end; hydroquinone (the flow rate is 53.75 kg / h) is introduced into the polyurethane chain extender reactor from the second inlet end, and the reaction is carried out under the condition that the temperature is 160 DEG C, so that carbon dioxide and hydroquinone dihydroxyethyl ether are obtained; the carbon dioxide (the flow rate is 43.0 kg / h) is output from the second gas phase outlet end and is recycled to the inlet end of the ethylene carbonate reactor after compression; the hydroquinone dihydroxyethyl ether, the tetrabutylammonium bromide and the ethylene carbonate (the flow rate of hydroquinone dihydroxyethyl ether is 96.75 kg / h, the flow rate of tetrabutylammonium bromide is 26 kg / h, and the flow rate of ethylene carbonate is 88 kg / h) are introduced into the crystallization kettle from the second liquid phase outlet end; the crystallization kettle is first cooled to 60 DEG C to make the hydroquinone dihydroxyethyl ether crystallize; the tetrabutylammonium bromide and the unreacted ethylene carbonate (the flow rate of tetrabutylammonium bromide is 25.85 kg / h, and the flow rate of ethylene carbonate is 87.5 kg / h) are output from the third liquid phase outlet end and are recycled to the inlet end of the ethylene carbonate reactor; then the crystallization kettle is heated to 110 DEG C to make the hydroquinone dihydroxyethyl ether melt; the hydroquinone dihydroxyethyl ether is obtained from the fourth liquid phase outlet end and is further refined to obtain hydroquinone dihydroxyethyl ether with a purity of 99.3%.

[0053] Embodiment 2

[0054] The embodiment provides a combined production process of ethylene carbonate and polyurethane chain extender, and comprises the following steps:

[0055] The 2756kg / h ethylene oxide, 3380kg / h carbon dioxide and 26kg / h tetrabutylammonium bromide are respectively introduced into the ethylene carbonate reactor from the inlet end of the ethylene carbonate reactor, and the reaction is carried out under the conditions of a temperature of 200℃ and a pressure of 10Mpa, and the product mixture is introduced into the thin film evaporator from the outlet end of the ethylene carbonate reactor, and the treatment is carried out under the conditions of a temperature of 130℃ and a pressure of 2kpa, and 99.8% of the ethylene carbonate (the flow rate is 5541kg / h) is collected from the first gas phase outlet end and is further rectified to obtain the electronic grade ethylene carbonate product or the industrial grade ethylene carbonate product;

[0056] The tetrabutylammonium bromide and the remaining part of the ethylene carbonate (the flow rate of the tetrabutylammonium bromide is 26kg / h, and the flow rate of the ethylene carbonate is 174kg / h) are introduced into the polyurethane chain extender reactor from the first liquid phase outlet end, the 1,6-hexanediamine (the flow rate is 56.68kg / h) is introduced into the polyurethane chain extender reactor from the second inlet end, and the reaction is carried out at a temperature of 160℃ to obtain carbon dioxide and 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane, the carbon dioxide (the flow rate is 43.0kg / h) is output from the second gas phase outlet end and is recycled to the inlet end of the ethylene carbonate reactor after being compressed, the 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane, the tetrabutylammonium bromide and the ethylene carbonate (the flow rate of the 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane is 96.75kg / h, the flow rate of the tetrabutylammonium bromide is 26kg / h, and the flow rate of the ethylene carbonate is 88kg / h) are introduced into the crystallization kettle from the second liquid phase outlet end; the crystallization kettle is first cooled to 60℃ to crystallize the 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane, the tetrabutylammonium bromide and the unreacted ethylene carbonate (the flow rate of the tetrabutylammonium bromide is 25.85kg / h, and the flow rate of the ethylene carbonate is 87.5kg / h) are output from the third liquid phase outlet end and are recycled to the inlet end of the ethylene carbonate reactor, and then the crystallization kettle is heated to 110℃ to melt the 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane, which is collected from the fourth liquid phase outlet end and is further refined to obtain the 1,6-bis(2-hydroxy-ethoxycarbonyl amine) hexane with a purity of 98.9%.

[0057] It is obvious for those skilled in the art that the present application is not limited to the details of the above exemplary embodiments, and the present application can be implemented in other specific forms without departing from the spirit or essential characteristics of the present application. Therefore, the embodiments should be regarded as exemplary and non-limiting, and the scope of the present application is defined by the appended claims rather than the above description, and all changes falling within the meaning and scope of the equivalent elements of the claims are intended to be included in the present application. Any reference signs in the claims should not be regarded as limiting the claims involved.

[0058] Furthermore, it should be understood that although the description is made according to the embodiments, not every embodiment contains only one independent technical solution, and the description is made in this way only for the sake of clarity, and the person skilled in the art should consider the description as a whole, and the technical solutions in each embodiment can also be combined appropriately to form other embodiments that the person skilled in the art can understand.

Claims

1. A combined production device of ethylene carbonate and polyurethane chain extender, comprising a device main body, characterized in that, The device body comprises a first raw material conveying unit, an ethylene carbonate reactor, a thin film evaporator, a second raw material conveying unit, a polyurethane chain extender reactor, and a crystallization kettle. The outlet end of the first raw material conveying unit is in communication with the inlet end of the ethylene carbonate reactor. The outlet end of the ethylene carbonate reactor is in communication with the inlet end of the thin film evaporator. The thin film evaporator comprises a first liquid phase outlet end and a first gas phase outlet end. The first liquid phase outlet end is in communication with the first inlet end of the polyurethane chain extender reactor. The first gas phase outlet end is used to extract ethylene carbonate. The outlet end of the second raw material conveying unit is in communication with the second inlet end of the polyurethane chain extender reactor. The polyurethane chain extender reactor comprises a second liquid phase outlet end and a second gas phase outlet end. The crystallization kettle comprises a third liquid phase outlet end and a fourth liquid phase outlet end. The second liquid phase outlet end is in communication with the inlet end of the crystallization kettle. The second gas phase outlet end and the third liquid phase outlet end are both in communication with the inlet end of the ethylene carbonate reactor. The fourth liquid phase outlet end is used to extract polyurethane chain extender.

2. The ethylene carbonate and polyurethane chain extender combined production apparatus according to claim 1, characterized by, The first raw material conveying unit comprises an ethylene oxide conveying pipe, a carbon dioxide conveying pipe, and an alkaline catalyst conveying pipe. The ethylene oxide conveying pipe, the carbon dioxide conveying pipe, and the alkaline catalyst conveying pipe are respectively in communication with the inlet end of the ethylene carbonate reactor by pipelines.

3. The ethylene carbonate and polyurethane chain extender combined production apparatus according to claim 1, characterized by, The second raw material conveying unit comprises a functional monomer conveying pipe. The functional monomer conveying pipe is in communication with the second inlet end of the polyurethane chain extender reactor.

4. The ethylene carbonate and polyurethane chain extender combined production apparatus according to claim 1, characterized by, A compression device is arranged between the second gas phase outlet end and the inlet end of the ethylene carbonate reactor, to pressurize and liquefy the carbon dioxide for recycling.

5. The ethylene carbonate and polyurethane chain extender combined production device according to claim 4, characterized by, The compression device is a carbon dioxide compressor.

6. The ethylene carbonate, polyurethane chain extender combined production device according to claim 1, characterized by, The first liquid phase outlet end is in communication with the polyurethane chain extender reactor by a pipeline.

7. The ethylene carbonate, polyurethane chain extender combined production device according to claim 1, characterized by, The first gas phase outlet end and the third liquid phase outlet end are both in communication with the inlet end of the ethylene carbonate reactor by pipelines.

8. The ethylene carbonate, polyurethane chain extender combined production device according to claim 1, characterized by, The inlet end of the ethylene carbonate reactor is arranged at one side of the bottom of the ethylene carbonate reactor. The outlet end of the ethylene carbonate reactor is arranged at one side of the top of the ethylene carbonate reactor.

9. The ethylene carbonate, polyurethane chain extender combined production device according to claim 1, characterized by, The first gas phase outlet end is arranged at the top of the thin film evaporator. The first liquid phase outlet end is arranged at the bottom of the thin film evaporator.

10. The ethylene carbonate, polyurethane chain extender combined production device according to claim 1, characterized by, The second gas phase outlet end is arranged at one side of the top of the polyurethane chain extender reactor. The second liquid phase outlet end is arranged at the bottom of the polyurethane chain extender reactor.

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