CN218686448U - Device for producing methyl ethyl carbonate by impinging stream ester exchange tubular reactor - Google Patents
Device for producing methyl ethyl carbonate by impinging stream ester exchange tubular reactor Download PDFInfo
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- CN218686448U CN218686448U CN202222767203.6U CN202222767203U CN218686448U CN 218686448 U CN218686448 U CN 218686448U CN 202222767203 U CN202222767203 U CN 202222767203U CN 218686448 U CN218686448 U CN 218686448U
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Abstract
The utility model relates to a device for producing methyl ethyl carbonate by an impinging stream ester exchange tubular reactor. The device comprises a batching tank, an impinging stream ester exchange tubular reactor, a rear ester exchange tower system, a light component removal tower system and a methyl ethyl carbonate rectifying tower system which are connected in sequence; the batching tank is also directly connected with a rear ester exchange tower system, a light component removing tower system and a methyl ethyl carbonate rectifying tower system. The utility model adopts the impinging stream ester exchange tubular reactor to carry out ester exchange reaction, two heterogeneous fluids flow oppositely at high speed to form a highly turbulent impact area through impact, the impinging stream effectively improves the mixing and mass transfer effects in the reactor, and the reaction rate and the product yield are improved; the reaction time is shortened, the energy is saved, the production efficiency is improved, and the method is green, environment-friendly and environment-friendly.
Description
Technical Field
The utility model belongs to the technical field of the chemical industry, concretely relates to striking flows device of ester exchange tubular reactor production methyl ethyl carbonate.
Background
Methyl ethyl carbonate (EMC) has the name of green chemical and the molecular formula is C 4 H 8 O 3 Unique molecular structure (C) 2 H 5 O-CO-OCH 3 ) Is an organic carbonate compound with asymmetric molecular structure. EMC molecules contain a plurality of active groups at the same time, so that the chemical properties are very active, and the EMC has a wide application prospect in many fields. Because the methyl ethyl carbonate has small viscosity, high dielectric constant and strong solubility to lithium salt, the methyl ethyl carbonate is an excellent lithium ion battery electrolyte solvent, can improve the energy density and discharge capacity of the battery, and can further improve the safety performance and service life of the battery.
The industrial production method of ethyl methyl carbonate generally adopts phosgene method, carbonyl oxidation method, ester exchange method and the like. In the presence of catalyst, dimethyl carbonate and ethanol or diethyl carbonate are subjected to ester exchange to produce methyl ethyl carbonate. The method for producing the methyl ethyl carbonate by the ester exchange method has the advantages of low toxicity of raw materials, small pollution, simple process, mild reaction conditions and the like. But the transesterification method for producing the methyl ethyl carbonate also has the outstanding problems of large catalyst dosage, low raw material conversion rate, long reaction time and the like. The reason is that the preparation process of the ethyl methyl carbonate generally adopts a mechanical stirring tank type reactor or a tower type reactor, and the preparation equipment has the defects of low heat transfer and mass transfer efficiency, long reaction period, high energy consumption, cost rise caused by the increase of the energy consumption and is not beneficial to industrial production.
The art is eagerly looking for a low-energy-consumption and environment-friendly device for preparing ethyl methyl carbonate, which can overcome the technical problems.
Disclosure of Invention
The utility model provides a device of ester exchange tubular reactor production methyl ethyl carbonate is flowed in striking, its purpose is overcome above-mentioned current preparation equipment and is had heat transfer, mass transfer efficiency low, and the reaction cycle is long, the high problem of energy consumption.
In order to achieve the above purpose, the utility model adopts the following technical scheme:
a device for producing ethyl methyl carbonate by an impinging stream ester exchange tubular reactor comprises a dosing tank, the impinging stream ester exchange tubular reactor, a rear ester exchange tower system, a light component removal tower system and an ethyl methyl carbonate rectifying tower system which are connected in sequence; the batching tank is also directly connected with a rear ester exchange tower system, a light component removal tower system and a methyl ethyl carbonate rectifying tower system;
the impinging stream ester exchange tubular reactor comprises a power fluid pump, a Laval nozzle, a high-speed jet impinging cavity, a gas-liquid coupler, a tubular reactor, a heater and an ethanol vaporizer; the Laval nozzle, the high-speed jet impact cavity, the gas-liquid coupler and the tubular reactor are all arranged in the heater; the end parts, back to each other, of the two Laval spray pipes are fixedly communicated with gas-liquid couplers, and the pipe orifices of the gas-liquid couplers are communicated with the outlet end of the ethanol vaporizer; the two Laval nozzles are arranged in opposite directions and communicated, a cavity formed by the middle communication part is a mixing cavity, the vertical direction of the middle part of the mixing cavity is communicated with a high-speed jet impact cavity, the high-speed jet impact cavity is communicated with one end of the tubular reactor, and the other end of the tubular reactor is communicated with a liquid inlet in the middle part of the rear ester exchange tower.
Furthermore, the batching jar is provided with the heating jacket for the outer periphery, and inside is provided with the tank structure of mechanical agitator, and the feed inlet has been seted up at batching jar top, and the methyl alcohol-dimethyl ester azeotrope pump of back ester exchange tower is connected to the feed inlet, and the inlet end of power fluid pump is connected to batching tank bottom liquid outlet, and the outlet end of power fluid pump is connected the gas-liquid coupler liquid inlet end of impinging stream ester exchange tubular reactor.
Furthermore, the back ester exchange tower system consists of a back ester exchange tower, a back ester exchange tower reboiler, a back ester exchange tower plate type tower plate, a back ester exchange tower white steel regular packing, a back ester exchange tower condenser, a methanol-dimethyl ester azeotrope receiving tank, a methanol-dimethyl ester azeotrope pump, a back ester exchange tower bottom pump and a catalyst filter; the rear ester exchange tower is of a tower body structure that the bottom of the interior of the rear ester exchange tower is provided with a rear ester exchange tower plate type tower plate, the upper part of the rear ester exchange tower is provided with a rear ester exchange tower white steel regular packing, a tubular reactor is communicated with the rear ester exchange tower, the top of the rear ester exchange tower is sequentially communicated with a rear ester exchange tower condenser, a methanol-dimethyl ester azeotrope receiving tank and an inlet of a methanol-dimethyl ester azeotrope pump, and the outlet end of the methanol-dimethyl ester azeotrope pump is respectively communicated with the rear ester exchange tower, a feed inlet at the top of a batching tank and a methanol recovery system; the bottom end of the rear ester exchange tower is respectively connected with the inlet ends of a reboiler of the rear ester exchange tower and a catalyst filter through a bottom pump of the rear ester exchange tower, the outlet end of the reboiler of the rear ester exchange tower is connected with the rear ester exchange tower, and the outlet end of the catalyst filter is respectively connected with a light component removal tower and a catalyst recovery system of the light component removal tower system.
Further, the light component removal tower system consists of a light component removal tower, a light component removal tower reboiler, light component removal tower white steel structured packing, a light component removal tower condenser, a light component receiving tank, a light component pump and a light component removal tower bottom pump; a light component removing tower white steel structured packing is arranged in the light component removing tower, the top end of the light component removing tower is sequentially communicated with a light component removing tower condenser, a light component receiving tank and a light component pump, and the outlet end of the light component pump is respectively communicated with the light component removing tower and a batching tank; the bottom end of the light component removing tower is communicated with a light component removing tower bottom pump, the light component removing tower bottom pump is respectively communicated with a light component removing tower reboiler and a methyl ethyl carbonate rectifying tower of a methyl ethyl carbonate rectifying tower system, and the light component removing tower reboiler is communicated with a light component removing tower.
Further, the ethyl methyl carbonate rectifying tower system consists of an ethyl methyl carbonate rectifying tower, a rectifying tower reboiler, a rectifying tower condenser, an ethyl methyl carbonate receiving tank, an ethyl methyl carbonate pump, an ethyl methyl carbonate storage tank and an ethyl methyl carbonate rectifying tower bottom pump; a rectifying tower white steel structured packing is arranged in the ethyl methyl carbonate rectifying tower, the top end of the ethyl methyl carbonate rectifying tower is sequentially communicated with a rectifying tower condenser, an ethyl methyl carbonate receiving tank and an ethyl methyl carbonate pump, and the ethyl methyl carbonate pump is respectively communicated with the ethyl methyl carbonate rectifying tower and an ethyl methyl carbonate storage tank; the bottom end of the ethyl methyl carbonate rectifying tower is communicated with a bottom pump of the ethyl methyl carbonate rectifying tower, the bottom pump of the ethyl methyl carbonate rectifying tower is respectively communicated with a rectifying tower reboiler and a dosing tank, and the rectifying tower reboiler is communicated with the ethyl methyl carbonate rectifying tower.
Further, the tubular reactor is a tube with the length-diameter ratio of more than 1000, the diameter of the tube is phi 75mm or phi 100mm, and the tubular reactor is arranged to be a reciprocating type or a spring type.
The utility model discloses a device of ester exchange tubular reactor production methyl ethyl carbonate is flowed in striking, compares with prior art, and beneficial effect is:
1. an impinging stream ester exchange tubular reactor is adopted for carrying out ester exchange reaction, two heterogeneous fluids flow oppositely at high speed to form a highly turbulent impinging zone through impingement, the impinging stream effectively improves the mixing and mass transfer effects in the reactor, and the reaction rate and the product yield are improved;
2. the reaction time is shortened, the energy is saved, the production efficiency is improved, and the method is green, environment-friendly and environment-friendly;
3. the quality of the prepared methyl ethyl carbonate is higher than the standard of HG/T5158-2017 industrial methyl ethyl carbonate; the utility model discloses the technology is ripe, and equipment is advanced, continuous operation, and degree of automation is high.
Drawings
FIG. 1 is a schematic diagram of an apparatus for producing ethyl methyl carbonate by using an impinging stream transesterification tubular reactor according to the present invention;
reference numerals: 1. 1-1 parts of a batching tank, 1-2 parts of a mechanical stirrer and 1-2 parts of a heating jacket; 2. 2-1 parts of an impinging stream ester exchange tubular reactor, 2-1 parts of a power fluid pump, 2-2 parts of a Laval nozzle, 2-3 parts of a high-speed jet impinging cavity, 2-4 parts of a gas-liquid coupler, 2-5 parts of a tubular reactor, 2-6 parts of a heater, 2-7 parts of an ethanol vaporizer; 3. a rear ester exchange tower, 3-1, a rear ester exchange tower reboiler, 3-2, a rear ester exchange tower plate, 3-3, rear ester exchange tower white steel structured packing, 3-4, a rear ester exchange tower condenser, 3-5, a methanol-dimethyl ester azeotrope receiving tank, 3-6, a methanol-dimethyl ester azeotrope pump, 3-7, a rear ester exchange tower bottom pump, 3-8 and a catalyst filter; 4. the method comprises the following steps of (1) a light component removal tower, 4-1 a light component removal tower reboiler, 4-2 light component removal tower white steel structured packing, 4-3 a light component removal tower condenser, 4-4 a light component receiving tank, 4-5 a light component pump, 4-6 and a light component removal tower bottom pump; 5. the device comprises a methyl ethyl carbonate rectifying tower, 5-1 parts of a rectifying tower reboiler, 5-2 parts of rectifying tower white steel structured packing, 5-3 parts of a rectifying tower condenser, 5-4 parts of a methyl ethyl carbonate receiving tank, 5-5 parts of a methyl ethyl carbonate pump, 5-6 parts of a methyl ethyl carbonate storage tank and 5-7 parts of a methyl ethyl carbonate rectifying tower bottom pump.
Detailed Description
In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is further described in detail with reference to the following embodiments. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the invention.
Aiming at the engineering problems and the market demand, in order to overcome the problems existing in the prior art, the utility model provides a mature process, continuous operation, high automation degree, advanced reactor technology, high reaction efficiency, energy conservation and environmental protection; the advanced impinging stream ester exchange tubular reactor is adopted for carrying out ester exchange reaction, so that the heat transfer and mass transfer are enhanced, the reaction rate and the product yield are improved, and the quality of the prepared methyl ethyl carbonate is higher than the HG/T5158-2017 industrial methyl ethyl carbonate standard.
Example 1
As shown in fig. 1, the apparatus for producing ethyl methyl carbonate by using an impinging stream transesterification tubular reactor comprises a dosing tank 1, an impinging stream transesterification tubular reactor 2, a post-transesterification column system, a light component removal column system, and an ethyl methyl carbonate rectification column system which are connected in sequence; the batching tank 1 is also directly connected with a rear ester exchange tower system, a light component removing tower system and a methyl ethyl carbonate rectifying tower system.
The system comprises a mixing tank 1, a methanol-dimethyl ester azeotrope pump 3-6, a heating jacket 1-2, a mechanical stirrer 1-1, a liquid inlet, a liquid outlet, a power fluid pump 2-1, a gas-liquid coupler 2-4 and a liquid inlet, wherein the heating jacket 1-2 is arranged on the outer periphery of the mixing tank 1, the mechanical stirrer 1-1 is arranged in the mixing tank, the liquid inlet is formed in the top of the mixing tank 1, the liquid inlet is connected with the methanol-dimethyl ester azeotrope pump 3-6 of a rear ester exchange tower 3, the liquid outlet at the bottom end of the mixing tank 1 is connected with the inlet end of the power fluid pump 2-1, and the outlet end of the power fluid pump 2-1 is connected with the liquid inlet end of the gas-liquid coupler 2-4 of an impinging stream ester exchange tubular reactor 2; the batching tank 1 is used for batching dimethyl carbonate, a catalyst and recycled materials (methanol, dimethyl carbonate, ethyl methyl carbonate and diethyl carbonate), and simultaneously the dimethyl carbonate, the catalyst and the recycled materials are uniformly mixed under the stirring action of the mechanical stirrer 1-1 to obtain a mixed solution; the mixed liquid reaches the reaction temperature under the heating of a heating medium and enters the tubular reactor 2 of the impinging stream transesterification through a power fluid pump 2-1. The heating jacket 1-2 is a structure in which a heating medium flows inside.
The impinging stream transesterification tubular reactor 2 is used for carrying out transesterification reaction on ethanol steam and dimethyl carbonate; the impinging stream ester exchange tubular reactor 2 comprises a power fluid pump 2-1, a Laval nozzle 2-2, a high-speed jet impinging cavity 2-3, a gas-liquid coupler 2-4, a tubular reactor 2-5, a heater 2-6 and an ethanol vaporizer 2-7; the Laval nozzle 2-2, the high-speed jet impact cavity 2-3, the gas-liquid coupler 2-4 and the tubular reactor 2-5 are all arranged inside the heater 2-6; the two Laval nozzles 2-2 are oppositely arranged and communicated, a cavity formed at the middle communicated part is a mixing cavity, the middle part of the mixing cavity is communicated with a high-speed jet impact cavity 2-3 in the vertical direction, the high-speed jet impact cavity 2-3 is communicated with one end of a tubular reactor 2-5, and the other end of the tubular reactor 2-5 is communicated with a liquid inlet at the middle part of the rear ester exchange tower 3; the end parts of the two Laval spray pipes 2-2, which are opposite to each other, are respectively fixed with a gas-liquid coupler 2-4, the pipe orifice of the gas-liquid coupler 2-4 is provided with a gas inlet, the gas inlet is communicated with the outlet end of an ethanol vaporizer 2-7, the ethanol vaporizer 2-7 is of a structure with a heating medium arranged outside, fresh ethanol is introduced into the ethanol vaporizer 2-7, and enters the gas-liquid coupler 2-4 from the gas inlet after vaporization to react with the mixed liquid from the batching tank 1. The tubular reactors 2-5 are tubes with a length to diameter ratio of more than 1000, can be phi 75mm or phi 100mm, and can be arranged as a reciprocating type or a spring type. The heaters 2-6 are closed box structures, and flowing heat medium structures are arranged in the heaters.
Two opposite Laval nozzles 2-2 are communicated with a batching tank 1 through a first power fluid pump 2-1 and are communicated with the outlet end of an ethanol vaporizer 2-7, mixed liquid of the batching tank 1 is pumped into a gas-liquid coupler 2-4 of the two opposite Laval nozzles 2-2 through the first power fluid pump 2-1, the gas inlet of the gas-liquid coupler 2-4 simultaneously sucks ethanol steam vaporized at the outlet end of the ethanol vaporizer 2-7, two high-speed jet flows (the mixed liquid of the batching tank 1 and the ethanol steam of the ethanol vaporizer 2-7) sprayed from the Laval nozzles 2-2 collide with each other in a high-speed jet flow collision cavity 2-3 through a mixing cavity and then enter a tubular reactor 2-5 for ester exchange reaction, and ester exchange liquid continuously enters a rear ester exchange tower 3 of a rear ester exchange tower system;
because the mixed liquid is sprayed out at a high speed through the Laval pipe, a negative pressure area is generated at a gas suction inlet of the gas-liquid coupler 2-4, so that the gas is sucked, rapidly expands in the negative pressure area and is beaten into tiny bubbles by power fluid to enter a mixing cavity; at the moment, in the mixing cavity, gas and liquid are fully mixed in the mixing cavity, and are discharged at an accelerated speed due to energy exchange, the speed can reach the sonic speed, the potential energy of the mixed liquid is increased to the maximum through the diffusion cavity of the Laval tube, and the effects of mass transfer and heat transfer are further enhanced; two heterogeneous fluids flow oppositely at high speed to form a highly turbulent impact region through impact, so that the heat and mass transfer in the process is greatly enhanced; the strong micromixing and pressure fluctuation characteristics of the impinging stream can enable the chemical reaction to be rapidly carried out, and the effective and uniform supersaturation degree is instantly generated; and due to the chaotic flow state, the mixing scale is rapidly reduced, the vortexes with different scales and the vortexes with different scales are folded and collided with each other, so that the turbulent intensity and the energy diffusion are enhanced, more effective high-energy-level collision is achieved when molecules are subjected to chemical reaction, the mixing and mass transfer effects in the reactor are effectively improved by the impinging stream, and the reaction rate and the product yield are improved.
The rear ester exchange tower system is used for continuously carrying out ester exchange reaction on the ethanol and the dimethyl carbonate and simultaneously separating methanol generated by the reaction. The rear ester exchange tower system consists of a rear ester exchange tower 3, a rear ester exchange tower reboiler 3-1, a rear ester exchange tower plate type tower plate 3-2, rear ester exchange tower white steel regular packing 3-3, a rear ester exchange tower condenser 3-4, a methanol-dimethyl ester azeotrope receiving tank 3-5, a methanol-dimethyl ester azeotrope pump 3-6, a rear ester exchange tower bottom pump 3-7 and a catalyst filter 3-8; the rear ester exchange tower 3 is a tower body structure, the bottom of the interior of the tower body is provided with a rear ester exchange tower plate type tower plate 3-2, and the upper part of the tower body is provided with a rear ester exchange tower white steel regular packing 3-3. The tubular reactor 2-5 is communicated with the rear ester exchange tower 3, the top of the rear ester exchange tower 3 is sequentially communicated with a condenser 3-4 of the rear ester exchange tower, a methanol-dimethyl ester azeotrope receiving tank 3-5 and an inlet of a methanol-dimethyl ester azeotrope pump 3-6, and an outlet end of the methanol-dimethyl ester azeotrope pump 3-6 is respectively communicated with the rear ester exchange tower 3, a feed inlet at the top of the batching tank 1 and a methanol recovery system; the bottom end of the rear ester exchange tower 3 is respectively connected with the inlet ends of a rear ester exchange tower reboiler 3-1 and a catalyst filter 3-8 through a rear ester exchange tower bottom pump 3-7, the outlet end of the rear ester exchange tower reboiler 3-1 is connected with the rear ester exchange tower 3, and the outlet end of the catalyst filter 3-8 is respectively connected with a light component removal tower 4 and a catalyst recovery system of a light component removal tower system.
Continuously carrying out ester exchange reaction of ethanol and dimethyl carbonate on a reaction tower plate at the lower half part of a rear ester exchange tower 3, simultaneously separating out a methanol-dimethyl carbonate azeotrope at the upper half part of the tower, allowing separated methanol-dimethyl carbonate azeotrope vapor to enter a condenser 3-4 of the rear ester exchange tower, allowing the methanol-dimethyl carbonate azeotrope condensed by the condenser 3-4 of the rear ester exchange tower to enter a methanol-dimethyl carbonate azeotrope receiving tank 3-5, allowing part of the methanol-dimethyl carbonate azeotrope in the methanol-dimethyl carbonate azeotrope receiving tank 3-5 to enter the rear ester exchange tower 3 as reflux, allowing part of the methanol-dimethyl carbonate azeotrope to enter a methanol recovery system and allowing part of the methanol-dimethyl carbonate azeotrope to directly return to a batching tank 1 through a methanol-dimethyl carbonate azeotrope pump 3-6; and the tower bottom liquid of the rear ester exchange tower 3 passes through a tower bottom pump 3-7 of the rear ester exchange tower, part of the tower bottom liquid enters a reboiler 3-1 of the rear ester exchange tower to be heated and then returns to the rear ester exchange tower 3, part of the tower bottom liquid passes through a catalyst filter 3-8 to filter out the catalyst, the filtrate enters a light component removal tower 4, and the filtered catalyst enters a catalyst recovery system.
The light component removing tower system is used for removing light components in clear filtrate, mainly dimethyl carbonate; the light component removal tower system consists of a light component removal tower 4, a light component removal tower reboiler 4-1, light component removal tower white steel structured packing 4-2, a light component removal tower condenser 4-3, a light component receiving tank 4-4, a light component pump 4-5 and a light component removal tower bottom pump 4-6; a light component removing tower white steel regular packing 4-2 is arranged in the light component removing tower 4. The top end of the light component removing tower 4 is sequentially communicated with a light component removing tower condenser 4-3, a light component receiving tank 4-4 and a light component pump 4-5, and the outlet end of the light component pump 4-5 is respectively communicated with the light component removing tower 4 and the batching tank 1; the bottom end of the light component removing tower 4 is communicated with a light component removing tower bottom pump 4-6, the light component removing tower bottom pump 4-6 is respectively communicated with a light component removing tower reboiler 4-1 and a methyl ethyl carbonate rectifying tower 5 of a methyl ethyl carbonate rectifying tower system, and the light component removing tower reboiler 4-1 is communicated with the light component removing tower 4.
The clear filtrate from the catalyst filter 3-8 enters a light component removal tower 4, the dimethyl carbonate gas separated from the light component removal tower 4 enters a light component removal tower condenser 4-3, the dimethyl carbonate condensed by the light component removal tower condenser 4-3 enters a dimethyl carbonate light component receiving tank 4-4, the dimethyl carbonate in the light component receiving tank 4-4 passes through a dimethyl carbonate light component pump 4-5, part of the dimethyl carbonate enters the light component removal tower 4 as reflux, and part of the dimethyl carbonate directly returns to the batching tank 1; and part of the tower bottom liquid of the light component removing tower 4 enters a light component removing tower reboiler 4-1 through a light component removing tower bottom pump 4-6 to be heated, then returns to the light component removing tower 4, and part of the tower bottom liquid enters a methyl ethyl carbonate rectifying tower 5 of a methyl ethyl carbonate rectifying tower system.
The ethyl methyl carbonate rectifying tower system is used for rectifying the ethyl methyl carbonate from tower bottom liquid of the light component removing tower; the ethyl methyl carbonate rectifying tower system consists of an ethyl methyl carbonate rectifying tower 5, a rectifying tower reboiler 5-1, a rectifying tower condenser 5-3, an ethyl methyl carbonate receiving tank 5-4, an ethyl methyl carbonate pump 5-5, an ethyl methyl carbonate storage tank 5-6 and an ethyl methyl carbonate rectifying tower bottom pump 5-7; and 5-2 parts of white steel structured packing of the rectifying tower are arranged in the methyl ethyl carbonate rectifying tower 5. The top end of a methyl ethyl carbonate rectifying tower 5 is sequentially communicated with a rectifying tower condenser 5-3, a methyl ethyl carbonate receiving tank 5-4 and a methyl ethyl carbonate pump 5-5, and the methyl ethyl carbonate pump 5-5 is respectively communicated with a methyl ethyl carbonate rectifying tower 5 and a methyl ethyl carbonate storage tank 5-6; the bottom end of the ethyl methyl carbonate rectifying tower 5 is communicated with a bottom pump 5-7 of the ethyl methyl carbonate rectifying tower, the bottom pump 5-7 of the ethyl methyl carbonate rectifying tower is respectively communicated with a rectifying tower reboiler 5-1 and a batching tank 1, and the rectifying tower reboiler 5-1 is communicated with the ethyl methyl carbonate rectifying tower 5.
The tower bottom liquid from the lightness-removing tower enters a methyl ethyl carbonate rectifying tower 5, the methyl ethyl carbonate vapor rectified by the methyl ethyl carbonate rectifying tower 5 enters a rectifying tower condenser 5-3, the methyl ethyl carbonate condensed by the rectifying tower condenser 5-3 enters a methyl ethyl carbonate receiving tank 5-4, the methyl ethyl carbonate in the methyl ethyl carbonate receiving tank 5-4 passes through a methyl ethyl carbonate pump 5-5, part of the methyl ethyl carbonate enters the methyl ethyl carbonate rectifying tower 5 as reflux, and the other part of the methyl ethyl carbonate directly enters a methyl ethyl carbonate storage tank 5-6; and (3) allowing the tower bottom liquid of the ethyl methyl carbonate rectifying tower 5 to pass through a bottom pump 5-7 of the ethyl methyl carbonate rectifying tower, allowing part of the tower bottom liquid to enter a rectifying tower reboiler 5-1 for heating, returning the heated part of the tower bottom liquid to the ethyl methyl carbonate rectifying tower 5, and directly returning part of the tower bottom liquid to the batching tank 1.
The raw materials adopted by the utility model are industrial dimethyl carbonate (mass content is more than 99.5%), industrial ethanol (mass content is more than 99.5%), catalyst and the like; the used public engineering steam is superheated steam with 0.4 MPa and 290 ℃; the water vapor of the public engineering mainly provides heat sources for a heating medium of the batching tank 1, a heating medium of the heater 2-6, a heating medium of the ethanol vaporizer 2-7, a heating medium of the post-ester exchange column reboiler 3-1, a heating medium of the light component removal column reboiler 4-1 and a heating medium of the rectifying column reboiler 5-1; the devices of the device are connected through corresponding pipelines, and the heat medium structure of the tower kettle is the structure of the prior reboiler. The light component receiving tank 4-4 and the methyl ethyl carbonate receiving tank 5-4 are both connected with a vacuum system. And introducing cooling water into the rear ester exchange tower condenser 3-4, the light component removal tower condenser 4-3 and the rectifying tower condenser 5-3 for condensation, wherein when the pipelines in the attached drawing 1 are crossed on the drawing and actually do not intersect, the drawing is performed according to the principle of vertical and continuous intersection.
The process method for producing the methyl ethyl carbonate by the impinging stream ester exchange tubular reactor comprises the following steps:
(1) Raw materials of dimethyl carbonate, a catalyst and recycled materials (methanol, dimethyl carbonate, ethyl methyl carbonate and diethyl carbonate recycled by a methanol-dimethyl ester azeotrope pump 3-6, a light component pump 4-5 and a methyl ethyl carbonate rectifying tower bottom pump 5-7) enter a batching tank 1, and the dimethyl carbonate, the catalyst and the recycled materials are uniformly mixed under the stirring action of a mechanical stirrer 1-1 to obtain a mixed solution; the mixed solution reaches the reaction temperature under the heating of a heating medium and enters an impinging stream ester exchange tubular reactor 2 through a power fluid pump 2-1;
the raw material dimethyl carbonate (the mass content is more than 99.9 percent), the temperature in the batching tank 1 is 85-90 ℃, the pressure is 0.22-0.26 MPa, the catalyst is 0.2-0.4 percent of the mass of the dimethyl carbonate, and the retention time of the materials is 0.5-0.75 h;
(2) The mixed liquid in the batching tank 1 is pumped into two gas-liquid couplers 2-4 through a power fluid pump 2-1, the gas-liquid couplers 2-4 simultaneously suck ethanol steam from an ethanol vaporizer 2-7, two high-speed jet flows sprayed out of opposite Laval nozzles 2-2 mutually collide with each other in a high-speed jet flow collision cavity 2-3 and then enter a tubular reactor 2-5, the ethanol steam and dimethyl carbonate undergo ester exchange reaction in the tubular reactor to obtain ester exchange liquid, and the ester exchange liquid continuously enters a rear ester exchange tower 3;
ethanol (mass content is more than 99.5%) steam of the ethanol vaporizers 2-7, dimethyl carbonate: the molar ratio of ethanol (ethanol vaporizer 2-7 feed ethanol) was 1: (1.2-1.4), the temperature in the tubular reactor is 105-110 ℃, and the pressure is 0.42-0.48 MPa.
(3) Continuously carrying out ester exchange reaction on the ethanol and the dimethyl carbonate in the rear ester exchange tower 3, and simultaneously separating the methanol generated by the reaction; ester exchange reaction of ethanol and dimethyl carbonate is continuously carried out on a plate type tower plate 3-2 of the rear ester exchange tower 3 at the lower half part of the rear ester exchange tower 3, meanwhile, a methanol-dimethyl carbonate azeotrope is separated out at the upper half part of the tower, separated methanol-dimethyl carbonate azeotrope vapor enters a condenser 3-4 of the rear ester exchange tower, the methanol-dimethyl carbonate azeotrope condensed by the condenser 3-4 of the rear ester exchange tower enters a receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope, part of the methanol-dimethyl carbonate azeotrope of the receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope enters the rear ester exchange tower 3 as reflux, part of the methanol-dimethyl carbonate azeotrope enters a methanol recovery system and part of the methanol-dimethyl carbonate azeotrope directly returns to the batching tank 1 through a methanol-dimethyl carbonate azeotrope pump 3-6; the tower bottom liquid of the rear ester exchange tower 3 passes through a tower bottom pump 3-7 of the rear ester exchange tower, part of the tower bottom liquid enters a reboiler 3-1 of the rear ester exchange tower to be heated and then returns to the rear ester exchange tower 3, part of the tower bottom liquid passes through a catalyst filter 3-8 to filter out a catalyst, the filtrate enters a light component removal tower 4, and the filtered catalyst enters a catalyst recovery system;
the temperature of the top of the rear ester exchange tower 3 is 64 ℃, the pressure of the top of the tower is normal pressure, the temperature of the bottom of the tower is 90-110 ℃, the reflux ratio is 1.0-1.5, and the retention time of the materials is 1.0-1.5 h;
(4) The clear filtrate from the catalyst filter enters a light component removing tower 4, and light components in the clear filtrate, mainly dimethyl carbonate, are removed; dimethyl carbonate gas separated by the light component removing tower 4 enters a light component removing tower condenser 4-3, dimethyl carbonate condensed by the light component removing tower condenser 4-3 enters a light component receiving tank 4-4, part of the dimethyl carbonate in the light component receiving tank 4-4 enters the light component removing tower 4 as reflux, and part of the dimethyl carbonate directly returns to the batching tank 1 through a light component pump 4-5; part of the tower bottom liquid of the light component removing tower 4 enters a light component removing tower reboiler 4-1 through a light component removing tower bottom pump 4-6 to be heated, and then returns to the light component removing tower 4, and part of the tower bottom liquid enters a methyl ethyl carbonate rectifying tower 5;
the tower top temperature of the light component removing tower is 60 ℃, the tower top pressure is 0.035MPa, the tower bottom temperature is 75-85 ℃, and the reflux ratio is 1;
(5) The ethyl methyl carbonate gas rectified by the ethyl methyl carbonate rectifying tower 5 enters a rectifying tower condenser 5-3, the ethyl methyl carbonate condensed by the rectifying tower condenser 5-3 enters an ethyl methyl carbonate receiving tank 5-4, part of the ethyl methyl carbonate in the ethyl methyl carbonate receiving tank 5-4 enters the ethyl methyl carbonate rectifying tower 5 as reflux through an ethyl methyl carbonate pump 5-5, and part of the ethyl methyl carbonate directly enters an ethyl methyl carbonate storage tank 5-6; and (3) allowing the tower bottom liquid of the ethyl methyl carbonate rectifying tower 5 to pass through a bottom pump 5-7 of the ethyl methyl carbonate rectifying tower, allowing part of the tower bottom liquid to enter a rectifying tower reboiler 5-1 for heating, returning the heated part of the tower bottom liquid to the ethyl methyl carbonate rectifying tower 5, and directly returning part of the tower bottom liquid to the batching tank 1.
The temperature of the top of the ethyl methyl carbonate rectifying tower 5 is 66 ℃, the pressure of the top of the tower is 0.026MPa, the temperature of the bottom of the tower is 80-85 ℃, and the reflux ratio is 2.
Example 2
The method for producing methyl ethyl carbonate based on the device for preparing methyl ethyl carbonate based on the impinging stream transesterification tubular reactor 2, which is described in the embodiment 1, comprises the following steps:
91kg/h of raw material dimethyl carbonate (the mass content is more than 99.9 percent) in the step (1), 0.364kg/h of catalyst and recycled materials (methanol, dimethyl carbonate, ethyl methyl carbonate and diethyl carbonate) enter a batching tank 1, and the dimethyl carbonate, the catalyst and the recycled materials are uniformly mixed under the action of stirring; the mixed solution reaches the reaction temperature under the heating of a heating medium and enters the impinging stream ester exchange tubular reactor 2 through a power fluid pump; the temperature in the batching tank 1 is 85 ℃, the pressure is 0.22MPa, and the pressure of dimethyl carbonate: ethanol (ethanol vaporizer feed ethanol) was 1:1.4 (molar ratio), the catalyst is 0.4 percent (mass) of dimethyl carbonate, and the retention time of the materials is 0.75h;
(2) The mixed liquid in the batching tank 1 is pumped into two gas-liquid couplers 2-4 through a power fluid pump 2-1, the gas-liquid couplers 2-4 simultaneously suck ethanol steam from an ethanol vaporizer 2-7, two high-speed jet flows sprayed out of opposite Laval nozzles 2-2 mutually collide with each other in a high-speed jet flow collision cavity 2-3 and then enter a tubular reactor 2-5, the ethanol steam and dimethyl carbonate undergo ester exchange reaction in the tubular reactor to obtain ester exchange liquid, and the ester exchange liquid continuously enters a rear ester exchange tower 3; the temperature in the tubular reactor is 105 ℃, and the pressure is 0.42MPa;
(3) Continuously carrying out ester exchange reaction on the ethanol and the dimethyl carbonate in the rear ester exchange tower 3, and simultaneously separating the methanol generated by the reaction; ester exchange reaction of ethanol and dimethyl carbonate is continuously carried out on a plate type tower plate 3-2 of the rear ester exchange tower 3 at the lower half part of the rear ester exchange tower 3, meanwhile, a methanol-dimethyl carbonate azeotrope is separated out at the upper half part of the tower, separated methanol-dimethyl carbonate azeotrope vapor enters a condenser 3-4 of the rear ester exchange tower, the methanol-dimethyl carbonate azeotrope condensed by the condenser 3-4 of the rear ester exchange tower enters a receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope, part of the methanol-dimethyl carbonate azeotrope of the receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope enters a methanol recovery system as reflux, and part of the methanol-dimethyl carbonate azeotrope enters a proportioning tank 1 directly; the tower bottom liquid of the rear ester exchange tower 3 passes through a tower bottom pump 3-7 of the rear ester exchange tower, part of the tower bottom liquid enters a reboiler 3-1 of the rear ester exchange tower to be heated and then returns to the rear ester exchange tower 3, part of the tower bottom liquid passes through a catalyst filter 3-8 to filter out a catalyst, the filtrate enters a light component removal tower 4, and the filtered catalyst enters a catalyst recovery system;
the temperature of the top of the rear ester exchange tower 3 is 64 ℃, the pressure of the top of the tower is normal pressure, the temperature of the bottom of the tower is 90 ℃, the reflux ratio is 1.0, and the retention time of the materials is 1.5h;
(4) The clear filtrate from the catalyst filter enters a light component removing tower 4, and light components in the clear filtrate, mainly dimethyl carbonate, are removed; dimethyl carbonate gas separated by the light component removing tower 4 enters a light component removing tower condenser 4-3, dimethyl carbonate condensed by the light component removing tower condenser 4-3 enters a light component receiving tank 4-4, and part of the dimethyl carbonate in the light component receiving tank 4-4 enters the light component removing tower 4 as reflux through a light component pump 4-5, and part of the dimethyl carbonate directly returns to the batching tank 1; part of the tower bottom liquid of the light component removing tower 4 enters a light component removing tower reboiler 4-1 through a light component removing tower bottom pump 4-6 to be heated, and then returns to the light component removing tower 4, and part of the tower bottom liquid enters a methyl ethyl carbonate rectifying tower 5;
the tower top temperature of the light component removing tower is 60 ℃, the tower top pressure is 0.035MPa, the tower bottom temperature is 75 ℃, and the reflux ratio is 1;
(5) The ethyl methyl carbonate gas rectified by the ethyl methyl carbonate rectifying tower 5 enters a rectifying tower condenser 5-3, the ethyl methyl carbonate condensed by the rectifying tower condenser 5-3 enters an ethyl methyl carbonate receiving tank 5-4, part of the ethyl methyl carbonate in the ethyl methyl carbonate receiving tank 5-4 enters the ethyl methyl carbonate rectifying tower 5 as reflux through an ethyl methyl carbonate pump 5-5, and part of the ethyl methyl carbonate directly enters an ethyl methyl carbonate storage tank 5-6; and (3) allowing the tower bottom liquid of the ethyl methyl carbonate rectifying tower 5 to pass through a bottom pump 5-7 of the ethyl methyl carbonate rectifying tower, allowing part of the tower bottom liquid to enter a rectifying tower reboiler 5-1 for heating, returning the heated part of the tower bottom liquid to the ethyl methyl carbonate rectifying tower 5, and directly returning part of the tower bottom liquid to the batching tank 1.
The temperature of the top of the ethyl methyl carbonate rectifying tower 5 is 66 ℃, the pressure of the top of the tower is 0.026MPa, the temperature of the bottom of the tower is 80-85 ℃, and the reflux ratio is 2.
The temperature of the top of the ethyl methyl carbonate rectifying tower 5 is 66 ℃, the pressure of the top of the rectifying tower is 0.026MPa, the temperature of the bottom of the rectifying tower is 80 ℃, the reflux ratio is 2, 102.2kg/h of ethyl methyl carbonate is extracted, and the yield of the ethyl methyl carbonate is 97.180% (the mass content is more than 99.9%).
Example 3
A method for producing methyl ethyl carbonate based on the device for producing methyl ethyl carbonate by using the impinging stream transesterification tubular reactor in example 1 comprises the following steps:
91kg/h of raw material dimethyl carbonate (the mass content is more than 99.9 percent) and 0.182kg/h of catalyst in the step (1), and recycled materials (methanol, dimethyl carbonate, ethyl methyl carbonate and diethyl carbonate) enter the batching tank 1, and the dimethyl carbonate, the catalyst and the recycled materials are uniformly mixed under the action of stirring; the mixed solution reaches the reaction temperature under the heating of a heating medium and enters the impinging stream ester exchange tubular reactor 2 through a power fluid pump; the temperature in the batching tank 1 is 90 ℃, the pressure is 0.26MPa, and the pressure of dimethyl carbonate: ethanol (ethanol vaporizer feed ethanol) was 1:1.2 (molar ratio), the catalyst is 0.2 percent (mass) of dimethyl carbonate, and the retention time of the materials is 0.5h;
(2) The mixed liquid in the batching tank 1 is pumped into two gas-liquid couplers 2-4 through a power fluid pump 2-1, the gas-liquid couplers 2-4 simultaneously suck ethanol steam from an ethanol vaporizer 2-7, two high-speed jet flows sprayed out of opposite Laval nozzles 2-2 mutually collide with each other in a high-speed jet flow collision cavity 2-3 and then enter a tubular reactor 2-5, the ethanol steam and dimethyl carbonate undergo ester exchange reaction in the tubular reactor to obtain ester exchange liquid, and the ester exchange liquid continuously enters a rear ester exchange tower 3; the temperature in the tubular reactor is 110 ℃, and the pressure is 0.48MPa;
(3) Continuously carrying out ester exchange reaction on the ethanol and the dimethyl carbonate in the rear ester exchange tower 3, and simultaneously separating the methanol generated by the reaction; ester exchange reaction of ethanol and dimethyl carbonate is continuously carried out on a plate type tower plate 3-2 of the rear ester exchange tower 3 at the lower half part of the rear ester exchange tower 3, meanwhile, a methanol-dimethyl carbonate azeotrope is separated out at the upper half part of the tower, separated methanol-dimethyl carbonate azeotrope vapor enters a condenser 3-4 of the rear ester exchange tower, the methanol-dimethyl carbonate azeotrope condensed by the condenser 3-4 of the rear ester exchange tower enters a receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope, part of the methanol-dimethyl carbonate azeotrope of the receiving tank 3-5 of the methanol-dimethyl carbonate azeotrope enters the rear ester exchange tower (3) as reflux, part of the methanol-dimethyl carbonate azeotrope enters a methanol recovery system, and part of the methanol-dimethyl carbonate azeotrope directly returns to the batching tank 1 through a methanol-dimethyl carbonate azeotrope pump 3-6; the tower bottom liquid of the rear ester exchange tower 3 passes through a tower bottom pump 3-7 of the rear ester exchange tower, part of the tower bottom liquid enters a reboiler 3-1 of the rear ester exchange tower to be heated and then returns to the rear ester exchange tower 3, part of the tower bottom liquid passes through a catalyst filter 3-8 to filter out a catalyst, the filtrate enters a light component removal tower 4, and the filtered catalyst enters a catalyst recovery system;
the temperature of the top of the rear ester exchange tower 3 is 64 ℃, the pressure of the top of the tower is normal pressure, the temperature of the bottom of the tower is 110 ℃, the reflux ratio is 1.5, and the retention time of the materials is 1.0h;
(4) The clear filtrate from the catalyst filter enters a light component removing tower 4, and light components in the clear filtrate, mainly dimethyl carbonate, are removed; dimethyl carbonate gas separated by the light component removing tower 4 enters a light component removing tower condenser 4-3, dimethyl carbonate condensed by the light component removing tower condenser 4-3 enters a light component receiving tank 4-4, and part of the dimethyl carbonate in the light component receiving tank 4-4 enters the light component removing tower 4 as reflux through a light component pump 4-5, and part of the dimethyl carbonate directly returns to the batching tank 1; part of the tower bottom liquid of the light component removing tower 4 enters a light component removing tower reboiler 4-1 through a light component removing tower bottom pump 4-6 to be heated, and then returns to the light component removing tower 4, and part of the tower bottom liquid enters a methyl ethyl carbonate rectifying tower 5;
the tower top temperature of the light component removing tower is 60 ℃, the tower top pressure is 0.035MPa, the tower bottom temperature is 85 ℃, and the reflux ratio is 1;
(5) The ethyl methyl carbonate gas rectified by the ethyl methyl carbonate rectifying tower 5 enters a rectifying tower condenser 5-3, the ethyl methyl carbonate condensed by the rectifying tower condenser 5-3 enters an ethyl methyl carbonate receiving tank 5-4, part of the ethyl methyl carbonate in the ethyl methyl carbonate receiving tank 5-4 enters the ethyl methyl carbonate rectifying tower 5 as reflux through an ethyl methyl carbonate pump 5-5, and part of the ethyl methyl carbonate directly enters an ethyl methyl carbonate storage tank 5-6; and (3) allowing the tower bottom liquid of the ethyl methyl carbonate rectifying tower 5 to pass through a bottom pump 5-7 of the ethyl methyl carbonate rectifying tower, allowing part of the tower bottom liquid to enter a rectifying tower reboiler 5-1 for heating, returning the heated part of the tower bottom liquid to the ethyl methyl carbonate rectifying tower 5, and directly returning part of the tower bottom liquid to the batching tank 1.
The temperature of the top of the ethyl methyl carbonate rectifying tower 5 is 66 ℃, the pressure of the top of the tower is 0.026MPa, the temperature of the bottom of the tower is 85 ℃, the reflux ratio is 2, 102.4kg/h of ethyl methyl carbonate is extracted, and the yield of the ethyl methyl carbonate is 97.370% (the mass content is more than 99.9%).
According to the production method for preparing ethyl methyl carbonate based on the impinging stream transesterification tubular reactor, the quality of the prepared ethyl methyl carbonate is higher than that of the industrial ethyl methyl carbonate standard HG/T5158-2017.
Above technical scheme has explained the utility model discloses a technical thought can not prescribe a limit to with this the utility model discloses a protection scope, everything does not break away from the utility model discloses technical scheme's content, the foundation the utility model discloses a technical entity all belongs to the protection scope of the utility model technical scheme to any change and the decoration of above technical scheme institute.
Claims (6)
1. A device for producing methyl ethyl carbonate by using an impinging stream ester exchange tubular reactor is characterized in that: the device comprises a batching tank (1), an impinging stream ester exchange tubular reactor (2), a rear ester exchange tower system, a light component removal tower system and a methyl ethyl carbonate rectifying tower system which are connected in sequence; the batching tank (1) is also directly connected with a rear ester exchange tower system, a light component removal tower system and a methyl ethyl carbonate rectifying tower system;
the impinging stream transesterification tubular reactor (2) comprises a power fluid pump (2-1), a Laval nozzle (2-2), a high-speed jet impinging cavity (2-3), a gas-liquid coupler (2-4), a tubular reactor (2-5), a heater (2-6) and an ethanol vaporizer (2-7); the Laval nozzle (2-2), the high-speed jet impact cavity (2-3), the gas-liquid coupler (2-4) and the tubular reactor (2-5) are all arranged inside the heater (2-6); the end parts of the two Laval spray pipes (2-2) which are opposite to each other are fixedly communicated with gas-liquid couplers (2-4), and the pipe orifices of the gas-liquid couplers (2-4) are communicated with the outlet ends of the ethanol vaporizers (2-7); the two Laval nozzles (2-2) are arranged in opposite directions and communicated, a cavity formed by the middle communicated part is a mixing cavity, the high-speed jet impact cavity (2-3) is communicated in the vertical direction of the middle part of the mixing cavity, the high-speed jet impact cavity (2-3) is communicated with one end of the tubular reactor (2-5), and the other end of the tubular reactor (2-5) is communicated with a liquid inlet in the middle part of the rear ester exchange tower (3).
2. The apparatus for producing ethyl methyl carbonate in an impinging stream transesterification pipe reactor of claim 1, wherein: the mixing tank (1) is provided with a heating jacket (1-2) on the outer periphery, a tank structure of a mechanical stirrer (1-1) is arranged in the mixing tank, a liquid inlet is formed in the top of the mixing tank (1), the liquid inlet is connected with a methanol-dimethyl ester azeotrope pump (3-6) of the rear ester exchange tower (3), a liquid outlet at the bottom end of the mixing tank (1) is connected with an inlet end of a power fluid pump (2-1), and an outlet end of the power fluid pump (2-1) is connected with a liquid inlet end of a gas-liquid coupler (2-4) of the impinging stream ester exchange tubular reactor (2).
3. The apparatus for producing ethyl methyl carbonate in an impinging stream transesterification pipe reactor of claim 1, wherein: the rear ester exchange tower system consists of a rear ester exchange tower (3), a rear ester exchange tower reboiler (3-1), a rear ester exchange tower plate type tower plate (3-2), rear ester exchange tower white steel regular packing (3-3), a rear ester exchange tower condenser (3-4), a methanol-dimethyl ester azeotrope receiving tank (3-5), a methanol-dimethyl ester azeotrope pump (3-6), a rear ester exchange tower bottom pump (3-7) and a catalyst filter (3-8); the rear ester exchange tower (3) is of a tower body structure, a rear ester exchange tower plate type tower plate (3-2) is arranged at the bottom of the interior of the rear ester exchange tower (3), a rear ester exchange tower white steel regular packing (3-3) is arranged above the rear ester exchange tower (3), a tubular reactor (2-5) is communicated with the rear ester exchange tower (3), the top of the rear ester exchange tower (3) is sequentially communicated with a rear ester exchange tower condenser (3-4), a methanol-dimethyl ester azeotrope receiving tank (3-5) and an inlet of a methanol-dimethyl ester azeotrope pump (3-6), and the outlet end of the methanol-dimethyl ester azeotrope pump (3-6) is respectively communicated with the rear ester exchange tower (3), a feed inlet at the top of a proportioning tank (1) and a methanol recovery system; the bottom end of the rear ester exchange tower (3) is respectively connected with the inlet ends of a rear ester exchange tower reboiler (3-1) and a catalyst filter (3-8) through a rear ester exchange tower bottom pump (3-7), the outlet end of the rear ester exchange tower reboiler (3-1) is connected with the rear ester exchange tower (3), and the outlet end of the catalyst filter (3-8) is respectively connected with a light component removal tower (4) and a catalyst recovery system of a light component removal tower system.
4. The apparatus for producing ethyl methyl carbonate in an impinging stream transesterification pipe reactor of claim 1, wherein: the light component removal tower system consists of a light component removal tower (4), a light component removal tower reboiler (4-1), light component removal tower white steel structured packing (4-2), a light component removal tower condenser (4-3), a light component receiving tank (4-4), a light component pump (4-5) and a light component removal tower bottom pump (4-6); a light component removing tower white steel structured packing (4-2) is arranged in the light component removing tower (4), the top end of the light component removing tower (4) is sequentially communicated with a light component removing tower condenser (4-3), a light component receiving tank (4-4) and a light component pump (4-5), and the outlet end of the light component pump (4-5) is respectively communicated with the light component removing tower (4) and the batching tank (1); the bottom end of the light component removing tower (4) is communicated with a light component removing tower bottom pump (4-6), the light component removing tower bottom pump (4-6) is respectively communicated with a light component removing tower reboiler (4-1) and a methyl ethyl carbonate rectifying tower (5) of a methyl ethyl carbonate rectifying tower system, and the light component removing tower reboiler (4-1) is communicated with the light component removing tower (4).
5. The apparatus for producing ethyl methyl carbonate in an impinging stream transesterification pipe reactor of claim 1, wherein: the ethyl methyl carbonate rectifying tower system consists of an ethyl methyl carbonate rectifying tower (5), a rectifying tower reboiler (5-1), a rectifying tower condenser (5-3), an ethyl methyl carbonate receiving tank (5-4), an ethyl methyl carbonate pump (5-5), an ethyl methyl carbonate storage tank (5-6) and an ethyl methyl carbonate rectifying tower bottom pump (5-7); a rectifying tower white steel structured packing (5-2) is arranged in the ethyl methyl carbonate rectifying tower (5), the top end of the ethyl methyl carbonate rectifying tower (5) is sequentially communicated with a rectifying tower condenser (5-3), an ethyl methyl carbonate receiving tank (5-4) and an ethyl methyl carbonate pump (5-5), and the ethyl methyl carbonate pump (5-5) is respectively communicated with the ethyl methyl carbonate rectifying tower (5) and an ethyl methyl carbonate storage tank (5-6); the bottom end of the ethyl methyl carbonate rectifying tower (5) is communicated with a bottom pump (5-7) of the ethyl methyl carbonate rectifying tower, the bottom pump (5-7) of the ethyl methyl carbonate rectifying tower is respectively communicated with a rectifying tower reboiler (5-1) and a batching tank (1), and the rectifying tower reboiler (5-1) is communicated with the ethyl methyl carbonate rectifying tower (5).
6. The apparatus for producing ethyl methyl carbonate in an impinging stream transesterification pipe reactor of claim 1, wherein: the tubular reactor (2-5) is a tube with the length-diameter ratio of more than 1000, the diameter of the tube is phi 75mm or phi 100mm, and the tube is arranged to be a reciprocating type or a spring type.
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