CN115337893B - Device and method for preparing ethylene carbonate by high-speed jet impact on tubular reactor - Google Patents

Device and method for preparing ethylene carbonate by high-speed jet impact on tubular reactor Download PDF

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CN115337893B
CN115337893B CN202210985499.0A CN202210985499A CN115337893B CN 115337893 B CN115337893 B CN 115337893B CN 202210985499 A CN202210985499 A CN 202210985499A CN 115337893 B CN115337893 B CN 115337893B
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tank
ethylene carbonate
tubular reactor
speed jet
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CN115337893A (en
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程贵刚
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Shenyang University of Technology
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Shenyang University of Technology
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2415—Tubular reactors
    • B01J19/242—Tubular reactors in series
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/14—Fractional distillation or use of a fractionation or rectification column
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/42—Regulation; Control
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F27/00—Mixers with rotary stirring devices in fixed receptacles; Kneaders
    • B01F27/80—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis
    • B01F27/90—Mixers with rotary stirring devices in fixed receptacles; Kneaders with stirrers rotating about a substantially vertical axis with paddles or arms 
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/30—Driving arrangements; Transmissions; Couplings; Brakes
    • B01F35/32—Driving arrangements
    • B01F35/32005—Type of drive
    • B01F35/3204—Motor driven, i.e. by means of an electric or IC motor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/75—Discharge mechanisms
    • B01F35/754—Discharge mechanisms characterised by the means for discharging the components from the mixer
    • B01F35/7544—Discharge mechanisms characterised by the means for discharging the components from the mixer using pumps
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F35/00—Accessories for mixers; Auxiliary operations or auxiliary devices; Parts or details of general application
    • B01F35/90—Heating or cooling systems
    • B01F35/92—Heating or cooling systems for heating the outside of the receptacle, e.g. heated jackets or burners
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0053—Details of the reactor
    • B01J19/0066—Stirrers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D317/00—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms
    • C07D317/08—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3
    • C07D317/10—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings
    • C07D317/32—Heterocyclic compounds containing five-membered rings having two oxygen atoms as the only ring hetero atoms having the hetero atoms in positions 1 and 3 not condensed with other rings with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
    • C07D317/34—Oxygen atoms
    • C07D317/36—Alkylene carbonates; Substituted alkylene carbonates
    • C07D317/38—Ethylene carbonate
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00058—Temperature measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00054—Controlling or regulating the heat exchange system
    • B01J2219/00056—Controlling or regulating the heat exchange system involving measured parameters
    • B01J2219/00065—Pressure measurement
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00162—Controlling or regulating processes controlling the pressure

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention relates to a device and a method for preparing ethylene carbonate by a high-speed jet impact tubular reactor, wherein the device comprises a material mixing tank, a first high-speed jet impact tubular reactor, a gas-liquid separation tank, a second high-speed jet impact tubular reactor, a curing tank system, a glycol removal tower system and an ethylene carbonate rectifying tower system which are sequentially communicated; the batching jar is still with taking off ethylene glycol tower system intercommunication, curing jar system still communicates with first high-speed jet impact tubular reactor, gas-liquid separation jar and second high-speed jet impact tubular reactor respectively. The device and the method solve the problems of low heat and mass transfer efficiency, long reaction period, high energy consumption, cost rise caused by the increase of the energy consumption, and the like of the traditional preparation equipment.

Description

Device and method for preparing ethylene carbonate by high-speed jet impact on tubular reactor
Technical Field
The invention belongs to the technical field of chemical industry, and particularly relates to a device and a method for preparing ethylene carbonate by impacting a tubular reactor through high-speed jet flow.
Background
The industrial production method of ethylene carbonate generally adopts phosgene method, ester exchange method, addition method of ethylene oxide and carbon dioxide, alcoholysis method of urea and ethylene glycol, etc. The preparation process of the ethylene carbonate generally adopts a kettle-type reactor and mechanical stirring, and the preparation equipment has the defects of low heat and mass transfer efficiency, long reaction period, high energy consumption and cost rise caused by the increase of the energy consumption, and is not beneficial to industrial production.
The field is urgent to find a low-energy-consumption and environment-friendly process and equipment for preparing ethylene carbonate so as to overcome the technical problems.
Disclosure of Invention
The invention provides a device and a method for preparing ethylene carbonate by impacting a tubular reactor through high-speed jet flow, and aims to solve the problems of low heat and mass transfer efficiency, long reaction period, high energy consumption, cost rise caused by energy consumption increase, and the like of the existing preparation equipment, which are not beneficial to industrial production.
In order to achieve the above purpose, the present invention adopts the following technical scheme:
The device comprises a material mixing tank, a first high-speed jet impact tubular reactor, a gas-liquid separation tank, a second high-speed jet impact tubular reactor, a curing tank system, a glycol removal tower system and a ethylene carbonate rectifying tower system which are communicated in sequence; the batching jar is still with taking off ethylene glycol tower system intercommunication, curing jar system still communicates with first high-speed jet impact tubular reactor, gas-liquid separation jar and second high-speed jet impact tubular reactor respectively.
Further, the material mixing tank is a tank body structure with a heating medium arranged on the periphery, the upper part of the material mixing tank is communicated with a powder conveyer, a mechanical stirrer of the material mixing tank is arranged in the material mixing tank, and a liquid inlet at the top of the material mixing tank is communicated with a glycol removal tower system; the liquid outlet at the bottom of the batching tank is communicated with the inlet end of a first power fluid pump, and the outlet end of the first power fluid pump is communicated with the liquid inlet end of a first Laval nozzle of the first high-speed jet impact tubular reactor.
Further, the first high-speed jet impact tubular reactor comprises a first Laval nozzle, a first high-speed jet impact cavity, a first tubular reactor and a first heater; the first Laval nozzles, the first high-speed jet impact cavity and the first tubular reactor are all arranged in the first heater, the two first Laval nozzles are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the first high-speed jet impact cavity is communicated in the vertical direction of the middle part of the cavity, the first high-speed jet impact cavity is communicated with one end of the first tubular reactor, the other end of the first tubular reactor is communicated with a liquid inlet at the top of the vapor-liquid separation tank, and air inlets are formed at the pipe orifices of the two first Laval nozzles and are respectively communicated with a curing tank of the curing tank system and the vapor-liquid separator; the first tubular reactor is a tube with an aspect ratio of more than 1000, a diameter of phi 75mm or phi 100mm, and the tube is arranged in a reciprocating type or spring type.
Further, the steam-liquid separation tank is provided with a heating medium for the periphery circle, a tank body structure of a mechanical stirrer of the separation tank is arranged in the steam-liquid separation tank, an inlet end of the upper end of the steam-liquid separation tank is communicated with an outlet end of the first tubular reactor, a steam outlet end of the upper end of the steam-liquid separation tank is communicated with an ammonia compressor of the curing tank system through a separation tank condenser, and an outlet end of the bottom end of the steam-liquid separation tank is communicated with two second Laval nozzles of the second high-speed jet impact tubular reactor through a second power fluid pump.
Further, the second high-speed jet impact tubular reactor comprises a second Laval nozzle, a second high-speed jet impact cavity, a second tubular reactor and a second heater; the second Laval nozzle, the second high-speed jet impact cavity and the second tubular reactor are all arranged in the second heater, the two second Laval nozzles are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the second high-speed jet impact cavity is communicated in the vertical direction of the middle part of the cavity, the second high-speed jet impact cavity is communicated with one end of the second tubular reactor, and the other end of the second tubular reactor is communicated with a liquid inlet at the top of the curing tank; the pipe orifices of the two second Laval nozzles are provided with steam inlets which are respectively communicated with a curing tank and a gas-liquid separator of the curing tank system; the second tubular reactor is a tube with an aspect ratio of more than 1000, a diameter of phi 75mm or phi 100mm, and the tube is arranged in a reciprocating type or spring type. Further, the curing tank system comprises a curing tank, a curing tank condenser, an ammonia compressor, a gas-liquid separator, a nitrogen buffer tank and a liquid ammonia storage tank which are sequentially communicated, wherein the nitrogen buffer tank and the liquid ammonia storage tank are both communicated with the gas-liquid separator, the curing tank is a tank body structure, the periphery of the tank body is provided with a heating medium, and a mechanical stirrer of the curing tank is arranged in the tank body structure; the liquid inlet at the top end of the curing tank is communicated with the outlet end of a second tubular reactor of the second high-speed jet impact tubular reactor, the air inlet at the top end of the curing tank is communicated with a nitrogen buffer tank, and the curing tank is communicated with an ethylene glycol white steel structured packing tower of the ethylene glycol removal tower system through a crude ethylene carbonate pump.
Further, the destoner column system includes first reboiler, ethylene glycol white steel regular packing tower, ethylene glycol condenser, ethylene glycol receiving tank, ethylene glycol pump and ethylene glycol white steel regular packing tower bottom pump, the steam outlet intercommunication ethylene glycol condenser of ethylene glycol white steel regular packing tower, ethylene glycol condenser intercommunication ethylene glycol receiving tank, the ethylene glycol receiving tank is through ethylene glycol pump intercommunication ethylene glycol white steel regular packing tower and batching jar respectively, ethylene glycol white steel regular packing tower bottom is through the bottom of ethylene glycol white steel regular packing tower bottom pump intercommunication first reboiler and the ethylene carbonate white steel regular packing tower of ethylene carbonate rectifying column system respectively, the top of first reboiler is again with the intercommunication of ethylene glycol white steel regular packing tower bottom, first reboiler is the structure that is provided with the heat medium.
Further, the ethylene carbonate rectifying tower system comprises a second reboiler, an ethylene carbonate white steel structured packing tower, an ethylene carbonate condenser, an ethylene carbonate receiving tank, an ethylene carbonate pump, an ethylene carbonate storage tank and an ethylene carbonate rectifying tower bottom pump, wherein a steam outlet of the ethylene carbonate white steel structured packing tower is communicated with one end of the ethylene carbonate condenser, the other end of the ethylene carbonate condenser is communicated with one end of the ethylene carbonate receiving tank, and the other end of the ethylene carbonate receiving tank is respectively communicated with the ethylene carbonate white steel structured packing tower and the ethylene carbonate storage tank through the ethylene carbonate pump; the bottom of the ethylene carbonate white steel structured packing tower is respectively communicated with one end of a second reboiler and a catalyst recovery system through a pump at the bottom of the ethylene carbonate rectifying tower, the other end of the second reboiler is communicated with the bottom of the ethylene carbonate white steel structured packing tower, and the second reboiler is of a structure provided with a heating medium. The method for preparing the ethylene carbonate by using the high-speed jet impact tubular reactor specifically comprises the following steps of:
step 1, raw materials of urea particles, glycol and a catalyst are fed into a batching tank, the urea particles are dissolved under the stirring of a mechanical stirrer of the batching tank, the dissolved urea, glycol and the catalyst are uniformly mixed to obtain a mixed solution, and meanwhile, the mixed solution is heated to a reaction temperature through a heating medium; continuously feeding the mixed liquid into a first high-speed jet flow impact tubular reactor through a first power fluid pump;
Step 2, pumping the mixture from the material mixing tank into two opposite first Laval nozzles, sucking nitrogen separated by the curing tank system, mutually impacting two high-speed jet flows ejected from the first Laval nozzles in a first high-speed jet impact cavity, then entering a first tubular reactor for alcoholysis reaction, and continuously entering a gas-liquid separation tank from the nitrogen ejected from the first high-speed jet impact tubular reactor, ammonia generated by reaction and alcoholysis liquid;
Step 3, separating the ammonia generated by the nitrogen and the reaction from the alcoholysis liquid in a gas-liquid separation tank, enabling the separated gas to enter an ammonia compressor of a curing tank system, and enabling the alcoholysis liquid after the gas separation to continuously enter a second high-speed jet flow to impact a tubular reactor;
step 4, pumping the alcoholysis liquid in the step 3 into two opposite second Laval nozzles through a second power fluid pump, sucking nitrogen separated by a curing tank system, mutually impacting two high-speed jet streams ejected from the second Laval nozzles in a second high-speed jet stream impacting cavity, then entering a second tubular reactor for alcoholysis reaction, and continuously entering the curing tank from nitrogen ejected from the second high-speed jet stream impacting tubular reactor and ammonia alcoholysis liquid generated by reaction;
Step 5, separating the nitrogen and the ammonia generated by the reaction from the alcoholysis liquid in a curing tank, and simultaneously continuously introducing the separated nitrogen to carry out supplementary alcoholysis reaction; the nitrogen and the ammonia separated from the gas-liquid separation tank and the curing tank enter an ammonia compressor together, and the ammonia is liquefied and separated from the nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank, and the separated nitrogen gas enters a nitrogen buffer tank; the nitrogen in the nitrogen buffer tank is continuously used for alcoholysis reaction; continuously pumping the alcoholysis liquid after separating gas in the curing tank into a glycol removal tower system through a crude ethylene carbonate pump;
Step 6, removing residual glycol from the alcoholysis reaction in a glycol white steel structured packing tower of a glycol removal tower system, and cooling the removed glycol by a glycol condenser and then entering a glycol receiving tank; part of ethylene glycol is taken as reflux of the ethylene glycol white steel structured packing tower through an ethylene glycol pump, and part of ethylene glycol is extracted to a batching tank; the tower bottom liquid of the ethylene glycol white steel structured packing tower enters a first reboiler through a part of a pump at the bottom of the ethylene glycol white steel structured packing tower to be heated, and then returns to the ethylene glycol white steel structured packing tower, and part of the tower bottom liquid continuously enters a ethylene carbonate rectifying tower system;
step 7, rectifying the ethylene carbonate in a ethylene carbonate rectifying tower system, and cooling the rectified ethylene carbonate by a ethylene carbonate condenser and then feeding the cooled ethylene carbonate into a ethylene carbonate receiving tank; part of ethylene carbonate is taken as reflux of the ethylene carbonate white steel structured packing tower through an ethylene carbonate pump, and part of ethylene carbonate is extracted to an ethylene carbonate storage tank; and (3) feeding the tower bottom liquid of the ethylene carbonate rectifying tower into a second reboiler through a pump part at the bottom of the ethylene carbonate rectifying tower to be heated, returning the tower bottom liquid to the ethylene carbonate white steel structured packing tower, and feeding part of the tower bottom liquid into a catalyst recovery system to recover the catalyst.
Further, the reaction temperature in the material mixing tank is 137-141 ℃, the pressure is normal pressure, and the urea: the molar ratio of the ethylene glycol is 1:1.5 to 1.75 percent, the mass of the catalyst is 2 to 3 percent of that of urea, and the retention time of the materials is 0.5 to 0.75h;
The reaction temperature in the first high-speed jet impact tubular reactor is 137-141 ℃, the pressure is 0.4-0.5 MPa, the length-diameter ratio of the tubular reactor is 1000, and 1kmol urea is absorbed into nitrogen gas 10Nm 3;
The reaction temperature in the gas-liquid separation tank is 137-141 ℃, the pressure is normal pressure, and the retention time of the materials is 0.5-0.75 h;
The second high-speed jet impact pipe reactor has the internal temperature of 137-141 ℃ and the pressure of 0.4-0.5 MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
The reaction temperature in the curing tank is 141-145 ℃ and the pressure is normal pressure; the nitrogen pressure at the outlet of the ammonia compressor is 0.25MPa,1kmol urea is blown into 10Nm 3 of nitrogen, and the retention time of materials is 1.5-2 h;
The temperature of the top of the ethylene glycol white steel structured packing tower is 150 ℃, and the pressure of the top of the tower is 0.02MPa; the bottom temperature is 178 ℃, and the molar reflux ratio is 0.15;
The temperature of the top of the ethylene carbonate white steel structured packing tower is 140 ℃, and the pressure of the top of the tower is 0.002MPa; the bottom temperature was 155℃and the molar reflux ratio was 0.2.
The beneficial effects are as follows:
1. The device adopts a high-speed jet flow impact tubular reactor to carry out alcoholysis reaction, two heterogeneous fluids flow at a high speed in opposite directions, a highly turbulent impact area is formed by impact, the impact flow effectively improves the mixing and mass transfer effects in the reactor, and the reaction rate and the product yield are improved;
2. the device shortens the reaction time, saves energy, improves the production efficiency, and is environment-friendly;
3. The yield of the ethylene carbonate is more than 92%, and the quality of the ethylene carbonate is better than that of the industrial national standard; the invention has mature process, advanced equipment, continuous operation and high automation degree.
Drawings
FIG. 1 is a schematic diagram of an apparatus for preparing ethylene carbonate based on a high velocity jet impingement tube reactor according to the present invention;
Reference numerals: 1. 1-1 parts of a batching tank, 1-2 parts of a batching tank mechanical stirrer and a powder conveyer; 2. the first high-speed jet stream impacts the tubular reactor, 2-1, a first power fluid pump, 2-2, a first Laval nozzle, 2-3, a first high-speed jet stream impacts the cavity, 2-4, a first tubular reactor, 2-5, a first heater; 3. 3-1 parts of a gas-liquid separation tank, 3-2 parts of a separation tank mechanical stirrer and 3-2 parts of a separation tank condenser; 4. the second high-speed jet stream impacts the tubular reactor, 4-1, the second power fluid pump, 4-2, the second Laval nozzle, 4-3, the second high-speed jet stream impacts the cavity, 4-4, the second tubular reactor, 4-5, the second heater; 5. 5-1 parts of curing tank, 5-2 parts of curing tank mechanical stirrer, 5-3 parts of curing tank condenser, 5-3 parts of ammonia gas compressor, 5-4 parts of gas-liquid separator, 5-5 parts of nitrogen buffer tank, 5-6 parts of liquid ammonia storage tank, 5-7 parts of crude ethylene carbonate pump; 6. the system comprises a glycol removal tower system, 6-1 parts of a first reboiler, 6-2 parts of a glycol white steel structured packing tower, 6-3 parts of a glycol condenser, 6-4 parts of a glycol receiving tank, 6-5 parts of a glycol pump, 6-6 parts of a glycol white steel structured packing tower bottom pump; 7. the system comprises 7-1 parts of ethylene carbonate rectifying tower system, a second reboiler, 7-2 parts of ethylene carbonate white steel structured packing tower, 7-3 parts of ethylene carbonate condenser, 7-4 parts of ethylene carbonate receiving tank, 7-5 parts of ethylene carbonate pump, 7-6 parts of ethylene carbonate storage tank, and 7-7 parts of ethylene carbonate white steel structured packing tower bottom pump.
Detailed Description
The present invention will be described in further detail with reference to the following examples in order to make the objects, technical solutions and advantages of the present invention more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the invention.
As shown in fig. 1, a device for preparing ethylene carbonate based on a high-speed jet impact tubular reactor comprises a material preparation tank 1, a first high-speed jet impact tubular reactor 2, a gas-liquid separation tank 3, a second high-speed jet impact tubular reactor 4, a curing tank system, a glycol removal tower system 6 and an ethylene carbonate rectifying tower system 7 which are sequentially communicated; the batching tank 1 is also communicated with a glycol removal tower system 6, and the curing tank system is also respectively communicated with a first high-speed jet impact tubular reactor 2, a gas-liquid separation tank 3 and a second high-speed jet impact tubular reactor 4.
The material mixing tank 1 is a tank body structure with a heat medium arranged on the periphery, the upper part of the material mixing tank is communicated with the powder material conveyer 1-2, a material mixing tank mechanical stirrer 1-1 is arranged in the material mixing tank, a catalyst and ethylene glycol liquid inlet are formed in the top of the material mixing tank 1, and the liquid inlet in the top of the material mixing tank 1 is communicated with the ethylene glycol removal tower system 6; the liquid outlet at the bottom of the material mixing tank 1 is communicated with the inlet end of a first power fluid pump 2-1, and the outlet end of the first power fluid pump 2-1 is communicated with the liquid inlet end of a first Laval nozzle 2-2 of a first high-speed jet impact tubular reactor 2; the preparation tank 1 is used for dissolving urea particles by glycol, and uniformly mixing the catalyst, glycol and dissolved urea under the action of stirring; the mixed liquid reaches the reaction temperature under the heating of the heating medium, and enters the first high-speed jet flow through the first power fluid pump 2-1 to strike the tubular reactor 2.
The first high-speed jet impact pipe reactor 2 comprises a first Laval nozzle 2-2, a first high-speed jet impact cavity 2-3, a first pipe reactor 2-4 and a first heater 2-5; the first Laval nozzles 2-2, the first high-speed jet impact cavities 2-3 and the first tubular reactors 2-4 are all arranged inside the first heater 2-5, the two first Laval nozzles 2-2 are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the first high-speed jet impact cavities 2-3 are communicated in the vertical direction of the middle part of the cavity, the first high-speed jet impact cavities 2-3 are communicated with one end of the first tubular reactor 2-4, the other end of the first tubular reactor 2-4 is communicated with a liquid inlet at the top of the vapor-liquid separation tank 3, the first tubular reactor 2-4 is a pipe with the length-diameter ratio larger than 1000, can be phi 75mm or phi 100mm, and can be arranged as a reciprocating type or spring type. The pipe orifices of the two first Laval nozzles 2-2 are provided with air inlets which are communicated with a curing tank 5 and a gas-liquid separator 5-4 of the curing tank system. The first high-speed jet impact pipe reactor 2 is used for alcoholysis reaction; the mixed solution of the material mixing tank 1 is pumped into two opposite first Laval nozzles 2-2 through a first power fluid pump 2-1, nitrogen gas of a curing tank system is sucked at the same time, two high-speed jet flows sprayed out of the first Laval nozzles 2-2 collide with each other in a high-speed jet flow collision cavity, then the mixed solution enters a first tubular reactor 2-4 for alcoholysis reaction, and the nitrogen gas, ammonia gas generated by the reaction and alcoholysis solution continuously enter a gas-liquid separation tank 3.
The mixed liquid output by the material mixing tank 1 is sprayed out at a high speed through the first Laval nozzle 2-2, so that a negative pressure area is generated at a gas suction inlet, nitrogen is sucked in, rapidly expands in the negative pressure area and is beaten into tiny bubbles by a power fluid, and the tiny bubbles enter a mixing cavity; at this time, in the mixing cavity, the gas (nitrogen) and the liquid are fully mixed in the mixing cavity, and the gas (nitrogen) and the liquid are accelerated to be discharged due to energy exchange, the speed can reach the sonic speed, and the potential energy of the mixed liquid is increased to the maximum through the diffusion cavity of the first Laval nozzle 2-2, so that the effects of mass transfer and heat transfer are stronger; two heterogeneous fluids flow at a high speed in opposite directions, and form a highly turbulent first high-speed jet impact cavity 2-3 through impact, so that the heat and mass transfer in the process is greatly enhanced; the strong microscopic mixing and pressure fluctuation characteristics of the impinging stream can enable the chemical reaction to be fast carried out, and the effective and uniform supersaturation degree is generated instantaneously; and because the chaotic flow state enables the mixing scale to be rapidly reduced, the vortex with different scales and mutually folded collision enhance the turbulence intensity and the energy diffusion, so that molecules are caused to achieve more effective high-level collision when chemical reaction occurs, 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 gas-liquid separation tank 3 is a tank body structure with a heat medium arranged on the outer periphery and a separation tank mechanical stirrer 3-1 arranged inside, the inlet end of the upper end of the gas-liquid separation tank 3 is communicated with the outlet end of the first tubular reactor 2-4, the gas outlet end of the upper end of the gas-liquid separation tank 3 is communicated with the ammonia gas compressor 5-3 of the curing tank system through a separation tank condenser 3-2, and the outlet end of the bottom end of the gas-liquid separation tank 3 is communicated with two second Laval nozzles 4-2 of the second high-speed jet impact tubular reactor 4 through a second power fluid pump 4-1. The gas-liquid separation tank 3 is used for separating nitrogen, ammonia generated by the reaction and alcoholysis liquid; the alcoholysis liquid from the first high-speed jet impact tubular reactor 2 continuously enters a gas-liquid separation tank 3, the gas-liquid separation tank 3 separates nitrogen and ammonia generated by reaction from the alcoholysis liquid, the separated gas enters an ammonia compressor 5-3, and the alcoholysis liquid enters a second high-speed jet impact tubular reactor 4 through a second power fluid pump 4-1.
The structure of the second high-speed jet impact tubular reactor 4 is consistent with that of the first high-speed jet impact tubular reactor 2, the second high-speed jet impact tubular reactor 4 comprises a second Laval nozzle 4-2, a second high-speed jet impact cavity 4-3, a second tubular reactor 4-4 and a second heater 4-5; the second Laval nozzles 4-2, the second high-speed jet impact cavity 4-3 and the second tubular reactor 4-4 are all arranged inside the second heater 4-5, the two second Laval nozzles 4-2 are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the second high-speed jet impact cavity 4-3 is communicated in the vertical direction of the middle of the cavity, the second high-speed jet impact cavity 4-3 is communicated with one end of the second tubular reactor 4-4, and the other end of the second tubular reactor 4-4 is communicated with a liquid inlet at the top of the curing tank 5. The second tubular reactor 4-4 is a tube having an aspect ratio of more than 1000, which may be Φ75mm or Φ100deg.M, and which may be of the reciprocating type or of the spring type. The pipe orifices of the two second Laval nozzles 4-2 are provided with steam inlets which are communicated with a curing tank 5 and a gas-liquid separator 5-4 of the curing tank system. The second high-speed jet stream impacts the tubular reactor 4 for alcoholysis reaction; the alcoholysis liquid after separating gas in the gas-liquid separation tank 3 is pumped into two opposite second Laval nozzles 4-2 through a second power fluid pump 4-1, and simultaneously is sucked into nitrogen of a curing tank system, two high-speed jet flows ejected from the second Laval nozzles 4-2 are mutually impacted in a high-speed jet flow impact cavity, then enter a second tubular reactor 4-4 for alcoholysis reaction, and the alcoholysis liquid continuously enters a curing tank 5.
The curing tank system comprises a curing tank 5, a curing tank condenser 5-2, an ammonia compressor 5-3, a gas-liquid separator 5-4, a nitrogen buffer tank 5-5 and a liquid ammonia storage tank 5-6 which are communicated with the gas-liquid separator 5-4 in sequence. The curing tank 5 is of a tank body structure with a heating medium arranged on the periphery and a mechanical stirrer 5-1 arranged in the curing tank; the top liquid inlet of the curing tank 5 is communicated with the outlet end of a second tubular reactor 4-4 of the second high-speed jet impact tubular reactor 4, the top air inlet of the curing tank 5 is communicated with a nitrogen buffer tank 5-5, and the curing tank 5 is communicated with an ethylene glycol white steel structured packing tower 6-2 of an ethylene glycol removal tower system 6 through a crude ethylene carbonate pump 5-7; the curing tank 5 is used for gas-liquid separation and supplementary alcoholysis reaction; the alcoholysis liquid from the second high-speed jet impact tubular reactor 4 continuously enters a curing tank 5, nitrogen and ammonia generated by the reaction are separated from the alcoholysis liquid in the curing tank 5, and meanwhile, nitrogen is continuously introduced into the reactor through a nitrogen buffer tank 5-5 for supplementing alcoholysis reaction. The nitrogen and the ammonia separated from the gas-liquid separation tank 3 and the curing tank 5 enter an ammonia compressor 5-3 together, and the ammonia compressor 5-3 separates ammonia liquefaction from nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank 5-6, and the separated nitrogen gas enters a nitrogen buffer tank 5-5; the nitrogen in the nitrogen buffer tank 5-5 is continuously used for alcoholysis reaction carried out by the first high-speed jet impinging on the tubular reactor 2 and the second high-speed jet impinging on the tubular reactor 4; the alcoholysis liquid after separating gas in the curing tank 5 is continuously pumped into the glycol removal tower system 6 through the crude ethylene carbonate pump 5-7.
The glycol removal tower system 6 comprises a first reboiler 6-1, a glycol white steel structured packing tower 6-2, a glycol condenser 6-3, a glycol receiving tank 6-4, a glycol pump 6-5 and a glycol white steel structured packing tower bottom pump 6-6, a steam outlet of the glycol white steel structured packing tower 6-2 is communicated with the glycol condenser 6-3, the glycol condenser 6-3 is communicated with the glycol receiving tank 6-4, the glycol receiving tank 6-4 is respectively communicated with the glycol white steel structured packing tower 6-2 and the batching tank 1 through the glycol pump 6-5, the bottom of the glycol white steel structured packing tower 6-2 is respectively communicated with the bottom of the first reboiler 6-1 and the ethylene carbonate white steel structured packing tower 7-2 of the ethylene carbonate rectifying tower system 7 through the glycol white steel structured packing tower bottom pump 6-6, the top of the first reboiler 6-1 is further communicated with the bottom of the glycol white steel structured packing tower 6-2, and the first reboiler 6-1 is of a structure provided with a heating medium. The glycol removal tower system 6 is used for removing residual glycol in the alcoholysis reaction; continuously pumping the alcoholysis solution after gas separation in the curing tank 5 into an ethylene glycol white steel structured packing tower 6-2 through a crude ethylene carbonate pump 5-7, removing residual ethylene glycol in the ethylene glycol white steel structured packing tower 6-2, and cooling a removed ethylene glycol condenser 6-3 to enter an ethylene glycol receiving tank 6-4; part of ethylene glycol is taken as reflux of the ethylene glycol white steel structured packing tower 6-2 through the ethylene glycol pump 6-5, and part of ethylene glycol is extracted to the batching tank 1; the tower bottom liquid of the ethylene glycol white steel structured packing tower 6-2 enters a first reboiler 6-1 through a tower bottom pump 6-6 part of the ethylene glycol white steel structured packing tower to be heated and then returns to the ethylene glycol white steel structured packing tower 6-2, and enters a ethylene carbonate white steel structured packing tower 7-2 of a ethylene carbonate rectifying tower system 7 part of the ethylene carbonate white steel structured packing tower continuously.
The ethylene carbonate rectifying tower system 7 comprises a second reboiler 7-1, an ethylene carbonate white steel structured packing tower 7-2, an ethylene carbonate condenser 7-3, an ethylene carbonate receiving tank 7-4, an ethylene carbonate pump 7-5, an ethylene carbonate storage tank 7-6 and an ethylene carbonate rectifying tower bottom pump 7-7. The steam outlet of the ethylene carbonate white steel structured packing tower 7-2 is communicated with one end of an ethylene carbonate condenser 7-3, the other end of the ethylene carbonate condenser 7-3 is communicated with one end of an ethylene carbonate receiving tank 7-4, and the other end of the ethylene carbonate receiving tank 7-4 is respectively communicated with the ethylene carbonate white steel structured packing tower 7-2 and an ethylene carbonate storage tank 7-6 through an ethylene carbonate pump 7-5; the bottom of the ethylene carbonate white steel structured packing tower 7-2 is respectively communicated with one end of a second reboiler 7-1 and a catalyst recovery system through an ethylene carbonate rectifying tower bottom pump 7-7, the other end of the second reboiler 7-1 is communicated with the bottom of the ethylene carbonate white steel structured packing tower 7-2, and the second reboiler 7-1 is of a structure provided with a heating medium. The ethylene carbonate rectifying tower system 7 is used for rectifying ethylene carbonate; the tower bottom liquid from which the glycol is removed by the glycol removal tower system 6 continuously enters a ethylene carbonate white steel structured packing tower 7-2 through a part of a tower bottom pump 6-6 of the ethylene glycol white steel structured packing tower, ethylene carbonate is rectified in the ethylene carbonate white steel structured packing tower 7-2, and the rectified ethylene carbonate enters a ethylene carbonate receiving tank 7-4 through a ethylene carbonate condenser 7-3 for cooling; part of ethylene carbonate is used as reflux of an ethylene carbonate white steel structured packing tower 7-2 through an ethylene carbonate pump 7-5, and part of ethylene carbonate is extracted to an ethylene carbonate storage tank 7-6; and (3) part of tower bottom liquid of the ethylene carbonate white steel structured packing tower 7-2 enters a second reboiler 7-1 through a pump 7-7 at the bottom of the ethylene carbonate rectifying tower to be heated, and then returns to the ethylene carbonate white steel structured packing tower 7-2, and part of tower bottom liquid enters a catalyst recovery system to recover the catalyst.
The raw materials adopted by the invention are industrial urea particles (the mass content is more than 98 percent), industrial glycol (the mass content is more than 99 percent), catalysts and the like; the utility steam is 0.4MPa, and the temperature of the super-heated steam is 290 ℃; the public engineering water vapor mainly provides heat sources for heating media of the batching tank 1, heating media of the first heater 2-5 in the first high-speed jet stream impinging tubular reactor 2, heating media of the gas-liquid separation tank 3, heating media of the second heater 4-5 in the second high-speed jet stream impinging tubular reactor 4, heating media of the curing tank 5, heating media of the first reboiler 6-1 in the glycol removal tower system 6 and heating media of the second reboiler 7-1 in the ethylene carbonate rectifying tower system 7; the heat medium structure is an existing jacket structure; the heat medium structure of the tower kettle is the existing reboiler structure. The devices of the device are communicated through corresponding pipelines, and when the pipelines in the figure 1 are crossed but are not crossed in practice, the pipelines are drawn according to the principle of continuous vertical and horizontal cutting.
The method for producing the ethylene carbonate by the device specifically comprises the following steps:
(1) Raw materials of urea particles (the mass content is more than 98 percent), ethylene glycol (the mass content of industrial ethylene glycol is more than 99 percent) and a catalyst are fed into a batching tank 1, the urea particles are dissolved under the stirring of a batching tank mechanical stirrer 1-1, and the dissolved urea, the ethylene glycol and the catalyst are uniformly mixed and are heated to the reaction temperature through a heating medium; the mixed liquid continuously enters a first high-speed jet flow through a first power fluid pump 2-1 to strike the tubular reactor 2; the temperature in the batching tank 1 is 137-141 ℃, the pressure is normal pressure, and urea: ethylene glycol was 1: (1.5-1.75) (molar ratio), the catalyst is 2-3 percent (mass) of urea, and the retention time of the materials is 0.5-0.75 h;
(2) The mixed liquid from the material preparing tank 1 is pumped into two opposite first Laval nozzles 2-2, and simultaneously nitrogen separated by the curing tank system is sucked, two high-speed jet flows ejected from the first Laval nozzles 2-2 collide with each other in a first high-speed jet flow collision cavity 2-3, then enter a first tubular reactor 2-4 for alcoholysis reaction, and the nitrogen ejected from the first high-speed jet flow collision tubular reactor 2, ammonia generated by reaction and alcoholysis liquid continuously enter a gas-liquid separation tank 3; the first high-speed jet impact pipe reactor 2 has the temperature of 137-141 ℃ and the pressure of 0.4-0.5 MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
(3) The gas-liquid separation tank 3 separates the nitrogen and the ammonia generated by the reaction from the alcoholysis liquid, the separated gas enters an ammonia compressor 5-3 of the curing tank system, and the alcoholysis liquid after the gas separation continuously enters a second high-speed jet flow to impact the tubular reactor 4; the temperature in the gas-liquid separation tank 3 is 137-141 ℃, the pressure is normal pressure, and the retention time of the materials is 0.5-0.75 h;
(4) Pumping the alcoholysis liquid into two opposite second Laval nozzles 4-2 through a second power fluid pump 4-1, sucking nitrogen separated by a curing tank system, mutually impacting two high-speed jet streams ejected from the second Laval nozzles 4-2 in a second high-speed jet stream impacting cavity 4-3, then entering a second tubular reactor 4-4 for alcoholysis reaction, and continuously entering a curing tank 5 from the nitrogen ejected from the second high-speed jet stream impacting the tubular reactor 4 and ammonia alcoholysis liquid generated by the reaction; the second high-speed jet impact pipe reactor 4 has the temperature of 137-141 ℃ and the pressure of 0.4-0.5 MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
(5) Separating nitrogen and ammonia generated by the reaction from alcoholysis liquid in a curing tank 5, and simultaneously continuously introducing the separated nitrogen to carry out supplementary alcoholysis reaction; the nitrogen and the ammonia separated from the gas-liquid separation tank 3 and the curing tank 5 enter an ammonia compressor 5-3 together to separate ammonia liquefaction from nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank 5-6, and the separated nitrogen gas enters a nitrogen buffer tank 5-5; the nitrogen in the nitrogen buffer tank 5-5 is continuously used for alcoholysis reaction; the alcoholysis liquid after gas separation in the curing tank 5 is continuously pumped into a glycol removal tower system 6 through a crude ethylene carbonate pump; the temperature in the curing tank 5 is 141-145 ℃ and the pressure is normal pressure; the nitrogen pressure at the outlet of the ammonia compressor 5-3 is 0.25MPa,1kmol urea is blown into 10Nm 3 of nitrogen, and the retention time of materials is 1.5-2 h;
(6) The residual glycol from the alcoholysis reaction is removed in a glycol white steel structured packing tower 6-2 of a glycol removal tower system 6, and the removed glycol is cooled by a glycol condenser 6-3 and enters a glycol receiving tank 6-4; part of ethylene glycol is taken as reflux of the ethylene glycol white steel structured packing tower 6-2 through the ethylene glycol pump 6-5, and part of ethylene glycol is extracted to the batching tank 1; the tower bottom liquid of the ethylene glycol white steel structured packing tower 6-2 enters a first reboiler 6-1 through a part of an ethylene glycol white steel structured packing tower bottom pump 6-6 to be heated and then returns to the ethylene glycol white steel structured packing tower 6-2, and part of the tower bottom liquid continuously enters a ethylene carbonate rectifying tower system 7; the temperature of the top of the ethylene glycol white steel structured packing tower 6-2 is 150 ℃, and the pressure of the top of the tower is 0.02MPa; the bottom temperature was 178℃and the reflux ratio was 0.15 (mol);
(7) Rectifying ethylene carbonate in an ethylene carbonate rectifying tower system 7, and cooling the rectified ethylene carbonate in an ethylene carbonate condenser 7-3 to enter an ethylene carbonate receiving tank 7-4; part of ethylene carbonate is used as reflux of an ethylene carbonate white steel structured packing tower 7-2 through an ethylene carbonate pump 7-5, and part of ethylene carbonate is extracted to an ethylene carbonate storage tank 7-6; and (3) partially feeding the tower bottom liquid of the ethylene carbonate rectifying tower into a second reboiler 7-1 through a pump 7-7 at the bottom of the ethylene carbonate rectifying tower, heating, returning to the ethylene carbonate white steel structured packing tower 7-2, and partially feeding into a catalyst recovery system to recover the catalyst. The temperature of the top of the 7-2 column of the ethylene carbonate white steel structured packing column is 140 ℃, and the pressure of the top of the column is 0.002MPa; the bottom temperature was 155℃and the reflux ratio was 0.2 (mol).
Example 1
A method for producing ethylene carbonate based on a device for preparing ethylene carbonate by high-speed jet impact pipe type reactor, comprising the following steps:
61kg/h of raw material industrial urea particles (the mass content is more than 98%), 93.6kg/h of industrial ethylene glycol (the mass content is more than 99%) and 1.22kg/h of catalyst are fed into a batching tank 1, the urea particles are dissolved under the stirring of a batching tank mechanical stirrer 1-1, and the dissolved urea, the ethylene glycol and the catalyst are uniformly mixed and are heated to the reaction temperature through a heating medium (jacket); the mixed liquid continuously enters a first high-speed jet flow to strike the tubular reactor 2; the temperature in the batching tank 1 is 137 ℃, the pressure is normal pressure, and urea: ethylene glycol was 1:1.5 (molar ratio), the catalyst is 2 percent (mass) of urea, and the retention time of the materials is 0.75h;
continuously feeding the mixed liquid from the material mixing tank 1 into a first high-speed jet impact tubular reactor 2, pumping two opposite first Laval nozzles 2-2 through a first power fluid pump 2-1, simultaneously sucking nitrogen, mutually impacting two high-speed jets ejected from the first Laval nozzles 2-2 in a first high-speed jet impact cavity 2-3, then feeding the mixed liquid into the first tubular reactor 2-4 for alcoholysis reaction, and continuously feeding alcoholysis liquid discharged from the first high-speed jet impact tubular reactor 2 into a gas-liquid separation tank 3; the first high-speed jet impact pipe reactor 2 has the temperature of 137 ℃, the pressure of 0.4MPa, the length-diameter ratio of the pipe reactor of 1000, and the suction nitrogen of 1kmol urea of 10Nm 3;
The alcoholysis liquid from the first high-speed jet stream impacting the tubular reactor 2 continuously enters a gas-liquid separation tank 3, the gas-liquid separation tank 3 separates nitrogen and ammonia generated by the reaction from the alcoholysis liquid, the separated gas enters an ammonia compressor 5-3, and the alcoholysis liquid after separating the gas continuously enters a second high-speed jet stream impacting the tubular reactor 4; the temperature in the gas-liquid separation tank 3 is 137 ℃, the pressure is normal pressure, and the retention time of the materials is 0.75h;
continuously introducing the alcoholysis liquid after gas separation from the gas-liquid separation tank 3 into a second high-speed jet impact tubular reactor 4, pumping the alcoholysis liquid after gas separation in the gas-liquid separation tank 3 into two opposite second Laval nozzles 4-2 through a second power fluid pump 4-1, simultaneously sucking nitrogen, mutually impacting two high-speed jets ejected from the second Laval nozzles 4-2 in a second high-speed jet impact cavity 4-3, then introducing the alcoholysis liquid into the second tubular reactor 4-4 for alcoholysis reaction, and continuously introducing the alcoholysis liquid from the second high-speed jet impact tubular reactor 4 into a curing tank 5 of a curing tank system; the second high-speed jet impact pipe reactor 4 has the temperature of 137 ℃ and the pressure of 0.4MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
The step (5) is that the alcoholysis liquid from the high second high-speed jet flow impinging on the tubular reactor 4 continuously enters the curing tank 5, the nitrogen and the ammonia generated by the reaction are separated from the alcoholysis liquid in the curing tank 5, and meanwhile, the nitrogen is continuously introduced to carry out the supplementary alcoholysis reaction; the nitrogen and the ammonia separated from the gas-liquid separation tank 3 and the curing tank 5 enter an ammonia compressor 5-3 together to separate ammonia liquefaction from nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank 5-6, and the separated nitrogen gas enters a nitrogen buffer tank 5-5; the nitrogen in the nitrogen buffer tank 5-5 is continuously used for alcoholysis reaction; the alcoholysis liquid after gas separation in the curing tank 5 is continuously pumped into an ethylene glycol white steel structured packing tower 6-2 of an ethylene glycol removal tower system 6 through a crude ethylene carbonate pump 5-7; the temperature in the curing tank 5 is 141 ℃ and the pressure is normal pressure; the nitrogen pressure at the outlet of the ammonia compressor 5-3 is 0.25MPa,1kmol urea is blown into 10Nm 3 of nitrogen, and the retention time of materials is 2h;
Continuously pumping the alcoholysis solution obtained after gas separation in the curing tank 5 into the ethylene glycol white steel structured packing tower 6-2 through the coarse ethylene carbonate pump 5-7, removing residual ethylene glycol in the ethylene glycol white steel structured packing tower 6-2, and cooling the removed ethylene glycol through the ethylene glycol condenser 6-3 to enter the ethylene glycol receiving tank 6-4; part of ethylene glycol is taken as reflux of the ethylene glycol white steel structured packing tower 6-2 through the ethylene glycol pump 6-5, and part of ethylene glycol is extracted to the batching tank 1; the tower bottom liquid of the ethylene glycol white steel structured packing tower 6-2 enters a first reboiler 6-1 through a part of an ethylene glycol white steel structured packing tower bottom pump 6-6 to be heated and then returns to the ethylene glycol white steel structured packing tower 6-2, and part of the ethylene glycol white steel structured packing tower enters a ethylene carbonate white steel structured packing tower 7-2 of a ethylene carbonate rectifying tower system 7 continuously; the temperature of the top of the ethylene glycol white steel structured packing tower 6-2 is 150 ℃, and the pressure of the top of the tower is 0.02MPa; the bottom temperature was 178℃and the reflux ratio was 0.15 (mol);
Continuously feeding tower bottom liquid from the ethylene glycol white steel structured packing tower 6-2 into a ethylene carbonate white steel structured packing tower 7-2, rectifying ethylene carbonate in the ethylene carbonate white steel structured packing tower 7-2, and cooling the rectified ethylene carbonate by a ethylene carbonate condenser 7-3 and feeding the cooled ethylene carbonate into a ethylene carbonate receiving tank 7-4; part of ethylene carbonate is used as reflux of an ethylene carbonate white steel structured packing tower 7-2 through an ethylene carbonate pump 7-5, and part of ethylene carbonate is extracted to an ethylene carbonate storage tank 7-6; part of the tower bottom liquid of the ethylene carbonate rectifying tower enters a second reboiler 7-1 through a pump 7-7 at the bottom of the ethylene carbonate rectifying tower to be heated and then returns to the ethylene carbonate white steel structured packing tower 7-2, and the other part enters a catalyst recovery system to recover the catalyst; the temperature of the top of the ethylene carbonate rectifying tower is 140 ℃, and the pressure of the top of the tower is 0.002MPa; the bottom temperature was 155℃and the reflux ratio was 0.2 (mol), and 81kg/h of ethylene carbonate was recovered in a yield of 92.32%.
Example 2
A method for producing ethylene carbonate based on a device for preparing ethylene carbonate by high-speed jet impact pipe type reactor, comprising the following steps:
61kg/h of raw material industrial urea particles (the mass content is more than 98%), 109kg/h of industrial ethylene glycol (the mass content is more than 99%) and 1.83kg/h of catalyst are fed into a batching tank 1, the urea particles are dissolved under the stirring of a mechanical stirrer 1-1 of the batching tank, and the dissolved urea, the ethylene glycol and the catalyst are uniformly mixed and heated to the reaction temperature through a jacket; the mixed liquid continuously enters a first high-speed jet flow to strike the tubular reactor 2; the temperature in the batching tank 1 is 141 ℃, the pressure is normal pressure, urea: ethylene glycol was 1:1.75 (molar ratio), the catalyst is 2 percent (mass) of urea, and the retention time of the materials is 0.5h;
Continuously feeding the mixed liquid from the material mixing tank 1 into a first high-speed jet impact tubular reactor 2, pumping two opposite first Laval nozzles 2-2 through a first power fluid pump 2-1, simultaneously sucking nitrogen, mutually impacting two high-speed jets ejected from the first Laval nozzles 2-2 in a first high-speed jet impact cavity 2-3, then feeding the mixed liquid into the first tubular reactor 2-4 for alcoholysis reaction, and continuously feeding alcoholysis liquid discharged from the first high-speed jet impact tubular reactor 2 into a gas-liquid separation tank 3; the temperature in the first high-speed jet impact tubular reactor 2 is 141 ℃, the pressure is 0.5MPa, the length-diameter ratio of the first tubular reactor 2-4 is 1000, and 1kmol urea is absorbed into nitrogen gas 10Nm 3;
The alcoholysis liquid from the first high-speed jet stream impacting the tubular reactor 2 continuously enters a gas-liquid separation tank 3, the gas-liquid separation tank 3 separates nitrogen and ammonia generated by the reaction from the alcoholysis liquid, the separated gas enters an ammonia compressor 5-3, and the alcoholysis liquid after separating the gas continuously enters a second high-speed jet stream impacting the tubular reactor 4; the temperature in the gas-liquid separation tank 3 is 141 ℃, the pressure is normal pressure, and the retention time of the materials is 0.5h;
Continuously introducing the alcoholysis liquid after gas separation from the gas-liquid separation tank 3 into a second high-speed jet impact tubular reactor 4, pumping the alcoholysis liquid after gas separation in the gas-liquid separation tank 3 into two opposite second Laval nozzles 4-2 through a second power fluid pump 4-1, simultaneously sucking nitrogen, mutually impacting two high-speed jets ejected from the second Laval nozzles 4-2 in a second high-speed jet impact cavity 4-3, then introducing the high-speed jets into the second tubular reactor 4-4 for alcoholysis reaction, and continuously introducing the alcoholysis liquid from the second high-speed jet impact tubular reactor 4 into a curing tank 5; the second high-speed jet impact pipe reactor 4 has the temperature of 141 ℃ and the pressure of 0.5MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
The step (5) is that the alcoholysis liquid from the second high-speed jet flow impacting the tubular reactor 4 continuously enters a curing tank 5, nitrogen and ammonia generated by the reaction are separated from the alcoholysis liquid in the curing tank 5, and meanwhile, nitrogen is continuously introduced to carry out the supplementary alcoholysis reaction; the nitrogen and the ammonia separated from the gas-liquid separation tank 3 and the curing tank 5 enter an ammonia compressor 5-3 together to separate ammonia liquefaction from nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank 5-6, and the separated nitrogen gas enters a nitrogen buffer tank 5-5; the nitrogen in the nitrogen buffer tank 5-5 is continuously used for alcoholysis reaction; the alcoholysis liquid after gas separation in the curing tank 5 is continuously pumped into an ethylene glycol white steel structured packing tower 6-2 of an ethylene glycol removal tower system 6 through a crude ethylene carbonate pump 5-7; the temperature in the curing 5 tank is 145 ℃ and the pressure is normal pressure; the nitrogen pressure at the outlet of the ammonia compressor 5-3 is 0.25MPa,1kmol urea is blown into 10Nm 3 of nitrogen, and the retention time of materials is 1.5h;
Continuously pumping the alcoholysis solution obtained after gas separation in the curing tank 5 into the ethylene glycol white steel structured packing tower 6-2 through the coarse ethylene carbonate pump 5-7, removing residual ethylene glycol in the ethylene glycol white steel structured packing tower 6-2, and cooling the removed ethylene glycol through the ethylene glycol condenser 6-3 to enter the ethylene glycol receiving tank 6-4; part of ethylene glycol is taken as reflux of the ethylene glycol white steel structured packing tower 6-2 through the ethylene glycol pump 6-5, and part of ethylene glycol is extracted to the batching tank 1; the tower bottom liquid of the ethylene glycol white steel structured packing tower 6-2 enters a first reboiler 6-1 through a part of an ethylene glycol white steel structured packing tower bottom pump 6-6 to be heated and then returns to the ethylene glycol white steel structured packing tower 6-2, and part of the ethylene glycol white steel structured packing tower enters a ethylene carbonate white steel structured packing tower 7-2 of a ethylene carbonate rectifying tower system 7 continuously; the temperature of the top of the ethylene glycol white steel structured packing tower 6-2 is 150 ℃, and the pressure of the top of the tower is 0.02MPa; the bottom temperature was 178℃and the reflux ratio was 0.15 (mol);
Continuously feeding tower bottom liquid from the ethylene glycol white steel structured packing tower 6-2 into the ethylene carbonate white steel structured packing tower 7-2, rectifying ethylene carbonate in the ethylene carbonate rectifying tower, and cooling the rectified ethylene carbonate by a condenser and feeding the cooled ethylene carbonate into the ethylene carbonate receiving tank 7-4; part of ethylene carbonate is used as reflux of an ethylene carbonate white steel structured packing tower 7-2 through an ethylene carbonate pump 7-5, and part of ethylene carbonate is extracted to an ethylene carbonate storage tank 7-6; the tower bottom liquid of the ethylene carbonate white steel structured packing tower 7-2 enters a second reboiler 7-1 through a part of a pump 7-7 at the bottom of the ethylene carbonate rectifying tower to be heated, returns to the ethylene carbonate white steel structured packing tower 7-2, and enters a catalyst recovery system to recover the catalyst; the temperature of the top of the 7-2 column of the ethylene carbonate white steel structured packing column is 140 ℃, and the pressure of the top of the column is 0.002MPa; the bottom temperature was 155℃and the reflux ratio was 0.2 (mol), and 81.5kg/h of ethylene carbonate was recovered in a yield of 92.89%.
The high-speed jet impact tubular reactor of the embodiment is used for preparing the ethylene carbonate; the quality of the prepared ethylene carbonate is higher than that of HG/T5391-2018 industrial grade ethylene carbonate.
The technical scheme of the invention is explained in the technical scheme, the protection scope of the invention cannot be limited by the technical scheme, and any changes and modifications to the technical scheme according to the technical substance of the invention belong to the protection scope of the technical scheme of the invention.

Claims (8)

1. A device for preparing ethylene carbonate by high-speed jet impact pipe type reactor is characterized in that: the device comprises a batching tank (1), a first high-speed jet impact tubular reactor (2), a gas-liquid separation tank (3), a second high-speed jet impact tubular reactor (4), a curing tank system, a glycol removal tower system (6) and a ethylene carbonate rectifying tower system (7) which are sequentially communicated; the batching tank (1) is also communicated with a glycol removal tower system (6), and the curing tank system is also respectively communicated with a first high-speed jet impact tubular reactor (2), a gas-liquid separation tank (3) and a second high-speed jet impact tubular reactor (4);
The first high-speed jet impact tubular reactor (2) comprises a first Laval nozzle (2-2), a first high-speed jet impact cavity (2-3), a first tubular reactor (2-4) and a first heater (2-5); the first Laval nozzles (2-2), the first high-speed jet impact cavity (2-3) and the first tubular reactor (2-4) are arranged inside the first heater (2-5), the two first Laval nozzles (2-2) are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the first high-speed jet impact cavity (2-3) is communicated in the vertical direction of the middle part of the cavity, the first high-speed jet impact cavity (2-3) is communicated with one end of the first tubular reactor (2-4), the other end of the first tubular reactor (2-4) is connected with a top liquid inlet of the ventilation liquid separation tank (3), and air inlets are formed in the pipe orifices of the two first Laval nozzles (2-2) and are respectively communicated with the curing tank (5) and the gas-liquid separator (5-4) of the curing tank system; the first tubular reactor (2-4) is a tube with the length-diameter ratio of more than 1000, the diameter of which is phi 75mm or phi 100mm, and the tube is arranged as a reciprocating type or spring type;
The second high-speed jet impact tubular reactor (4) comprises a second Laval nozzle (4-2), a second high-speed jet impact cavity (4-3), a second tubular reactor (4-4) and a second heater (4-5); the second Laval nozzles (4-2), the second high-speed jet impact cavity (4-3) and the second tubular reactor (4-4) are arranged inside the second heater (4-5), the two second Laval nozzles (4-2) are oppositely arranged and communicated, a cavity formed by the middle communicating part is a mixing cavity, the second high-speed jet impact cavity (4-3) is communicated in the vertical direction of the middle of the cavity, the second high-speed jet impact cavity (4-3) is communicated with one end of the second tubular reactor (4-4), and the other end of the second tubular reactor (4-4) is communicated with a liquid inlet at the top of the curing tank (5); the pipe orifices of the two second Laval nozzles (4-2) are provided with steam inlets which are respectively communicated with a curing tank (5) and a gas-liquid separator (5-4) of the curing tank system; the second tubular reactor (4-4) is a tube with an aspect ratio of more than 1000, the diameter of which is phi 75mm or phi 100mm, and the tube is arranged as a reciprocating type or a spring type.
2. The apparatus for preparing ethylene carbonate by high-speed jet impact tube reactor according to claim 1, wherein: the material mixing tank (1) is a tank body structure with a material mixing tank mechanical stirrer (1-1) arranged in the interior, a heating medium is arranged on the outer periphery of the material mixing tank (1), the upper part of the material mixing tank is communicated with a powder material conveyer (1-2), and a liquid inlet at the top of the material mixing tank (1) is communicated with a glycol removal tower system (6); the liquid outlet at the bottom of the material mixing tank (1) is communicated with the inlet end of a first power fluid pump (2-1), and the outlet end of the first power fluid pump (2-1) is communicated with the liquid inlet end of a first Laval nozzle (2-2) of the first high-speed jet impact tubular reactor (2).
3. The apparatus for preparing ethylene carbonate by high-speed jet impact tube reactor according to claim 1, wherein: the gas-liquid separation tank (3) is a tank body structure with a heat medium arranged on the outer periphery, a mechanical separator (3-1) is arranged in the tank body structure, the inlet end of the upper end of the gas-liquid separation tank (3) is communicated with the outlet end of the first tubular reactor (2-4), the gas outlet end of the upper end of the gas-liquid separation tank (3) is communicated with the ammonia gas compressor (5-3) of the curing tank system through a separator condenser (3-2), and the outlet end of the bottom end of the gas-liquid separation tank (3) is communicated with two second Laval nozzles (4-2) of the second high-speed jet impact tubular reactor (4) through a second power fluid pump (4-1).
4. The apparatus for preparing ethylene carbonate by high-speed jet impact tube reactor according to claim 1, wherein: the curing tank system comprises a curing tank (5), a curing tank condenser (5-2), an ammonia compressor (5-3) and a gas-liquid separator (5-4) which are sequentially communicated, and a nitrogen buffer tank (5-5) and a liquid ammonia storage tank (5-6) which are both communicated with the gas-liquid separator (5-4), wherein the curing tank (5) is a tank body structure of which the periphery is provided with a heating medium and the inside is provided with a curing tank mechanical stirrer (5-1); the top liquid inlet of the curing tank (5) is communicated with the outlet end of a second tubular reactor (4-4) of the second high-speed jet impact tubular reactor (4), the top air inlet of the curing tank (5) is communicated with a nitrogen buffer tank (5-5), and the curing tank (5) is communicated with an ethylene glycol white steel structured packing tower (6-2) of the ethylene glycol removal tower system (6) through a coarse ethylene carbonate pump (5-7).
5. The apparatus for preparing ethylene carbonate by high-speed jet impact tube reactor according to claim 1, wherein: the system for removing the ethylene glycol comprises a first reboiler (6-1), an ethylene glycol white steel structured packing tower (6-2), an ethylene glycol condenser (6-3), an ethylene glycol receiving tank (6-4), an ethylene glycol pump (6-5) and an ethylene glycol white steel structured packing tower bottom pump (6-6), a steam outlet of the ethylene glycol white steel structured packing tower (6-2) is communicated with the ethylene glycol condenser (6-3), the ethylene glycol condenser (6-3) is communicated with the ethylene glycol receiving tank (6-4), the ethylene glycol receiving tank (6-4) is respectively communicated with the ethylene glycol white steel structured packing tower (6-2) and the batching tank (1) through the ethylene glycol pump (6-5), the bottoms of the ethylene glycol white steel structured packing tower (6-2) are respectively communicated with the bottoms of the first reboiler (6-1) and the ethylene carbonate white steel structured packing tower (7-2) of the ethylene carbonate structured packing tower system (7), and the bottoms of the first reboiler (6-1) and the ethylene glycol white steel structured packing tower (6-2) are respectively communicated with each other.
6. The apparatus for preparing ethylene carbonate by high-speed jet impact tube reactor according to claim 1, wherein: the ethylene carbonate rectifying tower system (7) comprises a second reboiler (7-1), an ethylene carbonate white steel structured packing tower (7-2), an ethylene carbonate condenser (7-3), an ethylene carbonate receiving tank (7-4), an ethylene carbonate pump (7-5), an ethylene carbonate storage tank (7-6) and an ethylene carbonate rectifying tower bottom pump (7-7), a steam outlet of the ethylene carbonate white steel structured packing tower (7-2) is communicated with one end of the ethylene carbonate condenser (7-3), the other end of the ethylene carbonate condenser (7-3) is communicated with one end of the ethylene carbonate receiving tank (7-4), and the other end of the ethylene carbonate receiving tank (7-4) is respectively communicated with the ethylene carbonate white steel structured packing tower (7-2) and the ethylene carbonate storage tank (7-6) through the ethylene carbonate pump (7-5); the bottom end of the ethylene carbonate white steel structured packing tower (7-2) is respectively communicated with one end of a second reboiler (7-1) and a catalyst recovery system through an ethylene carbonate rectifying tower bottom pump (7-7), the other end of the second reboiler (7-1) is communicated with the bottom of the ethylene carbonate white steel structured packing tower (7-2), and the second reboiler (7-1) is of a structure provided with heating media.
7. A method of preparing ethylene carbonate in a high velocity jet impingement tubular reactor apparatus as defined in claim 1, wherein: the method specifically comprises the following steps:
Step 1, raw materials of urea particles, glycol and a catalyst are fed into a batching tank (1), the urea particles are dissolved under the stirring of a mechanical stirrer (1-1) of the batching tank, and the dissolved urea, glycol and the catalyst are uniformly mixed to obtain a mixed solution, and are heated to a reaction temperature through a heating medium; continuously feeding the mixed liquid into a first high-speed jet flow impact tubular reactor (2) through a first power fluid pump (2-1);
Step 2, pumping the mixed liquid from the material mixing tank (1) into two opposite first Laval nozzles (2-2), sucking nitrogen separated by the curing tank system, mutually impacting two high-speed jet flows sprayed out of the first Laval nozzles (2-2) in a first high-speed jet flow impacting cavity (2-3), then entering a first tubular reactor (2-4) for alcoholysis reaction, and continuously entering a gas-liquid separation tank (3) from nitrogen discharged from the first high-speed jet flow impacting the tubular reactor (2), ammonia generated by reaction and alcoholysis liquid;
Step 3, separating the ammonia generated by the nitrogen and the reaction from the alcoholysis liquid by a gas-liquid separation tank (3), enabling the separated gas to enter an ammonia compressor (5-3) of a curing tank system, and enabling the alcoholysis liquid after gas separation to continuously enter a second high-speed jet flow impact tubular reactor (4);
Step 4, pumping the alcoholysis liquid in the step 3 into two opposite second Laval nozzles (4-2) through a second power fluid pump (4-1), sucking nitrogen separated by a curing tank system, mutually impacting two high-speed jet streams ejected from the second Laval nozzles (4-2) in a second high-speed jet stream impacting cavity (4-3), then entering a second tubular reactor (4-4) for alcoholysis reaction, and continuously entering a curing tank (5) from nitrogen ejected from the second high-speed jet stream impacting the tubular reactor (4) and ammonia alcoholysis liquid generated by reaction;
step 5, separating nitrogen and ammonia generated by the reaction from alcoholysis liquid in a curing tank (5), and simultaneously continuously introducing the separated nitrogen to carry out supplementary alcoholysis reaction; the nitrogen and the ammonia separated from the gas-liquid separation tank (3) and the curing tank (5) enter an ammonia compressor (5-3) together to liquefy the ammonia and separate the nitrogen; the separated liquefied ammonia gas enters a liquid ammonia storage tank (5-6), and the separated nitrogen gas enters a nitrogen buffer tank (5-5); the nitrogen in the nitrogen buffer tank (5-5) is continuously used for alcoholysis reaction; the alcoholysis liquid after gas separation in the curing tank (5) is continuously pumped into a glycol removal tower system (6) through a crude ethylene carbonate pump;
Step 6, removing residual glycol from the alcoholysis reaction in a glycol white steel structured packing tower (6-2) of a glycol removal tower system (6), and cooling the removed glycol by a glycol condenser (6-3) to enter a glycol receiving tank (6-4); part of ethylene glycol is taken as reflux of an ethylene glycol white steel structured packing tower (6-2) through an ethylene glycol pump (6-5), and part of ethylene glycol is extracted to a batching tank (1); the tower bottom liquid of the ethylene glycol white steel structured packing tower (6-2) enters a first reboiler (6-1) through a part of an ethylene glycol white steel structured packing tower bottom pump (6-6) and returns to the ethylene glycol white steel structured packing tower (6-2) after being heated, and part of the tower bottom liquid continuously enters a ethylene carbonate rectifying tower system (7);
Step 7, rectifying the ethylene carbonate in the ethylene carbonate rectifying tower system (7), and cooling the rectified ethylene carbonate by the ethylene carbonate condenser (7-3) and then feeding the cooled ethylene carbonate into the ethylene carbonate receiving tank (7-4); part of ethylene carbonate is taken as reflux of an ethylene carbonate white steel structured packing tower (7-2) through an ethylene carbonate pump (7-5), and part of ethylene carbonate is extracted to an ethylene carbonate storage tank (7-6); and (3) partially feeding the tower bottom liquid of the ethylene carbonate rectifying tower into a second reboiler (7-1) through a pump (7-7) at the bottom of the ethylene carbonate rectifying tower, heating, returning to the ethylene carbonate white steel structured packing tower (7-2), and partially feeding into a catalyst recovery system to recover the catalyst.
8. A method of preparing ethylene carbonate in a high velocity jet impingement tubular reactor apparatus as defined in claim 7, wherein:
The reaction temperature in the batching tank (1) is 137-141 ℃, the pressure is normal pressure, and the urea is prepared by the following steps: the molar ratio of the ethylene glycol is 1: (1.5-1.75), the mass of the catalyst is 2-3% of that of urea, and the retention time of the materials is 0.5-0.75 h;
the reaction temperature in the first high-speed jet impact tubular reactor (2) is 137-141 ℃, the pressure is 0.4-0.5 MPa, the length-diameter ratio of the tubular reactor is 1000, and 1kmol urea is absorbed into nitrogen gas 10Nm 3;
the reaction temperature in the gas-liquid separation tank (3) is 137-141 ℃, the pressure is normal pressure, and the retention time of the materials is 0.5-0.75 h;
the second high-speed jet impact pipe reactor (4) has the internal temperature of 137-141 ℃ and the pressure of 0.4-0.5 MPa, the length-diameter ratio of the pipe reactor is 1000, and 1kmol urea is absorbed into nitrogen gas of 10Nm 3;
The reaction temperature in the curing tank (5) is 141-145 ℃ and the pressure is normal pressure; the nitrogen pressure at the outlet of the ammonia compressor (5-3) is 0.25MPa,1kmol urea is blown into 10Nm 3 of nitrogen, and the retention time of materials is 1.5-2 h;
The temperature of the top of the ethylene glycol white steel structured packing tower (6-2) is 150 ℃, and the pressure of the top of the tower is 0.02MPa; the bottom temperature is 178 ℃, and the molar reflux ratio is 0.15;
the temperature of the top of the ethylene carbonate white steel structured packing tower (7-2) is 140 ℃, and the pressure of the top of the tower is 0.002MPa; the bottom temperature was 155℃and the molar reflux ratio was 0.2.
CN202210985499.0A 2022-08-17 2022-08-17 Device and method for preparing ethylene carbonate by high-speed jet impact on tubular reactor Active CN115337893B (en)

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