CN217164324U - Reaction system for synthesizing carbonic ester by heterogeneous method - Google Patents
Reaction system for synthesizing carbonic ester by heterogeneous method Download PDFInfo
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- CN217164324U CN217164324U CN202122586787.2U CN202122586787U CN217164324U CN 217164324 U CN217164324 U CN 217164324U CN 202122586787 U CN202122586787 U CN 202122586787U CN 217164324 U CN217164324 U CN 217164324U
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Abstract
The utility model provides a reaction system of heterogeneous method synthetic carbonic ester, this reaction system includes: a gas-liquid bubbling bed reactor I and a buffer tank which are communicated in series along the material flow direction; and a full liquid phase fixed bed reactor; and a circulation cooler and a circulation pump; the liquid phase outlet of the gas-liquid bubbling bed reactor is communicated with the inlet of a buffer tank, the outlet of the buffer tank is communicated with the inlet of a circulating cooler, and the outlet of the circulating cooler is communicated with the inlet of a circulating pump; the outlet of the circulating pump is communicated with the liquid phase inlets of the gas-liquid bubbling bed reactor and the full liquid phase fixed bed reactor; the bottoms of the gas-liquid bubbling bed reactor and/or the whole-liquid phase fixed bed reactor are set to inclined planes, and the inclination angles with respect to the horizontal plane are preferably 5 to 30 degrees respectively. The utility model discloses can solve among the current carbonic ester apparatus for producing temperature control insensitive, easy temperature runaway, the liquid circulation volume is big, the reaction is removed the problem that the heat is lagged, can be applied to in the carbonic ester industrial production, have very high industrial application and worth.
Description
Technical Field
The utility model relates to a reaction system for synthesizing carbonic ester by a heterogeneous method.
Background
The carbonate is a very important organic compound in industry and has wide market prospect. Commercially important carbonates are dimethyl carbonate, diphenyl carbonate, ethylene carbonate and propylene carbonate. These carbonates are widely used in engineering plastics, i.e., pigments for polycarbonates and polyurethanes, electrolyte solvents for lithium ion batteries, organic solvents, fuel additives, and alkylating and acylating agents, etc.
Currently, the current practice is. The industrial synthesis of carbonate at home and abroad mainly comprises phosgene method, ester exchange, halogenated alcohol method, ethylene and carbon dioxide synthesis method and ethylene oxide and carbon dioxide synthesis method. The phosgene method is the earliest method for preparing carbonate, and the process has long flow, low yield and serious pollution and elimination of trace organic chloride; the halohydrin process requires a high temperature at which the carbonate decomposes, thus resulting in high raw material consumption, high by-products and no industrialization; the synthesis of ethylene and carbon dioxide requires high pressure and is not easily industrialized due to the danger of explosion.
CN109647134A discloses a multi-stage serial bubbling bed-transport bed stacked CO 2 An adsorption reactor and method. The reactor comprises an air chamber, a central air pipe, a lifting pipe and a bubbling bed. The bubbling bed includes a grid plate on which CO is prevented 2 The adsorbent, the central air pipe is arranged in the middle of the air distribution plate at the bottommost layer, the lifting pipes are arranged in the rest air distribution plates in a penetrating way, and the lifting pipes are positioned in each bubbling bedThe dense phase zone of the water cooling coil is provided with a water cooling coil. According to the claims, containing CO 2 The flue gas enters from the side of the air chamber, passes through the first stage air distribution plate at the lowest part, enters the first stage bubbling bed, and fluidizes CO in the first stage bubbling bed 2 Simultaneously carrying out decarburization reaction on the adsorbent; meanwhile, the first-stage water-cooling disc operates to absorb the reaction heat in the first-stage bubbling bed and stabilize the carbonation reaction temperature in the first-stage bubbling bed. Because the process is a gas-solid phase reaction, the water-cooling coil pipe is adopted to remove the heat in the gas-phase substances, the efficiency is low, and the process is not suitable for removing a system with strong heat release and is not beneficial to the wide application of the process.
CN1371900A discloses a method and a reactor for preparing propylene carbonate or ethylene carbonate. According to the method, the catalyst is loaded into the reactor which is provided with the heat transfer device and is separated from the product area, and in the reactor, heat can be transferred out while the reaction is carried out, so that the high-temperature inactivation of the catalyst is avoided, and the service life of the catalyst is prolonged. However, in the method, the materials are easily unevenly distributed, the reaction is severe near the catalyst filling equipment, the catalyst filling equipment is slow in reaction or does not react in principle, and when heat is not transferred in time, local temperature rise is easily too high, so that the catalyst is inactivated, and the reaction is influenced.
CN106478583B discloses a method for synthesizing ethylene carbonate. The process mainly comprises a first-stage synthesis reactor, a second-stage synthesis reactor and the like, wherein in the synthesis method, in the first-stage synthesis reactor, ethylene oxide and carbon dioxide which is not completely reacted in the second-stage reactor are in countercurrent contact reaction; in the two-stage synthesis reactor, a reaction product and fresh carbon dioxide are subjected to countercurrent contact reaction, heat is removed mainly in an external circulation mode in the synthesis process, a large amount of liquid is required to circulate, and the control of temperature rise in the reactor is lagged, so that the reaction is not facilitated.
SUMMERY OF THE UTILITY MODEL
The heterogeneous synthesis method can reduce the subsequent separation process of the product and the catalyst, effectively reduce energy consumption and investment, and obtain the carbonate with higher purity and better industrial applicability. However, in the production process, a large amount of heat is released in the process of generating carbonic ester from ethylene oxide and carbon dioxide, if the heat cannot be removed in time to cause temperature rise, the carbonic ester can be decomposed, and the catalyst is volatile to cause the yield of the product to be reduced, so that the strict and timely control of the temperature rise in the reaction process plays a crucial role in the reaction.
The utility model discloses a main objective is in order to solve the insensitive, the easy temperature runaway of temperature control, the liquid circulation volume is big, the reaction is removed the thermal lag's problem in the carbonic ester apparatus for producing, provides a heterogeneous method synthetic carbonic ester's reaction system and the heterogeneous method synthetic carbonic ester's of method.
According to the first aspect of the utility model, the utility model provides a reaction system of heterogeneous method synthetic carbonic ester, this reaction system includes: a gas-liquid bubbling bed reactor and a buffer tank which are communicated in series along the material flow direction; and a full liquid phase fixed bed reactor; and a circulation cooler and a circulation pump;
the liquid phase outlet of the gas-liquid bubbling bed reactor is communicated with the inlet of a buffer tank, the outlet of the buffer tank is communicated with the inlet of a circulating cooler, and the outlet of the circulating cooler is communicated with the inlet of a circulating pump; the outlet of the circulating pump is communicated with the liquid phase inlets of the gas-liquid bubbling bed reactor and the full liquid phase fixed bed reactor;
the bottoms of the gas-liquid bubbling bed reactor and/or the all-liquid fixed-phase bed reactor are arranged as inclined planes, and the inclination angles relative to the horizontal plane are preferably 5-30 degrees respectively, and are preferably 10-20 degrees respectively.
The utility model discloses can solve among the current carbonic ester apparatus for producing temperature control insensitive, easy temperature runaway, the liquid circulation volume is big, the reaction is removed the problem that the heat is lagged, can be applied to in the carbonic ester industrial production, there is fine practicality, has very high industrial application and worth.
The utility model discloses contrast other gas-liquid tympanic bulla bed technology, gas gets into from the reactor bottom, and the top is extracted, and liquid gets into from the top, and the bottom is extracted. The utility model discloses bed temperature is more even, and the reactor presss from both sides the cover and removes the heat effect more obvious, therefore the circulation volume reduces 5% -15%.
The utility model discloses contrast other reactor internals, the bottom sets up horizontally silk screen and grid, and the catalyst loads on silk screen and grid. The utility model discloses simple structure unloads the catalyst more convenient, and remaining catalyst reduces greatly in the reactor.
Drawings
Fig. 1 is a system diagram for synthesizing carbonate according to a preferred embodiment of the present invention.
Description of the reference numerals
I is a gas-liquid bubbling bed reactor, II is a buffer tank,
III is a circulating cooler, IV is a circulating pump;
v, a full liquid phase fixed bed reactor;
1 is carbon dioxide, 2 is ethylene oxide, 3 is a circulating liquid, 4 is a liquid reaction product, 5 is buffer tank liquid discharge, 7 is liquid fixed bed reactor feed, and 8 is liquid fixed bed reactor discharge;
11 is a first intercepting silk screen, 12 is a first distributor, and 13 is a discharge opening;
FC is a flow controller, PC is a pressure controller, and LC is a liquid level controller.
Detailed Description
The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.
As shown in fig. 1, the present invention provides a reaction system for synthesizing carbonate by a heterogeneous method, comprising: a gas-liquid bubbling bed reactor I and a buffer tank II which are communicated in series along the material flow direction; and a full liquid phase fixed bed reactor V; and a recirculation cooler III and a recirculation pump IV;
the liquid phase outlet of the gas-liquid bubbling bed reactor I is communicated with the inlet of a buffer tank II, the outlet of the buffer tank is communicated with the inlet of a circulating cooler III, and the outlet of the circulating cooler III is communicated with the inlet of a circulating pump IV; an outlet of the circulating pump IV is communicated with liquid phase inlets of the gas-liquid bubbling bed reactor and the full liquid phase fixed bed reactor;
the bottoms of the gas-liquid bubbling bed reactor and/or the all-liquid fixed-phase bed reactor are arranged as inclined planes, and the inclination angles relative to the horizontal plane are preferably 5-30 degrees respectively, and are preferably 10-20 degrees respectively.
The utility model discloses a set up aforementioned reaction system carbon dioxide and ethylene oxide and circulating liquid and get into the reactor from up mixing back down, can make carbon dioxide dissolve earlier in circulating liquid, increase reaction efficiency, can utilize gas and liquid to go upward again and make the catalyst bed present loose state, the misce bene has reinforceed the mass transfer and has conducted heat, makes bed temperature more even, and reaction system's control is more stable. The bottom is provided with an inclination angle, which is beneficial to the unloading of heterogeneous catalysts.
According to a preferred embodiment of the present invention, the discharge openings of the gas-liquid bubbling bed reactor and/or the full liquid-phase fixed bed reactor are each level with the bottom of the reactor, and the diameter of each discharge opening is preferably 50-2000mm, preferably 1000-1500 mm. Through adopting the setting, the utility model has the advantages of simple operation and convenient agent unloading.
As shown in fig. 1, according to the utility model discloses a preferred embodiment, gas-liquid bubbling bed reactor I sets up the overflow mouth, and gas-liquid bubbling bed reactor I's overflow mouth and buffer tank II entry intercommunication, full liquid phase fixed bed reactor V sets up the exit control valve, the buffer tank sets up liquid level controller, and the liquid level controller of buffer tank links to each other with full liquid phase fixed bed reactor's exit control valve, uses through the two cooperation, realizes the automatic buffer tank that flows in of overflow mouth.
As shown in fig. 1, according to a preferred embodiment of the system of the present invention, the gas-liquid bubbling bed reactor comprises a bubbling bed reactor housing, a first distributor 12 and a first solid intercepting screen 11 which are arranged inside the bubbling bed reactor housing, and an agent loading port, a discharge port 13, an overflow port and a gas outlet which are arranged on the bubbling bed reactor housing, wherein the overflow port is used as a liquid phase outlet of the gas-liquid bubbling bed reactor; the first distributor is positioned at the bottom of the gas-liquid bubbling bed reactor and used for distributing gas and liquid mixed materials; the first solid intercepting wire mesh is positioned at the middle upper part of the gas-liquid bubbling bed reactor and used for intercepting solids; the agent loading port is positioned on the side surface of the bubbling bed reactor and below the first solid interception wire mesh; the discharge opening is positioned on the side surface of the bubbling bed reactor and at the bottom of the side surface of the reactor; the overflow port is positioned at the upper part of the bubbling bed reactor and above the first solid intercepting screen; a gas outlet: located at the top of the bubbling bed reactor. Through adopting the aforesaid setting, the utility model discloses it is few to have the catalyst loss, controls simple advantage.
According to a preferred embodiment of the system of the present invention, wherein the full liquid phase fixed bed reactor comprises a fixed bed reactor housing, and a second distributor, a second solid intercepting screen, an agent loading port, a discharge port, and a material outlet, which are disposed inside the fixed bed reactor housing; the second distributor is positioned at the bottom of the fixed bed reactor and used for distributing liquid; the second solid interception silk screen is positioned at the middle upper part of the fixed bed reactor and is used for intercepting the solid catalyst; the agent loading port is positioned on the side surface of the fixed bed reactor and below the second solid interception wire mesh; the discharge opening is positioned at the bottom of the side surface of the fixed bed reactor; an outlet at the top of the fixed bed reactor; and the outlet control valve is arranged on the pipeline of the outlet. Through adopting the aforesaid setting, the utility model has the advantages of easy operation, catalyst unload the agent convenient.
According to a preferred embodiment of the present invention, the buffer tank is provided with a liquid level controller; the liquid level controller of the optimized buffer tank is connected with the outlet control valve of the full liquid phase fixed bed reactor, and the overflow port automatically flows into the buffer tank through the matching use of the liquid level controller and the outlet control valve.
According to a preferred embodiment of the present invention, the distance from the first distributor to the bottom of the bubbling bed reactor is 100-500mm, preferably 200-400 mm; through adopting the aforesaid setting, the utility model discloses catalyst utilization rate height advantage has.
According to a preferred embodiment of the present invention, the distance from the second distributor to the bottom of the fixed bed reactor is 100-; through adopting the aforesaid setting, the utility model discloses catalyst utilization rate height advantage has.
According to a preferred embodiment of the present invention, the first distributor and the second distributor are each a tubular distributor, preferably with holes opened up and down, with a diameter of phi 5-10; through adopting the aforesaid setting, the utility model discloses have the even advantage of gas distribution.
According to a preferred embodiment of the present invention, the first distributor and the second distributor are each wrapped with a 40-60 mesh screen. Through adopting the aforesaid setting, the utility model discloses have and prevent to cause the jam in heterogeneous catalyst gets into the distributor, and gaseous redistribution, mix more even advantage.
According to a preferred embodiment of the present invention, the first and/or second solid intercepting screens are preferably each in the shape of an arc, arch or cone. Through adopting the aforesaid setting, the utility model discloses it is big to have silk screen flux, and the reactor resistance reduces the advantage.
According to a preferred embodiment of the present invention, the ratio of the area of the first solid intercepting screen to the sectional area of the bubbling bed reactor is 1.5 to 5; through adopting the aforesaid setting, the utility model discloses it is big to have silk screen flux, and the reactor resistance reduces the advantage.
According to a preferred embodiment of the present invention, the ratio of the area of the second solid intercepting screen to the sectional area of the fixed-bed reactor is 1.5 to 5. Through adopting the aforesaid setting, the utility model discloses it is big to have silk screen flux, and the reactor resistance reduces the advantage.
According to a preferred embodiment of the present invention, the gas-liquid bubbling bed reactor I and/or the full liquid phase fixed bed reactor V are/is configured to be heat-removed by means of jacket/coil, and the heat-removing medium is preferably saturated water at 100-.
According to a preferred embodiment of the present invention, the cooling medium of the circulation cooler III is selected from one of saturated water, hot water and cooling water.
The utility model discloses in, each structure in each unit and the unit can install flow control valve as required, parts such as temperature measurement, pressure measurement, if the utility model discloses the flow control valve on the different pipelines that figure 1 is shown, FC is flow controller, control circulation volume, and PC is pressure controller, controls reaction system's pressure, and LC is liquid level controller, controls the liquid level of buffer tank.
Specifically, as shown in fig. 1, a pressure controller PC is provided at the top of the gas-liquid bubbling bed reactor I for controlling the pressure of the reaction system.
And a liquid level controller LC is communicated with the side wall of the buffer tank and used for controlling the liquid level of the buffer tank.
Control valves are arranged on outlet pipelines at the tops of the gas-liquid bubbling bed reactor I and the full liquid-phase fixed bed reactor V, and the stable control of the temperature, the pressure and the liquid level of a reaction system can be realized by combining the LC of the side wall of the buffer tank with the control valves.
All other structures can be provided with various auxiliary accessories according to the needs, which is resin for the technical personnel in the field, and the utility model is not described in detail here.
As shown in FIG. 1, the method for synthesizing carbonic ester by heterogeneous phase method is carried out in the reaction system of the utility model, wherein, the gas carbon dioxide 1, the liquid ethylene oxide 2 and the circulating liquid 3 from the circulating pump IV are mixed and then enter the gas-liquid bubbling bed reactor I from a liquid phase inlet through a first distributor, the catalyst is intercepted by a first solid intercepting wire mesh after the reaction, the gas-liquid separation is carried out on the reaction product at the top of the gas-liquid bubbling bed reactor I, the liquid reaction product 4 enters a buffer tank II through an overflow port, then the liquid discharged from the buffer tank 5 enters a circulating cooler III for cooling and heat removal, then a part of the liquid is circulated back to the gas-liquid bubbling bed reactor I through a circulating pump IV, the other part of the liquid fixed bed reactor is fed with a material 7 which enters a full liquid phase fixed bed reactor V through a second distributor, the extraction of the whole reaction system is controlled by the liquid level of the buffer tank, and the liquid fixed bed reactor discharge 8 is extracted from the top of the full liquid phase fixed bed reactor V.
In the present invention, the operating conditions of the various units can be adjusted as required, the following examples set forth preferred embodiments, but are not intended to limit the scope of the invention accordingly.
According to a preferred embodiment of the present invention, the operating conditions of the gas-liquid bubbling bed reactor I include: the temperature is 80-150 ℃, and the pressure is 2-5 MPa.
According to a preferred embodiment of the present invention, the operating conditions of buffer tank II include: the temperature is 80-150 ℃.
According to a preferred embodiment of the present invention, the operating conditions of the circulation cooler III include: the temperature is 60-100 ℃.
According to a preferred embodiment of the present invention, the operating conditions of the circulation pump IV include: the temperature is 60-100 ℃, and the pressure is increased by 0.2-0.5 MPa.
According to a preferred embodiment of the present invention, the operating conditions of the full liquid phase fixed bed reactor V include: 100-150 ℃.
According to a preferred embodiment of the invention, the ratio of the amounts of gaseous carbon dioxide and liquid ethylene oxide is between 1.02 and 1.3.
According to a preferred embodiment of the present invention, the catalyst is one or more of an ionic liquid immobilized catalyst, a resin, and an alkaline earth metal solid catalyst.
According to the utility model discloses a preferred embodiment, the method of through the production of buffer tank liquid level control whole reaction system includes: and the liquid level controller of the buffer tank is connected with an outlet control valve of the full liquid phase fixed bed reactor, and when the liquid level of the buffer tank is high, the large control valve is opened, otherwise, the small control valve is closed.
The utility model discloses in, full liquid phase fixed bed reactor does not supply CO alone 2 And in the case of liquid-phase full-tank operation, the extraction amount is controlled by the liquid level of the buffer tank.
The utility model discloses in, the measure of gaseous carbon dioxide accessible increase dissolution time and dispersion microbubble strengthens the solubility of carbon dioxide in reaction material.
The utility model discloses in, CO among this reaction system 2 One strand or a plurality of strands of the mixture enter the middle lower part of the gas-liquid bubbling bed reactor and are uniformly distributed by the gas distributor after entering the reactor.
The following examples were conducted in accordance with the scheme shown in FIG. 1 to synthesize carbonates, in which,
the gas-liquid bubbling bed reactor comprises a bubbling bed reactor shell, a first distributor, a first solid intercepting screen, an agent loading port, a discharging port, an overflow port and a gas outlet, wherein the first distributor and the first solid intercepting screen are arranged in the bubbling bed reactor shell;
the full liquid phase fixed bed reactor comprises a fixed bed reactor shell, and a second distributor, a second solid interception silk screen, an agent loading port, a discharging port, an outlet and an outlet control valve which are arranged in the fixed bed reactor shell, wherein the buffer tank is provided with a liquid level controller, the liquid level controller of the buffer tank is connected with the outlet control valve of the full liquid phase fixed bed reactor, and an overflow port automatically flows into the buffer tank through the matching use of the liquid level controller and the outlet control valve;
the bottoms of the gas-liquid bubbling bed reactor and the full liquid-phase fixed bed reactor are both arranged to be inclined planes, the inclination angles are respectively 15 degrees and 20 degrees,
the diameters of the discharge openings of the gas-liquid bubbling bed reactor and the full liquid-phase fixed bed reactor are respectively 1500mm and 1000 mm;
the distance between the first distributor and the bottom of the bubbling bed reactor is 300 mm;
the distance between the second distributor and the bottom of the fixed bed reactor is 200 mm;
the first distributor and the second distributor are both tubular distributors, holes are formed in the upper part and the lower part, the aperture phi is 8, and the first distributor and the second distributor are wrapped by 50-mesh silk screens;
the ratio of the area of the first solid interception wire mesh to the sectional area of the bubbling bed reactor is 3;
the ratio of the area of the second solid intercepting screen to the cross-sectional area of the fixed bed reactor was 1.5.
Example 1
Gaseous carbon dioxide 1, liquid ethylene oxide 2 and circulating liquid 3 from a circulating pump IV are mixed and then enter a gas-liquid bubbling bed reactor I from a liquid phase inlet through a first distributor, a catalyst is intercepted by a first solid intercepting wire mesh after reaction, gas-liquid separation is carried out on reaction products at the top of the gas-liquid bubbling bed reactor I, liquid reaction products 4 enter a buffer tank II through an overflow port, then a buffer tank liquid discharge 5 enters a circulating cooler III for cooling and heat removal, then a part of the liquid discharge is circulated back to the gas-liquid bubbling bed reactor I through the circulating pump IV, the other part of liquid fixed bed reactor feed 7 enters a full liquid fixed bed reactor V through a second distributor, the extraction of the whole reaction system is controlled through the liquid level of the buffer tank, and the liquid fixed bed reactor discharge 8 is extracted from the top of the full liquid fixed bed reactor V. The method for controlling the extraction of the whole reaction system through the liquid level of the buffer tank comprises the following steps: the liquid level signal of the buffer tank is connected with the control valve at the outlet of the full liquid phase fixed bed reactor, when the liquid level of the buffer tank is high, the control valve is opened, otherwise, the control valve is closed.
In the catalyst unloading process, no catalyst residue exists in the reactor.
The gas-liquid bubbling bed reactor and the full-liquid-phase fixed bed reactor are arranged to adopt a jacket mode to remove heat, and a heat removal medium is saturated water at the temperature of 110 ℃;
the cooling medium of the circulating cooler is selected from saturated water at 32 ℃.
The operating conditions of the gas-liquid bubbling bed reactor include: the temperature is 100 ℃, and the pressure is 3.5 MPa;
the operating conditions of the buffer tank include: the temperature is 100 ℃;
the operating conditions of the recycle cooler include: the temperature of the cooled material is 85 ℃;
the operating conditions of the circulation pump include: the temperature is 85 ℃;
the operating conditions of the full liquid phase fixed bed reactor include: the temperature is 100-;
the dosage ratio of the gas carbon dioxide and the liquid ethylene oxide is 1.2;
the catalyst is resin catalyst, and the dosage of the catalyst is 8 tons.
Example 2
The same as in example 1, except that the bottoms of the gas-liquid bubbling bed reactor and the all-liquid phase fixed bed reactor were each set to an inclined plane at an inclination angle of 3 °. At least 5% of the catalyst remained in the reactor during the catalyst unloading process relative to example 1.
Example 3
The same as in example 1, except that the first distributor is at a distance of 1000mm from the bottom of the reactor, the ethylene oxide conversion is reduced by at least 1%.
The preferred embodiments of the present invention have been described in detail above, but the present invention is not limited thereto. In the technical idea scope of the present invention, it can be right to the technical solution of the present invention perform multiple simple modifications, including each technical feature combined in any other suitable manner, these simple modifications and combinations should be regarded as the disclosed content of the present invention, and all belong to the protection scope of the present invention.
Claims (10)
1. A reaction system for synthesizing a carbonate by a heterogeneous process, the reaction system comprising: a gas-liquid bubbling bed reactor (I) and a buffer tank (II) which are communicated in series along the material flow direction; and a full liquid phase fixed bed reactor (V); and a circulation cooler (III) and a circulation pump (IV);
wherein, the liquid phase outlet of the gas-liquid bubbling bed reactor (I) is communicated with the inlet of the buffer tank (II), the outlet of the buffer tank is communicated with the inlet of the circulating cooler (III), and the outlet of the circulating cooler (III) is communicated with the inlet of the circulating pump (IV); an outlet of the circulating pump (IV) is communicated with liquid phase inlets of the gas-liquid bubbling bed reactor and the full liquid phase fixed bed reactor;
the bottom of the gas-liquid bubbling bed reactor and/or the full liquid-phase fixed bed reactor is set to be an inclined plane.
2. The reaction system according to claim 1, wherein the inclined planes of the gas-liquid bubbling bed reactor and/or the all-liquid-phase fixed bed reactor each have an inclination angle of 5 ° to 30 ° with respect to a horizontal plane.
3. The reaction system according to claim 2, wherein the inclined planes of the gas-liquid bubbling bed reactor and/or the all-liquid-phase fixed bed reactor are each inclined at an angle of 10 ° to 20 ° with respect to a horizontal plane.
4. The reaction system of any one of claims 1 to 3, wherein the gas-liquid bubbling bed reactor (I) is provided with an overflow port, the overflow port of the gas-liquid bubbling bed reactor (I) is communicated with the inlet of the buffer tank (II), the full liquid phase fixed bed reactor (V) is provided with an outlet control valve, the buffer tank is provided with a liquid level controller, the liquid level controller of the buffer tank is connected with the outlet control valve of the full liquid phase fixed bed reactor, and the overflow port can automatically flow into the buffer tank by matching the overflow port with the buffer tank.
5. The reaction system according to any one of claims 1 to 3,
the discharge openings of the gas-liquid bubbling bed reactor and/or the full-liquid phase fixed bed reactor are respectively level with the bottom of the reactor, and the diameter of each discharge opening is 50-2000 mm.
6. The reaction system according to claim 5,
the diameters of the discharge openings of the gas-liquid bubbling bed reactor and/or the full liquid-phase fixed bed reactor are 1000-1500 mm.
7. The reaction system according to any one of claims 1 to 3,
the device comprises a gas-liquid bubbling bed reactor, a gas-liquid bubbling bed reactor and a gas-liquid bubbling bed reactor, wherein the gas-liquid bubbling bed reactor comprises a bubbling bed reactor shell, a first distributor, a first solid intercepting wire net, an agent loading port, a discharging port, an overflow port and a gas outlet, wherein the first distributor and the first solid intercepting wire net are arranged in the bubbling bed reactor shell;
the first distributor is positioned at the bottom of the gas-liquid bubbling bed reactor and used for distributing gas and liquid mixed materials;
the first solid intercepting wire mesh is positioned at the middle upper part of the gas-liquid bubbling bed reactor and used for intercepting solids;
the agent loading port is positioned on the side surface of the bubbling bed reactor and below the first solid interception wire mesh;
the discharge opening is positioned on the side surface of the bubbling bed reactor and at the bottom of the side surface of the reactor;
the overflow port is positioned at the upper part of the bubbling bed reactor and above the first solid intercepting screen;
a gas outlet positioned at the top of the bubbling bed reactor;
and/or
The full liquid phase fixed bed reactor comprises a fixed bed reactor shell, and a second distributor, a second solid interception silk screen, an agent loading port, a discharging port and a material outlet which are arranged in the fixed bed reactor shell;
the second distributor is positioned at the bottom of the fixed bed reactor and used for distributing liquid;
the second solid interception silk screen is positioned at the middle upper part of the fixed bed reactor and is used for intercepting the solid catalyst;
the agent loading port is positioned on the side surface of the fixed bed reactor and below the second solid interception wire mesh;
the discharge opening is positioned at the bottom of the side surface of the fixed bed reactor;
an outlet at the top of the fixed bed reactor;
an outlet control valve disposed on a line of the outlet; and/or
The buffer tank is provided with a liquid level controller;
the liquid level controller of the buffer tank is connected with the outlet control valve of the full liquid phase fixed bed reactor, and the overflow port automatically flows into the buffer tank through the matching use of the liquid level controller and the outlet control valve.
8. The reaction system according to claim 7,
the distance between the first distributor and the bottom of the bubbling bed reactor is 100-500 mm; and/or
The distance between the second distributor and the bottom of the fixed bed reactor is 100-500 mm; and/or
The first distributor and the second distributor respectively adopt tubular distributors, the upper part and the lower part of each distributor are provided with holes, and the aperture phi is 5-10; and/or
The first distributor and the second distributor are respectively wrapped by 40-60 meshes of silk screen.
9. The reaction system according to claim 7,
the first solid intercepting screen and/or the second solid intercepting screen are/is arc-shaped, arched or conical; and/or
The ratio of the area of the first solid interception wire mesh to the sectional area of the bubbling bed reactor is 1.5-5; and/or
The ratio of the area of the second solid intercepting screen to the cross-sectional area of the fixed bed reactor is 1.5-5.
10. The reaction system according to any one of claims 1 to 3,
the gas-liquid bubbling bed reactor (I) and/or the full liquid-phase fixed bed reactor (V) are/is set to adopt a jacket/coil mode to remove heat.
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