CN218516672U - Continuous trickle bed liquid phase hydrogenation reaction device - Google Patents
Continuous trickle bed liquid phase hydrogenation reaction device Download PDFInfo
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- CN218516672U CN218516672U CN202222373347.3U CN202222373347U CN218516672U CN 218516672 U CN218516672 U CN 218516672U CN 202222373347 U CN202222373347 U CN 202222373347U CN 218516672 U CN218516672 U CN 218516672U
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Abstract
The utility model provides a continuous trickle bed liquid phase hydrogenation reaction device, which comprises a two-stage continuous trickle bed liquid phase hydrogenation reactor, a flash tank and a purge gas condenser, wherein the flash tank and the purge gas condenser are used for performing flash evaporation and condensation recovery on hydrogenation products and purge gas, and a raw material tank is used for stabilizing the pressure of hydrogenation raw materials; wherein, the bottom material flow of the second-stage liquid phase hydrogenation reactor is divided into two parts, one part is conveyed to a flash tank, and the other part is pressurized by a circulating pump and then mixed with the hydrogenation raw material from a raw material tank and conveyed back to the first-stage liquid phase hydrogenation reactor again; the utility model discloses a reaction unit is applicable to the saturated hydrogenation reaction of ketone, aldehyde, hydrocarbons, can effectively solve the big and insufficient problem of hydrogenation of the big and technological safety risk that present raney nickel stirred tank intermittent type batch reaction exists.
Description
Technical Field
The utility model relates to a ketone, aldehyde, the saturated hydrogenation reaction's of hydrocarbons technical field, concretely relates to continuous trickle bed liquid phase hydrogenation reaction unit.
Background
In the industries of fine chemical industry, pharmaceutical chemical industry, coal chemical industry, petrochemical industry and the like, hydrogenation reaction is a very common and very important reaction, and for gas, liquid and solid three-phase reaction, the common reactor types are a stirred tank reactor, a bubbling bed and a trickle bed reactor. For most saturated hydrogenation reactions, as the gas-solid phase contact of the trickle bed reactor is more sufficient, the hydrogenation is more sufficient, and the reaction effect is obviously superior to that of a bubbling bed reactor and a stirred tank reactor.
In the fine chemical industry and the pharmaceutical chemical industry, stirred tank hydrogenation reactors are widely applied, an intermittent batch reaction mode is adopted, and a Raney nickel catalyst is used, so that the method has the characteristics of high investment, low automation degree, high safety risk and the like. In recent years, accidents involving hydrogenation reactions have occurred many times in the above-mentioned industries, causing some irreparable losses. Hydrogenation reactions in these industries are demanding continuous upgrading and engineering to use intrinsically safe catalysts and process technologies to increase the safety level.
SUMMERY OF THE UTILITY MODEL
An object of the utility model is to provide a serialization trickle bed liquid phase hydrogenation reaction unit has set up the purpose that two-stage serialization trickle bed liquid phase hydrogenation reactor reaches hydrogenation for the serialization technology upgrading transformation and the product hydrofining of raney nickel stirred tank intermittent type batch reaction have solved the big and insufficient problem of hydrogenation of process safety risk that raney nickel stirred tank intermittent type reaction exists.
The utility model adopts the technical scheme as follows:
providing a continuous trickle bed liquid phase hydrogenation reaction device, which comprises a primary liquid phase hydrogenation reactor and a secondary liquid phase hydrogenation reactor; liquid phase hydrogenation catalysts are filled in the first-stage liquid phase hydrogenation reactor and the second-stage liquid phase hydrogenation reactor; the top of each two-stage hydrogenation reactor is provided with a feeding hole, and the bottom of each two-stage hydrogenation reactor is provided with a discharging hole; the feeding port at the top of the primary liquid-phase hydrogenation reactor is used for inputting a mixture of a hydrogenation raw material and hydrogen, the discharging port at the bottom of the primary liquid-phase hydrogenation reactor is connected with the feeding port at the top of the secondary liquid-phase hydrogenation reactor, and the feeding port at the top of the secondary liquid-phase hydrogenation reactor is also connected with a hydrogen main pipe through a second hydrogen branch pipe; a discharge hole at the bottom of the secondary liquid-phase hydrogenation reactor is connected with a feed hole at the top of the primary liquid-phase hydrogenation reactor through a circulating pipe; the circulating pipe is provided with a circulating pump, and the circulating pipe on the upstream side of the circulating pump is also connected with a production pipe.
Preferably, an interstage cooler is arranged on a pipeline connected between the first-stage liquid-phase hydrogenation reactor and the second-stage liquid-phase hydrogenation reactor.
Preferably, the reaction device further comprises a flash tank, and the flash tank is communicated with a production pipe and is used for carrying out flash separation on a produced material flow at the bottom of the secondary liquid-phase hydrogenation reactor; and a hydrogenation product is extracted from the bottom of the flash tank.
Preferably, the reaction device further comprises a raw material tank and a raw material pump, the hydrogenation raw material from outside is firstly input into the raw material tank, the inlet end of the raw material pump is connected to the bottom of the raw material tank, the outlet end of the raw material pump is connected with a circulating pipe at the downstream side of the circulating pump, and the connecting point is connected with a feeding hole at the top of the primary liquid-phase hydrogenation reactor through a dilution pipe; the dilution pipe is also connected with a hydrogen main pipe through a first hydrogen branch pipe; and the first hydrogen branch pipe and the second hydrogen branch pipe are both provided with hydrogen feeding emergency closing valves.
Preferably, a pipeline mixer is arranged on both the upstream side and the downstream side of the connection point of the dilution pipe and the first hydrogen branch pipe; and a feed preheater is also arranged on the dilution pipe at the upstream side of the connection point.
Preferably, a circulating cooler is arranged on the circulating pipe.
Preferably, the reaction device further comprises a purge gas pipe; the raw material tank and the flash tank are both connected with the purge gas pipe through pipelines with valves; the primary liquid-phase hydrogenation reactor and the secondary liquid-phase hydrogenation reactor are respectively communicated with the flash tank through a purge gas flow regulating loop, and regulating valves are arranged on the purge gas flow regulating loops and can regulate the concentration of hydrogen in the corresponding reactors by controlling the purge amount of the hydrogen; the purge gas regulating loop located at the upstream of the regulating valve is also directly communicated with a purge gas pipe through a pipeline with an emergency emptying valve.
Preferably, the top of the stock tank is further provided with a nitrogen supplementing pipe with a valve, a pressure sensor and a range controller (not shown in the figure), and the range controller is respectively connected and controlled with the pressure sensor, the valve on the nitrogen supplementing pipe and the valve on the pipeline connecting the stock tank with the purge gas pipe; the split-range controller is used for maintaining the pressure environment in the raw material tank at 0.2MPaG, supplementing nitrogen into the raw material tank when the pressure in the raw material tank is reduced, and discharging purge gas outwards when the pressure is increased.
Preferably, liquid level and flow cascade regulating loops and emergency shut-off valves are arranged on outlet pipelines at the bottoms of the raw material tank, the secondary liquid-phase hydrogenation reactor and the flash evaporation tank; the liquid level and flow cascade regulating loop is controlled by a liquid level meter arranged on a corresponding container and a flow meter and a control valve on an outlet pipeline in a linkage way; the flow regulating circuit is used for controlling the liquid level in the corresponding container.
Preferably, a purge gas cooler is further arranged on a pipeline with a valve, which is connected with the purge gas pipe of the flash tank.
When the device is used, a hydrogenation raw material from outside is firstly fed into a raw material tank, is pressurized by a raw material pump and then is mixed with a circulating liquid through a pipeline mixer on a dilution pipe (the dilution mixing process can be used for diluting the concentration of the hydrogenation raw material from outside, and can control the adiabatic temperature rise of a liquid-phase hydrogenation reactor), and then is fed into a feed preheater for preheating, and the preheated raw material and hydrogen are mixed by the pipeline mixer and then are fed into a primary liquid-phase hydrogenation reactor for reaction;
in the first-stage liquid-phase hydrogenation reactor, a liquid-phase hydrogenation catalyst is filled, most of fresh raw materials are subjected to hydrogenation saturation, a small part of fresh raw materials are sent to the second-stage liquid-phase hydrogenation reactor for continuous reaction, and an interstage cooler is arranged between the two-stage liquid-phase hydrogenation reactors in order to prevent the reaction temperature of the second-stage liquid-phase hydrogenation reactor from being overhigh;
a liquid phase hydrogenation catalyst is filled in the second-stage liquid phase hydrogenation reactor, the material to be hydrogenated in the hydrogenation raw material is basically completely hydrogenated, the hydrogenated material is divided into two parts, one part is sent to a flash tank for low-pressure flash evaporation, and the other part is pressurized by a hydrogenation circulating pump and cooled by a circulating cooler and then is mixed with the raw material;
hydrogen-containing purge gas of the two-stage liquid-phase hydrogenation reactor and the hydrogenation material of the two-stage liquid-phase hydrogenation reactor are sent to a flash tank through a flow regulating loop, the flashed gas is sent to a purge gas cooler for cooling and then sent to the outside, and the flashed hydrogenation product is sent to the outside.
The first-stage and second-stage liquid-phase hydrogenation reactors adopt trickle bed reactors, gas-liquid-solid three-phase reactions (hydrogen is a gas phase, a hydrogenation material is a liquid phase, and a catalyst is a solid phase) are carried out, hydrogen atmosphere is in the reactors, the hydrogenation material flows through a catalyst bed layer in a trickle shape, gas-liquid separation is carried out at the bottom of the reactors, and the concentration of hydrogen in the reactors is controlled by a flow regulating loop on a purge gas pipeline.
Wherein, the circulation ratio of the circulating liquid and the hydrogenation raw material is 0 to 20, preferably 2 to 10.
The operating conditions of the first-stage and second-stage liquid phase hydrogenation reactors are 70-150 ℃ and 0.5-6.0 MPaG, preferably 80-140 ℃ and 1.0-4.0 MPaG.
The liquid phase hydrogenation catalyst used in the first-stage and second-stage liquid phase hydrogenation reactors is a supported nickel catalyst, preferably a supported high nickel catalyst with higher activity than Raney nickel.
Compared with the prior art, the utility model discloses possess following beneficial effect at least: compared with the batch liquid phase hydrogenation process of the traditional stirred tank reactor, the continuous trickle bed liquid phase hydrogenation reaction device has low investment, high automation degree and intrinsically safe process technology; compared with the traditional bubbling bed liquid phase hydrogenation process, the gas-solid contact in the continuous trickle bed liquid phase hydrogenation reaction device is more sufficient, and the hydrogenation effect is better; compared with a Raney nickel catalyst, the intrinsically safe supported nickel catalyst has high safety level; the conventional process adopts a large amount of hydrogen to circularly cool so as to remove reaction heat, a circulating hydrogen compressor is required to be arranged, the investment is increased, and the power consumption is increased. The continuous trickle bed liquid phase hydrogenation reaction adopts circulating liquid for cooling and heat removal, and hydrogen is not circulated, so that the investment and the running power consumption are reduced; the continuous trickle bed liquid phase hydrogenation reaction device adopts a series of automatic control means and interlocking, has high process operation stability, and meets the requirement of 'stable, long and excellent' of a chemical device.
Drawings
FIG. 1 is a schematic diagram of a continuous trickle-bed liquid-phase hydrogenation reactor.
In the figure: the device comprises a raw material tank 1, a raw material pump 2, a feed preheater 3, a primary liquid phase hydrogenation reactor 4, an interstage cooler 5, a circulation cooler 6, a hydrogenation circulating pump 7, a secondary liquid phase hydrogenation reactor 8, a flash tank 9, a purge gas cooler 10, a hydrogenation raw material pipe 11, a hydrogen header pipe 12, a hydrogenation product 13, a purge gas 14, a temperature control circuit TC, a flow control circuit FC, a pressure control circuit PC, a liquid level control circuit LC, a low-pressure nitrogen gas N2, a low-pressure steam LS, a low-pressure steam condensate LC, a circulating water CWS, a circulating water CWR, a circulating water backwater CHWS, and a chilled water backwater CHWR.
Wherein: the control loop in the utility model refers to the corresponding sensor converting the detection signal into an electric signal and controlling the opening degree of the valve related to the sensor; such as a TC temperature control loop, converts a signal of a temperature sensor into an electrical signal, and controls the opening of a valve associated with the temperature sensor according to the electrical signal and a preset program.
Detailed Description
In order to illustrate the present invention more clearly, the present invention will be further described with reference to the following examples. It is to be understood by persons skilled in the art that the following detailed description is illustrative and not restrictive, and is not to be taken as limiting the scope of the invention.
Example 1
Referring to fig. 1, the present embodiment provides a continuous trickle bed liquid phase hydrogenation apparatus, which includes a primary liquid phase hydrogenation reactor 4 and a secondary liquid phase hydrogenation reactor 8; liquid phase hydrogenation catalysts are filled in the first-stage liquid phase hydrogenation reactor 4 and the second-stage liquid phase hydrogenation reactor 8; the top of each two-stage hydrogenation reactor is provided with a feeding hole, and the bottom of each two-stage hydrogenation reactor is provided with a discharging hole; a feed inlet at the top of the primary liquid-phase hydrogenation reactor 4 is used for inputting a mixture of a hydrogenation raw material and hydrogen, a discharge outlet at the bottom of the primary liquid-phase hydrogenation reactor is connected with a feed inlet at the top of the secondary liquid-phase hydrogenation reactor 8, and the feed inlet at the top of the secondary liquid-phase hydrogenation reactor 8 is also connected with a hydrogen main pipe 12 through a second hydrogen branch pipe 18; a discharge hole at the bottom of the secondary liquid phase hydrogenation reactor 8 is connected with a feed hole at the top of the primary liquid phase hydrogenation reactor 4 through a circulating pipe 15; the circulating pipe 15 is provided with a circulating pump 7, and the circulating pipe 15 on the upstream side of the circulating pump 7 is also connected with a production pipe.
Preferably, an interstage cooler 5 is arranged on a pipeline connected between the first-stage liquid-phase hydrogenation reactor 4 and the second-stage liquid-phase hydrogenation reactor 8.
Preferably, the reaction device further comprises a flash tank 9, and the flash tank 9 is communicated with a production pipe and is used for carrying out flash separation on a production material flow at the bottom of the secondary liquid-phase hydrogenation reactor 8; the bottom of the flash tank 9 produces a hydrogenated product 13.
Preferably, the reaction device further comprises a raw material tank 1 and a raw material pump 2, the hydrogenation raw material 11 from outside is firstly input into the raw material tank 1, the inlet end of the raw material pump 2 is connected to the bottom of the raw material tank 1, the outlet end of the raw material pump 2 is connected with a circulating pipe 15 at the downstream side of the circulating pump 7, and the connecting point is connected with the feeding hole at the top of the primary liquid-phase hydrogenation reactor 4 through a dilution pipe; the dilution pipe is also connected with the hydrogen main pipe 12 through a first hydrogen branch pipe 17; the first hydrogen branch pipe 17 and the second hydrogen branch pipe 18 are both provided with a hydrogen feeding emergency closing valve.
Preferably, a pipeline mixer 16 is arranged on both the upstream side and the downstream side of the connection point of the dilution pipe and the first hydrogen branch pipe 17; and a feed preheater 3 is also provided on the dilution pipe on the upstream side of the connection point.
Preferably, the circulation pipe 15 is provided with a circulation cooler 6.
Preferably, the reaction device further comprises a purge gas pipe 14; the raw material tank 1 and the flash tank 9 are both connected with the purge gas pipe 14 through pipelines with valves; the primary liquid-phase hydrogenation reactor 4 and the secondary liquid-phase hydrogenation reactor 8 are respectively communicated with a flash tank 9 through a purge gas flow regulating loop, and regulating valves are arranged on the purge gas flow regulating loops and can regulate the hydrogen concentration in the corresponding reactors by controlling the purge amount of hydrogen; wherein, the purge gas adjusting loop positioned at the upstream of the adjusting valve is also directly communicated with a purge gas pipe 14 through a pipeline with an emergency emptying valve.
Preferably, the top of the raw material tank 1 is further provided with a nitrogen supplementing pipe with a valve, a pressure sensor and a split-range controller (not shown in the figure), and the split-range controller is respectively connected and controlled with the pressure sensor, the valve on the nitrogen supplementing pipe and the valve on the pipeline connecting the raw material tank 1 with the purge gas pipe 14; the split-range controller is used for maintaining the pressure environment in the raw material tank 1 at 0.2MPaG, supplementing nitrogen into the raw material tank 1 when the pressure in the raw material tank 1 is reduced, and discharging purge gas outwards when the pressure is increased.
Preferably, the outlet pipelines at the bottoms of the raw material tank 1, the primary liquid-phase hydrogenation reactor 4, the secondary liquid-phase hydrogenation reactor 8 and the flash tank 9 are respectively provided with a liquid level and flow cascade regulating loop and an emergency closing valve; the liquid level and flow cascade regulation loop is in linkage control by a liquid level meter arranged on a corresponding container and a flow meter and a control valve on an outlet pipeline; the flow regulating circuit is used for controlling the liquid level in the corresponding container.
Preferably, a purge gas cooler 10 is further provided in a valved pipe connecting the flash tank 9 and the purge gas pipe 14.
The working principle of the reaction device is illustrated by liquid-phase hydrogenation of n-butyraldehyde:
(1) The method comprises the following steps of firstly feeding hydrogenation raw materials from outside into a raw material tank 1, pressurizing the hydrogenation raw materials to 4.0MPaG through a raw material pump 2, mixing the hydrogenation raw materials with a circulating liquid from a circulating pipe 15 through a pipeline mixer 16, wherein the circulating mass ratio of the circulating liquid to the hydrogenation raw materials is 8, diluting the concentration of materials to be hydrogenated in the raw materials to about 10wt%, then feeding the materials into a feed preheater 3 for preheating to 90 ℃, mixing the preheated raw materials with hydrogen, and feeding the mixture into a primary liquid phase hydrogenation reactor 4 for reaction.
The operation pressure of the raw material tank 1 is controlled by the process adjustment, nitrogen is supplemented when the pressure is low, purge gas is exhausted when the pressure is high, and the pressure is controlled at 0.2MPaG.
(2) In the first-stage liquid-phase hydrogenation reactor 4, under the action of a catalyst, most of fresh raw materials are subjected to hydrogenation saturation, a small part of fresh raw materials are sent to the second-stage liquid-phase hydrogenation reactor 8 for continuous reaction, and the interstage cooler 5 cools the raw materials so as to prevent the reaction temperature of the second-stage liquid-phase hydrogenation reactor 8 from being too high.
Wherein the operating conditions in the first-stage liquid phase hydrogenation reactor 4 are 90-125 ℃ and 4.0MPaG. The operating pressure of the reactor is regulated by feeding hydrogen and the temperature of the reactor is regulated by feeding a preheater 3 and a circulation cooler 6. The adiabatic temperature rise of the reactor is adjusted by the circulation mass ratio of the circulation liquid to the hydrogenation raw material (the hydrogenation reaction is an exothermic reaction, the concentration of reactants fed into the reactor can be controlled by the circulation ratio, and the lower the concentration of the reactants fed into the reactor, the smaller the temperature difference between the outlet and the inlet of the reactor for the adiabatic reactor).
The hydrogen concentration in the primary liquid phase hydrogenation reactor 4 is controlled by a purge flow regulating circuit.
The liquid level of the primary liquid-phase hydrogenation reactor 4 is regulated by a bottom liquid level control valve.
(3) In the second-stage liquid phase hydrogenation reactor 8, under the action of the hydrogenation catalyst, the material to be hydrogenated in the hydrogenation raw material is basically completely hydrogenated, the hydrogenated material is divided into two parts, one part is sent to a flash tank 9 for low-pressure flash evaporation, and the other part is pressurized by a hydrogenation circulating pump 7 and cooled to 90 ℃ by a circulating cooler 6 and then mixed with the hydrogenation raw material through a circulating pipe 15.
The operating conditions of the second-stage liquid phase hydrogenation reactor 8 are 90-93 ℃ and 3.8MPaG, and the settings of the operating temperature and the operating pressure of the second-stage liquid phase hydrogenation reactor 8 and the adjustment of the hydrogen concentration in the reactor are the same as those of the first-stage liquid phase hydrogenation reactor 4.
(4) Hydrogen-containing gas purge gas of the two-stage liquid-phase hydrogenation reactor and the hydrogenation material of the two-stage liquid-phase hydrogenation reactor are sent to a flash tank 9, the gas flashed off is sent to a purge gas cooler 10 for cooling and then sent to the outside, and the hydrogenation product flashed off is sent to the outside.
The gas-phase hydrogenation product carried in the purge gas is recovered by freezing water in the purge gas cooler 10, and the pressure of the flash tank 9 is controlled at 0.3MPaG.
A hydrogenated product discharge pipeline at the bottom of the flash tank 9 is provided with a hydrogenated product emergency closing valve and a flow regulating loop, and is in cascade control with the liquid level of the flash tank 9.
Obviously, the above embodiments of the present invention are only examples for clearly illustrating the present invention, and are not intended to limit the embodiments of the present invention, and it is obvious for those skilled in the art to make other variations or changes based on the above descriptions, and all the embodiments cannot be exhausted here, and all the obvious variations or changes that belong to the technical solutions of the present invention are still in the protection scope of the present invention.
Claims (10)
1. A continuous trickle bed liquid phase hydrogenation reaction device is characterized in that: comprises a primary liquid-phase hydrogenation reactor (4) and a secondary liquid-phase hydrogenation reactor (8); liquid phase hydrogenation catalysts are filled in the first-stage liquid phase hydrogenation reactor (4) and the second-stage liquid phase hydrogenation reactor (8); the top of each two-stage hydrogenation reactor is provided with a feeding hole, and the bottom of each two-stage hydrogenation reactor is provided with a discharging hole; wherein, the feed inlet at the top of the primary liquid phase hydrogenation reactor (4) is used for inputting a mixture of hydrogenation raw materials and hydrogen, the discharge outlet at the bottom of the primary liquid phase hydrogenation reactor is connected with the feed inlet at the top of the secondary liquid phase hydrogenation reactor (8), and the feed inlet at the top of the secondary liquid phase hydrogenation reactor (8) is also connected with a hydrogen main pipe (12) through a second hydrogen branch pipe (18); a discharge hole at the bottom of the secondary liquid-phase hydrogenation reactor (8) is connected with a feed hole at the top of the primary liquid-phase hydrogenation reactor (4) through a circulating pipe (15); and a circulating pump (7) is arranged on the circulating pipe (15), and a production pipe is also connected to the circulating pipe (15) on the upstream side of the circulating pump (7).
2. The reactor apparatus of claim 1, wherein: the system also comprises a flash tank (9), wherein the flash tank (9) is communicated with an extraction pipe; and a hydrogenated product (13) is extracted from the bottom of the flash tank (9).
3. The reactor apparatus of claim 2, wherein: the hydrogenation device is characterized by further comprising a raw material tank (1) and a raw material pump (2), wherein a hydrogenation raw material (11) from the outside is firstly input into the raw material tank (1), the inlet end of the raw material pump (2) is connected to the bottom of the raw material tank (1), the outlet end of the raw material pump (2) is connected with a circulating pipe (15) on the downstream side of the circulating pump (7), and the connecting point is connected with a feeding hole in the top of the primary liquid-phase hydrogenation reactor (4) through a dilution pipe; the dilution pipe is also connected with a hydrogen main pipe (12) through a first hydrogen branch pipe (17); and hydrogen feeding emergency closing valves are arranged on the first hydrogen branch pipe (17) and the second hydrogen branch pipe (18).
4. A reaction apparatus as claimed in claim 3, wherein: an interstage cooler (5) is arranged on a pipeline connected between the primary liquid-phase hydrogenation reactor (4) and the secondary liquid-phase hydrogenation reactor (8); a pipeline mixer (16) is arranged on both the upstream side and the downstream side of the connection point of the dilution pipe and the first hydrogen branch pipe (17); a feeding preheater (3) is also arranged on the dilution pipe positioned at the upstream side of the connection point; and a circulating cooler (6) is arranged on the circulating pipe (15).
5. The reaction device of claim 4, wherein: also comprises a relief air pipe (14); the raw material tank (1) and the flash tank (9) are both connected with the purge gas pipe (14) through a pipeline with a valve; the primary liquid-phase hydrogenation reactor (4) and the secondary liquid-phase hydrogenation reactor (8) are respectively communicated with the flash tank (9) through a purge gas flow regulating loop, regulating valves are arranged on the purge gas flow regulating loops, and a purge gas pipe (14) is directly communicated with the purge gas regulating loop positioned at the upstream of the regulating valves through a pipeline with an emergency vent valve.
6. The reactor apparatus of claim 5, wherein: the top of the raw material tank (1) is also provided with a nitrogen supplementing pipe with a valve, a pressure sensor and a range controller, and the range controller is respectively connected and controlled with the pressure sensor, the valve on the nitrogen supplementing pipe and the valve on the pipeline connecting the raw material tank (1) with the purge gas pipe (14).
7. The reaction device of claim 6, wherein: outlet pipelines at the bottoms of the raw material tank (1), the secondary liquid-phase hydrogenation reactor (8) and the flash tank (9) are respectively provided with a liquid level and flow cascade regulating loop and an emergency closing valve; the liquid level and flow cascade regulation loop is in linkage control by a liquid level meter arranged on a corresponding container and a flow meter and a control valve on an outlet pipeline.
8. The reactor apparatus of claim 7, wherein: and a purge gas cooler (10) is also arranged on a pipeline with a valve, which is connected with the purge gas pipe (14) of the flash tank (9).
9. The reactor apparatus of claim 8, wherein: the primary liquid-phase hydrogenation reactor (4) and the secondary liquid-phase hydrogenation reactor (8) are both trickle bed reactors, the hydrogen atmosphere is in the reactors, the hydrogenation materials flow through the catalyst bed layer in a dripping manner, gas-liquid separation is carried out at the bottom of the reactors, and the hydrogen concentration in the reactors is controlled through a flow regulating loop on a purge gas pipeline.
10. The reaction device of claim 9, wherein: the mass circulation ratio of the circulating liquid to the hydrogenation raw material is 0-20.
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| CN202222373347.3U CN218516672U (en) | 2022-09-06 | 2022-09-06 | Continuous trickle bed liquid phase hydrogenation reaction device |
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| CN202222373347.3U CN218516672U (en) | 2022-09-06 | 2022-09-06 | Continuous trickle bed liquid phase hydrogenation reaction device |
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