CN211463089U - Gas, liquid, solid three-phase hydrogenation reaction system - Google Patents
Gas, liquid, solid three-phase hydrogenation reaction system Download PDFInfo
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- CN211463089U CN211463089U CN201921921597.8U CN201921921597U CN211463089U CN 211463089 U CN211463089 U CN 211463089U CN 201921921597 U CN201921921597 U CN 201921921597U CN 211463089 U CN211463089 U CN 211463089U
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Abstract
The utility model relates to a gas, liquid and solid three-phase hydrogenation reaction system, which comprises a trickle bed reactor, wherein the trickle bed reactor comprises a lower tube box, a shell side cylinder and an upper tube box from bottom to top, a tube bundle is arranged in the shell side cylinder, and a catalyst is filled in the tube bundle reaction tube; a liquid phase material inlet is formed in the top of the upper pipe box, and a liquid distributor is arranged below the liquid phase material inlet; the liquid distributor comprises a liquid disc and a drip assembly arranged on the liquid disc, the bottom of the drip assembly extends into a reaction tube of a tube bundle in the shell side cylinder body, and liquid entering from a liquid phase material inlet is guided to the reaction tube point to point. The utility model discloses a trickle bed reactor adopts point-to-point liquid distribution design, has avoided the inhomogeneous phenomenon of liquid phase distribution, adopts the liquid holdup adjustment of distributor, can realize the accurate control of liquid phase load, makes things convenient for three-phase hydrogenation reaction system's elasticity operation.
Description
Technical Field
The utility model relates to the technical field of chemical industry, concretely relates to gas, liquid, solid three-phase hydrogenation reaction system.
Background
Catalytic hydrogenation is an important chemical method for preparing organic intermediates and chemical products, and is widely applied to multiple fields of fine chemical industry, coal chemical industry, petrochemical industry and the like at present. With the continuous increase of living and industrial demands in recent years, the chemical industry is in a deep development opportunity, and new products based on the catalytic hydrogenation reaction technology are more and more; however, the industrialization of new products also puts higher requirements on the existing chemical production equipment, and the gas, liquid and solid three-phase catalytic hydrogenation reaction system which is efficient, stable, easy to regulate and control and convenient to operate becomes an important direction for the innovation of the chemical technology at present.
A three-phase hydrogenation reaction system belongs to the field of heterogeneous catalysis technology, and generally refers to a chemical reaction unit for generating a liquid-phase product by hydrogen and a liquid-phase material under the action of a solid-phase catalyst. The traditional three-phase hydrogenation reaction system mainly comprises a slurry stirring hydrogenation reaction system, a jet hydrogenation reaction system, a trickle bed hydrogenation reaction system and the like, but has certain defects in actual production.
The slurry stirring hydrogenation reaction system takes a stirring reaction kettle as a core, utilizes a fluid stirring and mixing technology, and is characterized in that a liquid-phase material and a solid catalyst are stirred and wetted in the reaction kettle, then react with introduced hydrogen on the surface of the catalyst, keep for a certain time under the conditions of continuous heat preservation and continuous stirring, and separate products after the reaction is finished, such as a domestic dinitrobenzene hydrogenation reaction system. The slurry stirring hydrogenation reaction system is suitable for occasions with low catalyst consumption and is widely applied in laboratories, but the reaction process of the system is difficult to control accurately, the sealing problem of the device is not easy to solve, the large-scale equipment is difficult, and the industrial yield is small.
The jet hydrogenation system takes a jet reaction container as a core, and utilizes the Venturi principle to suck low-pressure hydrogen through a high-speed liquid phase material mixed with a solid catalyst, so that a gas phase and a liquid phase are fully contacted on the surface of the solid catalyst, and then are uniformly dispersed or suspended in the reaction container to finish the reaction; the device is matched with a settling kettle to form a circulating reaction kettle, and the double processes of hydrogenation reaction and liquid-solid separation are completed; for example, domestic processes for liquid-phase hydrogenation of dinitrotoluene and hydrogenation of rubber antioxidants. The material conveying energy consumption of the jet hydrogenation reaction system is large, and the device investment is high; meanwhile, the solid-phase catalyst is easy to wear when being in a high-speed flowing state for a long time, and has higher requirements on the wear resistance of a reactor, a pipeline and a fluid delivery pump.
The trickle bed hydrogenation reaction system takes a trickle bed reactor as a core, a liquid phase material flows from top to bottom along the gravity direction, and the liquid phase material is fully contacted with hydrogen flowing in a countercurrent or parallel way in a solid catalyst particle bed layer and reacts; such as domestic coal liquefaction fraction hydrogenation and maleic anhydride hydrogenation reactions. The trickle bed hydrogenation reaction system is suitable for occasions with high catalyst consumption, has the characteristics of simple reaction system structure, easy operation, high yield and small device investment, and is also the most advantageous technology in the industrialization of a three-phase catalytic hydrogenation reaction system. However, the system is often accompanied with the problem of non-uniformity of liquid phase materials in the industrial scale-up process, so that the scaled-up system can not achieve the reaction effect of a laboratory.
Disclosure of Invention
For overcoming prior art's defect, the utility model provides a gas, liquid, solid three-phase hydrogenation reaction system, gas, liquid phase distribution are effectual, and reaction temperature control is accurate, and operation elasticity is big, and easily the industrialization is enlarged, and the efficiency height is synthesized in production.
The utility model discloses the technical scheme who adopts does:
a gas, liquid, solid three-phase hydrogenation reaction system, its characterized in that:
the system comprises a trickle bed reactor, wherein the trickle bed reactor comprises a lower tube box, a shell pass cylinder and an upper tube box from bottom to top, a tube bundle is arranged in the shell pass cylinder, and a catalyst is filled in the tube bundle reaction tube;
a liquid phase material inlet is formed in the top of the upper pipe box, and a liquid distributor is arranged below the liquid phase material inlet; the liquid distributor comprises a liquid disc and a drip assembly arranged on the liquid disc, the bottom of the drip assembly extends into a reaction tube of a tube bundle in the shell side cylinder body, and liquid entering from a liquid phase material inlet is guided to the reaction tube point to point; a liquid-phase product outlet is formed at the bottom of the lower pipe box;
the side wall of the upper pipe box is provided with a hydrogen inlet, and hydrogen is introduced into the upper pipe box through a gas phase distributor and enters the reaction tubes of the tube bundle; the side wall of the lower pipe box is provided with a tail gas outlet.
The system also comprises a heat exchange medium buffer tank and a cooler;
an upper ring channel and a lower ring channel are arranged on the outer wall of a shell pass cylinder of the trickle bed reactor, and an opening is formed in the outer wall of the corresponding shell pass cylinder;
the upper ring is connected with a cooler, the cooler is connected with a heat exchange medium buffer tank, the heat exchange medium buffer tank is connected back to the lower ring, and a circulating pump is arranged between the lower ring and the heat exchange medium buffer tank.
A weir cylinder is arranged on the periphery of the liquid disc of the liquid distributor;
the drip assembly of the liquid distributor comprises a drip tube, a nozzle and a conduit from top to bottom, wherein the drip tube is inserted into the nozzle and is positioned above the liquid disc, the nozzle is connected into the conduit below the liquid disc, and the conduit extends into a reaction tube of a tube bundle in the shell pass cylinder.
The liquid phase material inlet is connected with an inward extending connecting pipe downwards, the connecting pipe is installed under liquid, the bottom of the connecting pipe is blocked, and a circumferential lateral hole is formed.
The lateral holes are arranged on a dropper of the liquid distributor, and liquid enters the drip assembly through the lateral holes of the dropper and then is guided to the reaction tubes of the tube bundle.
The liquid distributor comprises A, B type two types of drip assemblies; the A-type drip component is arranged at the position of a non-temperature-measuring point; the B-type drip assembly is arranged at the position of the temperature measuring point, the diameter of the B-type drip assembly is 5-10 mm larger than that of the A-type drip assembly, and the temperature measuring sleeve penetrates through the B-type drip assembly in a centering mode and goes deep into the deep part of the reaction tube.
The gas phase distributor comprises a ring pipe and branch pipes, and the branch pipes are uniformly arranged along the circumferential direction.
The upper loop is provided with a heat exchange medium outlet, and the cooler is connected with the upper loop through the heat exchange medium outlet;
the lower loop is provided with a heat exchange medium inlet, and the heat exchange medium buffer tank is connected with the lower loop through the heat exchange medium inlet by a circulating pump.
The upper pipe box is provided with a top gas phase temperature measuring port, a heat exchange medium temperature measuring port, a catalyst temperature measuring port and a top gas phase pressure measuring port, and the lower pipe box is provided with a bottom gas phase temperature measuring port and a bottom gas phase pressure measuring port.
The utility model has the advantages of it is following:
(1) the utility model provides a pair of gas, liquid, solid three-phase hydrogenation reaction system, core device trickle bed reactor can guarantee that gas-liquid-solid three-phase contact state and reaction process in the reaction shell and tube are experimental unanimous completely, have fine amplification advantage, easily reaction system's maximization.
(2) The utility model discloses a trickle bed reactor adopts point-to-point liquid distribution design, has avoided the inhomogeneous phenomenon of liquid phase distribution, adopts the liquid holdup adjustment of distributor, can realize the accurate control of liquid phase load, makes things convenient for three-phase hydrogenation reaction system's elasticity operation.
(3) The utility model discloses a trickle bed reactor adopts the design of differential drip subassembly, effectively solves liquid distributor and reaction temperature measurement structure interference problem, makes things convenient for the installation of temperature measurement thermocouple, guarantees the accuracy of reactor temperature measurement, improves three-phase hydrogenation reaction system operability and usability.
(4) The reaction heat exchange medium of the trickle bed reactor can be various media such as steam, heat transfer oil, molten salt and the like, the heat exchange medium is distributed and collected through unequal-diameter holes which are uniformly distributed in the circumferential direction of a loop and a shell, the temperature uniformity of the trickle reaction tube is controlled by utilizing the flow guidance of the ring-cake baffle plate, and the accurate control of the reaction temperature is realized by adjusting the circulation quantity of the heat transfer medium.
Drawings
Fig. 1 is a schematic diagram of the system structure of the present invention.
Fig. 2 is a schematic view of a liquid distributor.
In the figure, V is a heat exchange medium buffer tank; e-a cooler; r-trickle bed reactor; p-a circulating pump;
1-a lower tube box; 2-shell pass cylinder; 3, tube bundle; 4, feeding a tube box; 5-liquid distributor; 6-gas phase distributor; 7, upper loop; 8-lower loop;
n1-liquid phase feed inlet; n2 — hydrogen inlet; n3 — liquid phase product outlet; n4-tail gas outlet; n5 — heat exchange medium inlet; n6-outlet for heat exchange medium; t1-top gas phase temperature measurement port; t2-bottom gas phase temperature measurement port; t3-temperature measuring port for heat exchange medium I; t4-temperature measuring port for heat exchange medium II; t5-first catalyst temperature measuring port; T6-No. two catalyst temperature measurement ports; t7-third catalyst temperature measuring port; T8-No. four catalyst temperature measuring port; t9-catalyst temperature measuring port five; t10-temperature measuring port of catalyst VI; p1 — top gas phase pressure tap; p2 — bottom gas phase pressure tap;
5-1-liquid tray; 5-2-weir cylinder; 5-3-dropper; 5-4-nozzle; 5-conduit.
Detailed Description
The present invention will be described in detail with reference to the following embodiments.
The utility model relates to a gas, liquid, solid three-phase hydrogenation reaction system, the system includes trickle bed reactor R, trickle bed reactor R includes lower tube case 1, shell side barrel 2 and top tube case 4 from bottom to top, arranges tube bank 3 in shell side barrel 2, packs the catalyst in the tube bank 3 reaction tube; a liquid phase material inlet N1 is arranged at the top of the upper channel box 4, and a liquid distributor 5 is arranged below the liquid phase material inlet N1; the liquid distributor 5 comprises a liquid disc 5-1 and a trickle component arranged on the liquid disc, the bottom of the trickle component extends into the reaction tube of the tube bundle 3 in the shell-side cylinder 2, and liquid entering from a liquid-phase material inlet N1 is guided to the reaction tube point to point; the bottom of the lower tube box 1 is provided with a liquid-phase product outlet N3; a hydrogen inlet N2 is arranged on the side wall of the upper channel box 4, and gas is introduced into the upper channel box 4 and enters the reaction tubes of the tube bundle 3 through the gas phase distributor 6; the side wall of the lower pipe box 1 is provided with an exhaust gas outlet N4.
The system also comprises a heat exchange medium buffer tank V and a cooler E; an upper ring channel 7 and a lower ring channel 8 are arranged on the outer wall of the shell pass cylinder 2 of the trickle bed reactor R, and different-diameter holes are formed in the outer wall of the corresponding shell pass cylinder 2; go up the loop 7 and insert cooler E, cooler E inserts heat transfer medium buffer tank V, and heat transfer medium buffer tank V connects back lower loop 8, is provided with circulating pump P between lower loop 8 and the heat transfer medium buffer tank V.
A weir cylinder 5-2 is arranged on the periphery of a liquid disc 5-1 of the liquid distributor 5; the drip assembly of the liquid distributor 5 comprises a drip pipe 5-3, a nozzle 5-4 and a conduit 5-5 from top to bottom, wherein the drip pipe 5-3 is inserted into the nozzle 5-4 and is positioned above the liquid disc 5-1, the nozzle 5-4 is connected with the conduit 5-5 below the liquid disc 5-1, and the conduit 5-5 extends into the reaction tube of the tube bundle 3 in the shell side cylinder 2.
The liquid phase material inlet N1 is connected with an inward extending connecting pipe downwards, the connecting pipe is installed under liquid and the bottom of the connecting pipe is sealed, and a circumferential lateral hole is formed. A dropper 5-3 of the liquid distributor 5 is provided with a lateral hole, and liquid enters the drip assembly through the lateral hole of the dropper 5-3 and then is guided to the reaction tube of the tube bundle 3. The liquid distributor 5 adopts A, B type two-class drip components, the A type drip component is arranged at the position without a temperature measuring point; the B-type drip assembly is arranged at the position of the temperature measuring point, the diameter of the B-type drip assembly is 5-10 mm larger than that of the A-type drip assembly, and the temperature measuring sleeve penetrates through the B-type drip assembly in a centering mode and goes deep into the deep part of the reaction tube.
The gas phase distributor 6 comprises a loop pipe and branch pipes, and the branch pipes are uniformly arranged along the circumferential direction.
A heat exchange medium outlet N6 is arranged on the upper loop 7, and the upper loop 7 is connected to the cooler E through a heat exchange medium outlet N6; the lower loop 8 is provided with a heat exchange medium inlet N5, and a heat exchange medium buffer tank V is connected to the lower loop 8 through a heat exchange medium inlet N5 by a circulating pump P.
The upper tube box 4 is provided with a top gas phase temperature measuring port T1, a top gas phase pressure measuring port P1, heat exchange medium temperature measuring ports (T3 and T4) and catalyst temperature measuring ports (T5-T10), and the lower tube box 1 is provided with a bottom gas phase temperature measuring port T2 and a bottom gas phase pressure measuring port P2.
Referring to fig. 1, the N1 nozzle is installed under liquid, the distance from the tail end to the disc surface of the liquid distributor is 5-10 mm, the bottom of the nozzle is blocked, and 4-6 groups of circumferential side holes are formed; the tube bundle is of a tube array fixed bed structure, and a tube distribution area is arranged in the center of the tube bundle. The gas phase distributor adopts a 'ring pipe-branch pipe' structure to distribute hydrogen, wherein 4-6 branch pipes are evenly distributed along the circumferential direction. And the positions of the shell barrel bodies corresponding to the upper/lower ring channels are uniformly provided with holes with different diameters along the circumferential direction.
The liquid distributor of the trickle bed reactor mainly comprises a liquid disc, a weir cylinder, a dropper, a nozzle and a guide pipe. The bottom of the dropper is provided with a 0.1-5 mm lateral hole. The drip tube, the nozzle and the conduit form an A, B type drip assembly, wherein the diameter of the drip tube, the nozzle and the conduit of the B type drip assembly is 5-10 mm larger than that of the A type drip assembly; at the non-temperature-measuring point, the A-type drip component is adopted, and at the temperature-measuring point, the B-type drip component is adopted, so that the point-to-point corresponding drip relation with the reaction tube is finally formed. The guide pipe extends into the reaction pipe for 2-5 mm.
When the three-phase hydrogenation reaction system operates, liquid-phase materials entering the interior of the trickle bed reactor are guided by the aid of the N1 connecting pipes arranged under liquid, enter the liquid distributor through the lateral holes in the end portion of the liquid distributor, and are accurately guided to each reaction pipe point to point by the aid of the trickle component arranged on the liquid distributor under the driving of liquid-phase static pressure. Hydrogen entering from N2 is distributed by a loop pipe and a branch pipe of a gas phase distributor and then enters the upper pipe box space; then, the mixture is uniformly fed into the reaction tube under the driving of pressure difference. Flowing the liquid phase material and hydrogen through the solid catalyst in a cocurrent mode in the reaction tube; under the action of the catalyst, the liquid phase material adsorbed on the surface of the catalyst and hydrogen gas are subjected to hydrogenation reaction to generate heat. Meanwhile, the low-temperature working medium stored in the heat exchange medium buffer tank is conveyed by a circulating pump, enters a lower loop from an N5 port of the trickle bed reactor, and uniformly enters a shell pass of the reactor at equal flow through a circumferential hole of a shell at the lower loop; through the diversion of the ring-cake type baffle plate, the dividing wall type heat exchange with a reaction medium is realized, the reaction heat is removed in real time, the optimal reaction temperature is maintained, and the uniformity of the radial temperature of the reactor is ensured; then the high-temperature working medium enters the upper loop from a circumferential hole of the shell at the upper loop of the reactor with uniform flow, is discharged out of the shell pass of the reactor from an N6 port, enters a cooler for dividing wall water cooling, and then returns to the heat exchange medium storage tank for recycling. Finally, reaction tail gas and liquid phase products are discharged from N4 and N3 ports on a lower pipe box of the reactor.
The reaction liquid phase operation load of the reaction system is adjusted according to the liquid level height fed back by the L port, and the flow of liquid materials in each reaction tube is accurately adjusted point to point by utilizing the hydrostatic pressure difference generated by different liquid holding heights. The reaction heat exchange medium of the system can be various media such as steam, heat transfer oil, molten salt and the like, the heat exchange medium is distributed and collected through unequal-diameter holes which are uniformly distributed in the circumferential direction of the ring channel and the shell, and the uniformity of the temperature in the reactor is controlled by utilizing the diversion of the ring-cake type baffle plate; and adjusting the reaction operation temperature according to the catalyst temperature and the heat exchange medium temperature fed back by T3-T10, and adjusting the circulation quantity of the heat exchange medium through a pipeline valve.
The operation process of the system is as follows:
before a three-phase hydrogenation reaction system is started to operate, a solid catalyst is pre-loaded in a reaction tube of a trickle bed reactor; the components of the liquid distributor are assembled according to the figure 2, the orientation is adjusted, after the directional relation of the components and each reaction tube point pair is formed, the components are installed at the position with a certain height away from the tube plate on the reactor and the level is adjusted; after an upper tube box and an upper tube plate of the reactor are sealed and fastened, installing a T1-10 tube opening flange cover pre-welded with a temperature measuring sleeve in place, and ensuring that the temperature measuring sleeve passes through a B-type trickle component of a liquid distributor in a centering manner and is inserted into the deep part of a corresponding reaction tube; other components and devices of the system are configured and installed in place as required by conventional chemical systems.
When the system is continuously operated, liquid-phase materials enter the trickle bed reactor from a port N1 at the top of the trickle bed reactor. Inside the reactor, liquid material gets into the liquid distributor by the N1 takeover of installing under the liquid and seting up circumference side opening, and under the hydrostatic pressure drive of liquid phase, liquid material gets into inside the reaction tube by setting up and the point-to-point accurate water conservancy diversion of drip subassembly on the liquid distributor. In the process, the flow is guided through a side hole at the bottom of the dropper according to the operating load and the working condition requirement, and the elastic adjustment of the operating load is carried out by utilizing the liquid holding height of the liquid distributor; at the beginning of starting and feeding, the liquid-phase material has less reaction requirement, and liquid is led out from the side hole at the bottom through the lower liquid holding height; when the normal production is carried out, the reaction requirement of the liquid-phase material is increased, the liquid holdup is increased, the hydrostatic pressure is increased, and the flow guiding speed of the side holes is increased, so that the liquid-phase load of a single reaction tube is increased; in the heavy-load operation, the liquid holding height can be continuously increased, and the heavy-liquid-phase load operation of a single reaction tube is realized by utilizing the overflow of the opening at the upper end of the dropper.
Meanwhile, high-pressure hydrogen enters through an N2 port, and enters an upper pipe box space of the reactor after being distributed by a circular pipe and a branch pipe of the gas distributor, and uniformly enters each reaction pipe under the action of pressure difference at two sides of each reaction pipe, and the hydrogen load can be elastically adjusted through a pipeline valve in cooperation with a liquid phase load according to the operation requirement.
When the system is operated, in the trickle bed reactor, the liquid-phase material entering the reaction tube fully wets the surface of the pre-loaded catalyst, and hydrogen is adsorbed and activated by the catalyst and then undergoes hydrogenation reaction with the liquid-phase material to generate a liquid-phase product and generate a large amount of heat;
at the moment, the low-temperature working medium stored in the heat exchange medium buffer tank is conveyed by a circulating pump, enters a lower loop from an N5 port of the trickle bed reactor, passes through a circumferential hole of a shell at the lower loop, and enters a shell pass of the reactor at equal flow; through the diversion of the ring-cake type baffle plate, the dividing wall type heat exchange with a reaction medium is realized, the reaction heat is removed in real time, the optimal reaction temperature is maintained, and the uniformity of the radial temperature of the reactor is ensured; then the high-temperature working medium enters the upper loop from a circumferential hole of the shell at the upper loop of the reactor at equal flow, is discharged out of the shell pass of the reactor through an N6 port, enters an E cooler for dividing wall water cooling, and then returns to the heat exchange medium storage tank for recycling. In the process, the circulating amount of the heat exchange medium can be adjusted through a pipeline valve according to the catalyst temperature and the heat exchange medium temperature fed back by temperature measuring thermocouples at T3-T10 ports on the trickle bed reactor, the temperature runaway inside the reactor is avoided, and the reaction process is reasonably controlled to be carried out mildly.
And then, mixing the liquid-phase product with the materials which do not participate in the reaction, discharging the mixed liquid-phase product and the materials which do not participate in the reaction from the bottom of the reaction tube along with reaction tail gas, and allowing the mixed liquid-phase product and the materials to enter a subsequent product refining unit and a tail gas recovery unit through N3 and N4 ports of a lower tube box of the reactor, wherein the unreacted hydrogen and the liquid-phase materials are purified and discharged and then return to the system for reuse.
The content of the present invention is not limited to the examples, and any equivalent transformation adopted by the technical solution of the present invention is covered by the claims of the present invention by those skilled in the art through reading the present invention.
Claims (9)
1. A gas, liquid, solid three-phase hydrogenation reaction system, its characterized in that:
the system comprises a trickle bed reactor (R), the trickle bed reactor (R) comprises a lower tube box (1), a shell side cylinder (2) and an upper tube box (4) from bottom to top, a tube bundle (3) is arranged in the shell side cylinder (2), and a catalyst is filled in a reaction tube of the tube bundle (3);
a liquid phase material inlet (N1) is arranged at the top of the upper channel box (4), and a liquid distributor (5) is arranged below the liquid phase material inlet (N1); the liquid distributor (5) comprises a liquid disc (5-1) and a trickle component arranged on the liquid disc, the bottom of the trickle component extends into a reaction tube of a tube bundle (3) in the shell-side cylinder (2), and liquid entering from a liquid-phase material inlet (N1) is guided to the reaction tube point to point; the bottom of the lower tube box (1) is provided with a liquid-phase product outlet (N3);
a hydrogen inlet (N2) is arranged on the side wall of the upper channel box (4), and hydrogen is introduced into the upper channel box (4) and enters the reaction tubes of the tube bundle (3) through a gas phase distributor (6); the side wall of the lower tube box (1) is provided with an exhaust gas outlet (N4).
2. The gas, liquid and solid three-phase hydrogenation reaction system of claim 1, wherein:
the system also comprises a heat exchange medium buffer tank (V) and a cooler (E);
an upper ring road (7) and a lower ring road (8) are arranged on the outer wall of the shell pass cylinder (2) of the trickle bed reactor (R), and an opening is arranged on the outer wall of the corresponding shell pass cylinder (2);
go up circuit (7) and insert cooler (E), cooler (E) inserts heat transfer medium buffer tank (V), and heat transfer medium buffer tank (V) connect back down circuit (8), sets up circulating pump (P) between lower circuit (8) and heat transfer medium buffer tank (V).
3. The gas, liquid and solid three-phase hydrogenation reaction system of claim 2, wherein:
a weir cylinder (5-2) is arranged on the periphery of a liquid disc (5-1) of the liquid distributor (5);
the dripping component of the liquid distributor (5) comprises a dripping pipe (5-3), a nozzle (5-4) and a conduit (5-5) from top to bottom, wherein the dripping pipe (5-3) is inserted into the nozzle (5-4) and is positioned above the liquid disc (5-1), the nozzle (5-4) is connected into the conduit (5-5) below the liquid disc (5-1), and the conduit (5-5) extends into a reaction tube of the tube bundle (3) in the shell side cylinder (2).
4. The gas, liquid and solid three-phase hydrogenation reaction system of claim 3, wherein:
the liquid phase material inlet (N1) is connected with an inward extending connecting pipe downwards, the connecting pipe is installed under liquid and the bottom of the connecting pipe is blocked, and a circumferential lateral hole is formed.
5. The gas, liquid and solid three-phase hydrogenation reaction system of claim 4, wherein:
lateral holes are formed in a dropper (5-3) of the liquid distributor (5), and liquid enters the drip assembly through the lateral holes of the dropper (5-3) and then is guided to the reaction tubes of the tube bundle (3).
6. The gas, liquid and solid three-phase hydrogenation reaction system of claim 5, wherein:
the liquid distributor (5) comprises A, B type two-type drip components; the A-type drip component is arranged at the position of a non-temperature-measuring point; the B-type drip assembly is arranged at the position of the temperature measuring point, the diameter of the B-type drip assembly is 5-10 mm larger than that of the A-type drip assembly, and the temperature measuring sleeve penetrates through the B-type drip assembly in a centering mode and goes deep into the deep part of the reaction tube.
7. The gas, liquid and solid three-phase hydrogenation reaction system of claim 6, wherein:
the gas phase distributor (6) comprises a ring pipe and branch pipes, and the branch pipes are uniformly arranged along the circumferential direction.
8. The gas, liquid and solid three-phase hydrogenation reaction system of claim 7, wherein:
the upper loop (7) is provided with a heat exchange medium outlet (N6), and the cooler (E) is connected with the upper loop (7) through the heat exchange medium outlet (N6);
the lower loop (8) is provided with a heat exchange medium inlet (N5), and the heat exchange medium buffer tank (V) is connected with the lower loop (8) through the heat exchange medium inlet (N5) by a circulating pump (P).
9. The gas, liquid and solid three-phase hydrogenation reaction system of claim 8, wherein:
the upper tube box (4) is provided with a top gas phase temperature measuring port (T1), a heat exchange medium temperature measuring port, a catalyst temperature measuring port and a top gas phase pressure measuring port (P1), and the lower tube box (1) is provided with a bottom gas phase temperature measuring port (T2) and a bottom gas phase pressure measuring port (P2).
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| CN110787740A (en) * | 2019-11-08 | 2020-02-14 | 西安航天华威化工生物工程有限公司 | Gas, liquid and solid three-phase hydrogenation reaction system |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110787740A (en) * | 2019-11-08 | 2020-02-14 | 西安航天华威化工生物工程有限公司 | Gas, liquid and solid three-phase hydrogenation reaction system |
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