CN108940132B - Fixed bed reactor - Google Patents

Fixed bed reactor Download PDF

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CN108940132B
CN108940132B CN201810765655.6A CN201810765655A CN108940132B CN 108940132 B CN108940132 B CN 108940132B CN 201810765655 A CN201810765655 A CN 201810765655A CN 108940132 B CN108940132 B CN 108940132B
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cooling
heating medium
reaction
fixed bed
bed reactor
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CN108940132A (en
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涂维峰
时彦玲
韩一帆
王仁铨
窦竞
陈高翔
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Zhengzhou University
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Zhengzhou University
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
    • B01J8/067—Heating or cooling the reactor
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/50—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon dioxide with hydrogen

Abstract

A fixed bed reactor is provided. The fixed bed reactor comprises a shell and an inner cavity enclosed by the shell; the fixed bed reactor comprises a preheating section and a reaction section which are sequentially arranged along the flowing direction of reactants, wherein the preheating section comprises a reactant inlet, a first heat exchange medium inlet and a first heat exchange medium outlet which are arranged on the shell, and a preheating pipe set which is communicated with the reactant inlet and is used for conveying the reactants to the reaction section; the reaction section comprises an upper tube plate, a lower tube plate and a reaction unit which are arranged in the inner cavity, and a second heat exchange medium inlet and a second heat exchange medium outlet which are arranged on the shell, wherein the reaction unit is arranged between the upper tube plate and the lower tube plate; the upper tube plate comprises an upper plate body which is in sealing joint with the inner wall of the shell and a first through hole which is formed on the upper plate body and is used for the reaction tube to pass through; the lower tube plate includes a lower plate body sealingly engaged with an inner wall of the shell and a second through-hole formed in the upper plate body and through which the reaction tube passes.

Description

Fixed bed reactor
Technical Field
The invention relates to the technical field of chemical reactors, in particular to a tubular fixed bed reactor.
Background
The fixed bed reactor is a common chemical reactor form, and means that a granular solid catalyst or a solid reactant is filled in the reactor to form a stacked bed layer with a certain height, and a gas or liquid material flows through a static fixed bed layer through a granular gap and simultaneously realizes a heterogeneous reaction process. The reactor is characterized in that solid particles filled in the reactor are fixed, and the reactor is different from a moving bed and a fluidized bed in which solid materials move in the reactor, and is also called a packed bed reactor. Fixed bed reactors are widely used in gas-solid phase reactions and liquid-solid phase reaction processes, for example, fixed semi-aqueous gas generators in the ammonia synthesis industry, fixed bed ion exchange columns in water treatment, and the like.
The prior fixed bed reactor has the following problems to be solved: the catalyst has large dosage, low utilization rate and high cost; reaction heat is difficult to recover, and comprehensive energy efficiency is low; the reaction tube axially and radially forms a larger reaction temperature gradient, and a catalyst bed layer generates local overheating coking, so that the utilization rate of the catalyst is reduced; difficult reaction amplification, need to amplify step by step and carry out a circulation test, difficult realization of production capacity expansion and the like.
Disclosure of Invention
In view of the deficiencies in the prior art, it is an object of the present invention to address one or more of the problems in the prior art as set forth above. For example, it is an object of the present invention to provide a fixed bed reactor which avoids the scaling-up effect of laboratory to industrial scale.
In order to achieve the above object, the present invention provides a fixed bed reactor, comprising a housing and an inner cavity enclosed by the housing, the fixed bed reactor comprising a preheating section and a reaction section sequentially arranged along a flow direction of a reactant, wherein the preheating section comprises a reactant inlet, a first cooling/heating medium inlet and a first cooling/heating medium outlet arranged on the housing, and a preheating pipe set communicated with the reactant inlet to deliver the reactant to the reaction section; the reaction section comprises an upper tube plate, a lower tube plate, a reaction unit, a second cooling/heating medium inlet and a second cooling/heating medium outlet, wherein the upper tube plate, the lower tube plate and the reaction unit are arranged in the inner cavity, the second cooling/heating medium inlet and the second cooling/heating medium outlet are arranged on the shell, the reaction unit is arranged between the upper tube plate and the lower tube plate, and comprises reaction tubes and catalysts filled in the reaction tubes; the upper tube plate comprises an upper plate body which is in sealing joint with the inner wall of the shell and a first through hole which is formed on the upper plate body and is used for the reaction tube to pass through; the lower tube plate includes a lower plate body sealingly engaged with an inner wall of the shell and a second through-hole formed on the lower plate body and through which the reaction tube passes.
According to an exemplary embodiment of the present invention, the first cooling/heating medium inlet may communicate with the second cooling/heating medium outlet, and the first cooling/heating medium outlet may communicate with the second cooling/heating medium inlet.
According to an exemplary embodiment of the present invention, the second cooling/heating medium inlet may be adjacent to the lower tube sheet, and the second cooling/heating medium outlet may be adjacent to the upper tube sheet; the first cooling/heating medium inlet may be adjacent the upper tube sheet and the first cooling/heating medium outlet may be adjacent the reactant inlet.
According to an exemplary embodiment of the present invention, the preheating tube set may include a plurality of preheating winding tubes, and the preheating section may further include a distributor and a first header disposed in the inner cavity, wherein the distributor is in communication with the reactant inlet and may include a plurality of reactant outlets; the first header may include a cover plate, an outer edge of which may be in sealing engagement with an inner wall of the case, and a boss, which may protrude from a middle portion of the cover plate; one end of each of the preheating winding pipes may be communicated with the plurality of reactant outlets, and the other end of each of the preheating winding pipes may be communicated with the boss.
According to an exemplary embodiment of the present invention, the fixed bed reactor may further include a regenerative section disposed downstream of the reaction section in the flow direction of the reactant, and the regenerative section may include a reaction product outlet, a third cooling/heating medium inlet, and a third cooling/heating medium outlet disposed on the housing, and a regenerative tube bank disposed in the inner cavity and communicating with the third cooling/heating medium inlet and the third cooling/heating medium outlet.
According to an exemplary embodiment of the present invention, the first cooling/heating medium outlet may communicate with the third cooling/heating medium inlet, and the first cooling/heating medium inlet may communicate with the third cooling/heating medium outlet.
According to an exemplary embodiment of the present invention, the third cooling/heating medium inlet may be close to the reaction product outlet, and the third cooling/heating medium outlet may be close to the lower tube sheet.
According to an exemplary embodiment of the present invention, the regenerative tube bank may include a plurality of regenerative coils, and the regenerative section further includes a second header disposed between the third cooling/heating medium outlet and one end of the plurality of regenerative coils and a third header disposed between the third cooling/heating medium inlet and the other end of the plurality of regenerative coils.
According to an exemplary embodiment of the present invention, the reaction unit may further include a baffle plate disposed between the second cooling/heating medium inlet and the second cooling/heating medium outlet.
According to an exemplary embodiment of the present invention, the baffle plate may include a baffle body and a third through-hole formed on the baffle body and through which the reaction tube passes, an opening through which the cooling/heating medium passes being formed between a portion of the baffle body and the shell, and the remaining portion of the baffle body being sealingly engaged with the shell.
According to an exemplary embodiment of the present invention, the openings of two adjacent baffles of the plurality of baffles through which the cooling/heating medium passes may be staggered with respect to each other, preferably symmetrical with respect to each other.
According to an exemplary embodiment of the present invention, the number of the reaction tubes may be 20 to 100000, the inner diameter of the reaction tube may be 15 to 20mm, the length may be 200 to 2000mm, and the filling height of the catalyst in the reaction tube may be 60 to 1500 mm.
According to an exemplary embodiment of the present invention, the reaction unit may further include inert quartz sand particles filled above and below the catalyst in the reaction tube.
According to an exemplary embodiment of the present invention, the filling height of the inert quartz sand particles may be 70 to 500 mm.
According to an exemplary embodiment of the present invention, the fixed bed reactor may further comprise a reaction starting heat source bypass provided between the first cooling/heating medium inlet and the second cooling/heating medium outlet and/or the third cooling/heating medium outlet.
According to an exemplary embodiment of the present invention, a fixed bed reactor may be used as the CO2A reactor for preparing olefin by hydrogenation. The reactants may be gas phase reactants or liquid phase reactants.
According to an exemplary embodiment of the present invention, the cooling/heating medium may be distilled water or inorganic silicone oil.
Compared with the prior art, the beneficial technical effect of this application includes: avoidance of CO2The scale-up effect of hydrogenation reaction from laboratory to industrial production is easy to produce and expand energy; the temperature in the reactor is uniform, and the temperature of the catalyst is easy to control; the heat generated by the reaction is effectively recycled and utilized, the temperature required by the reaction is maintained, and the energy-saving effect is good; the reaction unit that easily dismouting was changed became invalid, and the maintenance cost is low.
Drawings
These and/or other aspects will become apparent and more readily appreciated from the following description of the exemplary embodiments, taken in conjunction with the accompanying drawings of which:
FIG. 1 is a schematic diagram of a fixed bed reactor according to an exemplary embodiment of the present invention;
FIG. 2 is a view of the internal structure of the fixed bed reactor shown in FIG. 1 according to an exemplary embodiment of the present invention;
FIG. 3 is a schematic view of the upper tube sheet of FIG. 2; and
FIG. 4 is a schematic view of the baffle of FIG. 2.
Description of reference numerals:
10-preheating section, 11-reaction gas inlet, 12-first cooling/heating medium inlet, 13-first cooling/heating medium outlet, 14-preheating tube set, 15-distributor, 16-first header, 16 a-cover plate, 16 b-bulge, 20-reaction section, 21-upper tube plate, 22-lower tube plate, 23-reaction unit, 24-second cooling/heating medium inlet, 25-second cooling/heating medium outlet, 26-baffle plate, 30-heat recovery section, 31-reaction product outlet, 32-third cooling/heating medium inlet, 33-third cooling/heating medium outlet, 34-heat recovery coil, 35-second header, 36-third header, 36-heat recovery section, 40-reaction start heat source bypass and 50-circulation pump.
Detailed Description
Embodiments of the present invention will now be described more fully with reference to the accompanying drawings, in which exemplary embodiments of the invention are shown. This invention may, however, be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the concept of the embodiments of the invention to those skilled in the art.
In the following description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the various exemplary embodiments. It may be evident, however, that the various exemplary embodiments may be practiced without these specific details or with one or more equivalent arrangements.
Furthermore, relative terms, such as "lower" or "bottom" and "upper" or "top," may be used herein to describe one element's relationship to another (other) element as illustrated in the figures. It will be understood that relative terms are intended to encompass different orientations of the device in addition to the orientation depicted in the figures. For example, if the device in one of the figures is turned over, elements described as being on the "lower" side of other elements would then be oriented on "upper" sides of the other elements. Thus, the exemplary term "lower" can encompass both an orientation of "lower" and "upper," depending on the particular orientation of the figure. Likewise, if the device in one of the figures is turned over, elements described as "below" or "beneath" other elements would then be oriented "above" the other elements. Thus, the exemplary terms "below … …" or "below … …" can encompass both an orientation of above and below.
CO2The direct hydrogenation for preparing low-carbon olefin is to reduce CO2Emission and CO2One of the important ways of recycling. CO 22The reactor for directly preparing olefin by hydrogenation needs to meet various basic conditions for stable and efficient operation of the catalyst. For example, heat needs to be supplied to reach the starting temperature of the reaction, and the heat released by the reaction needs to be removed in time, so that the reaction is always operated in the optimal temperature range, the energy consumption of production is reduced, and CO is increased2The catalyst for preparing low-carbon olefin by direct hydrogenation has the advantages of catalytic effect and service life, thereby obtaining stable and high-efficiency olefin yield.
In the actual production operation, in order to remove the heat released by the reaction in time, various synthesis tower internals are designed, such as direct cooling by arranging cold shock gas or indirect cooling by arranging cooling pipes, or different catalyst bed layer filling modes are designed to change the direction of reaction gas flow, such as axial flow, radial flow, axial-radial flow and the like. However, existing fixed bed reactors are used for CO2The problems of difficult recovery of reaction heat, low comprehensive energy efficiency and the like still exist in the preparation of olefin by hydrogenation, and in addition, CO2The preparation of olefins by hydrogenation is still in the laboratory research stage, aiming at CO2The industrial reactor for preparing olefin by hydrogenation has not been reported, and the industrial reaction is difficult to amplify and needs to be amplified step by stepAnd the cyclic test is adopted, and the production capacity expansion is not easy to realize.
Exemplary embodiments of the present disclosure disclose a shell and tube fixed bed coil regenerative cycle reactor for CO2And H2The olefin is directly synthesized by a one-step method. The reactor comprises a tubular fixed bed reaction tube unit, an upper tube plate, a lower tube plate, a preheating winding tube, a header, a reaction starting heat source inlet, a reaction starting heat source outlet and the like. The tubular fixed bed reaction tube unit is filled with a catalyst required by reaction, is the largest reactor unit under a small test strip condition in a laboratory, and can be combined into a reactor with the capacity required by industrial production by a plurality of reactor unit arrays; the heat generated by the reaction is utilized to preheat the reaction medium by adopting a sectional heat return and preheating circulation mode so as to reach the optimal reaction temperature.
Hereinafter, embodiments of the invention will be described with reference to the drawings.
FIG. 1 is a schematic diagram of a fixed bed reactor according to an exemplary embodiment of the present invention. Fig. 2 is a view illustrating an internal structure of a fixed bed reactor according to an exemplary embodiment of the present invention shown in fig. 1. Fig. 3 is a schematic view of the upper tube plate 21 in fig. 2. Fig. 4 is a schematic view of the baffle 26 of fig. 2.
Referring to FIGS. 1 and 2, with CO2The fixed bed reactor for directly preparing olefin by hydrogenation comprises a shell and an inner cavity surrounded by the shell. The fixed bed reactor includes a preheating section 10, a reaction section 20, and a reheating section 30, which are sequentially disposed along a flow direction of reaction gas.
In an embodiment, the preheating section 10 may include a reactant inlet (e.g., a reaction gas inlet) 11, a first cooling/heating medium inlet 12, and a first cooling/heating medium outlet 13 provided on the housing, and a preheating pipe set 14 communicating with the reaction gas inlet 11 to send the reaction gas to the reaction section 20.
The preheat tube bank 14 may include one or more preheat coils, among other things. In fig. 2, only two pre-heat coils are shown, but the disclosure is not limited thereto, and the number of the pre-heat coils may be two or more. Each preheating winding pipe can be arranged in the preheating section in a spiral mode so as to strengthen the heat exchange process between the preheating winding pipe and the shell side fluid.
In an alternative embodiment, when the number of pre-heating coils is multiple, the pre-heating section 10 may further include a distributor 15 and a first header 16 disposed in the inner cavity.
Wherein the distributor 15 may be disposed between the reaction gas inlet 11 and the preheating pipe group 14, and the distributor 15 is communicated with the reaction gas inlet 11 and includes a plurality of reaction gas outlets, i.e., has a "one-in-many-out" structure, to distribute the reaction gas fed from the reaction gas inlet 11 to a plurality of preheating winding pipes.
Since the temperature of the gas flowing out of each preheating tube may be different, it is necessary to mix the gas flowing out of the respective preheating tubes again. In an alternative embodiment, a first header 16 having a "confluent" configuration may be disposed between the preheat tube bank 14 and the reaction section 20 to collect the reactant gases in the plurality of preheat coils and deliver them to the reaction section 20. In an embodiment, as shown in fig. 2, first header 16 may have a cover plate 16a and a boss 16b, an outer edge of cover plate 16a being in sealing engagement with an inner wall of the housing, boss 16b projecting upward from a middle portion of cover plate 16a to form a boss.
One end of the preheating winding pipe is communicated with the reaction gas outlet of the distributor 15, and the other end of the preheating winding pipe is communicated with the boss 16b of the first header 16.
In an embodiment, the reaction section 20 may include an upper tube plate 21, a lower tube plate 22, a reaction unit 23 disposed in the inner cavity, and a second cooling/heating medium inlet 24 and a second cooling/heating medium outlet 25 disposed on the shell.
Wherein, the reaction unit 23 (i.e. tubular fixed bed reactor unit) is arranged between the upper tube plate 21 and the lower tube plate 22. The reaction unit 23 includes one or more reaction tubes and a catalyst filled in the reaction tubes.
As shown in fig. 3, the upper tube sheet 21 may include an upper plate body sealingly engaged with the inner wall of the shell and a plurality of first through-holes formed in the upper plate body and through which a plurality of reaction tubes pass. The lower tube sheet 22 may include a lower plate body sealingly engaged with the inner wall of the shell and a plurality of second through-holes formed on the lower plate body and through which the plurality of reaction tubes pass, corresponding to the plurality of first through-holes. In the present embodiment, the fixed reactor is cylindrical, and thus, the sectional shapes of the upper tube plate 21 and the lower tube plate 22 are circular, but the disclosure is not limited thereto, and the shapes of the upper tube plate 21 and the lower tube plate 22 may vary according to the shape of the inner cavity of the fixed reactor, i.e., the upper tube plate 21 and the lower tube plate 22 may have other shapes matching the shape of the inner cavity of the fixed reactor.
The plurality of reaction tubes pass through the plurality of first through holes and the plurality of second through holes, respectively, and are fixed between the tube plate 21 and the lower tube plate 22. In an embodiment, one end of each of the plurality of reaction tubes passes through one of the plurality of first through holes and is in sealing engagement with the upper plate body, and the other end passes through a second through hole of the plurality of second through holes corresponding to the one first through hole through which the one end passes and is in sealing engagement with the lower plate body.
Each reaction tube in the reaction unit 23 is directly used as a reaction minimum unit after being filled with a catalyst for reaction, that is, each reaction tube can be used as a maximum reactor for a laboratory bench. When a step-by-step amplification and a circulation test are needed, in order to realize production energy expansion, a plurality of reaction tubes can be stacked in parallel, namely a plurality of reaction tubes are arrayed to form a reactor with the required capacity. The array tube type reaction unit is convenient to disassemble, assemble and replace, the amplification effect generated in the process from a laboratory to a pilot plant test is avoided, and the direct transition from the laboratory to the industrial production stage can be realized. The reaction tube can be made into a standard part, so that the reaction capacity expansion, the overhaul, the replacement and the like are convenient.
The cross section in fig. 2 shows only 14 reaction tubes, but the number of reaction tubes is not limited thereto. For example, 20 to 100000 reaction tubes can be arranged in the array tube type reaction unit, the inner diameter of each reaction tube can be 15 to 20mm, the length can be 200 to 2000mm, and the olefin yield can be 0.01 to 100 kilotons per year. The filling height of the catalyst in the reaction tube can be 60-1500 mm, and inert quartz sand particles of 70-500 mm can be filled above and below the catalyst to fix the position of a catalyst bed layer. That is, the catalyst is filled in the middle of the reaction tube, and the inert quartz sand particles for fixing the catalyst position are filled in the two ends of the reaction tube.
In an alternative embodiment, the reaction section 20 may further comprise a baffle 26 between the second cooling/heating medium inlet 24 and the second cooling/heating medium outlet 25. As shown in fig. 4, the baffle plate 26 includes a baffle body and a plurality of third through-holes formed in the baffle body for the passage of a plurality of reaction tubes, an opening for the passage of a cooling/heating medium is formed between a portion of the baffle body and the shell, and the remaining portion of the baffle body is sealingly engaged with the shell. In the present embodiment, the stationary reactor is cylindrical, and therefore, the cross-sectional shape of the baffle plate 26 is a circular shape with a notch, but the disclosure is not limited thereto, and the shape of the baffle plate 26 may vary according to the shape of the inner cavity of the stationary reactor. In fig. 2, four baffles 26 are shown, but the present disclosure is not limited thereto, and the number of baffles 26 may be selected according to actual needs. Wherein the openings of two adjacent baffles of the plurality of baffles through which the cooling/heating medium passes are staggered, preferably symmetrical to each other. For example, as shown in fig. 4, the openings of the baffles 26 through which the cooling/heating medium passes may be provided on the left side, and the openings of the upper and lower baffles adjacent thereto through which the cooling/heating medium passes may be provided on the right side.
The recuperator 30 includes a reaction product outlet 31, a third cooling/heating medium inlet 32, and a third cooling/heating medium outlet 33 disposed on the housing, and a recuperator tube bank disposed in the interior chamber and in communication with the third cooling/heating medium inlet and the third cooling/heating medium outlet.
The regenerative coil pack includes one or more regenerative coils 34. The regenerative coil may employ serpentine coils to increase the tube side in the regenerative section 30 to enhance the heat exchange process between the regenerative coil and the shell side fluid, but the disclosure is not limited thereto.
In an alternative embodiment, when the regenerative tube bank includes a plurality of regenerative coils 34, a second header 35 and a third header 36 may also be provided. A second header 35 is disposed between the third cooling/heating medium outlet 33 and one end of the plurality of regenerative coils 34 to collect the gas flowing from the plurality of regenerative coils 34. A third header 36 is disposed between the third cooling/heating medium inlet 32 and the other end of the plurality of regenerative coils 34 to split the flow of cooling/heating medium introduced from the third cooling/heating medium inlet 32 to the plurality of regenerative coils 34.
As shown in fig. 1 and 2, in order to achieve the recycling of the exothermic heat of reaction and to maintain the catalyst bed at the optimum operating temperature, the first cooling/heating medium inlet 12 may be communicated with the second cooling/heating medium outlet 25 and/or the third cooling/heating medium outlet 33, and the first cooling/heating medium outlet 13 may be communicated with the second cooling/heating medium inlet 24 and/or the third cooling/heating medium inlet 32. The fixed bed reactor may further comprise a circulation pump 50 arranged between the first cooling/heating medium outlet 13 and the second cooling/heating medium inlet 24 and/or the third cooling/heating medium inlet 32.
To improve the heat exchange effect, in the embodiment, the second cooling/heating medium inlet 24 is close to the lower tube sheet 22, and the second cooling/heating medium outlet 25 is close to the upper tube sheet 21. The first cooling/heating medium inlet 12 is close to the upper tube sheet 21, and the first cooling/heating medium outlet 13 is close to the reaction gas inlet 11. The third cooling/heating medium inlet 32 is adjacent to the reaction product outlet 31 and the third cooling/heating medium outlet 33 is adjacent to the lower tube sheet 22.
In addition, the fixed bed reactor may further include a reaction-starting heat source bypass 40 provided between the first cooling/heating medium inlet 12 and the second cooling/heating medium outlet 25 and/or the first cooling/heating medium inlet 12 and the third cooling/heating medium outlet 33 for providing heat during the start-up of the fixed bed reactor. The reaction-starting heat source bypass 40 may include a heat source device such as a steam boiler, a hot water boiler, or the like.
The use of a fixed reactor according to the disclosed embodiments is described below with reference to the accompanying drawings:
in the preheating section 10, the reaction gas introduced from the reaction gas inlet 11 flows through the distributor 15, the preheating tube group 14 and the first header 16, absorbs heat of the heating medium to reach a reaction start temperature, and then enters the reaction section 20. Wherein the heating medium enters from the bottom of the preheating section 10 through the first cooling/heating medium inlet 12, flows through the area between the preheating coil and the housing, and then flows out through the first cooling/heating medium outlet 13.
In the reaction section 20, the reaction gas passes through the tubular reaction unit 23 from top to bottom, and the catalyst bed layer flowing through the reaction tube participates in the reaction. Wherein the cooling medium enters from the second cooling/heating medium inlet 24, flows through the region between the reaction tube and the shell of the reaction section 20, carries the heat generated by the reaction out of the array tube type reaction unit 23, and then flows out through the second cooling/heating medium outlet 25.
In the regenerative section 30, the reaction product and part of the unreacted reactant flow out of the reaction tubes, and flow out of the reactor from the reaction product outlet after passing through the outer wall of the regenerative tube set from top to bottom. Wherein, the cooling medium is brought out of the reactor after the reaction heat release is recovered through a third cooling/heating medium inlet 32, a third header 36, a regenerative coil 34, a second header 35 and a third cooling/heating medium outlet 33.
In the present embodiment, the heating medium flowing out of the first cooling/heating medium outlet 13 is used as the cooling medium for the reaction section 20 and the regenerative section 30. And the cooling flowing out from the second cooling/heating medium outlet 25 and the third cooling/heating medium outlet 33 is directly returned to be used as the heating medium of the preheating section 10, so that the heat generated by the reaction is effectively recovered and utilized, and the catalyst bed layer is kept at the optimal operation temperature.
The cooling/heating medium can also be called as a heat exchange medium or a heat transfer medium, and can comprise distilled water (6.5-9.4 MPa), inorganic silicone oil and the like.
Fixed bed reactor according to the example: 1) a plurality of reaction tubes are adopted for parallel superposition. The reaction unit tube (reaction tube 23) is filled with the catalyst for reaction and then directly used as the minimum reaction unit, so that the reaction unit tube is convenient to disassemble, assemble and replace during actual production, the amplification effect generated from a laboratory to a pilot plant test process is avoided, and the direct transition from the laboratory to an industrial production stage is realized; 2) heat backflow is realized, and energy conservation and high efficiency are realized; 3) the heat exchange tube pass of the upper part and the lower part of the reactor adopts a flow winding tube (such as a spiral tube, a coiled tube and the like), so that the heat exchange process between the reaction tube and the shell pass fluid is enhanced.
The disclosed fixed bed reactor will be further described with reference to specific examples.
In the present example, to perform CO2Hydrogenation for preparing low-carbon olefin, designing and manufacturing column for annual production of tonnage olefinThe tubular fixed bed coil pipe backheating circulation reactor (namely a fixed bed reactor) is characterized in that 20 tubular fixed bed reaction tube units are arranged in a reaction section, the unit tubes are all of the same reaction tube size as that under laboratory single tube experimental conditions, the inner diameter is 18mm, the height of a catalyst bed layer is 60mm, and the upper end and the lower end of the catalyst bed layer are respectively filled with inert quartz sand (the particle size is 0.4-4 mm) with the thickness of 100 mm. The catalyst filled in the tubular fixed bed reaction tube unit was 9 g of iron zinc oxide catalyst (molar ratio 2: 1). The cooling/heating medium adopted in the reaction section, the heat return section and the preheating section is 7.44MPa of distilled water (the evaporation temperature is 290 ℃).
The process conditions are as follows: gas volume space velocity 30000h-1、CO2And H2The molar ratio is 1: 3, the reaction pressure is 1.5 MPa. CO 22The effect of hydrogenation to lower olefins is shown in Table 1.
TABLE 1 comparison of the effectiveness of laboratory single tubes with fixed bed reactors producing tonnage olefins annually
Figure BDA0001728969690000091
Figure BDA0001728969690000101
It can be seen that the disclosure realizes CO2Industrial reactor for preparing olefin by hydrogenation while keeping CO2The conversion rate and the olefin selectivity are based on, and the annual olefin yield is improved, for example, the annual olefin yield is improved from 55 kilograms to 2.50 tons.
In conclusion, the reactor with the capacity required by industrial production is formed by arranging the tubular reactors in the laboratory bench scale in an array manner, and CO is solved2Scale-up effects of hydrogenation from laboratory to industrial production; and the catalyst bed layer is kept at the optimal operation temperature by adopting sectional heat regeneration-preheating and recycling reaction heat release. However, the present disclosure is not limited thereto, and may be used as a reactor for other gas-solid reactions and liquid-solid reactions. CO can be avoided after the fixed bed reactor disclosed by the invention is adopted2Hydrogenation from the laboratory toThe scale amplification effect of industrial production is easy to produce and expand energy; the temperature in the reactor is uniform, and the temperature of the catalyst is easy to control; the heat generated by the reaction is effectively recycled and utilized, the temperature required by the reaction is maintained, and the energy-saving effect is good; the reaction unit that easily dismouting was changed became invalid, and the maintenance cost is low.
Although the present invention has been described above in connection with exemplary embodiments, it will be apparent to those skilled in the art that various modifications and changes may be made to the exemplary embodiments of the present invention without departing from the spirit and scope of the invention as defined in the appended claims.

Claims (8)

1. A fixed bed reactor comprises a shell and an inner cavity enclosed by the shell, and is characterized in that the fixed bed reactor comprises a preheating section and a reaction section which are sequentially arranged along the flowing direction of reactants, wherein,
the preheating section comprises a reactant inlet, a first cooling/heating medium inlet and a first cooling/heating medium outlet disposed on the housing, and a preheating tube bank in communication with the reactant inlet for delivering reactants to the reaction section, the preheating tube bank comprising a plurality of preheating coils, the preheating section further comprising a distributor and a first header disposed in the inner cavity, wherein,
the distributor is communicated with the reactant inlet and comprises a plurality of reactant outlets;
the first header comprises a cover plate and a bulge, the outer edge of the cover plate is in sealing joint with the inner wall of the shell, and the bulge protrudes upwards from the middle of the cover plate to form a bulge;
one end of each preheating winding pipe is communicated with the corresponding reactant outlet, and the other end of each preheating winding pipe is communicated with the corresponding lug boss;
the reaction section comprises an upper tube plate, a lower tube plate, a reaction unit, a second cooling/heating medium inlet and a second cooling/heating medium outlet which are arranged in the inner cavity, wherein,
the reaction unit is disposed between the upper tube plate and the lower tube plate, and includes reaction tubes and a catalyst filled in the reaction tubes;
the upper tube plate comprises an upper plate body which is in sealing joint with the inner wall of the shell and a first through hole which is formed on the upper plate body and is used for the reaction tube to pass through;
the lower tube plate comprises a lower plate body which is in sealing joint with the inner wall of the shell and a second through hole which is formed on the lower plate body and is used for the reaction tube to pass through;
the first cooling/heating medium inlet is in communication with the second cooling/heating medium outlet, and the first cooling/heating medium outlet is in communication with the second cooling/heating medium inlet.
2. The fixed bed reactor of claim 1, further comprising a recuperating section disposed downstream of the reaction section in a reactant flow direction, the recuperating section including a reaction product outlet, a third cooling/heating medium inlet, and a third cooling/heating medium outlet disposed on the housing, and a recuperating tube stack disposed in the inner cavity and in communication with the third cooling/heating medium inlet and the third cooling/heating medium outlet.
3. The fixed bed reactor of claim 2, wherein the first cooling/heating medium outlet communicates with the third cooling/heating medium inlet, and the first cooling/heating medium inlet communicates with the third cooling/heating medium outlet.
4. The fixed bed reactor of claim 2 wherein the set of recuperative coils comprises a plurality of recuperative coils,
the heat recovery section further comprises a second header and a third header, the second header is disposed between the third cooling/heating medium outlet and one end of the plurality of regenerative coils, and the third header is disposed between the third cooling/heating medium inlet and the other end of the plurality of regenerative coils.
5. The fixed bed reactor of claim 2, further comprising a reaction initiating heat source bypass disposed between the first cooling/heating medium inlet and the second cooling/heating medium outlet and/or the third cooling/heating medium outlet.
6. The fixed bed reactor of claim 1, wherein the reaction unit further comprises a baffle disposed between the second cooling/heating medium inlet and the second cooling/heating medium outlet.
7. The fixed bed reactor of claim 1, wherein the number of the reaction tubes is 20 to 100000, the reaction tubes have an inner diameter of 15 to 20mm and a length of 200 to 2000mm, and the packing height of the catalyst in the reaction tubes is 60 to 1500 mm.
8. The fixed bed reactor of any one of claims 1 to 7, characterized in that it is used as a CO reactor2A reactor for preparing olefin by hydrogenation.
CN201810765655.6A 2018-07-12 2018-07-12 Fixed bed reactor Active CN108940132B (en)

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CN110215882A (en) * 2019-06-25 2019-09-10 南京聚拓化工科技有限公司 Radial shaft is to hydrogenator
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