CN108114672B - Soaking type spiral plate fixed bed reactor for gas-solid catalytic reaction - Google Patents
Soaking type spiral plate fixed bed reactor for gas-solid catalytic reaction Download PDFInfo
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- 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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0465—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being concentric
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- 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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
- B01J8/0461—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds
- B01J8/0469—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical annular shaped beds the beds being superimposed one above the other
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- 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
- B01J8/04—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 the fluid passing successively through two or more beds
- B01J8/0496—Heating or cooling the reactor
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- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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Abstract
The invention relates to a soaking type spiral plate fixed bed reactor for gas-solid phase contact catalytic reaction, which comprises an inlet and an outlet of a gas phase and a heat exchange medium, wherein one or more spiral plate type fixed bed reaction sections are arranged in the reactor. The invention has the advantages that: 1) the shell-side heat exchange coefficient is obviously increased, so that the total heat transfer coefficient is increased, the heat transfer effect is enhanced, and the heat transfer temperature difference is reduced; 2) the heat transfer distance and the heat transfer area can be flexibly controlled, and the uniformity and the control of the temperature of the reaction bed layer are facilitated; 3) the volume utilization rate is high (the maximum can reach more than 70%, the maximum of the tubular reactors is about 40%), the capacity of a single set of equipment is high, and the occupied area and the investment are obviously reduced; 4) the heat exchange medium channel has a self-cleaning function and is not easy to produce dirt and block.
Description
Technical Field
The invention relates to a fixed bed reactor, in particular to a soaking type spiral plate fixed bed reactor for gas-solid catalytic reaction.
Background
Fixed bed catalytic reactors have found wide application in the chemical and petroleum industries.
The fixed bed reactor has the advantages that: the back mixing is small, the fluid can effectively contact with the catalyst, and higher selectivity can be obtained when the reaction is accompanied by series side reaction; the mechanical loss of the catalyst is small; and the structure is simple. The disadvantages are that: the shell side heat transfer effect is poor, and particularly for strong exothermic reaction, temperature runaway is easy to occur (the reaction temperature is out of control and rises rapidly and exceeds the allowable range); secondly, the catalyst can not be replaced in the operation process, the reaction that the catalyst needs to be frequently regenerated is generally not suitable for use, and the catalyst is often replaced by a fluidized bed reactor or a moving bed reactor.
Fixed bed reactors can be classified into adiabatic type, heat exchange type and self-heating type according to heat exchange mode. The heat-insulating fixed bed reactor and the self-heating fixed bed reactor are less applied in the actual industrial production, and the tubular fixed bed reactor in the heat exchange type fixed bed reactor is more widely and mature. It is used in strong exothermic reaction, and has yield sensitive to temperature and high conversion rate and high selectivity. The structure of the heat exchanger is similar to that of a shell-and-tube heat exchanger and comprises a tube bundle, a shell, two end sockets and the like. When the catalyst is applied to gas-solid catalytic reaction, catalyst particles are filled in the tube pass and are fixed by the bottom support piece, and the shell pass has a heat exchange medium flowing so as to exchange heat with the tube pass and maintain the stability of the reaction temperature of the tube pass.
Tube side structure of tubular fixed bed reactor is nimble, can be single tube, multitube parallelly connected, also can be U type pipe etc. compares with the fixed bed reactor of other forms, has: the radial heat transfer distance is small, so that the reaction heat can be transferred to the pipe wall in time, and the temperature of a catalyst bed layer can be accurately controlled; secondly, the advantages of easy realization in engineering and the like are provided by using the mature manufacturing technology of the tube type heat exchanger for reference. But there are: the shell side heat transfer coefficient is small, and the required heat transfer area is large; secondly, the space utilization rate of the catalyst bed layer is low, so that the reactor has the defects of large volume, high equipment manufacturing cost, difficult large-scale device and the like.
The spiral plate heat exchanger is a heat exchanger which is formed by coiling two parallel metal plates into two closed spiral channels and exchanges heat between cold and hot fluids through a spiral plate wall. The heat exchanger has the advantages of small volume, compact equipment, high heat transfer efficiency and low metal consumption, and is widely applied to the industries of chemical industry, petroleum, medicine, electric power and the like.
Disclosure of Invention
The invention provides a soaking type spiral plate fixed bed reactor for gas-solid phase contact catalytic reaction, aiming at solving the technical problems of poor shell-side heat transfer effect, low space utilization rate of a catalyst bed layer and difficult large-scale device of the existing tubular fixed bed reactor and referring to the structure and performance characteristics of a spiral plate heat exchanger.
The technical scheme of the invention is as follows:
a soaking type spiral plate fixed bed reactor for gas-solid phase catalytic reaction comprises an inlet and an outlet of a gas phase and a heat exchange medium, and one or more spiral plate type fixed bed reaction sections are arranged in the reactor. The structure of the reaction section of the spiral plate type fixed bed is similar to that of a spiral plate heat exchanger, two parallel metal plates are coiled into two spiral channels, the upper end and the lower end of one channel are closed to be used as a heat exchange medium channel, a heat exchange medium flows through the spiral channels and exchanges heat through the plate walls, and the heat exchange medium flows out from a heat exchange medium outlet connected with a central pipe after reaching the central pipe of the reactor; the upper end and the lower end of the other channel are not sealed, a fixed bed layer is formed after filling the catalyst, the uppermost end of the bed layer is communicated with a gas inlet, the lowermost end of the bed layer is communicated with a gas outlet, gas enters the reactor from the inlet, and is discharged from the gas outlet after axially passing through the catalyst fixed bed layer for reaction.
The spiral plate fixed bed reactor can be flexibly provided with one or more spiral plate reaction sections, and the specific number of the spiral plate reaction sections can be determined by the heat exchange area required by the reaction. Wherein, the gas channels of the multi-section spiral plate type reaction sections are connected in series in the axial direction, the gas passes through the catalyst fixed bed layer of each reaction section in sequence, and is discharged from the gas outlet after the reaction; the heat exchange medium channel of the multi-section spiral plate type reaction section can be provided with a heat exchange medium distribution device or a plurality of heat exchange medium inlets so as to realize that the heat exchange medium enters each spiral plate type reaction section in parallel in a multi-section mode, the heat exchange medium enters the central pipe in the center of the reactor in a spiral mode through the heat exchange medium channel and then flows out from the heat exchange medium outlet, the inlet and outlet temperature of the heat exchange medium of each spiral plate type reaction section is the same, and the uniformity and the control of the temperature of the reaction.
The space between the channels at the two sides of the spiral plate type reaction section can be flexibly designed. The channel spacing on one side of the heat exchange medium can be set according to the flow of the heat exchange medium, and the heat transfer coefficient is improved and the heat transfer effect is enhanced by increasing the flow speed of the heat exchange medium; the channel spacing on one side of the catalyst fixed bed layer is increased as much as possible on the premise of ensuring the heat exchange effect so as to improve the utilization rate of the volume of the reactor.
The gas inlet of the spiral plate fixed bed reactor is generally arranged at the top of the reactor, the outlet is generally arranged at the bottom of the reactor, which is beneficial to fixing the catalyst particles, but in some specific cases, the gas inlet can also be arranged at the bottom of the reactor, and the outlet is arranged at the top of the reactor.
When only one heat exchange medium inlet is needed in the spiral plate fixed bed reactor, the spiral plate fixed bed reactor can be arranged on one side of a flange at the top of the reactor, and an inlet pipe is inserted into the equipment and connected with a heat exchange medium distribution device; if a plurality of heat exchange medium inlets are needed, a heat exchange medium inlet can be arranged at each spiral plate type reaction section, and the plurality of inlets are arranged at the outer side of the reactor in parallel to realize segmented temperature control; the outlet is arranged at one side of the upper part of the reactor, and the outlet pipe is inserted into the reactor and connected with the central pipe. The heat exchange medium distribution device is an annular tube distributor arranged below the outlet pipe, and the annular tube distributor is communicated to each section of spiral plate type reaction section through a distribution pipe, so that the temperature and the flow rate of the heat exchange medium at the inlet of each reaction section are consistent; the outlet of the heat exchange medium in the reaction section is communicated with the central pipe, and the heat exchange medium is collected in the central pipe and flows out from the outlet of the heat exchange medium after heat exchange.
The bottom and the top of the spiral plate fixed bed reactor are both supported and sealed by inert magnetic balls.
The side wall annular gap of the spiral plate fixed bed reactor is also filled with inert magnetic balls to avoid local temperature runaway.
The manufacturing of the spiral plate fixed bed reactor is carried out by adopting a mode of single-section manufacturing and external assembly of the reaction section, the distributor and the distributor; when more than two sections are connected in parallel, grooves are reserved at the upper end and the lower end of the central pipe of the reaction section, and after the external assembly is finished, the welding mode of the internal central pipe has two modes: when the diameter of the central tube is smaller, an automatic welding rod can be adopted to deeply penetrate into the central tube for welding; if the diameter of the central pipe meets the condition of entering people, welding personnel can enter each reaction section through the central pipe to weld the internal central pipe, and the multiple sections of reaction sections form a whole. And after being connected with the top heat exchange medium distributor, the reactor is integrally hoisted and placed into the reactor for assembly, and the processing and manufacturing of the reactor are finished.
The top heat exchange medium distributor and the section exchange medium inlets of the spiral plate reactors can be connected by welding, threaded connection or pipe hoop connection.
The invention has the advantages that:
1) the shell-side heat exchange coefficient is obviously increased, so that the total heat transfer coefficient is increased, the heat transfer effect is enhanced, and the heat transfer temperature difference is reduced;
2) the heat transfer distance and the heat transfer area can be flexibly controlled, and the uniformity and the control of the temperature of the reaction bed layer are facilitated;
3) the volume utilization rate is high (the maximum can reach more than 70%, the maximum of the tubular reactors is about 40%), the capacity of a single set of equipment is high, and the occupied area and the investment are obviously reduced;
4) the heat exchange medium channel has a self-cleaning function and is not easy to produce dirt and block.
Drawings
Fig. 1 is a schematic structural view of the present invention, and fig. 2 is a top view of fig. 1.
Wherein: the heat exchange device comprises a heat exchange medium inlet 1, a heat exchange medium outlet 2, a gas inlet 3, a gas outlet 4, an annular tubular distributor 5, a liquid distribution pipe 6, a central pipe 7 and a spiral plate reaction section 8-N.
Fig. 3 is a schematic structural view of embodiment 1 of the present invention, and fig. 4 is a top view of fig. 3.
Wherein: the heat exchange device comprises a heat exchange medium inlet 1, a heat exchange medium outlet 2, a gas inlet 3, a gas outlet 4, an annular tubular distributor 5, a liquid distribution pipe 6, a central pipe 7 and spiral plate reaction sections 8-15.
Fig. 5 is a schematic structural view of embodiment 2 of the present invention, and fig. 6 is a top view of fig. 5.
Wherein: the heat exchange medium comprises a heat exchange medium outlet 1, a heat exchange medium inlet 2, a gas inlet 3, a gas outlet 4, a heat exchange medium inlet 5-1, a central tube 6-1 and a spiral plate reaction section 7-17.
Detailed Description
Example 1
15 ten thousand ton/year dimethyl oxalate (DMO) hydrogenation reactor
When the reactor is used as a 15 ten thousand ton/year DMO hydrogenation reactor, 8 spiral plate type reaction sections are required by accounting, and the structure of the reactor is shown in figures 3 and 4. The heat exchange medium inlet 1 is arranged on one side of the top of the reactor, and the outlet 2 is arranged on one side of the upper part of the reactor. Gas enters the reactor from a top gas inlet 3, passes through a catalyst fixed bed layer (8-15) to react, and then leaves the reactor together with a product from a bottom gas outlet 4; heat exchange media pass through an annular tubular distributor 5 at the top of the reactor, are distributed to inlets at the outer sides of spiral plate type reaction sections (08-15) by a plurality of distribution pipes 6 in proportion, are subjected to spiral heat exchange by a heat exchange medium channel, enter a central pipe 7 at the center of the reaction section, are collected and then flow out from a heat exchange medium outlet 2.
The performance indexes of a 15-ten-thousand-ton/year DMO hydrogenation reactor adopting the reactor disclosed by the invention and a tubular fixed bed reactor are compared and shown in table 1.
TABLE 1150 kt/aDMO reactor comparison
| Item | The invention relates to a fixed bed reactor | Tube array type fixed bed reactor |
| Equipment diameter (mm) | 3600 | 4000 |
| Height of catalyst bed (mm) | 8000 | 8000 |
| Catalyst loading (m)3) | 44 | 36 |
From the above table, it can be seen that the volumetric utilization of the catalyst beds of the two reactors are respectively: 54.06 percent and 35.83 percent, the loading of the catalyst is improved by more than 50 percent, the productivity of the device can be greatly improved, the diameter of the equipment is small, and the occupied area and the investment are small; meanwhile, the width of the heat exchange medium channel is controlled, the flow speed of the heat exchange medium is improved, the total heat transfer coefficient is increased, the heat transfer temperature difference is reduced, and the control of the temperature of the reaction bed layer is facilitated.
Example 2
3.5 ten thousand tons/year vinyl acetate synthesis reactor
When the reactor of the invention is used as a 3.5 ten thousand ton/year vinyl acetate synthesis reactor, 10 spiral plate type reaction sections are required by accounting, and the structure of the reactor is shown in figure 5 and figure 6. For further reinforcing heat transfer effect, each section spiral plate formula reaction section sets up one heat transfer medium, realizes segmentation accuse temperature, specifically is: the heat exchange medium inlets 2 and 5-1 (the medium temperature can be the same or different) are arranged at the lower part of the spiral plate type reaction section and are connected with the outer side of the heat exchange medium channel in the reaction section, the heat exchange medium channel carries out spiral heat exchange, and the heat exchange medium enters the central pipe 6-1 at the center of the reaction section and flows out from the heat exchange medium outlet 1 after being converged. Gas enters the reactor from a top gas inlet 3, passes through a catalyst fixed bed layer (7-17), reacts, and then leaves the reactor together with a product from a bottom gas outlet 4.
The performance indexes of a 3.5 ten thousand ton/year vinyl acetate synthesis reactor adopting the reactor of the invention and a tubular fixed bed reactor are compared and shown in table 2.
TABLE 23.5 Ten thousand ton/year vinyl acetate synthesis reactor comparison
| Item | The invention relates to a fixed bed reactor | Tube array type fixed bed reactor |
| Equipment diameter (mm) | 3800 | 4200 |
| Height of catalyst bed (mm) | 10000 | 10000 |
| Catalyst loading (m)3) | 61.5 | 49.6 |
From the above table, it can be seen that the volumetric utilization of the catalyst beds of the two reactors are respectively: 54.25 percent and 35.81 percent, the loading of the catalyst is improved by more than 50 percent, the capacity of the device can be greatly improved, the diameter of the device is small, and the occupied area and the investment are small; meanwhile, the width of the heat exchange medium channel is controlled, the flow speed of the heat exchange medium is improved, the total heat transfer coefficient is increased, the heat transfer temperature difference is reduced, and the control of the temperature of the reaction bed layer is facilitated.
Claims (4)
1. The utility model provides a soaking formula spiral plate fixed bed reactor of gas-solid phase contact catalytic reaction which characterized in that: comprises an inlet and an outlet of a gas phase and a heat exchange medium, and a plurality of spiral plate type fixed bed reaction sections are arranged in the reactor; each spiral plate type fixed bed reaction section is formed by coiling two parallel metal plates into two spiral channels, the upper end and the lower end of one channel are closed and used as heat exchange medium channels, heat exchange medium flows through the spiral channels and exchanges heat through the plate walls, and then flows out from a heat exchange medium outlet connected with the central tube after reaching the central tube in the center of the reactor; the upper end and the lower end of the other channel are not sealed, a fixed bed layer is formed after filling the catalyst, the uppermost end of the bed layer is communicated with a gas inlet, the lowermost end of the bed layer is communicated with a gas outlet, gas enters the reactor from the inlet, and is discharged from the gas outlet after axially passing through the catalyst fixed bed layer for reaction; the heat exchange medium channels of the plurality of spiral plate type fixed bed reaction sections are provided with the heat exchange medium distribution device, so that the heat exchange medium enters each spiral plate type fixed bed reaction section in a plurality of sections in parallel, enters the central pipe in the center of the reactor through the heat exchange medium channels and flows out from the heat exchange medium outlet, and the inlet and outlet temperatures of the heat exchange medium of each spiral plate type fixed bed reaction section are the same, thereby being beneficial to the uniformity and control of the temperature of the reaction bed layer; the heat exchange medium distribution device is connected with the heat exchange medium inlets of the reaction sections of the spiral plate type fixed bed through threads or pipe hoops; the heat exchange medium inlet of the spiral plate fixed bed reactor is arranged on one side of a flange at the top of the reactor, and the inlet pipe is inserted into the equipment and connected with the heat exchange medium distribution device; the outlet is arranged at one side of the upper part of the reactor, and the outlet pipe is inserted into the reactor and connected with the central pipe; the heat exchange medium distribution device is an annular tube distributor arranged below the outlet pipe, and the annular tube distributor is communicated to each section of the spiral plate type fixed bed reaction section through a distribution pipe so as to realize the consistency of the temperature and the flow of the heat exchange medium at the inlet of each reaction section; the gas channels of the reaction sections of the spiral plate type fixed bed are connected in series in the axial direction, the gas passes through the catalyst fixed bed layer of each reaction section in sequence, and the gas is discharged from a gas outlet after the reaction; the outlet of the heat exchange medium in the reaction section is communicated with the central pipe, and the heat exchange medium is collected in the central pipe and flows out from the outlet of the heat exchange medium after heat exchange.
2. A soaking spiral plate fixed bed reactor for gas-solid phase catalytic reaction according to claim 1, wherein: the number of reaction sections of the spiral plate type fixed bed is determined by the heat exchange area required by the reaction.
3. A soaking spiral plate fixed bed reactor for gas-solid phase catalytic reaction according to claim 1, wherein: the channel spacing on one side of the heat exchange medium is set according to the flow of the heat exchange medium.
4. A soaking spiral plate fixed bed reactor for gas-solid phase catalytic reaction according to claim 1, wherein: the gas inlet of the spiral plate fixed bed reactor is arranged at the top of the reactor, and the outlet of the spiral plate fixed bed reactor is arranged at the bottom of the reactor; or the gas inlet is arranged at the bottom of the reactor, and the outlet is arranged at the top of the reactor.
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| DE102018007737A1 (en) * | 2018-10-01 | 2020-04-02 | Hitachi Zosen Inova Etogas Gmbh | Fixed bed arrangement |
| CN109539555B (en) * | 2019-01-16 | 2024-09-10 | 深圳市睿碒科技有限公司 | Methanol catalytic heating equipment and heating method |
| CN109539556A (en) * | 2019-01-16 | 2019-03-29 | 佛山市无火发热新能源科技有限公司 | Methanol oxidation heating device and heating means |
| CN110201625A (en) * | 2019-07-09 | 2019-09-06 | 青岛科技大学 | A kind of contiguous segmentation feed auger tubular reactor for synthetic reaction |
| CN115947301B (en) * | 2023-01-09 | 2024-07-12 | 丽水学院 | Bionic spiral disc-shaped heat accumulating type gas-solid phase reactor |
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| JPS61118132A (en) * | 1984-11-14 | 1986-06-05 | Mitsubishi Petrochem Co Ltd | Catalytic reactor |
| JP2835851B2 (en) * | 1989-06-23 | 1998-12-14 | ヤマハ発動機株式会社 | Reformer for fuel cell |
| JP3052079B2 (en) * | 1998-11-20 | 2000-06-12 | 日本酸素株式会社 | Filling cylinder |
| JP4287608B2 (en) * | 2001-12-03 | 2009-07-01 | ソフタード工業株式会社 | Method for extracting spent catalyst in reaction tower |
| CN104162383A (en) * | 2013-05-17 | 2014-11-26 | 上海碧科清洁能源技术有限公司 | Sectionalized quenching fixed bed reactor and application method thereof |
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