CN201701922U - Catalytic reaction equipment - Google Patents
Catalytic reaction equipment Download PDFInfo
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- CN201701922U CN201701922U CN2010202346834U CN201020234683U CN201701922U CN 201701922 U CN201701922 U CN 201701922U CN 2010202346834 U CN2010202346834 U CN 2010202346834U CN 201020234683 U CN201020234683 U CN 201020234683U CN 201701922 U CN201701922 U CN 201701922U
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Abstract
The utility model relates to catalytic reaction equipment which mainly comprises a shell body 1, an upper plug 2 and a lower plug 3; the shell body 1 is connected with the upper plug 2 and the lower plug 3; the upper plug 2 is provide with a heat exchange medium outlet pipe 5 and a connecting pipe 4; the lower plug 3 is provided with a gas outlet pipe 7; the shell body 1 is provided with a heat exchange medium inlet pipe 8; a heat exchange outer pipe 10 which contains catalyst is connected with an upper pipe plate 11 and a lower pipe plate 12; and the utility model is used for methanol, hydrocarbon and other synthetic reaction processes as well as methane, ether and other synthetic processes, and provides a reactor which has the advantages of high production capacity, high catalytic activity, simple and reliable structure and good operation performance.
Description
Technical field
The utility model is a kind of consersion unit, be used for fluid catalytic reaction and diabatic process, belong to field of chemical engineering, be specially adapted to synthetic reaction process such as methyl alcohol, MAS, dimethyl ether, methane and hydro carbons, and be used for course of reaction and aforementioned exothermic reaction Chemical Manufacture and IGCC electric power joint processes such as methyl alcohol system hydro carbons, hydrogen sulfide oxidation system sulphur, carbon monodixe conversion, ethylene glycol and oxirane, also can be used for endothermic reaction process.
Background technology
For synthetic this class exothermic catalytic reactions such as, methyl ether synthetic by methyl alcohol under the pressurization, hydro carbons, along with the carrying out of course of reaction, the reaction heat of constantly emitting improves the catalyst layer temperature.In order to improve the efficient of reactor, need shift out reaction heat to reduce reaction temperature.In industrial reactor, once widely used as German Lurgi company be used for the synthetic shell and tube reactor of methyl alcohol, unstripped gas enters from the top air inlet and is distributed to each pipe, synthesizing methanol in pipe apparatus with catalyst inside layer, lateral inflow between pipe.Reaction heat is managed outer boiled water and is moved heat continuously, produces steam and is gone out by the side pipe, and reaction gas goes out tower by the bottom escape pipe, and this tower has a narrow range of temperature, but goes up lower perforated plate and the fixing welding of heat exchanger tube, need use two phase stainless steel and still fragile for solving thermal stress.
Task of the present utility model is the characteristics according to the catalytic exothermic reversible reaction, overcomes the shortcoming of prior art, provides a reliable in structure, production capacity is big, catalyst activity is high, the reactor of good operation performance.
The content of invention
The utility model provides a kind of catalytic reaction device, comprise housing 1, upper cover 2, low head 3, housing 1 and upper cover 2, low head 3 connects, the heat exchanger tube 10 of apparatus with catalyst inside 18 connects upper perforated plate 11 and lower perforated plate 12, mainly be that upper cover 2 has heat transferring medium outlet 5 and takes over 4, have in the upper cover 2 and go up interior end socket 23, end socket 23 connects and composes top inner chamber 24 with upper perforated plate 11 in going up, end socket 23 has the air inlet pipe 20 and the adapter 4 of upper cover 2 to link by airtight and watertight padding 26 activities in going up, perhaps air inlet pipe 20 with take over 4 and be connected by flexible pipe or expansion joint 22, lower perforated plate 12 is connected with low head 3, escape pipe 7 is arranged at low head 3 bottoms, housing 1 lower end has heat transferring medium inlet tube 8 to be communicated with heat transferring medium outlet 5 with heat exchanger tube 10 external spaces 9 through housing 1, end socket 19 in perhaps having down in the low head 3, lower perforated plate 12 connects and composes lower lumen 17 with down interior end socket 19, on the end socket 19 escape pipe 7 is arranged down, low head 3 has heat transferring medium inlet tube 8, is communicated with heat transferring medium outlet 5 with heat exchanger tube 10 external spaces 9 through housing 1.
The utility model provides a kind of catalytic reaction device, mainly be that upper cover 2 has heat transferring medium outlet 5, lower perforated plate 12 links with housing 1, there is heat transferring medium inlet tube 8 housing 1 lower end, low head 3 has escape pipe 7 and manhole 6, and there is porous top cover 13 on escape pipe 7 tops or the porous top cover 13 of connection pipe 15 is arranged.
The utility model provides a kind of catalytic reaction device, mainly be that end socket 19 connects and composes lower lumen 17 with lower perforated plate 12 in having down in the low head 3, escape pipe 7 is arranged at low head 3 bottoms, the connection pipe 15 usefulness fillers 14 of the porous top cover 13 of end socket 19 upper support Ceramic Balls and catalyst and escape pipe 7 movable sealings of low head 3 down, internals 40 by interior up and down end socket, heat exchanger tube, catalyst constitute are bearing on the low head 3 by down interior end socket 19 bottom supportings 16.
The utility model provides a kind of catalytic reaction device, mainly is upper cover 2 and directly welding or link and with lip weldering sealing by flange 30 on upper cover 2 and the housing 1 and bolt 31 nuts 32 of housing 1.
The utility model provides a kind of catalytic reaction device, mainly is upper thermal barrier catalyst layer 41 to be housed above the upper perforated plate 11 or adiabatic catalyst layer 42 is arranged at lower perforated plate 12 bottoms.
The utility model provides a kind of catalytic reaction device, the air inlet pipe 4 that mainly is the escape pipe 7 of this consersion unit 100 and housing 1 top of managing interior water-cooled reactor 200 is communicated with, the gas outlet 7 that responds of housing 1 bottom of reactor 200, heat exchange tube assemblies 34 is arranged in the housing 1,34 of housing 1 and heat exchange tube assemblies have catalyst layer 18, heat exchange tube assemblies 34 bottoms have heat transferring medium inlet tube 8 to pass housing 1 bottom (head), top has heat transferring medium outlet 5 to pass housing 1 top end socket by expansion joint or packing seal 26, the housing 1 top end socket of reactor 200 has manhole 16 to use for the dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst usefulness, and the heat transferring medium inlet tube 8 of the heat transferring medium inlet tube 8 of consersion unit 100 and outlet 5 and reactor 200 and outlet 5 and drum separately are connected.
The utility model provides a kind of catalytic reaction device, the air inlet 4 that mainly is the escape pipe 7 of this consersion unit 100 and housing 1 top of managing interior air cooling reactor 300 is communicated with, the gas outlet 7 that responds of housing 1 bottom of reactor 300, heat exchange tube assemblies 34 is arranged in the housing 1,34 of housing 1 and heat exchange tube assemblies have catalyst layer 18, heat exchange tube assemblies 34 bottoms have synthesis gas inlet tube 8 to pass housing 1 bottom (head), top has synthetic heat outlet pipe 5 to pass housing 1 top end socket by expansion joint or packing seal 26, housing 1 top end socket has manhole 16 to use for the dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst usefulness, and reactor 300 outlets 5 and consersion unit 100 inlet tubes 20 link.
The utility model provides a kind of catalytic reaction device, mainly be to be connected with water-cooled cross-current reactor 400 bottom inflow pipes 4 in the pipe with the escape pipe 7 of this consersion unit 100, the bottom is housed in the housing 1 of reactor 400 heat transferring medium inlet tube 8 is arranged, the heat exchange tube assemblies 34 of heat transferring medium outlet 5 is arranged at the top, the upper spacer 38 that the bottom has the lower clapboard 37 that is connected with housing 1 and top to be connected with housing 1 another side on one side, upper spacer 38 is connected with housing 1 with the porous gas distributor 39 on the left side and the porous gas gas collector 40 on the right respectively with lower clapboard 37, fills catalyst 18 at upper spacer 38 and lower clapboard 37 and left gas distributor 39 and right gas gas collector 40 and 10 of heat exchanger tubes.
The utility model provides a kind of catalytic reaction device, mainly be air inlet pipe 4 bindings of escape pipe 7 with the interior water-cooled radial reactor 500 of radial tubes of this consersion unit 100, in reactor 500 housings 1 heat exchange tube assemblies 34 is arranged, there is the porous gas distributor 22 of the porous plate 13 that connects supporting catalyst at heat exchange tube assemblies 34 centers, and 34 of housing 1 and heat exchange tube assemblies have the porous gas gatherer 23 that links with upper end open bottom and housing 1.
The utility model provides a kind of catalytic reaction device, mainly is two or is communicated with inlet manifold 50 more than each air inlet pipe 51,52 of two these catalytic reaction devices 101,102, and each escape pipe 71,72 is communicated with the house steward 70 that gives vent to anger, and constitutes many combinations in parallel.
Description of drawings
Specify below in conjunction with accompanying drawing.
Fig. 1 is the catalytic reaction device schematic diagram that an interior end socket is arranged.
Fig. 2 is the another kind of catalytic reaction device schematic diagram that an interior end socket is arranged.
Fig. 3 is the catalytic reaction device schematic diagram of end socket in having up and down.
Fig. 4 has last lower thermal insulating layer and shell that the catalytic reaction device schematic diagram of flange is arranged.
Fig. 5 is consersion unit 100 and the axial water pipe consersion unit 200 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.
Fig. 6 is consersion unit 100 and the axial air cooling consersion unit 300 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.
Fig. 7 is consersion unit 100 and the horizontal water cooling tube consersion unit 400 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.
Fig. 8 is the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and manages radially consersion unit 500 combination schematic diagrames of interior water-cooled.
Fig. 9 is a kind of two catalytic reaction devices 101 and the 102 combination schematic diagrames in parallel of above-mentioned Fig. 1 to Fig. 4 consersion unit.
The specific embodiment
Below in conjunction with accompanying drawing the technical solution of the utility model is described in detail.
Fig. 1 is the catalytic reaction device schematic diagram that an interior end socket is arranged.Fig. 1 middle shell 1 connects and composes pressure shell with upper cover 2, low head 3, and upper cover 2 has adapter 4 and heat transferring medium outlet 5, and heat transferring medium can be the steam that produces after the boiler soft water absorption reaction heat, also can be heating medium for high temperature.Low head 3 has manhole 6 and escape pipe 7.There is the inlet tube 8 of heat transferring medium such as water housing 1 lower end, the many heat exchanger tubes 10 of apparatus with catalyst inside connect upper perforated plate 11 and lower perforated plate 12 constitutes set of heat exchange tubes 40, have in the upper cover 2 and go up interior end socket 23, end socket 23 connects and composes top inner chamber 24 with upper perforated plate 11 in going up, end socket 23 has the air inlet pipe 20 and the adapter 4 of upper cover 2 to link by airtight and watertight padding 26 activities in going up, lower perforated plate 12 connects and composes lower lumen 17 with low head 3, connection pipe 15 and escape pipe 7 movable assemblings that the porous top cover 13 of supporting ceramic ball and catalyst is arranged in the escape pipe 7, upper perforated plate 11 has heat exchanger tube 10 to be connected with 12 of lower perforated plates, heat exchanger tube 10 apparatus with catalyst inside 18, heat exchanger tube 10 communicates with top inner chamber 24 and lower lumen 17.Adiabatic catalyst layer 41 is arranged at upper perforated plate 11 tops among the figure, there is manhole 6 to use among the figure for unloading catalyst and bottom Ceramic Balls, draw off as the connection pipe of not establishing in the manhole 6 desirable lower bottom part escape pipes 7 15, heat transferring medium inlet tube 8 links with removing outside drum in housing 1 lower end and outlet 5 among the figure, heat transferring medium for example water 10 the absorption reaction heat of many heat exchanger tubes of flowing through is vaporized into steam, catalyst can be packed into by top air inlet pipe 20, is drawn off by bottom manhole 6.
Unstripped gas is the H of synthesizing methanol for example
2, CO, CO
2Deng being pressurized to 5～12MPa, temperature is about in the of 210 ℃, by the top take over 4 enter in last adiabatic catalyst layer 41 on the upper perforated plate 11 of top inner chamber 24 of end socket 23 begin to react, enter copper base catalyst for methanol layer 18 catalytic reaction of set of heat exchange tubes 40 heat exchanger tubes 10 again, reaction heat is absorbed by heat exchanger tube 10 outer water, 220～280 ℃ of reaction gas temperature, CH
3OH content 8～26%, connection pipe 15 through bottom porous top cover 13 goes out reactor by escape pipe 7, heat exchanger tube 10 external spaces 9 of water in housing 1 that enter by inlet tube 8, absorption reaction heat outside heat exchanger tube 10, by-product 2～5MPa steam, between the end socket 23, draw through top upper cover 2 and in going up by outlet 5.
Fig. 2 is same as in figure 1 also to be the catalytic reaction device that an interior end socket is arranged at top, differently with Fig. 1 is that one is that top air inlet pipe 20 links by the adapter 4 of expansion joint 22 with upper cover 2; The 2nd, escape pipe 7 tops, bottom are by porous top cover 13 supporting catalysts; The 3rd, following adiabatic catalyst layer 42 is arranged below the lower perforated plate 12, catalyst and ceramic inert ball can be drawn off by manhole 6.Set of heat exchange tubes 40 also is provided with the polylith baffle plate, is used for fixing heat exchanger tube 10, and the cooling medium baffling is flowed, and baffle plate omits in institute's drawings attached, no longer draws.
Fig. 3 is the catalytic reaction device schematic diagram of end socket in having up and down.Fig. 3 and Fig. 1 structure difference are that one is that interior end socket 19 is arranged at the bottom, lower perforated plate 12 connects and composes lower lumen 17 with down interior end socket 19, the internals 40 that are made of interior up and down end socket, heat exchanger tube and catalyst are bearing on the low head 3 by down interior end socket 19 bottom supportings 16, the connection pipe 15 of porous top cover 13 that supporting ceramic ball and catalyst are arranged on the end socket 19 down is by filler 14 and escape pipe 7 movable assemblings, low head 3 bottoms have heat transferring medium for example the inlet tube 8 of water be communicated with the heat transferring medium outlet 5 of upper covers 2 by the outer space 9 of heat exchanger tube 10 pipes; The 2nd, 2 of housing 1 and upper covers with bolt 31 nuts 32 and is connected housing 1 with the lip weldering and constitutes pressure shell, are opened flange 30 by flange 30 like this, and the internals 40 that are made of last low head, tube sheet and heat exchanger tube can hang out shell, so that overhaul; The 3rd, lower perforated plate 12 bottoms are provided with down adiabatic catalyst layer 42, and last adiabatic catalyst layer 41 is also arranged at upper perforated plate 11 tops.
Fig. 4 is the same with Fig. 3 also to be the catalytic reaction device of end socket in having up and down, the heat transferring medium inlet tube 8 of consersion unit and outlet 5 are respectively on upper cover 2 and low head 3, and by 9 connections of the heat exchanger tube external space, can avoid Lurgi shell-and-tube reactor water inlet pipe and water outlet pipe to open like this and reduce equipment size in housing 1 side, different with Fig. 3 be one be housing 1 with upper cover 2 directly welding without flange; The 2nd, down interior end socket 19 has specializes in the adapter 28 and 30 sealings of low head 3 adapters 29 usefulness fillers of unloading catalyst or maintenance.
Fig. 5 is consersion unit 100 and the axial water pipe consersion unit 200 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.On the inlet tube 20 of end socket 23, inlet tube 20 was connected with the adapter 4 of upper cover 2 again in consersion unit 100 top expansion joints 22 were contained among Fig. 5.Axially housing 1 bottom of the water pipe reactor 200 gas outlet 7 that responds, heat exchange tube assemblies 34 is arranged in the housing 1,34 of housing 1 and heat exchange tube assemblies have catalyst layer 18, heat exchange tube assemblies 34 bottoms have heat transferring medium inlet tube 8 to pass housing 1 bottom (head), top has heat transferring medium outlet 5 to pass housing 1 top end socket by expansion joint or packing seal 26, the housing 1 top end socket of reactor 200 has manhole 16 to use for the dress catalyst, bottom bulkhead has manhole 6 to use for unloading catalyst, the heat transferring medium inlet tube 8 of the heat transferring medium inlet tube 8 of consersion unit 100 and outlet 5 and reactor 200 and outlet 5 and drum separately are connected, can pass through each self-regulation cooling medium and catalyst temperature like this, the air inlet 4 at housing 1 top of water-cooled reactor 200 is communicated with in the escape pipe 7 of consersion unit 100 and the pipe.When being used to produce methyl alcohol, contain H
2, CO, CO
2Deng synthesis gas can be earlier reach methanol content about 15% in that consersion unit 100 reactions are synthetic, advance axial water pipe reactor 200 again and further be synthesized to methyl alcohol about 25%.
Fig. 6 is consersion unit 100 and the axial air cooling consersion unit 300 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.Axially housing 1 bottom of the air cooling reactor 300 gas outlet 7 that responds, heat exchange tube assemblies 34 is arranged in the housing 1,34 of housing 1 and heat exchange tube assemblies have catalyst layer 18, heat exchange tube assemblies 34 bottoms have synthesis gas inlet tube 8 to pass housing 1 bottom (head), top has synthetic heat outlet pipe 5 to pass housing 1 top end socket by expansion joint or packing seal 26, housing 1 top end socket has manhole 16 to use for the dress catalyst, bottom bulkhead has manhole 6 to use for unloading catalyst, reactor 300 outlets 5 and reactor 100 inlet tubes 4 link, and the air inlet 4 at housing 1 top of the escape pipe 7 gentle cold reactors 300 of consersion unit 100 is communicated with.For example pressure contains H about 8MPa when being used for synthesizing methanol
2About 60 ℃ of the synthesis gas temperature of CO, enter about the reaction heat to 210 ℃ that absorbs heat exchanger tube 10 outer catalyst 18 in set of heat exchange tubes 34 pipe by reactor 300 bottom inlet pipes 8, by axial air cooling reactor 300 top exit pipes 7 enter consersion unit 100 top inlet pipes 20 enter consersion unit 100 the pipe inner catalyst react up and down at 260 ℃, advance from consersion unit 100 outlet at bottom pipes 7 to axial air cooling reactor 300 top inlet pipes 4 again that catalyst layer for example reaches methanol content 15% and goes out tower up and down 200～250 ℃ of reactions down outside the pipe of axial air cooling reactor 300.
Fig. 7 is consersion unit 100 and the horizontal water cooling tube consersion unit 400 combination schematic diagrames of one of above-mentioned Fig. 1 to Fig. 4.The inlet tube 8 of bottom water inlet is housed in water-cooled cross-current reactor 400 housings 1 in the pipe, the upper spacer 38 that the lower clapboard 37 that the top has heat exchange tube assemblies 34 bottoms of the outlet 5 of water outlet to have to be connected on one side with housing 1 and top are connected with housing 1 another side, upper spacer 38 is connected with housing 1 with the porous gas distribution grid 39 on the left side and the porous gas distribution grid 40 on the right respectively with lower clapboard 37, fills catalyst 18 at upper spacer 38 and lower clapboard 37 and left gas distribution grid 39 and right gas distribution grid 40 and 10 of heat exchanger tubes.Reactor 100 outlet at bottom pipes 7 are connected with cross-current reactor 400 bottom inlet 4, when the synthesis gas preparing dimethy ether, and CO, H
2, CO
2Earlier in consersion unit 100 in pipe the methyl alcohol of copper base catalyst for methanol Synthetic 2 0%, reaction gas is delivered to reactor 400 imports 4 by consersion unit 100 gas outlets 7 again and is entered the generation dimethyl ether that dewaters under the catalyst such as gama-alumina of tower set of heat exchange tubes 34 outside.
Fig. 8 is the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and manages radially consersion unit 500 combination schematic diagrames of interior water-cooled.In water-cooled radial reactor 500 housings 1 heat exchange tube assemblies 34 is arranged in the pipe, there is the porous gas distributor pipe 22 of the porous plate 13 that connects supporting catalyst at heat exchange tube assemblies 34 centers, 34 of housing 1 and heat exchange tube assemblies have the porous gas surge drum 23 that links with upper end open bottom and housing 1, and the bottom air inlet 4 of water-cooled radial reactor 500 links in the escape pipe 7 of consersion unit 100 and the pipe.When being used for synthesis gas system gasoline, synthesis gas is synthesizing methanol about in the of 30% in the catalyst for methanol in the pipe of consersion unit 100 earlier, enter radially water-cooled reactor 500 bottom inlet 4 by consersion unit 100 outlets 7 again, by center gas distributor pipe 22 outside water cooling tube group 34 in the molecular sieve methanol dehydration catalyst 18 the Radial Flow dehydration generate gasoline etc., reaction gas goes out tower to upwards flowing to outlet 7 between outer casing 1 and the gas porous gas collection plate 23 again, reaction heat by the cooling medium of heat exchanger tube courage 34 for example water absorb and reclaim heat and produce steam.
Fig. 9 is two catalytic reaction devices, 101, the 102 combination schematic diagrames in parallel by above-mentioned Fig. 1 to Fig. 4.Synthesis gas inlet manifold 50 is connected with the air inlet pipe 51,52 of consersion unit 101,102 respectively, and synthesis gas is catalytic reaction in two consersion units, and reaction gas gathers to the outlet header 70 who links through outlet 71,72 separately.
Embodiment
The utility model catalytic reaction device is used for synthesising gas systeming carbinol, use water as cooling medium, adopt Fig. 7 the utility model catalytic reaction device 100 and horizontal water cooling tube reactor 400 composite reaction equipments, 3.9 meters of the former consersion unit 100 diameters are adorned C306 copper base catalyst for methanol 50M in φ 42 * 2 pipes
3, 4 meters of latter reaction's device 400 diameters are adorned homemade C307 catalyst 135M between heat exchanger tube
3Form and the synthesis gas of tolerance and the circulating air of sequence number 4 converge with sequence number in the subordinate list 1, under synthesis pressure 8.8MPa, advance tower gas and advance methyl alcohol synthetic reactor 100 through being heated to about 220 ℃, about 260 ℃ of following synthesizing methanols under the district's catalytic action of synthesis catalytic reaction block in consersion unit 100 heat exchanger tubes 10, the temperature of this catalytic reaction can be regulated control by being communicated with the drum pressure for vaporization, go out tower by consersion unit 100 outlet at bottom pipes 7 then, enter by reactor 400 bottom inlet 4, porous gas distribution grid 39 in reactor 400 enters between heat exchanger tube the catalyst layer cross-current through catalyst layer, further synthesizing methanol under 210～250 ℃, catalytic synthesis temperature equally can be by being communicated with the heat exchanger tube water vapor temperature control that drum pressure is regulated.At circulating air and virgin gas ratio is 1.2 o'clock, and going out the tower methanol content is 20.8%, and methyl alcohol is produced 5000 ton per days daily, and data see attached list 1.
| Sequence number | Form mol% | H 2 | N 2 | CH 4 | CO | CO 2 | H 2O | CH 3OH | Nm
3/ |
| 1 | Virgin gas | 66.146 | 0.640 | 0.1001 | 29.885 | 3.2293 | 0.0000 | 0.0000 | 48182 |
| 2 | Inlet tower gas | 62.722 | 15.121 | 1.4000 | 15.901 | 4.6153 | 0.0430 | 0.1972 | 985222 |
| 3 | Exhaust gas | 46.301 | 21.312 | 1.9732 | 3.098 | 5.3463 | 1.2192 | 20.7495 | 712124 |
| 4 | Circulating air | 59.804 | 27.464 | 2.5078 | 3.983 | 5.7965 | 0.0796 | 0.3652 | 541872 |
| 5 | Drop a hint | 59.804 | 27.464 | 2.5078 | 3.983 | 5.7965 | 0.0796 | 0.3652 | 7050 |
Beneficial effect
Compared with the prior art the utility model has remarkable result, and the one, internals and housing free wxpansion are shunk, and eliminate lower perforated plate and the fixing welding of housing on the Lurgi shell-and-tube, the drawing crack of temperature stress generation in use, damage equipment, influence safety in production; The 2nd, reaction tube substitutes two phase stainless steel with homemade stainless steel, and housing replaces heat-resisting low-alloy steel with ordinary steel, reduces equipment investment, reduces reactor shell working pressure and serviceability temperature and hydrogen-type corrosion; The 3rd, with cooling medium for example steam (vapor) outlet change into upper cover or cooling medium inlet for example water inlet pipe also be low head, compare the minimizing contour size of the unit(s) with the Lurgi shell-and-tube, be convenient to maximize and transportation internals or internals and shell separately; The 4th, with water-cooled reacting phase ratio in the pipe, internals and housing seal, pressure and temperature is low, and for example methyl alcohol is synthetic, and the compression shell medium is owing to be water and steam pressure 2～4MPa, temperature＜260 ℃, and than shell-and-tube pressure～9MPa, 280 ℃ of temperature are low, and are difficult for leaking; The 5th, water-cooled reactor tandem compound in axial shell reactor and horizontal or the radial tubes both can be reduced recycle ratio, improve the methyl alcohol net value, comparable again external Lurgi water-cooled-air cooling holoaxial reduces resistance to reactor, and energy efficient improves and pays a producing steam output.
More than by numerous legends abundant description done in theme of the present utility model, according to design spirit of the present utility model, those of ordinary skill in the art can easily carry out various variations and the synthesis gas system of being applied to synthesizing methanol, dimethyl ether, hydrocarbon etc., can select Fig. 1 to Fig. 9 structure and various forms of combination according to actual needs for use in actual the enforcement, can place upper thermal insulating layer or lower thermal insulating layer or establish lower thermal insulating layer simultaneously and make up.Among the above-mentioned specific embodiment and the embodiment the catalyst type model of lifting and the reaction temperature, pressure, the composition that exemplify, do not represent can optimize according to actual needs to regulate and select to the qualification of these parameters.
Claims (10)
1. catalytic reaction device, comprise housing (1), upper cover (2), low head (3), housing (1) and upper cover (2), low head (3) connects, the heat exchanger tube (10) of apparatus with catalyst inside (18) connects upper perforated plate (11) and lower perforated plate (12), it is characterized in that upper cover (2) has heat transferring medium outlet (5) and takes over (4), have in the upper cover (2) and go up interior end socket (23), end socket (23) connects and composes top inner chamber (24) with upper perforated plate (11) in going up, end socket (23) has the air inlet pipe (20) and the adapter (4) of upper cover (2) to link by airtight and watertight padding (26) is movable in going up, perhaps air inlet pipe (20) is connected by flexible pipe or expansion joint (22) with adapter (4), lower perforated plate (12) is connected with low head (3), escape pipe (7) is arranged at low head (3) bottom, housing (1) lower end has heat transferring medium inlet tube (8) to be communicated with heat transferring medium outlet (5) with heat exchanger tube (10) external space (9) through housing (1), end socket (19) in perhaps having down in the low head (3), lower perforated plate (12) connects and composes lower lumen (17) with down interior end socket (19), on the end socket (19) escape pipe (7) is arranged down, low head (3) has heat transferring medium inlet tube (8), is communicated with heat transferring medium outlet (5) with heat exchanger tube (10) external space (9) through housing (1).
2. a kind of catalytic reaction device according to claim 1, it is characterized in that upper cover (2) has heat transferring medium outlet (5), lower perforated plate (12) links with housing (1), there is heat transferring medium inlet tube (8) housing (1) lower end, low head (3) has escape pipe (7) and manhole (6), and there is porous top cover (13) on escape pipe (7) top or the porous top cover (13) of connection pipe (15) is arranged.
3. a kind of catalytic reaction device according to claim 1, end socket (19) connects and composes lower lumen (17) with lower perforated plate (12) in it is characterized in that having in the low head (3) down, escape pipe (7) is arranged at low head (3) bottom, the connection pipe (15) of the porous top cover (13) of end socket (19) upper support Ceramic Balls and catalyst escape pipe (7) movable sealing of filler (14) and low head (3) down, internals (40) by interior up and down end socket, heat exchanger tube, catalyst constitute are bearing on the low head (3) by down interior end socket (19) bottom supporting (16).
4. a kind of catalytic reaction device according to claim 1 is characterized in that upper cover (2) and housing (1) directly welds or welds by the flange (30) on upper cover (2) and the housing (1) and bolt (31) nut (32) binding and with lip sealing.
5. a kind of catalytic reaction device according to claim 1 is characterized in that upper thermal barrier catalyst layer (41) is housed above the upper perforated plate (11) or adiabatic catalyst layer (42) is arranged at lower perforated plate (12) bottom.
6. a kind of catalytic reaction device according to claim 1, the air inlet pipe (4) that it is characterized in that housing (1) top of water-cooled reactor (200) in the escape pipe (7) of this consersion unit (100) and the pipe is communicated with, gas outlet (7) responds bottom the housing (1) of reactor (200), heat exchange tube assemblies (34) is arranged in the housing (1), between housing (1) and heat exchange tube assemblies (34) catalyst layer (18) is arranged, heat exchange tube assemblies (34) bottom has heat transferring medium inlet tube (8) to pass housing (1) bottom (head), top has heat transferring medium outlet (5) to pass housing (1) top end socket by expansion joint or packing seal (26), housing (1) the top end socket of reactor (200) has manhole (16) to use for the dress catalyst, bottom bulkhead has manhole (6) for unloading catalyst usefulness, and the heat transferring medium inlet tube (8) of the heat transferring medium inlet tube (8) of consersion unit (100) and outlet (5) and reactor (200) and outlet (5) and drum separately are connected.
7. a kind of catalytic reaction device according to claim 1, the air inlet (4) that it is characterized in that housing (1) top of air cooling reactor (300) in the escape pipe (7) of this consersion unit (100) and the pipe is communicated with, gas outlet (7) responds bottom the housing (1) of reactor (300), heat exchange tube assemblies (34) is arranged in the housing (1), between housing (1) and heat exchange tube assemblies (34) catalyst layer (18) is arranged, heat exchange tube assemblies (34) bottom has synthesis gas inlet tube (8) to pass housing (1) bottom (head), top has synthetic heat outlet pipe (5) to pass housing (1) top end socket by expansion joint or packing seal (26), housing (1) top end socket has manhole (16) to use for the dress catalyst, bottom bulkhead has manhole (6) for unloading catalyst usefulness, and reactor (300) outlet (5) and consersion unit (100) inlet tube (20) link.
8. a kind of catalytic reaction device according to claim 1, it is characterized in that being connected with water-cooled cross-current reactor (400) bottom inflow pipe (4) in the pipe with the escape pipe (7) of this consersion unit (100), the bottom is housed in the housing (1) of reactor (400) heat transferring medium inlet tube (8) is arranged, the heat exchange tube assemblies (34) of heat transferring medium outlet (5) is arranged at the top, the upper spacer (38) that the bottom has the lower clapboard (37) that is connected on one side with housing (1) and top to be connected with housing (1) another side, upper spacer (38) is connected with housing (1) with the porous gas distributor (39) on the left side and the porous gas gas collector (40) on the right respectively with lower clapboard (37), fills catalyst (18) between upper spacer (38) and lower clapboard (37) and left gas distributor (39) and right gas gas collector (40) and heat exchanger tube (10).
9. a kind of catalytic reaction device according to claim 1, it is characterized in that air inlet pipe (4) binding of escape pipe (7) with the interior water-cooled radial reactor (500) of radial tubes of this consersion unit (100), heat exchange tube assemblies (34) is arranged in reactor (500) housing (1), there is the porous gas distributor (22) of the porous plate (13) that connects supporting catalyst at heat exchange tube assemblies (34) center, and the porous gas gatherer (23) that links with upper end open bottom and housing (1) is arranged between housing (1) and heat exchange tube assemblies (34).
10. a kind of catalytic reaction device according to claim 1, it is characterized in that two or be communicated with inlet manifold (50) more than each air inlet pipe (51), (52) of two these catalytic reaction devices (101), (102), each escape pipe (71), (72) are communicated with the house steward that gives vent to anger (70), constitute many combinations in parallel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010202346834U CN201701922U (en) | 2010-02-24 | 2010-06-13 | Catalytic reaction equipment |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102160981A (en) * | 2010-02-24 | 2011-08-24 | 杭州林达化工技术工程有限公司 | Catalytic reaction equipment |
| CN102205221A (en) * | 2011-04-26 | 2011-10-05 | 华东理工大学 | Fixed bed catalyst reactor having heat-exchange medium distributing and gathering structure |
| CN102247783A (en) * | 2011-07-04 | 2011-11-23 | 常州市金州化工科技有限公司 | Shell-and-tube synthesizing tower |
| CN107754730A (en) * | 2016-08-19 | 2018-03-06 | 中国石化工程建设有限公司 | A kind of catalytic reactor |
-
2010
- 2010-06-13 CN CN2010202346834U patent/CN201701922U/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102160981A (en) * | 2010-02-24 | 2011-08-24 | 杭州林达化工技术工程有限公司 | Catalytic reaction equipment |
| CN102160981B (en) * | 2010-02-24 | 2015-01-07 | 杭州林达化工技术工程有限公司 | Catalytic reaction equipment |
| CN102205221A (en) * | 2011-04-26 | 2011-10-05 | 华东理工大学 | Fixed bed catalyst reactor having heat-exchange medium distributing and gathering structure |
| CN102205221B (en) * | 2011-04-26 | 2013-03-13 | 华东理工大学 | Fixed bed catalyst reactor having heat-exchange medium distributing and gathering structure |
| CN102247783A (en) * | 2011-07-04 | 2011-11-23 | 常州市金州化工科技有限公司 | Shell-and-tube synthesizing tower |
| CN107754730A (en) * | 2016-08-19 | 2018-03-06 | 中国石化工程建设有限公司 | A kind of catalytic reactor |
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