CN102160981B - Catalytic reaction equipment - Google Patents
Catalytic reaction equipment Download PDFInfo
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- CN102160981B CN102160981B CN201010208181.9A CN201010208181A CN102160981B CN 102160981 B CN102160981 B CN 102160981B CN 201010208181 A CN201010208181 A CN 201010208181A CN 102160981 B CN102160981 B CN 102160981B
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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 invention discloses catalytic reaction equipment, which mainly comprises a shell 1, an upper seal head 2 and a lower seal head 3, wherein the shell 1 is connected with the upper seal head 2 and the lower seal head 3; the upper seal head 2 is provided with a heat transfer medium outlet pipe 5 and an adapter 4; the lower seal head 3 is provided with an air outlet pipe 7; the shell 1 is provided with a heat transfer medium inlet pipe 8; and a heat transfer outer pipe 10 filled with catalysts consists of an upper tube plate 11 and a lower tube plate 12 in connection. The equipment is used for synthetic reaction processes of methanol, hydrocarbon and the like and synthetic processes of methane, methyl ether and the like, and a reactor which is high in production capacity, high in catalytic activity, simple and reliable in structure and good in operating performance is provided.
Description
Technical field
The present invention is a kind of consersion unit, for fluid catalyst reaction and diabatic process, belong to field of chemical engineering, be specially adapted to the synthetic reaction process such as methyl alcohol, MAS, dimethyl ether, methane and hydro carbons, and for the courses of reaction such as Methanol hydro carbons, Oxidation of Hydrogen Sulfide sulphur, carbon monodixe conversion, ethylene glycol and oxirane and aforementioned exothermic reaction Chemical Manufacture and IGCC electric power co process, also can be used for endothermic reaction process.
Background technology
Synthesize this kind of exothermic catalytic reaction for by pressurization lower methanol-fueled CLC, methyl ether, hydro carbons etc., along with the carrying out of course of reaction, the reaction heat of constantly releasing makes catalyst layer temperature improve.In order to improve the efficiency of reactor, need reaction heat to shift out to reduce reaction temperature.Once the shell and tube reactor for methanol-fueled CLC as German Lurgi company widely used in industrial reactor, unstripped gas enters from upper inlet port 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, and produce steam and gone out by side pipe, reaction gas goes out tower by bottom escape pipe, and this tower has a narrow range of temperature, but upper lower perforated plate fixedly welds with heat exchanger tube, for solution thermal stress need use two phase stainless steel and still fragile.
Task of the present invention is the feature according to catalytic exothermic reversible reaction, and overcome the shortcoming of prior art, structure is reliable, production capacity is large, catalyst activity is high, the reactor of good operation performance to provide one.
The content of invention
The invention 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 upper cover 2 has heat transferring medium outlet 5 and adapter 4, upper interior end socket 23 is had in upper cover 2, in upper, end socket 23 and upper perforated plate 11 connect and compose top inner chamber 24, in upper, end socket 23 has air inlet pipe 20 to be linked by airtight and watertight padding 26 activity with the adapter 4 of upper cover 2, or 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 had bottom low head 3, 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, or there is lower interior end socket 19 in low head 3, lower perforated plate 12 and lower interior end socket 19 connect and compose lower lumen 17, in lower, end socket 19 there is escape pipe 7, low head 3 has heat transferring medium inlet tube 8, be communicated with heat transferring medium outlet 5 with heat exchanger tube 10 external space 9 through housing 1.
The invention provides a kind of catalytic reaction device, mainly upper cover 2 has heat transferring medium outlet 5, and lower perforated plate 12 and housing 1 link, and 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 has the porous top cover 13 of union 15.
The invention provides a kind of catalytic reaction device, lower interior end socket 19 is mainly had to connect and compose lower lumen 17 with lower perforated plate 12 in low head 3, escape pipe 7 is had bottom low head 3, union 15 escape pipe 7 movable sealing of filler 14 with low head 3 of the porous top cover 13 of end socket 19 upper support Ceramic Balls and catalyst in lower, the internals 40 be made up of upper and lower interior end socket, heat exchanger tube, catalyst, are bearing on low head 3 by lower interior end socket 19 bottom supporting 16.
The invention provides a kind of catalytic reaction device, mainly upper cover 2 directly welds with housing 1 or is linked by the flange 30 on upper cover 2 and housing 1 and bolt 31 nut 32 and welded with lip and seals.
The invention provides a kind of catalytic reaction device, mainly upper perforated plate 11 is above equipped with upper thermal barrier catalyst layer 41 or adiabatic catalytic oxidant layer 42 is arranged at lower perforated plate 12 bottom.
The invention provides a kind of catalytic reaction device, mainly the escape pipe 7 of this consersion unit 100 is communicated with the air inlet pipe 4 at housing 1 top of water-cooled reactor 200 in pipe, the gas that responds bottom the housing 1 of reactor 200 outlet 7, heat exchange tube assemblies 34 is had in housing 1, catalyst layer 18 is had between housing 1 and heat exchange tube assemblies 34, there is heat transferring medium inlet tube 8 heat exchange tube assemblies 34 bottom through 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 for dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst, heat transferring medium inlet tube 8 and the outlet 5 of the heat transferring medium inlet tube 8 of consersion unit 100 and outlet 5 and reactor 200 are connected with respective drum.
The invention provides a kind of catalytic reaction device, mainly the escape pipe 7 of this consersion unit 100 is communicated with the air inlet 4 at housing 1 top of air cooling reactor 300 in pipe, the gas that responds bottom the housing 1 of reactor 300 outlet 7, heat exchange tube assemblies 34 is had in housing 1, catalyst layer 18 is had between housing 1 and heat exchange tube assemblies 34, there is synthesis gas inlet tube 8 heat exchange tube assemblies 34 bottom through housing 1 bottom (head), top has synthesis 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 for dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst, reactor 300 outlet 5 and consersion unit 100 inlet tube 20 link.
The invention provides a kind of catalytic reaction device, mainly with the escape pipe 7 of this consersion unit 100 and in manage water-cooled transverse direction flow reactor 400 bottom inflow pipe 4 be connected, the housing 1 of reactor 400 has heat transferring medium inlet tube 8 built with bottom, the heat exchange tube assemblies 34 of heat transferring medium outlet 5 is arranged at top, bottom has with housing 1 while the upper spacer 38 that is connected with housing 1 another side of the lower clapboard 37 be connected and top, upper spacer 38 and lower clapboard 37 are 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, at upper spacer 38 and lower clapboard 37 and left gas distributor 39 with fill catalyst 18 between right gas collection device 40 and heat exchanger tube 10.
The invention provides a kind of catalytic reaction device, mainly the escape pipe 7 of this consersion unit 100 links with the air inlet pipe 4 of water-cooled radial reactor 500 in radial tubes, heat exchange tube assemblies 34 is had in reactor 500 housing 1, there is the porous gas distributor 22 of porous plate 13 connecting supporting catalyst at heat exchange tube assemblies 34 center, have between housing 1 and heat exchange tube assemblies 34 with upper end open bottom the porous gas collector 23 that links with housing 1.
The invention provides a kind of method of catalytic reaction device, mainly in catalytic reaction device, carry out exothermic reaction, entering into by inlet tube 8 heat transferring medium that outlet 5 flows out is cooling medium, or the endothermic reaction is carried out in catalytic unit, entering into by inlet tube 8 heat transferring medium that outlet 5 flows out is heated air or liquid.
Accompanying drawing explanation
Illustrate below in conjunction with accompanying drawing.
Fig. 1 is the catalytic reaction device schematic diagram having an interior end socket.
Fig. 2 is the another kind of catalytic reaction device schematic diagram having an interior end socket.
Fig. 3 is the catalytic reaction device schematic diagram having end socket up and down.
Fig. 4 has upper lower thermal insulating layer and shell has the catalytic reaction device schematic diagram of flange.
Fig. 5 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and axial water pipe consersion unit 200 combine schematic diagram.
Fig. 6 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and axial air cooling consersion unit 300 combine schematic diagram.
Fig. 7 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and horizontal water cooling tube consersion unit 400 combine schematic diagram.
Fig. 8 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 combines schematic diagram with the radial consersion unit 500 of water-cooled in pipe.
Fig. 9 is a kind of two catalytic reaction devices 101 and 102 parallel combination schematic diagram of above-mentioned Fig. 1 to Fig. 4 consersion unit.
Detailed description of the invention
Below in conjunction with accompanying drawing, technical scheme of the present invention is described in detail.
Fig. 1 is the catalytic reaction device schematic diagram having an interior end socket.Fig. 1 middle shell 1 and upper cover 2, low head 3 connect and compose pressure shell, and upper cover 2 has adapter 4 and heat transferring medium outlet 5, and heat transferring medium can be the steam produced after 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 heat transferring medium housing 1 lower end as the inlet tube 8 of water, the many heat exchanger tubes 10 of apparatus with catalyst inside connect upper perforated plate 11 and lower perforated plate 12 forms set of heat exchange tubes 40, upper interior end socket 23 is had in upper cover 2, in upper, end socket 23 and upper perforated plate 11 connect and compose top inner chamber 24, in upper, end socket 23 has air inlet pipe 20 to be linked by airtight and watertight padding 26 activity with the adapter 4 of upper cover 2, lower perforated plate 12 and low head 3 connect and compose lower lumen 17, the union 15 of the porous top cover 13 of supporting ceramic ball and catalyst is had to assemble with escape pipe 7 activity in escape pipe 7, heat exchanger tube 10 is had to be connected between upper perforated plate 11 with lower perforated plate 12, heat exchanger tube 10 apparatus with catalyst inside 18, heat exchanger tube 10 communicates with top inner chamber 24 and lower lumen 17.In figure, adiabatic catalytic oxidant layer 41 is arranged at upper perforated plate 11 top, manhole 6 is had for unloading catalyst and bottom Ceramic Balls in figure, draw off if do not established the union 15 in the desirable lower bottom part escape pipe 7 of manhole 6, in figure heat transferring medium inlet tube 8 housing 1 lower end and outlet 5 with go outside drum to link, heat transferring medium is such as vaporized into steam with current through many heat exchanger tubes 10 absorption reaction heat, catalyst can be loaded by top air inlet pipe 20, is drawn off by bottom manhole 6.
The H of unstripped gas such as synthesizing methanol
2, CO, CO
2etc. being pressurized to 5 ~ 12MPa, temperature about 210 DEG C, react entered the upper adiabatic catalytic oxidant layer 41 on the upper perforated plate 11 of the top inner chamber 24 of upper interior end socket 23 by top adapter 4, enter copper-based methanol catalyst layer 18 catalytic reaction of set of heat exchange tubes 40 heat exchanger tube 10 again, reaction heat is absorbed by the water outside heat exchanger tube 10, reaction gas temperature 220 ~ 280 DEG C, CH
3oH content 8 ~ 26%, union 15 through bottom porous top cover 13 goes out reactor by escape pipe 7, heat exchanger tube 10 external space 9 of the water entered by inlet tube 8 in housing 1, in the outer absorption reaction heat of heat exchanger tube 10, by-product 2 ~ 5MPa steam, through between top upper cover 2 and upper interior end socket 23, drawn by outlet 5.
Fig. 2 catalytic reaction device being also top and having an interior end socket same as in figure 1, differently from Fig. 1 is one to be top air inlet pipe 20 is linked by the adapter 4 of expansion joint 22 with upper cover 2; Two is that escape pipe 7 top, bottom is by porous top cover 13 supporting catalyst; Three is that lower perforated plate 12 has lower adiabatic catalytic oxidant layer 42 below, and catalyst and ceramic inert ball can be drawn off by manhole 6.Set of heat exchange tubes 40 is also provided with polylith baffle plate, and for fixing heat exchanger tube 10, and make cooling medium baffling flowing between pipe, baffle plate omits in all of the figs, no longer draws.
Fig. 3 is the catalytic reaction device schematic diagram having end socket up and down.Fig. 3 and Fig. 1 structure difference is that one is that interior end socket 19 is arranged at bottom, lower perforated plate 12 and lower interior end socket 19 connect and compose lower lumen 17, be bearing on low head 3 by the internals 40 of end socket, heat exchanger tube and catalyst in up and down-form by lower interior end socket 19 bottom supporting 16, in lower, end socket 19 there is the union 15 of the porous top cover 13 of supporting ceramic ball and catalyst to be assembled by filler 14 and escape pipe 7 activity, bottom low head 3, have the inlet tube 8 of heat transferring medium such as water to be communicated with the heat transferring medium outlet 5 of upper cover 2 by the space 9 outside heat exchanger tube 10 pipe; Two is also form pressure shell with the soldered body contact body 1 of lip by flange 30 and bolt 31 nut 32 between housing 1 and upper cover 2, and open flange 30 like this, the internals 40 be made up of upper low head, tube sheet and heat exchanger tube can hang out shell, to overhaul; Three is that lower perforated plate 12 bottom is provided with lower adiabatic catalytic oxidant layer 42, and upper adiabatic catalytic oxidant layer 41 is also arranged at upper perforated plate 11 top.
Fig. 4 and Fig. 3 is the same is also the catalytic reaction device having end socket 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 be communicated with by the heat exchanger tube external space 9, Lurgi shell-and-tube reactor water inlet pipe and water outlet pipe can be avoided like this to open in housing 1 side and reduce equipment size, differently from Fig. 3 be that one is that housing 1 directly welds without flange with upper cover 2; Two is that lower interior end socket 19 has and specializes in the adapter 28 of unloading catalyst or maintenance and seal with filler 30 with low head 3 adapter 29.
Fig. 5 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and axial water pipe consersion unit 200 combine schematic diagram.In Fig. 5, consersion unit 100 top expansion joint 22 is contained on the inlet tube 20 of interior end socket 23, and inlet tube 20 is connected with the adapter 4 of upper cover 2 again.Respond bottom the housing 1 of axial water pipe reactor 200 gas outlet 7, heat exchange tube assemblies 34 is had in housing 1, catalyst layer 18 is had between housing 1 and heat exchange tube assemblies 34, there is heat transferring medium inlet tube 8 heat exchange tube assemblies 34 bottom through 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 for dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst, heat transferring medium inlet tube 8 and the outlet 5 of the heat transferring medium inlet tube 8 of consersion unit 100 and outlet 5 and reactor 200 are connected with respective drum, like this by each self-regulation cooling medium and catalyst temperature, the escape pipe 7 of consersion unit 100 is communicated with the air inlet 4 at housing 1 top of water-cooled reactor 200 in pipe.When for the production of methyl alcohol, containing H
2, CO, CO
2deng synthesis gas first can reach methanol content about 15% at consersion unit 100 Reactive Synthesis, then enter axial water pipe reactor 200 and be synthesized to methyl alcohol about 25% further.
Fig. 6 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and axial air cooling consersion unit 300 combine schematic diagram.Respond bottom the housing 1 of axial air cooling reactor 300 gas outlet 7, heat exchange tube assemblies 34 is had in housing 1, catalyst layer 18 is had between housing 1 and heat exchange tube assemblies 34, there is synthesis gas inlet tube 8 heat exchange tube assemblies 34 bottom through housing 1 bottom (head), top has synthesis 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 for dress catalyst, bottom bulkhead has manhole 6 for unloading catalyst, reactor 300 outlet 5 and reactor 100 inlet tube 4 link, the air inlet 4 at housing 1 top of the gentle cold reactor 300 of escape pipe 7 of consersion unit 100 is communicated with.When upper and lower at 8MPa for the synthesis of such as pressure during methyl alcohol, containing H
2, the synthesis gas temperature of CO about 60 DEG C, enter set of heat exchange tubes 34 by reactor 300 bottom inflow pipe 8 and manage the reaction heat of the outer catalyst 18 of interior absorption heat-exchange pipe 10 to about 210 DEG C, enter consersion unit 100 top inlet pipe 20 by axial air cooling reactor 300 top exit pipe 7 to enter consersion unit 100 and react about 260 DEG C at pipe inner catalyst, the pipe entering axial air cooling reactor 300 again from consersion unit 100 outlet at bottom pipe 7 to axial air cooling reactor 300 top inlet pipe 4, catalyst layer reacts at 200 ~ 250 DEG C, such as reach methanol content about 15% and go out tower.
Fig. 7 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 and horizontal water cooling tube consersion unit 400 combine schematic diagram.In pipe, horizontal flow reactor 400 housing 1 of water-cooled is built with the inlet tube 8 of bottom water inlet, top has heat exchange tube assemblies 34 bottom of the outlet 5 of water outlet to have with housing 1 while the upper spacer 38 that is connected with housing 1 another side of the lower clapboard 37 be connected and top, upper spacer 38 and lower clapboard 37 are 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, at upper spacer 38 and lower clapboard 37 and left gas distribution grid 39 with fill catalyst 18 between right gas distribution grid 40 and heat exchanger tube 10.Reactor 100 outlet at bottom pipe 7 is connected with horizontal flow reactor 400 bottom inlet 4, when synthesis gas preparing dimethy ether, and CO, H
2, CO
2the first methyl alcohol of copper-based methanol catalyst synthesis 20% in pipe in consersion unit 100, reaction gas is delivered to reactor 400 inlet tube 4 by consersion unit 100 gas outlet 7 again and is entered dehydration generation dimethyl ether under the catalyst such as the gama-alumina of tower outside set of heat exchange tubes 34.
Fig. 8 is that the consersion unit 100 of one of above-mentioned Fig. 1 to Fig. 4 combines schematic diagram with the radial consersion unit 500 of water-cooled in pipe.Heat exchange tube assemblies 34 is had in water-cooled radial reactor 500 housing 1 in pipe, there is the porous gas distributor pipe 22 of the porous plate 13 connecting supporting catalyst at heat exchange tube assemblies 34 center, have between housing 1 and heat exchange tube assemblies 34 with upper end open bottom the porous gas surge drum 23 that links with housing 1, the escape pipe 7 of consersion unit 100 links with the bottom air inlet 4 of water-cooled radial reactor 500 in pipe.When for the synthesis of gas gasoline, synthesis gas is synthesizing methanol about 30% in catalyst for methanol in the pipe of consersion unit 100 first, radial water cold reactor 500 bottom inlet 4 is entered again by consersion unit 100 outlet 7, gasoline etc. is generated by Radial Flow dehydration in center gas distributor pipe 22 to the outer molecular sieve methanol dehydration catalyst 18 of water cooling tube group 34, reaction gas arrives and upwards flow to outlet 7 between outer casing 1 and gas porosity gas collection plate 23 and go out tower, and reaction heat is absorbed by the cooling medium such as water of heat exchanger tube courage 34 and reclaims heat and produce steam.
Fig. 9 is by two of above-mentioned Fig. 1 to Fig. 4 catalytic reaction device 101,102 parallel combination schematic diagrames.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 linked through respective outlet 71,72.
embodiment
Catalytic reaction device of the present invention is for the synthesis of gas methyl alcohol, use water as cooling medium, adopt Fig. 7 catalytic reaction device of the present invention 100 and horizontal water cooling tube reactor 400 composite reaction equipment, the former consersion unit 100 diameter 3.9 meters, manage in-built C306 copper-based methanol catalyst 50M at φ 42 × 2
3, latter reaction's device 400 diameter 4 meters, fills domestic C307 catalyst 135M between heat exchanger tube
3, to form by sequence number in subordinate list 1 and the synthesis gas of tolerance and the circulating air of sequence number 4 converge, under synthesis pressure 8.8MPa, enter tower gas and enter methyl alcohol synthetic reactor 100 through being heated to about 220 DEG C, synthesizing methanol at about 260 DEG C under the district's catalytic action of synthesis catalytic reaction block in consersion unit 100 heat exchanger tube 10, the temperature of this catalytic reaction can carry out regulable control by being communicated with drum pressure for vaporization, then tower is gone out by consersion unit 100 outlet at bottom pipe 7, entered by reactor 400 bottom inlet 4, porous gas distribution grid 39 in reactor 400 enters catalyst layer between heat exchanger tube and laterally flows through catalyst layer, further synthesizing methanol at 210 ~ 250 DEG C, catalytic synthesis temperature can be controlled by the heat exchanger tube water vapor temperature being communicated with drum pressure adjustment equally.When circulating air and virgin gas ratio are 1.2, going out tower methanol content is 20.8%, and methyl alcohol produces 5000 ton per days daily, and data see attached list 1.
| Sequence number | Composition mol% | H 2 | N 2 | CH 4 | CO | CO 2 | H 2O | CH 3OH | Nm 3/h |
| 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 present invention has remarkable result, and one is that internals and housing free wxpansion are shunk, and eliminates lower perforated plate on Lurgi shell-and-tube and fixedly welds with housing, in use temperature stress generation drawing crack, damage equipment, impact safety in production; Two is that the domestic stainless steel of reaction tube substitutes two phase stainless steel, and housing ordinary steel replaces heat-resisting low-alloy steel, reduces equipment investment, reduces reactor shell and uses pressure and serviceability temperature and hydrogen-type corrosion; Three is that cooling medium such as steam (vapor) outlet to be changed into upper cover or cooling medium inlet such as water inlet pipe be also low head, minimizing contour size of the unit(s) compared with Lurgi shell-and-tube, be convenient to maximize and transport internals or internals and shell separately; Four are and water-cooled reacting phase ratio in pipe, internals and housing seal, and pressure and temperature is low, such as methanol-fueled CLC, compression shell medium is owing to being water and steam pressure 2 ~ 4MPa, temperature < 260 DEG C, than shell-and-tube pressure ~ 9MPa, temperature 280 DEG C is low, and not easily leaks; Five is that water-cooled reactor tandem compound in axial shell reactor and transverse direction or radial tubes both can be reduced recycle ratio, improves methyl alcohol net value, and the full axial flow reactor of comparable external Lurgi water-cooled-air cooling reduces resistance again, saves energy consumption, improves and pays producing steam output.
By numerous legend, abundant description is done to theme of the present invention above, according to intended spirit of the present invention, those of ordinary skill in the art can easily carry out various change and be applied to synthesis gas synthesizing methanol, dimethyl ether, hydrocarbon etc., Fig. 1 to Fig. 9 structure and various forms of combination can be selected according to actual needs in actual enforcement, upper thermal insulating layer or lower thermal insulating layer can be placed or establish lower thermal insulating layer to combine simultaneously.In above-mentioned detailed description of the invention and embodiment reaction temperature, pressure, the composition lifting catalyst type model and exemplify, do not represent the restriction of these parameters and can select by optimizing regulation according to actual needs.
Claims (6)
1. a 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 adapter (4), upper interior end socket (23) is had in upper cover (2), in upper, end socket (23) and upper perforated plate (11) connect and compose top inner chamber (24), in upper, end socket (23) has air inlet pipe (20) to be linked by airtight and watertight padding (26) activity with the adapter (4) of upper cover (2), or 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 cooling medium outlet (5) with heat exchanger tube (10) external space (9) through housing (1), or there is lower interior end socket (19) in low head (3), lower perforated plate (12) and lower interior end socket (19) connect and compose lower lumen (17), in lower, end socket (19) there is escape pipe (7), low head (3) has heat transferring medium inlet tube (8), be communicated with heat transferring medium outlet (5) with heat exchanger tube (10) external space (9) through housing (1),
Upper cover (2) has heat transferring medium outlet (5), lower perforated plate (12) and housing (1) link, 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 has the porous top cover (13) of union (15);
Lower interior end socket (19) and lower perforated plate (12) is had to connect and compose lower lumen (17) in low head (3), escape pipe (7) is arranged at low head (3) bottom, union (15) escape pipe (7) movable sealing of filler (14) with low head (3) of the porous top cover (13) of end socket (19) upper support Ceramic Balls and catalyst in lower, the internals be made up of upper and lower interior end socket, heat exchanger tube, catalyst, are bearing on low head (3) by lower interior end socket (19) bottom supporting (16);
Upper cover (2) directly welds with housing (1) or is linked by the flange (30) on upper cover (2) and housing (1) and bolt (31) nut (32) and welded with lip and seals;
Upper perforated plate (11) upper thermal barrier catalyst layer (41) is housed above or adiabatic catalytic oxidant layer (42) is arranged at lower perforated plate (12) bottom.
2. a kind of catalytic reaction device according to claim 1, it is characterized in that the escape pipe (7) of this consersion unit (100) is communicated with the air inlet pipe at housing (1) top of water-cooled reactor (200) in pipe, respond bottom the housing (1) of the interior water-cooled reactor (200) of pipe gas outlet, heat exchange tube assemblies (34) is had in housing (1), catalyst layer is had between housing (1) and heat exchange tube assemblies (34), there is heat transferring medium inlet tube (8) heat exchange tube assemblies (34) bottom through housing (1) bottom (head), there is heat transferring medium outlet (5) on top by expansion joint or airtight and watertight padding (26) through housing (1) top end socket, housing (1) the top end socket of reactor (200) has manhole for dress catalyst, bottom bulkhead has manhole (6) 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) are connected with respective drum.
3. a kind of catalytic reaction device according to claim 1, it is characterized in that the escape pipe (7) of this consersion unit (100) is communicated with the air inlet at housing (1) top of air cooling reactor (300) in pipe, respond bottom the housing (1) of reactor (300) gas outlet, heat exchange tube assemblies (34) is had in housing (1), catalyst layer is had between housing (1) and heat exchange tube assemblies (34), there is synthesis gas inlet tube heat exchange tube assemblies (34) bottom through housing (1) bottom (head), there is synthesis heat outlet pipe on top by expansion joint or airtight and watertight padding (26) through housing (1) top end socket, housing (1) top end socket has manhole for dress catalyst, bottom bulkhead has manhole (6) for unloading catalyst, reactor (300) outlet and consersion unit (100) inlet tube link.
4. a kind of catalytic reaction device according to claim 1, it is characterized in that with the escape pipe of this consersion unit (100) (7) and in managing horizontal flow reactor (400) the bottom inflow pipe of water-cooled be connected, the housing (1) of reactor (400) has heat transferring medium inlet tube (8) built with bottom, the heat exchange tube assemblies (34) of heat transferring medium outlet (5) is arranged at top, bottom has with housing (1) while the upper spacer (38) that is connected with housing (1) another side of the lower clapboard (37) be connected and top, upper spacer (38) and lower clapboard (37) are 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, at upper spacer (38) and lower clapboard (37) and left gas distributor (39) with fill catalyst (18) between right gas collection device (40) and heat exchanger tube (10).
5. a kind of catalytic reaction device according to claim 1, it is characterized in that the escape pipe (7) of this consersion unit (100) links with the air inlet pipe of water-cooled radial reactor (500) in radial tubes, heat exchange tube assemblies (34) is had in reactor (500) housing (1), there is the porous gas distributor of porous plate connecting supporting catalyst at heat exchange tube assemblies (34) center, have between housing (1) and heat exchange tube assemblies (34) with upper end open bottom the porous gas collector that links with housing (1).
6. the using method of an a kind of catalytic reaction device as claimed in claim 1, it is characterized in that carrying out exothermic reaction in catalytic reaction device, the heat transferring medium being entered into outlet outflow by inlet tube is cooling medium, or the endothermic reaction is carried out in catalytic unit, the heat transferring medium being entered into outlet outflow by inlet tube is heated air or liquid.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010208181.9A CN102160981B (en) | 2010-02-24 | 2010-06-13 | Catalytic reaction equipment |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201010133998 | 2010-02-24 | ||
| CN201010133998.4 | 2010-02-24 | ||
| CN201010208181.9A CN102160981B (en) | 2010-02-24 | 2010-06-13 | Catalytic reaction equipment |
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| Publication Number | Publication Date |
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| CN102160981A CN102160981A (en) | 2011-08-24 |
| CN102160981B true CN102160981B (en) | 2015-01-07 |
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| CN201010208181.9A Active CN102160981B (en) | 2010-02-24 | 2010-06-13 | Catalytic reaction equipment |
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| CN103044195B (en) * | 2012-11-30 | 2015-10-21 | 河南心连心化肥有限公司 | The synthetic method of low pressure methanol |
| CN103357355B (en) * | 2013-08-06 | 2015-04-29 | 北京华福工程有限公司 | High-temperature reactor and chemical engineering system using the same |
| CN103804119B (en) * | 2014-01-14 | 2015-12-16 | 衢州市鼎盛化工科技有限公司 | Cracking difluorochloromethane prepares the device and method of tetrafluoroethylene and R 1216 |
| CN104162387B (en) * | 2014-08-19 | 2016-04-06 | 宜昌恒友化工有限公司 | A kind of penta chloropyridine reaction unit being convenient to extending catalyst service life |
| CN108854517B (en) * | 2018-05-31 | 2021-03-30 | 上海化工研究院有限公司 | Heating catalytic decomposition type air purification device for vehicle |
| CN109277054B (en) * | 2018-11-15 | 2023-09-12 | 山东诺为制药流体系统有限公司 | Accurate feeding continuous flow reaction system capable of quenching |
| CN110368876A (en) * | 2019-06-28 | 2019-10-25 | 常州瑞凯化工装备有限公司 | Radial fixed-bed dehydration reactor |
| CN113217986B (en) * | 2021-04-30 | 2022-06-10 | 董荣华 | Chemical heat accumulator and heating system adopting same |
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