CN201211474Y - Fixed bed composite reaction equipment - Google Patents
Fixed bed composite reaction equipment Download PDFInfo
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- CN201211474Y CN201211474Y CNU2008200030276U CN200820003027U CN201211474Y CN 201211474 Y CN201211474 Y CN 201211474Y CN U2008200030276 U CNU2008200030276 U CN U2008200030276U CN 200820003027 U CN200820003027 U CN 200820003027U CN 201211474 Y CN201211474 Y CN 201211474Y
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- 238000003541 multi-stage reaction Methods 0.000 title claims abstract description 26
- 238000006243 chemical reaction Methods 0.000 claims abstract description 84
- 238000012546 transfer Methods 0.000 claims abstract description 75
- 239000003054 catalyst Substances 0.000 claims abstract description 58
- 239000002826 coolant Substances 0.000 claims abstract description 34
- 239000007789 gas Substances 0.000 claims abstract description 31
- 239000012495 reaction gas Substances 0.000 claims abstract description 26
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 19
- 230000008016 vaporization Effects 0.000 claims description 37
- 238000009834 vaporization Methods 0.000 claims description 36
- 238000006555 catalytic reaction Methods 0.000 claims description 30
- 230000033228 biological regulation Effects 0.000 claims description 20
- 238000001816 cooling Methods 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 8
- 230000009467 reduction Effects 0.000 claims description 5
- 230000001105 regulatory effect Effects 0.000 claims description 5
- 230000027455 binding Effects 0.000 claims description 4
- 238000009739 binding Methods 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 4
- 238000007789 sealing Methods 0.000 claims description 2
- 239000003507 refrigerant Substances 0.000 claims 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 104
- 238000003786 synthesis reaction Methods 0.000 abstract description 13
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 abstract description 12
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical group CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 abstract description 10
- 230000003647 oxidation Effects 0.000 abstract description 4
- 238000007254 oxidation reaction Methods 0.000 abstract description 4
- 230000008901 benefit Effects 0.000 abstract description 3
- XNGIFLGASWRNHJ-UHFFFAOYSA-N phthalic acid Chemical compound OC(=O)C1=CC=CC=C1C(O)=O XNGIFLGASWRNHJ-UHFFFAOYSA-N 0.000 abstract 2
- -1 methanation Chemical compound 0.000 abstract 1
- 229940078552 o-xylene Drugs 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 abstract 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 30
- 238000010586 diagram Methods 0.000 description 13
- 230000036632 reaction speed Effects 0.000 description 12
- 150000003839 salts Chemical class 0.000 description 9
- 150000001875 compounds Chemical class 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 230000018044 dehydration Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- 238000002309 gasification Methods 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 3
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 230000002194 synthesizing effect Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000945 filler Substances 0.000 description 2
- 229930195733 hydrocarbon Natural products 0.000 description 2
- 150000002430 hydrocarbons Chemical class 0.000 description 2
- 239000002480 mineral oil Substances 0.000 description 2
- 235000010446 mineral oil Nutrition 0.000 description 2
- 239000003921 oil Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 239000008096 xylene Substances 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 241000237983 Trochidae Species 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000003416 augmentation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 229910052802 copper Inorganic materials 0.000 description 1
- 239000010949 copper Substances 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 235000012149 noodles Nutrition 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 230000003389 potentiating effect Effects 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 150000003609 titanium compounds Chemical class 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to fixed bed composite reaction equipment, which mainly comprises a cylindrical shell provided with a shell cover, a reaction gas inlet and a reaction gas outlet on the shell, a porous gas distributor, a porous gas-collecting plate, a catalyst layer and a heat exchange tube for heat transfer of a cooling medium. The fixed bed composite reaction equipment is provided with steam manifolds of steam pressure control valves; and a cooling medium circulation loop is formed, wherein catalyst in at least one heat exchange reaction block is arranged inside the tube, so that heat exchange in the reaction is designed according to the required size of the reaction heat shifted. The fixed bed composite reaction equipment is used for strong reaction courses such as synthesis of methanol, synthesis of dimethyl ether, methanation, F-T reaction, preparation of phthalic acid through o-xylene oxidation and so on, and has the advantages of reducing the temperature difference, improving the reaction efficiency, improving the yield, saving energy, reducing the cost and realizing the large-scale aim.
Description
Technical field
The utility model is a kind of catalytic reaction device, be used for fluid catalytic reaction and diabatic process, belong to field of chemical engineering, be specially adapted to synthesizing methanol, dimethyl ether synthesis, fischer-tropsch reaction system liquid hydrocarbon and potent courses of reaction such as methane, o xylene oxidation system phthalic anhydride.
Background technology
For, synthesis gas preparing dimethy ether synthetic, fischer-tropsch reaction system liquid hydrocarbon and some strong exothermal reactions such as methane, o xylene oxidation system phthalic anhydride as methyl alcohol, in order to improve reaction efficiency, need shift out reaction heat simultaneously in reaction, for example Lurgi shell-and-tube methanol column is removed reaction heat in the reaction tube with shell side water, in the shell-and-tube reactor design, coolant temperature is constant in the full bed heat exchange of catalyst.Strengthening to move to adopt when hot when need increases the restriction that heat transfer area is subjected to structure, shell-and-tube than huyashi-chuuka (cold chinese-style noodles) promptly one cubic metre of catalyst heat exchange area be difficult to improve again up to more than 120 square metres.Therefore adopt and improve tower tolerance and gas linear velocity, prevent " overtemperature " and " temperature runaway " outward so that in time reaction heat is taken out of tower, need adopt up to 5～10 times of circulating air (being recycle ratio) for this reason and reduce in the synthetic tower gas effectively gas more than unstripped gas, otherwise the strong reaction heat that rapid reaction rate produces can make the catalyst overheating inactivation, but high recycle ratio need increase the equipment and the pipeline investment of corresponding methyl alcohol circle synthesis, and increases power and energy consumption.Calculating shows that with coal be the synthesis gas that raw material uses Shell coal gasification or Texaco coal water slurry gasification to make, adopt the methanol content that goes out synthetic tower when hanging down recycle ratio can reach more than 50%, and existing typical methyl alcohol synthesizes the tower methanol content and has only about 5%, only be above-mentioned 1/10th, document show " as adopting Lurgi method recycle ratio is 5, goes out tower methanol content 5～6%; Adopting ICI method recycle ratio is 10, goes out tower methanol content 3～4% " (Song Weiduan etc. write, methyl alcohol engineering, Chemical Industry Press, 1991.1,8178), high recycle ratio has increased difficulty and investment that commercial plant maximizes.
Task of the present utility model is the shortcoming that overcomes above-mentioned prior art, provides to realize low recycle ratio, energy-efficient consersion unit under high concentration unstripped gas, high reaction speed.Below the import from reactor is referred to as reaction gas in the explanation to exit gas course of reaction front and back.
Summary of the invention
Because catalytic reaction is carried out on catalyst and not according to front and back phase uniform velocity, general reactor front portion is from balanced remote, reaction speed is fast, it is also many to emit reaction heat, the rear portion is with reacting near balance, reaction speed slows down, it is also few to emit reaction heat, and existing as previously mentioned shell-and-tube water-cooled reactor, the same before and after the temperature of cooling agent, if reduce coolant temperature like this, strengthen heat transfer temperature difference and move heat, reach the heat request that moves of top or anterior high reaction speed and strong reaction heat, then reactor lower part or rear portion reaction heat reduce, move heat and cause reaction temperature to descend, reaction speed is further slowed down below catalyst activity, just stop reaction, therefore be difficult to the way that makes the best of both worlds of accomplishing that the front and rear part reaction is all carried out under optimal reaction temperature greater than reaction heat.The utility model is at this fundamental contradiction, break through existing cooling agent with same temperature, and adopt the different sections of reactor to adopt the different temperatures cooling agent to solve, make the size that heat exchange is shifted out by reaction heat in the reaction need design, a plurality of districts before and after specifically can being divided in proper order by reaction gas flow direction in catalyst layer, come indirect heat exchange by cooling agent by heat exchanger tube, for picture methyl alcohol synthetic reaction, reaction temperature is in 180 ℃～300 ℃ scopes, can adopt pressurized hot water to make thermophore, the sensible heat that the vaporizing liquid heat absorption absorbs far above the cooling medium temperature rise in reactor, then need with the low mineral oil of volatility for high reaction temperature more, conduction oil or fused salt are made cooling agent, heat is taken in the drum by cooling circuit, heat is passed to water generates vapor recovery heat by heat exchanger tube in the drum.Thermophore is removed the methyl alcohol synthesising reacting heat simultaneously directly during byproduct steam when using water as cooling agent, catalyst for methanol can be contained in the heat exchanger tube promptly as the Lurgi shell-and-tube reactor, at this moment heat exchanger tube is a reaction tube, the outer shell side of reaction tube is a boiler water, catalyst also can be contained in outside the heat exchanger tube, at this moment heat exchanger tube is that water pipe is the waterpipe type reactor, and water pipe can be a shell and tube, spiral, and also laterally water pipe is horizontal water-cooled methanol column.The one, different catalysts piece district in front and back adopts the grouping heat exchanger tube, every group of heat exchanger tube can be communicated with a drum of different pressures for vaporization, vapourizing temperature as required, for example reaction is positioned at the vaporization down of the anterior heat exchanger tube mesolow low temperature of reaction in earlier stage, increase the heat transfer temperature difference augmentation of heat transfer, solve the reaction problem that anterior reaction speed is fast, reaction heat is especially big; Be positioned at reaction rear portion catalytic reaction speed and reaction heat and reduce, the corresponding raising of heat exchanging water pipe's pressure for vaporization and temperature reduces heat transfer temperature difference, avoids because of rear portion reaction heat reduces, and moves heat too much, and reaction temperature is spent low.The 2nd, drum pressure can be regulated height, along with the catalyst increase of service time, catalytic reaction advances to the rear portion, when rear portion reaction heat increases, also heat exchanging water pipe's pressure for vaporization in the catalyst of rear portion can be reduced or link, the later stage water pipe is gasified under low-temp low-pressure strengthen heat transfer temperature difference and heat transfer rate with low-pressure drum.Above-mentioned set of heat exchange tubes and pressure regulation drum pressure for vaporization can be chosen between 0.2～13MPa as required, and in the different catalytic reaction pieces district 31,32, heat transfer block district 21,22 coupled pressure regulation drum 51,52 pressure reduction can be at 0.2～7MPa.
The utility model provides a kind of fixed bed composite reaction equipment, mainly by the cylindrical shell 1 of being with end socket, reaction gas inlet 2 on the housing 1 and reaction gas outlet 3, porous gas distributor 4 and porous gas collection plate 5, catalyst layer 6 and cooling medium 7 move the consersion unit of heat exchanger tube 8 compositions of heat, steam pressure control valve 61 is housed, 62 drum 51,52, it is characterized in that catalyst layer 6 is divided into several catalytic reaction piece districts, front and back in proper order according to the mobile direction of reaction gas, wherein have two piece districts 31 at least, constitute heat exchange reaction block district 21 by heat exchanger tube 8 and heat transferring medium 7 respectively in 32,22, wherein the catalyst 6 at least one catalytic reaction piece district is contained in the heat exchanger tube, each heat transfer block district is by the inlet tube 202 of consersion unit cooling medium 7,204 and outlet 201, but 203 link with the drum 51 or 52 of independent regulation pressure for vaporization separately, constitute at least two cooling medium closed circuits that different pressures for vaporization and temperature are arranged, reaction gas reacts with different heat transfer rates in catalytic reaction piece district successively.
The utility model provides a kind of fixed bed composite reaction equipment, can pretend in the heat exchange reaction block district of two various heat exchange temperature successively with catalyst 6, also can adorn different catalysts 6A, 6B respectively, successively on catalyst 6A, carry out the A reaction for reaction gas, on catalyst 6B, carry out the B reaction again, for example synthesis gas carries out the methyl alcohol synthetic reaction earlier on methanol synthesis catalyst under 250 ℃ of temperature, carries out Dehydration of methanol again under 300 ℃ on methanol dehydration catalyst.
Description of drawings
Fig. 1 has two heat transfer block districts respectively with the shell-and-tube composite reaction equipment schematic diagram of drum.
Fig. 2 has three heat transfer block districts respectively with the shell-and-tube composite reaction equipment schematic diagram of drum.
Fig. 3 is the compound composite reaction equipment schematic diagram of shell-water pipe.
Fig. 4 is that heat insulation layer is arranged at the top, the blue shell-water-cooled composite reaction equipment schematic diagram that links of last lower house usage.
Fig. 5 is two shell-and-tube reactor tandem compound schematic diagrames.
Fig. 6 is shell pipe type and water pipe type reactor tandem compound consersion unit schematic diagram.
Fig. 7 has two heat transfer block districts respectively with the shell-and-tube composite reaction equipment schematic diagram that heat exchanger tube is arranged in drum and the drum.
The specific embodiment
Below in conjunction with accompanying drawing the technical solution of the utility model is described in detail.
Fig. 1 has dividing plate to be divided into the shell-and-tube consersion unit schematic diagram in two heat transfer block districts, cylindrical shell 1 by the band end socket, reaction gas inlet 2 on the housing 1 and reaction gas outlet 3, porous gas distributor 4 and porous gas collection plate 5, catalyst layer 6 and cooling medium 7 move the consersion unit of heat exchanger tube 8 compositions of heat, the drum 51,52 of steam pressure control valve 61,62 is housed, also has filler pipe 71,72 to link on the drum.The pipe apparatus with catalyst inside, three tube sheets 11 are arranged in the housing 1,12,13 are separated into two heat transfer block districts 21 with shell side heat transferring medium 7,22 with piece district heat exchanger tube in catalytic reaction piece district 31,32 heat exchange, each heat transfer block district 21,22 have the inlet tube 202 of heat transferring medium, 204 and outlet 201, but 203 respectively with the drum 51 of independent regulation pressure for vaporization separately, 52 link, constitute different pressures for vaporization, the heat transferring medium closed circuit of vapourizing temperature, reaction gas enters the catalyst layer 6 of each reacting replacing heat pipe 8 by import 2, successively in catalytic reaction piece district with different heat transfer rate's reactions.
Fig. 2 has three heat transfer block districts respectively with the shell-and-tube composite reaction equipment schematic diagram of drum, four tube sheets 11 are arranged in the housing 1,12,13,14 are separated into three heat transfer block districts 21 with shell side heat transferring medium 7,22,23 with each piece district heat exchanger tube in catalytic reaction piece district 31,32,33 heat exchange, there is the communicating pipe 41 of band valve to link between the inlet tube 202 in heat transfer block district 21 and the outlet 203 in heat transfer block district 22, inlet tube 202 is linked with the circulating pump 81 that links drum 51 by the pipe 302 of band valve, outlet 203 is linked with drum 52 by the pipe 303 of band valve, there is the communicating pipe 42 of band valve to link between the inlet tube 204 in heat transfer block district 22 and the outlet 205 in heat transfer block district 23, inlet tube 204 is linked with the circulating pump 81 that links drum 51 by the pipe 304 of band valve, outlet 205 is linked with drum 52 by the pipe 305 of band valve, open pipe 304,305 and the valve of communicating pipe 41, blanked-off pipe 302,303 and the valve of communicating pipe 42, connecting to heat transfer block district 21 and 22 is communicated with and drum 51 formation heat transferring medium closed circuits, heat transfer block district 23 and drum 52 constitute the heat transferring medium closed circuit of independent regulation pressures for vaporization, perhaps blanked-off pipe 304,305 and the valve of communicating pipe 41, open pipe 302,303 and the valve of communicating pipe 42, connecting to heat transfer block district 22 and 23 is communicated with and drum 52 formation heat transferring medium closed circuits, heat transfer block district 21 and drum 51 constitute the heat transferring medium closed circuit of independent regulation pressures for vaporization, reaction gas enters laggard heat exchanger tube inner catalyst layer 6 by import 2, under the low heat exchange medium temperature in heat transfer block district 21, react earlier, again in heat transfer block district 22,23 higher heat exchange medium temperature is reaction down, wherein filler pipe 71 among Fig. 2,72 are connected to water circulating pump 81 among the figure, on 82 the water inlet pipe.
Fig. 3 is the compound composite reaction equipment schematic diagram of shell-water pipe.The continuous reactor top of last lower house is that catalyst 6 is contained in the heat exchanger tube 8, the pipe shell journey is the shell-and-tube heat transfer block district 21 and the catalytic reaction piece district 31 of cooling medium 7, the bottom is heat exchanger tube 8 outer dress catalyst 6, in the pipe is tubulation or the helix tube heat transfer block district 22 and the catalytic reaction piece district 32 of cooling medium 7, catalytic reaction piece district 31 up and down, catalyst 6 fuses in 32, pipe cooling medium outside 7 is linked with pressure regulation drum 51 by inlet tube 202 and outlet 201 in the shell cooling heat transferring piece district, top 21, cooling medium 7 is linked with pressure regulation drum 52 by inlet tube 204 and outlet 203 in the interior cooling heat transferring piece district 22 of bottom heat exchanger tube, formation can be regulated the closed circuit of pressure for vaporization and temperature separately, after reaction gas advances tower by import 2, earlier more lowly react to advance again in the waterpipe type pipe of bottom and react under the cooling medium 7 higher pressures for vaporization and coolant temperature at upper tube shell-type shell side pressure for vaporization and chilling temperature.
Fig. 4 structure and mark have much identical with Fig. 3, also be that top is shell-and-tube, the bottom is the composite reaction equipment of waterpipe type, different with Fig. 3 one be among Fig. 4 between top shell section body and bottom water pipe piece housing with 40 lips welderings of flange sealing, convenient maintenance, the 2nd, on tube sheet 11 tops, shell-and-tube reactor top one deck adiabatic catalyst layer 30 is arranged, after being entered by import 2 about 210 ℃ at a lower temperature, reaction gas can comparatively fast be warmed up to optimal reaction temperature.
Fig. 5 is two shell-and-tube reactor tandem compound schematic diagrames.Two pipe apparatus with catalyst inside, shell side is a heat transferring medium, each have steam regulation pressure drum 51,52 shell-and-tube heat transfer reactor A, series combination before and after the B, the gas vent 3 of shell-and-tube reactor layer A is communicated with the gas feed 4 usefulness pipe 100 of reactor B, reaction gas is entered in catalytic reaction piece district 31 pipe inner catalysts by reactor A gas feed 2 and reacts, enter through gas vent 3 and pipe 100 gas feeds 4 again to reactor B, continue reaction in catalytic reaction piece district 32 pipe inner catalysts, the pressure for vaporization of heat transfer block district 21 heat transferring mediums and temperature are lower than the pressure for vaporization and the temperature in heat transfer block district 22 in the reactor B in the reactor A.
Fig. 6 is shell pipe type and water pipe type reactor tandem compound consersion unit schematic diagram.A heat exchanger tube apparatus with catalyst inside 6 is a heat transferring medium 7 outside managing among the figure, it is heat transferring medium 7 that heat transferring medium is adorned outward in catalyst 6 pipes by the shell-and-tube heat transfer reactor A that imports and exports pipe 202,201 and 51 bindings of pressure regulation drum and a pipe, heat transferring medium is by importing and exporting the waterpipe type heat transfer reactor C that pipe 204,203 and pressure regulation drum 52 link, by 101 communicating pipe of pipe the shell-type reactor A outlet 3 and the import 4 of waterpipe type reactor C, shell side cooling heat transferring medium pressure for vaporization and temperature are lower than the pressure for vaporization and the temperature of cooling medium in the waterpipe type reactor C pipe among the shell-and-tube reactor A.
Fig. 7 has two heat transfer block districts respectively with the shell-and-tube composite reaction equipment schematic diagram that heat exchanger tube is arranged in drum and the drum.Fig. 7 structure and mark have much identical with Fig. 1, different with Fig. 1 one is that heat exchanger tube is arranged in the drum among Fig. 7, the 2nd, circulating pump 81,82 is arranged, be used for fused salt and make heat-conducting medium and absorb heat in shell reaction block district and produce steam to drum heat transfer feed-water flashing, arrive the shell reactor after the cooling again.
Embodiment 1:
The utility model composite reaction equipment is used for the methyl alcohol synthetic reaction, uses water as cooling medium, adopts consersion unit shown in Figure 2.Represent that with solid valve valve closes among Fig. 2, hollow valve represents that valve opens.Drum 51 is communicated with heat transfer block district 21 can vaporize under 0.5～3MPa low pressure, and drum 52 is communicated with heat transfer block district 22,23 and can vaporizes under 1～5MPa pressure.Reaction gas is reaction from top to bottom in catalytic reaction piece district 31,32,33, the top reaction speed is big, reaction heat is big, can be 230～280 ℃ of reactions up and down, tens of degree heat transfer temperature differences are arranged inside and outside the heat transfer block district 21, heat transfer block district 22,23 outer catalyst layer reaction heat are little, can be 220～270 ℃ of reactions up and down, heat transfer block district 22,23 inside and outside heat transfer temperature differences are little.Heat transfer block district 21 reaches high reaction hot-zone and matches with Qiang Yire, and 22,23 in heat transfer block district is a low reaction heat and move heat less and match, and reaches isothermal reaction or is undertaken by required optimal reaction temperature distribution.
3.9 meters of reactor diameters, dress C306 copper base catalyst for methanol 50M in φ 42 * 2 pipes
3Converge with Shell method producing synthesis gas from coal and circulating air, pressure 8.8MPa, advance methyl alcohol synthetic reactor through being heated to 220 ℃, first 250 ℃ of synthesizing methanols up and down under 31 catalytic action of synthesis catalytic reaction block district, top, the temperature in this catalytic reaction piece district 31 can be communicated with drums 51 pressures for vaporization by heat transfer block district 21 regulate control.The same heat transfer block district 22,23 that regulates is communicated with drum 52 pressures for vaporization, can make methyl alcohol catalytic reaction piece district 32,33 under 240 ℃ of left and right sides temperature, carry out the methyl alcohol synthetic reaction, at circulating air and virgin gas ratio is 1.0 o'clock, going out the tower methanol content is 21.85%, methyl alcohol is produced 1304 ton per days daily, and data see attached list 1.
When circulating air and virgin gas ratio are reduced to 0.3, synthesis pressure is brought up to 10MPa, and lower catalytic reaction block district 33 goes out the tower methanol concentration and can bring up to 46% when 200～210 ℃ of synthesizing methanols.
Embodiment 2: generate phthalic anhydride (B) with air catalytic oxidation ortho-xylene (A), document shows (ZhuBing Chen chief editor, Chemical Reaction Engineering, Chemical Industry Press, P167), " unstripped gas is air and ortho-xylene mixture; wherein ortho-xylene is 0.8432%, oxygen 20.33%, nitrogen 78.8268% (volume ratio); generating product main reaction reaction heat is 1285KJ/mol, and production side reaction CO, CO
2Reaction heat 4561KJ/mol, use V
2O
5With titanium compound be catalyst, operating pressure 0.1275MPa, with shell-and-tube reactor bore 26mm, pipe range 3m, the fused salt cooling of reaction tube external application pump forced circulation, reaction gas feeding gas concentration 40.8g/m
3, air speed 1500h
-1, during 360 ℃ of temperature of molten salt, when 353 ℃ of inlet gas temperature, the catalytic bed hot(test)-spot temperature is 383.8 ℃ during dark 0.8 meter of bed, is 367 ℃ behind dark 2 meters of the bed; When 357 ℃ of inlet gas temperature, 463 ℃ of the dark 1 meter temperature of bed, surpassing 727 ℃ in the dark 1.05 meters temperature of bed is temperature runaway.
Now adopt Fig. 7 in the utility model, reaction is divided into two heat transfer block districts 21, front and back, 22, two heat transfer block districts each have fused salt with pump with have the drum 51 of heat exchanger tube, 52 force independent loops, advance tower temperature degree and still be 353 ℃, but anterior heat transfer block district 21 temperature of molten salt are 356 ℃, hot(test)-spot temperature is 380 ℃ in the pipe, 24 ℃ of heat transfer temperature differences are promptly arranged, 365 ℃ of heat transfer block district, rear portion 22 temperature of molten salt, the inner reaction tube temperature is 370 ℃, 5 ℃ of heat transfer temperature differences, i.e. reaction speed maximum forwardly, sub-cooled is adopted in the maximum temperature runaway easily of reaction heat zone, improves the cooling medium temperature of molten salt and be difficult for temperature runaway out of control zone at postmedian, thereby the control higher temperature can improve input concentration, increases product yield.
Beneficial effect
Compared with the prior art the utility model has significant advantage, the one, to the different pressures for vaporization and the gasification temperature of reactor different piece catalyst layer set of heat exchange tubes employing heat transferring medium, fast to reaction speed especially, the previous section that reaction heat is big, adopt low vapor pressure vaporization to strengthen heat transfer temperature difference and fully remove reaction heat, make not overtemperature of catalyst, reaction speed and reaction heat smaller portions then adopt higher pressure for vaporization and temperature, avoid moving heat too much, make temperature low excessively, thereby make recycle ratio reduce more than one times than prior art, make methanol synthesis loop tolerance reduce half, thereby reduced the equipment size of synthesizer significantly, both significantly save investment, created advantage for maximizing again.The 2nd, the reduction recycle ratio goes out the methanol column methanol content simultaneously and reaches 10～50%, improve several times than prior art (promptly 3～6%), thereby reaching the circulator power consumption reduces at double with the reduction of recycle ratio, ton alcohol reclaims reaction heat and the byproduct steam amount significantly improves, significantly reduce and be used to cool off the water cooler consumption of cooling-water that reaction gas uses, therefore cut down the consumption of energy significantly, reach energy-saving and cost-reducing remarkable result.The 3rd, the catalyst different parts, temperature can be regulated according to the independence and freedom that requires of reaction, for example realize reaching the optimum temperature line of reaction speed maximum such as synthetic ammonia, and for example react the situation of moving behind the focus according to different times catalyst activity decline before and after the reaction, adjust top and the bottom catalyst layer heat exchanger tube pressure for vaporization, gasification temperature, make catalyst performance optimum efficiency.The 4th, high methanol content in the reaction gas, adopt the fixed bed reactors one-step method from syngas to create condition for producing dimethyl ether, reaction gas than the high several times methanol content of prior art, depress the dimethyl ether content that generates through methanol dehydration catalyst dehydration afterreaction gas up to more than 10% waiting, help the separation of dimethyl ether.
More than by numerous legends and embodiment abundant description done in theme of the present utility model, according to design of the present utility model spirit, those of ordinary skill in the art can easily carry out various variations and be applied in the methyl alcohol dimethyl ether synthesis.The utility model fixed bed composite reaction equipment can link to each other with two drums respectively but is not limited to two, also can be more than three.The water pipe that the combined reactor drum comes can be communicated with the water inlet of water pump forced circulation, also can be without water pump, and with the Natural Circulation water inlet, water inlet pipe and water outlet pipe can be by valve regulated, and the one group of heat exchanger tube that also can not have valve is to a drum.Heat exchanger tube can be that pipe also can be flat tube or heat exchanger plates, and heat transferring medium can be a water, also can be mineral oil, conduction oil or fused salt.
When reaction gas enters catalyst and begins to react, general temperature is lower, so before set of heat exchange tubes, also the adiabatic section can be set, but this adiabatic section catalytic amount should be no more than 1/10th of total amount after reduction is shunk, also the adiabatic section can be set at the catalyst rear portion behind the heat exchange conversion zone.
Claims (8)
1. fixed bed composite reaction equipment, mainly by the cylindrical shell (1) of being with end socket, reaction gas inlet (2) on the housing (1) and reaction gas outlet (3), porous gas distributor (4) and porous gas collection plate (5), catalyst layer (6) and cooling medium (7) move the consersion unit of heat exchanger tube (8) composition of heat, steam pressure control valve (61) is housed, (62) drum (51), (52), it is characterized in that catalyst layer (6) is divided into several catalytic reaction piece districts, front and back in proper order according to the mobile direction of reaction gas, wherein have two piece districts (31) at least, (32) constitute heat exchange reaction block district (21) by heat exchanger tube (8) and heat transferring medium (7) respectively in, (22), wherein the catalyst (6) at least one heat exchange reaction block district is contained in the heat exchanger tube, each heat transfer block district is by the inlet tube (202) of consersion unit cooling medium (7), (204) and outlet (201), (203) but link with the drum of independent regulation pressure for vaporization (51) separately or (52), constitute at least two cooling medium closed circuits that different pressures for vaporization and temperature are arranged, reaction gas is successively in catalytic reaction piece district (31), (32) with different heat transfer rate's reactions.
2. fixed bed composite reaction equipment according to claim 1, it is characterized in that consersion unit is the shell-and-tube reactor of pipe apparatus with catalyst inside, have three tube sheets (11) in the housing (1) at least, (12), (13) shell side heat transferring medium (7) is separated at least two heat transfer block districts (21), (22) with the interior catalytic reaction piece district (31) of piece district heat exchanger tube, (32) heat exchange, each heat transfer block district (21), (22) inlet tube (202) of heat transferring medium is arranged, (204) and outlet (201), (203) but respectively with the drum of independent regulation pressure for vaporization (51) separately, (52) link, constitute different pressures for vaporization, the heat transferring medium closed circuit of vapourizing temperature.
3. fixed bed composite reaction equipment according to claim 1, it is characterized in that consersion unit is the shell-and-tube reactor of pipe apparatus with catalyst inside, have four tube sheets (11) in the housing (1) at least, (12), (13), (14) shell side heat transferring medium (7) is separated at least three heat transfer block districts (21), (22), (23) with the interior catalytic reaction piece district (31) of each piece district heat exchanger tube, (32), (33) heat exchange, there is the communicating pipe (41) of band valve to link between the inlet tube (202) in heat transfer block district (21) and the outlet (203) of heat transfer block district (22), inlet tube (202) is linked with the circulating pump (81) that links drum (51) by the pipe (302) of band valve, outlet (203) is linked with drum (52) by the pipe (303) of band valve, there is the communicating pipe (42) of band valve to link between the inlet tube (204) in heat transfer block district (22) and the outlet (205) of heat transfer block district (23), inlet tube (204) is linked with the circulating pump (81) that links drum (51) by the pipe (304) of band valve, outlet (205) is linked with drum (52) by the pipe (305) of band valve, open pipe (304), (305) and the valve of communicating pipe (41), blanked-off pipe (302), (303) and the valve of communicating pipe (42), connecting to heat transfer block district (21) and (22) is communicated with and drum (51) formation heat transferring medium closed circuit, heat transfer block district (23) and drum (52) constitute the heat transferring medium closed circuit of independent regulation pressure for vaporization, perhaps blanked-off pipe (304), (305) and the valve of communicating pipe (41), open pipe (302), (303) and the valve of communicating pipe (42), connect to heat transfer block district (22) and (23) and be communicated with and drum (52) formation heat transferring medium closed circuit, heat transfer block district (21) and drum (51) constitute the heat transferring medium closed circuit of independent regulation pressure for vaporization.
4. fixed bed composite reaction equipment according to claim 1, it is characterized in that the continuous reactor top of lower house is that catalyst (6) is contained in the heat exchanger tube (8), the pipe shell journey is the shell-and-tube heat transfer block district (21) and the catalytic reaction piece district (31) of cooling medium (7), the bottom is to be the tubulation of cooling medium (7) or helix tube heat transfer block district (22) and catalytic reaction piece district (32) in heat exchanger tube (8) outer dress catalyst (6) pipe, catalytic reaction piece district (31) up and down, (32) catalyst (6) fuses in, pipe cooling medium outside (7) is linked with pressure regulation drum (51) by inlet tube (202) and outlet (201) in the shell cooling heat transferring piece district, top (21), the middle cooling medium (7) in cooling heat transferring piece district (22) is linked with pressure regulation drum (52) by inlet tube (204) and outlet (203) in the heat exchanger tube of bottom, formation can be regulated the closed circuit of pressure for vaporization and temperature separately, and upper tube shell-type shell side pressure for vaporization and temperature are lower than cooling medium (7) pressure for vaporization and temperature in the waterpipe type pipe of bottom.
5. according to each described fixed bed composite reaction equipment in the claim 1 to 5, the housing that it is characterized in that up and down two heat exchange that different pressures for vaporization and temperature arranged and reaction block district directly is connected as a single entity or with the lip weldering sealing binding that has flange (40).
6. fixed bed composite reaction equipment according to claim 1, it is characterized in that two pipe apparatus with catalyst inside, shell side is a heat transferring medium, each have shell-and-tube heat transfer reactor (A), (B) front and back series combination of steam regulation pressure drum (51), (52), the gas vent (3) of shell-and-tube reactor layer (A) is communicated with pipe (100) with the gas feed (4) of reactor (B).
7. fixed bed composite reaction equipment according to claim 1, it is characterized in that outside a heat exchanger tube apparatus with catalyst inside (6) pipe be heat transferring medium (7), heat transferring medium is by importing and exporting pipe (202), (201) adorning outward in catalyst (6) pipe with a pipe with the shell-and-tube heat transfer reactor (A) of pressure regulation drum (51) binding is heat transferring medium (7), heat transferring medium is by importing and exporting pipe (204), (203) the waterpipe type heat transfer reactor (C) that links with pressure regulation drum (52), be communicated with the outlet (3) of shell-and-tube reactor (A) and the import (4) of waterpipe type reactor (C) by pipe (101), shell side cooling heat transferring medium pressure for vaporization and temperature are lower than the pressure for vaporization and the temperature of cooling medium in waterpipe type reactor (C) pipe in the shell-and-tube reactor (A).
8. fixed bed composite reaction equipment according to claim 1 is characterized in that two pressure reduction with the refrigerant vaporizes pressure in the catalytic reaction piece district of different drum cooling medium closed circuits bindings are 0.2～7MPa.
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2008200030276U CN201211474Y (en) | 2008-01-12 | 2008-01-12 | Fixed bed composite reaction equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200030276U CN201211474Y (en) | 2008-01-12 | 2008-01-12 | Fixed bed composite reaction equipment |
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| CN201211474Y true CN201211474Y (en) | 2009-03-25 |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101480592B (en) * | 2008-01-12 | 2012-01-11 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| CN101927142B (en) * | 2009-06-18 | 2013-06-26 | 中国石油化工股份有限公司 | A tubular fixed bed reactor system |
| CN103566836A (en) * | 2013-11-25 | 2014-02-12 | 南京国昌化工科技有限公司 | Uniform-temperature hydrogenation reactor |
| CN103657559A (en) * | 2013-12-21 | 2014-03-26 | 兖矿集团有限公司 | Pilot plant for synthesizing methanol under catalytic effect of catalyst |
| CN103908929A (en) * | 2012-12-29 | 2014-07-09 | 新煤化工设计院（上海）有限公司 | Combined heat exchange type multi-shell side methanol-to-olefin fixed bed production equipment and production method thereof |
| CN107875980A (en) * | 2017-11-03 | 2018-04-06 | 中国科学院山西煤炭化学研究所 | A kind of fixed bed Fischer-Tropsch synthesis device and its application |
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2008
- 2008-01-12 CN CNU2008200030276U patent/CN201211474Y/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101480592B (en) * | 2008-01-12 | 2012-01-11 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| CN101927142B (en) * | 2009-06-18 | 2013-06-26 | 中国石油化工股份有限公司 | A tubular fixed bed reactor system |
| CN103908929A (en) * | 2012-12-29 | 2014-07-09 | 新煤化工设计院（上海）有限公司 | Combined heat exchange type multi-shell side methanol-to-olefin fixed bed production equipment and production method thereof |
| CN103908929B (en) * | 2012-12-29 | 2016-12-28 | 新煤化工设计院（上海）有限公司 | A kind of methanol-to-olefins fixed bed production equipment combining heat exchange type muitishell and production method thereof |
| CN103566836A (en) * | 2013-11-25 | 2014-02-12 | 南京国昌化工科技有限公司 | Uniform-temperature hydrogenation reactor |
| CN103657559A (en) * | 2013-12-21 | 2014-03-26 | 兖矿集团有限公司 | Pilot plant for synthesizing methanol under catalytic effect of catalyst |
| CN107875980A (en) * | 2017-11-03 | 2018-04-06 | 中国科学院山西煤炭化学研究所 | A kind of fixed bed Fischer-Tropsch synthesis device and its application |
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| C14 | Grant of patent or utility model | ||
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Granted publication date: 20090325 Effective date of abandoning: 20080112 |