CN1623644A - Process and equipment for internal heat exchanging catalytic reaction - Google Patents
Process and equipment for internal heat exchanging catalytic reaction Download PDFInfo
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- CN1623644A CN1623644A CN 200310121904 CN200310121904A CN1623644A CN 1623644 A CN1623644 A CN 1623644A CN 200310121904 CN200310121904 CN 200310121904 CN 200310121904 A CN200310121904 A CN 200310121904A CN 1623644 A CN1623644 A CN 1623644A
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Abstract
A catalytic reaction method and equipment with internal heat exchange is disclosed. Said equipment is composed of a pressure casing with inlet tube on the top and the outlet tube and catalyst discharging outlet at the bottom, an internal tubular heat exchanger on its supporter arranged at the bottom of said casing, and the catalyst outside the tubes and supported by the perforated plate. The heat exchange with gas or water cooling is used for the reaction of methanol, dimethylether, or methylamine for higher reaction efficiency.
Description
Invention field
The present invention is a kind of catalyst reaction device, is used for fluid catalytic reaction and diabatic process, belongs to field of chemical engineering, is specially adapted to synthetic reaction process such as methyl alcohol, hydro carbons, also can be used for building-up processes such as methylamine, ammonia, methane, methyl ether.
The background of invention
For synthetic this class exothermic catalytic reactions such as, methylamine synthetic by methyl alcohol under the pressurization, methyl ether, ammonia, 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 a kind of be that the cold shock of multistage unstripped gas reduces reaction temperature, this reactor has also reduced reactant concentration during because of the unstripped gas cold shock when reducing temperature of reactor, influenced synthetic ratio.The another kind of shell and tube reactor that methyl alcohol synthesizes that is used for as West Germany Lurgi company, unstripped gas enters from the top air inlet and is distributed to each pipe, synthesizing methanol in the dress catalyst layer in pipe, 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 the catalyst filling coefficient is little, and investment is big, and the maximization difficulty is big.
Task of the present invention is the characteristics according to the catalytic exothermic reversible reaction, overcomes the shortcoming of prior art, provides one production capacity is big, catalyst activity is high, the reactor of simple and reliable for structure, good operation performance.
The general introduction of invention
The invention provides a kind of inner heat-exchange catalytic reaction device, the compression shell P of catalyst outlet 5 is arranged and be supported on internal heat exchange tubes courage C on the housing bottom bearing support S by having the top mouth of pipe 1, the bottom mouth of pipe 2, bottom
R, the outer catalyst K of pipe that is supported on bottom catalyst porous bearing plates R forms, and mainly is the heat exchanger tube courage by the concentric multiple cold tube bag C in circle footpath that varies in size
R1, C
R2... suit is formed with one heart, each cold tube bag is by upper conduit A, last endless tube B and the cold pipe C that is attached on the endless tube B constitute, upper conduit A lower end is communicated with last endless tube B, the upper conduit upper end open is also by the stuffing-box G on the dividing plate F in the little cylindrical shell E in housing P upper end, dividing plate F is fastening and use washer sealing by little shell flange H between little cylindrical shell E, the cylindrical shell of compression shell P and upper cover I can seal with lip weldering between big flange Q, upper cover I also can directly weld with straight tube, wherein each cold tube bag middle cooling pipe C is that an end links the U-shaped pipe of going up another upper end open of endless tube, unstripped gas is entered to be distributed in the little cylindrical shell E by top air inlet pipe 1 draws dividing plate F, the air entraining pipe A of stuffing-box G, be distributed to again in the last endless tube B through A and link the cold pipe C of many rows U-shaped that goes up endless tube B, or the cold pipe C of each cold tube bag by connect the lower cooling pipe C that goes up endless tube B and following endless tube D and link under the up cold pipe C of endless tube D upper end open
1Form, lower cooling pipe C gas warp is endless tube D down, again through up cold pipe C
1Go out cold pipe and advance beds K reaction, go out tower through the bottom mouth of pipe 2 again, perhaps the cold pipe C of each cold tube bag all forms by connecting the cold pipe C that goes up endless tube B and following endless tube D, following endless tube D is communicated with downcomer L, L is connected with bottom manifold M, house steward M bottom connecting leg mouth 2, cooling medium such as cold air or water is distributed to each downcomer L by the mouth of pipe 2 through house steward M, respectively arrange cold pipe C through each endless tube D to connecting on the endless tube D again, upwards flow and absorb heat, endless tube B on each again, upper conduit A passes little cylindrical shell upper spacer J and goes up bedding and padding letter G and enter in the little cylindrical shell E and go out reactor through the top-portion apertures mouth of pipe 1 again on the last endless tube, housing P top has the ventilation mouth of pipe 3 to be communicated with catalyst layer K, the bottom mouth of pipe 4 of giving vent to anger, the catalyst layer K of inner heat transfer reactor only is contained in outside the cold pipe of cold tube bag layer, and catalyst layer also can be by cold tube bag layer catalyst layer K
1With lower thermal barrier layer K
2Form, inner heat transfer reactor can be that cylindrical shape porous gas distributor T and porous gas gas collector V are arranged in the housing, and gas is the Radial Flow reaction in catalyst layer K.
Reactor catalyst bed K of the present invention can be fixed bed reactors, also can be three-phase bed or slurry attitude bed, and at this moment gas is advanced by the bottom mouth of pipe 4, flows to be reacted to upper orifice 3 outlets on cold pipe extroversion.
The reactor RA of the present invention use of can connecting with another reactor RB, reactor RA upper orifice 1 of the present invention like this is communicated with reactor RB inlet tube 3, the RA mouth of pipe 3 and the reactor RB mouth of pipe 4 of giving vent to anger is communicated with, gas through first reactor RA cold tube bag heating goes out tower to the second a reactor RB reaction through the mouth of pipe 1, catalyst layer reaction outside second reaction gas advances first reactor RA pipe again goes out tower by the RA bottom mouth of pipe 4 again.Second reactor RB can be water-cooled reactor in the pipe of the present invention, also can be the shell-and-tube reactor of the outer water-cooled of pipe.
Specify below in conjunction with accompanying drawing.
Fig. 1 is a single tube baffling air cooling reactor.
Fig. 2 is a water-cooled gas solid catalytic reactor in the pipe.
Fig. 3 is an adverse current air cooling gas solid catalytic reactor in the pipe.
Fig. 4 is a radially flow process reactor of the interior air cooling of pipe.
Fig. 5 is air cooling reactor and a tubular type water-cooled reaction constitutional diagram in the pipe.
Fig. 6 is air cooling reactor and a shell-and-tube water-cooled reaction constitutional diagram in the pipe.
Fig. 7 is that a reactor schematic diagram is made up in air cooling up and down in tubular type water-cooled and the pipe.
Use below in conjunction with the description of drawings implementation.
Fig. 1 is single tube baffling air cooling reactor. By logical with open top pipe 1 little cylindrical shell E Cross flange H and be connected with cylindrical shell P top casing coupling I, use lip between cylindrical shell P top and the casing coupling I The blue Q of shape welding method connects, as cold tube bag CRNeed maintenance, then take flange apart and hang out cold tube bag. The dividing plate F of stuffing-box G is housed between flange. During as methanol synthesis reactor, material pressure Power 5～13MPa, hydrogeneous, carbon oxide feed gas about about 100 ℃ by open top pipe 1 Advance in the little cylindrical shell E of reactor, enter the upper conduit A that is loaded on stuffing-box G endless tube B on each, Cooling pipe courage CREach lower cooling pipe C1 and pipe outer catalyst layer K and flow heat exchange, arrive behind the lower endless tube D again through upper cooling pipe C2With the outer catalyst layer K countercurrent flow of pipe, go out upper cooling pipe C2Enter Manage outer catalyst layer K reaction, reaction gas goes out bottom escape pipe 2 through porous bearing plates R and goes out instead Answer device, bottom porose 5 is unloaded catalyst for stopping and is used.
Fig. 2 is water-cooled byproduct steam reactor in the pipe, cold tube bag CRCold pipe C by endless tube about upper endless tube B, lower endless tube D and the binding forms, cold tube bag is supported on the support S, lower endless tube D is linked by downcomer L and water inlet manifold M, upper endless tube B is by being communicated with in upper conduit A and the little cylindrical shell E, and hydrogen, carbon oxide feed gas entered reactor through cold tube bag C by inlet tube 3 when methyl alcohol was syntheticROuter catalyst layer reaction, reaction heat is absorbed by water in the cold pipe, goes out catalyst Layer K reaction gas goes out reactor through porous plate R by base apertures 4, boiler water by the bottom mouth of pipe 2, Bottom manifold M is diverted to each cold pipe C through each downcomer L to each time endless tube D, water in the pipe The reaction heat of the outer catalyst layer K of absorption tube produces steam, on flow on each endless tube B through upper In the little cylindrical shell E of conduit A to the dividing plate F, go out tower through upper port again.
Fig. 3 is the reactor of the air cooling of cold pipe adverse current and adiabatic combination. Unstripped gas such as methyl alcohol are synthetic Flow downward the same with Fig. 2 behind the laggard catalyst layer K of raw material gas inlet is earlier at cold tube bag CROuter catalyst layer K1Reaction, again adiabatic catalyst layer K outside lower guide tracheae L2Reaction, Heat insulation layer is established in the bottom can take full advantage of space reactor dress catalyst, improves reactor product Content increases output. The air cooling reactor is synthetic former by the low-temp methanol of about 100 ℃ of low temperature Bottom house steward M is advanced in material gas bottom 2, assigns to each downcomer L and enters lower endless tube D to cold pipe C Upwards flow with more than the outer catalyst layer countercurrent flow to 200 of pipe ℃ endless tube B on each again, warp Upper conduit A exports to dividing plate F and go out tower by 1 between little cylindrical shell E.
Fig. 4 is water-cooled or an air cooling radial flow reactors in the pipe, unstrpped gas is advanced reactor by air inlet 3, cross catalyst layer K through a porous distribution tube T radial flow, be reacted to gas collecting jar with ground-on cover plate V in the porous, reaction gas goes out reactor through catalyst porous bearing plates R to outlet 4, and cooling mediums such as cold air or water upwards flow in the cold pipe of cold tube bag.
Fig. 2, Fig. 3, Fig. 4 respectively have two import mouths of pipe and two outlet mouths of pipe, can be used for two reactor series combination.
Fig. 5 is air cooling reactor RA and tubular type water-cooled reactor RB tandem compound figure in the pipe.For example methyl alcohol is synthetic, and unstripped gas is advanced by the inner heat transfer reactor A of air cooling base apertures 2 in the pipe for about 100 ℃, through cold pipe C
RCourage middle cooling pipe adverse current upwards flows, the outer catalyst layer K reaction gas heat of absorption tube is heated to more than 200 ℃, go out tower through top opening 1 and arrive catalyst layer outside the tubular type water-cooled reactor RB pipe, 200～280 ℃ of reaction temperatures, reaction heat is absorbed by the outer boiler water of reaction tube and produces the Steam Recovery heat, go out tubular type water-cooled reactor gas return the pipe in air cooling reactor RA enter by blow vent 3, catalyst K layer reaction outside air cooling reactor RA pipe, reaction heat is absorbed by cold unstripped gas in the cold pipe of cold tube bag, goes out tower by bottom ports 4 then.
Fig. 6 is air cooling reactor RA and a shell water-cooled reactor RC constitutional diagram in the pipe.For example methyl alcohol is synthetic, and unstripped gas is advanced by the inner heat transfer reactor RA of air cooling base apertures 2 in the pipe for about 100 ℃, through cold tube bag C
RThe middle cooling pipe adverse current upwards flows, the outer catalyst layer K reaction gas heat of absorption tube is heated to more than 200 ℃, go out tower to shell-and-tube reactor RC pipe inner catalyst layer through top opening 1,200～280 ℃ of reaction temperatures, reaction heat is absorbed by the outer boiler water of reaction tube and produces the Steam Recovery heat, go out shell water-cooled reactor gas return the pipe in air cooling reactor RA enter by blow vent 3, boiler water is entered by pipe 1, heat absorption produces steam between catalyst K pipe, by pipe 2 outlets, catalyst K layer reaction outside the air cooling reactor tube, reaction heat is absorbed by cold unstripped gas in the cold pipe of cold tube bag, goes out tower by bottom ports 4 then.
Fig. 7 is that interior water-cooled reactor of pipe and the interior air cooling reactor of pipe are combined into the reactor schematic diagram in the same housing P up and down, gas by air cooling reactor mouth 2 in the lower tube through second line of a couplet pipe M, catalyst layer K countercurrent flow outside cold pipe C of cold tube bag and pipe, be communicated to central tube Y upward to top exit behind the endless tube B on each, be introduced into upper tube water-cooled catalyst layer K1 reaction, arrive bottom air cooled lamp catalyst layer K again
2Reaction, reaction gas goes out tower by base apertures 4, boiler water by import 6 through total endless tube W, divide water conduit N endless tube D under each water-cooled to be diverted to each water cooling tube C, catalyst layer reaction heat also produces steam outside the absorption tube, goes out tower by mouth 7 by conduit A again in the little cylindrical shell E in top again.
Structure of reactor of the present invention also can be used for starching attitude bed and three-phase bed, and primary structure such as Fig. 3 at this moment unstripped gas are reflected at cold tube bag and are carried out outward by bottom port 4 air inlets, and cold tube reaction product goes out tower by upper tube 3.Cooling medium water etc. equally by base apertures 3 through the pipe M to cold tube bag C
RInner cool tube C adverse current makes progress, the outer reaction heat of absorption tube, and generation steam etc. is gone out by the top mouth of pipe 1.
Reactor of the present invention both can rationally utilize reactor by-product middle pressure steam, can save into tower gas heat exchanger investment again, improved production capacity, and device especially suitably maximizes.More than just synthesize example, synthesize, also can be used for dimethyl ether, methylamine, preparing propylene from methanol, ammonia synthesis etc. but be not limited to methyl alcohol with methyl alcohol.
The present invention can illustrate by following examples:
Embodiment: with water-cooled radial reactor RB tandem compound such as Fig. 5 in Fig. 3 air cooling axial flow reactor RA and Fig. 4 pipe, reactor RA internal diameter 4.6M, dress NC307 catalyst for methanol 105M
34.6 meters of reactor RB internal diameters, dress NC307 catalyst 100M
3Under synthesis pressure 9MPA, synthesis gas 88125Kmol/H contains H
267.18%, CO10%, CO
21.5%, CH
4+ N
221%, H
2O0.06%, CH
3OH0.26%, 120 ℃ of temperature, advance the reactor RA mouth of pipe 2, reaction heat is warmed up to 220 ℃ outside the absorption tube in cold tube bag, goes out the RA tower to water-cooled reactor RB reaction by the mouth of pipe, and water absorbed and produces steam in reaction heat was managed, go out 250 ℃ of reactor RB gas temperatures, the outer catalyst layer reaction of air inlet cold reactor RA pipe, going out the tower reaction gas by reactor RA again is 75073Kmol/H, H
260.80%, CO3.74%, CO
21.1%, CH
4+ N
224.65%, H
2O0.73%, CH
3OH9.0%, 210 ℃ of temperature, methanol output 5000 ton per days.
Claims (10)
1. inner heat-exchange catalytic reaction method and apparatus mainly has catalyst to unload the compression shell P of outlet 5 and is supported on internal heat exchange tubes courage C on the housing bottom bearing support S by having the top mouth of pipe 1, the bottom mouth of pipe 2, bottom
R, the outer catalyst K of pipe that is supported on bottom catalyst porous bearing plates R forms, and it is characterized in that heat exchanger tube courage C
RBy the concentric multiple cold tube bag C in circle footpath that varies in size
R1, C
R2... suit is formed with one heart, each cold tube bag by upper conduit A, go up endless tube B and the cold pipe C of many rows that is attached on the endless tube B constitutes, upper conduit A lower end is communicated with last endless tube B, the upper conduit upper end open is also fastening and use washer sealing by little shell flange H between little cylindrical shell E by stuffing-box G, dividing plate F on the dividing plate F in the little cylindrical shell E in housing P upper end, the cylindrical shell of compression shell P and upper cover I seal with lip weldering between big flange Q, or upper cover I directly welds with straight tube.
2. reactor as claimed in claim 1, it is characterized in that each cold tube bag middle cooling pipe C be an end cold pipe C that link to go up the U-shaped pipe of another upper end open of endless tube or each cold tube bag by connect the many rows lower cooling pipe C that goes up endless tube B and following endless tube D and link under the up cold pipe C of many rows of upper end open of endless tube D
1Form.
3. reactor as claimed in claim 1, the cold pipe C that it is characterized in that each cold tube bag all forms by connecting the cold pipe C of many rows that goes up endless tube B and following endless tube D, following endless tube D is communicated with downcomer L, L is communicated with bottom manifold M, the mouth of pipe 2 is arranged at house steward M bottom, other cooling mediums such as cold air or water are distributed to each downcomer L by the mouth of pipe 2 through house steward M, respectively arrange cold pipe C through each time endless tube D to connecting on the endless tube D again, upwards flow and absorb heat, endless tube B on each again, the upper conduit A of endless tube passes little cylindrical shell upper spacer J and goes up bedding and padding letter G and enter in the little cylindrical shell E and go out reactor through the top mouth of pipe 1 again in the binding, housing P top has the mouth of pipe 3 to be communicated to catalyst layer for raw material gas inlet, and there is the mouth of pipe 4 bottom for the reaction gas outlet.
4. according to the described reactor of claim 1 to 3, it is characterized in that catalyst layer K only is contained in outside the cold pipe of cold tube bag layer, the endless tube bottom is fire-resistant pottery Ball support catalyst under the cold tube bag.
5. as the described equipment of claim 1 to 3, it is characterized in that catalyst layer K is by cold tube bag layer catalyst layer K
1One deck adiabatic catalyst layer K with the bottom
2Form.
6. according to the reactor of claim 1 to 3, it is characterized in that having in the housing cylindrical shape porous gas distributor T and porous gas gas collector V, gas is advancing to be in the catalyst layer between tower distributor T and the gas collector V Radial Flow reaction,
7. according to the reactor of claim 3, it is characterized in that catalyst bed K is three-phase bed or slurry attitude bed, gas is advanced by bottom blow vent 4, flows to be reacted to 3 outlets of top blow vent on cold pipe extroversion.
8. according to the reactor of claim 3, it is characterized in that this reactor RA upper opening 1 is communicated with tubular type water-cooling type RB Reactor inlet 3 axially or radially, RA opening 3 is communicated with tubular type water-cooling type reactor RB outlet 4, going out tower through the gas of first reactor RA cold tube bag heating through opening 1 reacts to reactor RB, the reaction gas outer catalyst layer reaction of air inlet cold reactor RA pipe again goes out tower by bottom ports 4 again.
9. according to the reactor of claim 3, it is characterized in that this reactor RA upper opening 1 is communicated with shell-and-tube water-cooling type reactor RC import 3, opening 3 is communicated with shell water-cooling type reactor outlet 4, going out tower through the gas of reactor RA cold tube bag heating through opening 1 reacts to shell water-cooling type reactor RC, reaction gas goes out the tower outer catalyst layer reaction of air inlet cold reactor RA pipe again by RC, goes out tower by RA bottom ports 4 again.
10. according to the reactor of claim 3, in it is characterized in that managing in water-cooled reactor and the pipe air cooling reactor be combined into up and down in the same housing P, gas by air cooling reactor mouth 2 in the lower tube through second line of a couplet pipe M, catalyst layer K outside the cold pipe C of cold tube bag and pipe
2Countercurrent flow, be communicated to central tube Y upward to top exit behind the endless tube B on each, be introduced into water-cooled catalyst layer K1 reaction in the upper tube, arrive air cooling catalyst layer K reaction in the lower tube again, reaction gas goes out tower by base apertures 4, boiler water is diverted to each water cooling tube through total endless tube W, branch water conduit N to each time endless tube D by import 6, and the outer catalyst layer reaction heat of absorption tube also produces steam, goes out tower by mouth 7 by conduit A again in the little cylindrical shell E in top again.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101219041A CN100386138C (en) | 2003-12-06 | 2003-12-06 | Process and equipment for internal heat exchanging catalytic reaction |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2003101219041A CN100386138C (en) | 2003-12-06 | 2003-12-06 | Process and equipment for internal heat exchanging catalytic reaction |
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| Publication Number | Publication Date |
|---|---|
| CN1623644A true CN1623644A (en) | 2005-06-08 |
| CN100386138C CN100386138C (en) | 2008-05-07 |
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| CNB2003101219041A Expired - Fee Related CN100386138C (en) | 2003-12-06 | 2003-12-06 | Process and equipment for internal heat exchanging catalytic reaction |
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Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103111239A (en) * | 2011-11-16 | 2013-05-22 | 西安核设备有限公司 | Gas-cooled methanol reactor |
| CN104399413A (en) * | 2014-11-18 | 2015-03-11 | 安徽新月化工设备有限公司 | Controllable heat-removing reactor |
| CN104930548A (en) * | 2015-06-07 | 2015-09-23 | 大连理工大学 | Stove type water heater |
| CN105062593A (en) * | 2015-08-18 | 2015-11-18 | 中国神华能源股份有限公司 | Methane preparation technological system |
| CN105218310A (en) * | 2015-10-23 | 2016-01-06 | 湖南安淳高新技术有限公司 | Methanol-fueled CLC reactive system and methanol-fueled CLC reaction method |
| CN106732311A (en) * | 2017-01-23 | 2017-05-31 | 南京敦先化工科技有限公司 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
| CN107670592A (en) * | 2017-10-10 | 2018-02-09 | 湖南安淳高新技术有限公司 | A kind of shell-and-tube reactor and methanol synthesizing process |
| CN109173937A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | Temperature-changeable methanol synthesis reaction system |
| CN110090602A (en) * | 2019-05-28 | 2019-08-06 | 中国神华煤制油化工有限公司 | A kind of hydrogenation reaction system |
| CN110143883A (en) * | 2019-05-28 | 2019-08-20 | 中国神华煤制油化工有限公司 | A kind of process for selective hydrogenation |
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| CN101703910B (en) * | 2009-08-20 | 2012-10-17 | 上海国际化建工程咨询公司 | Built-in cold wall type shift reactor for heat exchanger and direction connection structure for shift reactor and downstream heat exchanging equipment |
Family Cites Families (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2063942U (en) * | 1990-01-25 | 1990-10-17 | 浙江工学院 | Soaking temperature carbinol tower |
| CN2093693U (en) * | 1991-06-29 | 1992-01-22 | 南京化学工业(集团)公司设计院 | Combination cool pipes-type inside heat-exchanging catalytic reactor |
| CN1129205A (en) * | 1995-02-15 | 1996-08-21 | 楼寿林 | Energy-saving cold-tube type reactor for synthesizing methanol |
| CA2337824C (en) * | 1998-07-09 | 2006-01-24 | Washington Group International, Inc. | Radial flow reactor |
| CN2347653Y (en) * | 1998-08-21 | 1999-11-10 | 杭州林达工业技术设计研究所 | Synthetic tower internal member with cover plate and barrel sealing structure |
| CN2350120Y (en) * | 1998-09-14 | 1999-11-24 | 杭州林达工业技术设计研究所 | Thermal balance high-pressure energy-saving reactor |
| CN1320478A (en) * | 2000-04-24 | 2001-11-07 | 杭州林达化工技术工程有限公司 | Low-temp difference exothermic catalytic gas-solid phase reactor |
| CN1202061C (en) * | 2002-08-29 | 2005-05-18 | 华东理工大学 | Method for catalytic synthesising dimethyl ether in combined bed |
| CN2680348Y (en) * | 2003-12-06 | 2005-02-23 | 杭州林达化工科技有限公司 | Catalytic reactor with interior heat exchange |
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2003
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| CN103111239A (en) * | 2011-11-16 | 2013-05-22 | 西安核设备有限公司 | Gas-cooled methanol reactor |
| CN103111239B (en) * | 2011-11-16 | 2015-09-30 | 西安核设备有限公司 | A kind of air cooling methanol reactor |
| CN104399413A (en) * | 2014-11-18 | 2015-03-11 | 安徽新月化工设备有限公司 | Controllable heat-removing reactor |
| CN104930548A (en) * | 2015-06-07 | 2015-09-23 | 大连理工大学 | Stove type water heater |
| CN105062593A (en) * | 2015-08-18 | 2015-11-18 | 中国神华能源股份有限公司 | Methane preparation technological system |
| CN105218310A (en) * | 2015-10-23 | 2016-01-06 | 湖南安淳高新技术有限公司 | Methanol-fueled CLC reactive system and methanol-fueled CLC reaction method |
| CN105218310B (en) * | 2015-10-23 | 2017-06-13 | 湖南安淳高新技术有限公司 | Methanol synthesis reaction device and methanol synthesis reaction method |
| CN106732311A (en) * | 2017-01-23 | 2017-05-31 | 南京敦先化工科技有限公司 | A kind of spherical cavity header coil pipe reactor of water route Natural Circulation |
| CN107670592A (en) * | 2017-10-10 | 2018-02-09 | 湖南安淳高新技术有限公司 | A kind of shell-and-tube reactor and methanol synthesizing process |
| CN107670592B (en) * | 2017-10-10 | 2023-12-05 | 湖南安淳高新技术有限公司 | Shell-and-tube reactor and methanol synthesis process |
| CN109173937A (en) * | 2018-09-30 | 2019-01-11 | 中石化宁波工程有限公司 | Temperature-changeable methanol synthesis reaction system |
| CN109173937B (en) * | 2018-09-30 | 2021-06-11 | 中石化宁波工程有限公司 | Temperature-variable methanol synthesis reaction system |
| CN110090602A (en) * | 2019-05-28 | 2019-08-06 | 中国神华煤制油化工有限公司 | A kind of hydrogenation reaction system |
| CN110143883A (en) * | 2019-05-28 | 2019-08-20 | 中国神华煤制油化工有限公司 | A kind of process for selective hydrogenation |
| CN110090602B (en) * | 2019-05-28 | 2022-06-21 | 中国神华煤制油化工有限公司 | Hydrogenation reaction system |
| CN110143883B (en) * | 2019-05-28 | 2023-03-03 | 中国神华煤制油化工有限公司 | Hydrogenation reaction method |
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|---|---|
| CN100386138C (en) | 2008-05-07 |
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