CN101491751B - Heat-exchange catalytic reaction device - Google Patents
Heat-exchange catalytic reaction device Download PDFInfo
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- CN101491751B CN101491751B CN2008100044324A CN200810004432A CN101491751B CN 101491751 B CN101491751 B CN 101491751B CN 2008100044324 A CN2008100044324 A CN 2008100044324A CN 200810004432 A CN200810004432 A CN 200810004432A CN 101491751 B CN101491751 B CN 101491751B
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- pipe
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- housing
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- 238000006555 catalytic reaction Methods 0.000 title claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 51
- 239000003054 catalyst Substances 0.000 claims abstract description 34
- 238000007789 sealing Methods 0.000 claims description 13
- 230000006835 compression Effects 0.000 claims description 4
- 238000007906 compression Methods 0.000 claims description 4
- 230000027455 binding Effects 0.000 claims description 3
- 238000009739 binding Methods 0.000 claims description 3
- 239000011148 porous material Substances 0.000 claims description 2
- 239000002002 slurry Substances 0.000 claims description 2
- 238000006276 transfer reaction Methods 0.000 claims 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 48
- 238000006243 chemical reaction Methods 0.000 abstract description 17
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 abstract description 10
- 239000002826 coolant Substances 0.000 abstract description 5
- BAVYZALUXZFZLV-UHFFFAOYSA-N Methylamine Chemical compound NC BAVYZALUXZFZLV-UHFFFAOYSA-N 0.000 abstract description 4
- 229930195733 hydrocarbon Natural products 0.000 abstract description 3
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 3
- 230000002194 synthesizing effect Effects 0.000 abstract description 3
- 230000008093 supporting effect Effects 0.000 abstract description 2
- 239000004215 Carbon black (E152) Substances 0.000 abstract 1
- 238000007599 discharging Methods 0.000 abstract 1
- 238000004134 energy conservation Methods 0.000 abstract 1
- 239000007788 liquid Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 39
- 238000010521 absorption reaction Methods 0.000 description 6
- 230000015572 biosynthetic process Effects 0.000 description 5
- 238000003786 synthesis reaction Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 239000012495 reaction gas Substances 0.000 description 4
- 125000006850 spacer group Chemical group 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 229910052802 copper Inorganic materials 0.000 description 2
- 239000010949 copper Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 150000003839 salts Chemical class 0.000 description 2
- 239000003643 water by type Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 238000009955 starching Methods 0.000 description 1
- 230000008646 thermal stress Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 238000003466 welding Methods 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 invention relates to a heat-exchange catalytic reaction device, which mainly comprises a pressed shell 5, a heat-exchange pipe group 7, a water inlet pipe 14, a water outlet pipe 18, a catalyst 9 or a slurry-bed catalyst 9, wherein the pressed shell 5 is provided with a top suction pipe opening 1, a catalyst filling hole 1, an air multi-aperture distributing plate 10, a bottom vent port 3 and a catalyst discharging hole 4; the heat-exchange pipe group 7 is supported on a supporting frame 6 at the bottom of the shell; the catalyst 9 is supported at the bottom of a porous air collecting plate 8; or the slurry-bed catalyst 9 is filled between the shell 5 and the heat-exchange pipe group 7. The liquid is used as a cooling medium to remove the reacting heat for the reactions such as synthesizing methanol, dimethyl ether, methylamine, hydrocarbon, and the like. The heat-exchange catalytic reaction device has the advantages of little investment, high yield, energy conservation, consumption reduction and easy upsizing.
Description
Technical field
The present invention is a kind of heat-exchange catalytic 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 methane, methyl ether.
Background technology
For synthetic this type exothermic catalytic reactions such as, methyl ether synthetic by the pressurization methanol, 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.A kind of shell and tube reactor that methyl alcohol synthesizes that is used for like West Germany Lurgi company that in industrial reactor, once widely used, unstripped gas gets into from the top air inlet and is distributed to each pipe, in pipe, adorns synthesizing methanol in the catalyst layer, lateral inflow between pipe.Reaction heat is managed outer boiled water and is moved heat continuously, produces steam and is managed out by the side, 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 a kind of and removes reaction heat with fluid as cooling medium, and production capacity is big, catalyst activity is high, the reactor of simple and reliable for structure, good operation performance.Cooling medium is representative with water in the explanation below, but is not limited to water, can be conduction oil or fused salt.
Summary of the invention
The present invention provides a kind of heat-exchange catalytic reaction device, by having the top air inlet mouth of pipe 1, dress catalyst manhole 2; Gas multihole distributor 10; Gas outlet 3, bottom and the compression shell that unloads catalyst pores 45 be supported on the water-cooled set of heat exchange tubes 7 on the housing bottom bearing support 6, water inlet pipe 14 and outlet pipe 18 are supported on the catalyst 9 of bottom porous gas collection plate 8 or lower clapboard 22 or are loaded on housing 5 and the slurry attitude bed catalyst 9 of 7 of set of heat exchange tubes is formed; It is characterized in that set of heat exchange tubes 7 is made up of distributive pipe 11 and collector pipe 12 and many row heat exchanging water pipes 13 bindings of linking between distributive pipe and the collector pipe; Distributive pipe 11 linked with bottom communicating pipe 15, and communicating pipe 15 links with bottom water inlet pipe 14, and collector pipe 12 linked with top communicating pipe 17; Communicating pipe 17 links with water header 16; Water header 16 links with outlet pipe 18, and outlet pipe 18 is through housing upper end stuffing-box 19 movable sealings, bottom water inlet pipe 14 and housing bottom stuffing-box 20 movable sealings; 53 lip welderings of the big flange of the cylindrical shell 51 of housing 5 and upper cover 52 usefulness sealing, or upper cover 52 directly is connected with cylindrical shell 51.
It is endless tube or straight tube comb with collector pipe 12 that reactor of the present invention connects the distributive pipe 11 of organizing heat exchanging water pipe 13.
From top to bottom become axial flow in the reactor bed of the present invention.
Become Radial Flow in the reactor bed of the present invention from inside to outside or from outside to inside.
In the reactor bed of the present invention by about to from a side direction opposite side lateral flow.
Reactor heat exchanging water pipe of the present invention is pipe or flat tube or heat exchange plate.
Description of drawings
Specify below in conjunction with accompanying drawing.
Fig. 1 is that distributive pipe and collector pipe are the water-cooled reactor sketch map of endless tube.
Fig. 2 is that distributive pipe and collector pipe are the water-cooled reactor sketch map of straight tube comb.
Fig. 3 is the vertical view sketch map in water-cooled reactor heat exchange shown in Figure 2 area under control.
Fig. 4 is a water-cooled radial flow reactors sketch map in the pipe.
The specific embodiment
Below in conjunction with accompanying drawing technical scheme of the present invention is at length explained.
Fig. 1 is that distributive pipe and collector pipe are the water-cooled reactor of endless tube.51 of the top end socket 52 of compression shell 5 and cylindrical shells are fastening with big flange 53 among the figure, and with lip weldering sealing, take apart when flange is blown away the lip weldering and can hang out internals.Air inlet 1 and catalyst load hole 2 are arranged at upper cover 52 tops; Gas multihole distributor 10, housing bottom have gas outlet 3, and catalyst unloads outlet 4; Be welded with heat exchanging water pipe's internals of support plate 6 supportings in the housing; Many row's heat exchanger tubes 13 lower ends are communicated with the annular distributive pipe 11 of concentric suit, and the upper end is connected with the annular collector pipe 12 of concentric suit, and bottom communicating pipe 15 connects distributive pipe 11 and water inlet pipe 14; Between water inlet pipe 14 and housing bottom with stuffing-box 20 movable sealings; Top communicating pipes 17 connect collector pipe 12 and water header 16, and joint collection supply mains 16 outlet pipe 18 is through stuffing-box 19 and end socket 52 sealings, heat exchanger tube 13 outer with housing 5 in be equipped with catalyst 9 be bearing in bottom on the porous gas collection plate 8.Pressure 5～12Mpa when being used for methanol synthesis reactor; About 210 ℃ of the unstripped gas temperature of hydrogeneous, carbon monoxide, carbon dioxide, evenly being distributed through gas distributor 10 by top air inlet 1 gets into catalyst for synthesizing copper based methanol 9 and under 200～300 ℃, carries out the methyl alcohol synthetic reaction, and reaction gas goes out reactor by gas outlet 3 behind porous gas collection plate 8; Be higher than 100 ℃ for example 200 ℃ of left and right sides boiler waters get into by water inlet pipe 14; Be diverted to each distributive pipe 11 through the bottom communicating pipe 15, get into the reaction heat of respectively organizing the outer catalyst layer 9 of absorption tube in the heat exchanger tube 13 again, water heat absorption intensification vaporization under 2～8Mpa pressure; The outer catalyst layer temperature of pipe is evenly had a narrow range of temperature; Steam water interface after top communicating pipe 17 arrives water header 16, goes out reactor by outlet pipe 18 more again to collector pipe 12 in the heat exchanger tube 13; Outlet pipe 18 and upper cover 52 usefulness stuffing-boxes 19 movable sealings can make progress when making heat exchanging water pipe's expanded by heating and freely stretch.
Fig. 2 is that distributive pipe and collector pipe are the straight tube comb, in the bed by about to water-cooled reactor sketch map from a side direction opposite side lateral flow.The upper cover of compression shell 5 has air inlet 1 and catalyst load hole 2 among the figure, and low head has gas outlet 3 and catalyst to unload outlet 4, and end socket and housing directly weld among the figure, but also can adopt Fig. 1 to connect with flange.The heat exchanging water pipe who on bottom support panel 6, has many groups to connect the distributive pipe case 11 and the bobbin carriage 12 that catchments organizes 71,72,73,74,75,76.Bobbin carriage 12 places that catchment on top have the right to open the upper spacer 21 of gas port; Water pipe tank 11 places in lower part have the left side to open the lower clapboard 22 of gas port; Last lower clapboard 21 and 22 have gas multihole distributor 10 and porous gas collection plate 8, outside the heat exchanger tube 13 of 8 of upper spacer 21, lower clapboard 22, gas multihole distributor 10 and porous gas collection plates, catalyst layer 9 are housed.Pressure 5～12Mpa when being used for the dimethyl ether synthesis reactor; About 200 ℃～300 ℃ of the unstripped gas temperature of hydrogeneous, carbon monoxide, carbon dioxide and methyl alcohol; Air inlet 1 gets into the arcuate channel of housing 5 right sides and gas multihole distributor 10 by upper spacer 21 the right blow vents through the top, and evenly distributing through gas multihole distributor 10 gets into catalyst layers 9 and under 200～380 ℃, carry out the dimethyl ether synthetic reaction, and reaction gas goes out reactor by gas outlet 3 after the arcuate channel in porous gas collection plate 8 and housing 5 left sides is by lower clapboard 22 left side blow vents entering; Be higher than 100 ℃ for example 200 ℃ of left and right sides boiler waters get into by water inlet pipe 14; Be diverted to each minute water straight tube comb 11 through the bottom communicating pipe 15, get into the reaction heat of respectively organizing the outer catalyst layer 9 of absorption tubes in the heat exchanger tube 13 again, the water heat absorption heats up and under 2～12Mpa pressure, vaporizes; The outer catalyst layer temperature of pipe is evenly had a narrow range of temperature; Steam water interface after top communicating pipe 17 arrives water header 16, goes out reactor by outlet pipe 18 more again to collector pipe 12 in the heat exchanger tube 13; Outlet pipe 18 and upper cover 52 usefulness stuffing-boxes 19 movable sealings can make progress when making heat exchanging water pipe's expanded by heating and freely stretch.Water inlet pipe 14 seals with stuffing-box 20 with the housing bottom end socket.
Fig. 3 is Fig. 2 heat exchange area under control vertical view sketch map.Among Fig. 3 in six groups of rectangle set of heat exchange tubes 71,72 of 8 of gas multihole distributor 10 and porous gas collection plates ... 76; Corresponding with six groups of set of heat exchange tubes that connect the distributive pipe case 11 and the bobbin carriage 12 that catchments among Fig. 2; Every group of set of heat exchange tubes is three row's heat exchanger tubes 7 among the figure, but more than three rows in actual the use.
Fig. 4 is a water-cooled radial flow reactors in the pipe, and different with Fig. 1 on Fig. 4 structure is the porous gas distributor 23 that cylinder is arranged in housing 5, and the center has the porous gas collecting jar with ground-on cover plate 24 of top seal to link bottom porous gas collection plates 8, and all the other are identical with Fig. 1.Unstrpped gas is advanced reactor by air inlet 1; Cross catalyst layer 9 through porous gas distributor 23 radial flows and be reacted to porous gas collecting jar with ground-on cover plate 24; Reaction gas 3 goes out reactor to the gas outlet behind porous gas collection plate 8, cooling mediums such as water in heat exchanger tube 13 on situation about flowing identical with Fig. 1.
Structure of reactor of the present invention also can be used for starching attitude bed and three-phase bed, primary structure such as Fig. 1, and at this moment unstripped gas is reflected at cold tube bag and is carried out outward by 3 air inlets of the bottom mouth of pipe, and product goes out tower by upper orifice 1.Cooling medium water etc. are made progress to heat exchanger tube 13 adverse currents through lower communicating tube 15, branch water ring pipe 11 by base apertures 14 equally, the outer reaction heat of absorption tube, and generation steam etc. goes out tower through collector pipe 12, top communicating pipe 17, water header 16 and outlet pipe 18 by the top mouth of pipe 18.
Embodiment: with 3.6 meters of Fig. 1 water-cooled reactor internal diameters, dress copper base catalyst for methanol 80M
3Under synthesis pressure 9Mpa, 220 ℃ of synthesis gas temperature are advanced reactor from air inlet 1, and reaction heat is absorbed by water in the heat exchanger tube and produces steam, goes out 250 ℃ of gas reactor temperature, methanol output 2000 ton per days.Under pressure 2～4MPa, boiler water is heated to 220 ℃ and gets into reactor bottom water inlet pipe absorption reaction heat, and methyl alcohol per ton is paid 1.3 tons of producing steams.Related data sees attached list 1.
Subordinate list 1
| Title | Unstripped gas | Advance tower gas | Go out methanol column gas | |
| Tolerance Nm 3/h | 192000 | 800000 | 682481 | |
| Ingredient m ol% | H 2 | 67.20 | 65.64 | 58.94 |
| CO | 28.10 | 10.41 | 4.37 | |
| CO 2 | 3.20 | 2.38 | 2.01 | |
| N 2+CH 3 | 1.50 | 21.16 | 24.80 | |
| H 2O | 0 | 0.07 | 0.87 | |
| CH 3OH | 0 | 0.34 | 9.01 | |
Beneficial effect
The present invention and prior art compare, and the one, adopt movable sealing assembling between internal heat exchange tubes courage and housing, bottom water inlet pipe 14 all assembles the thermal expansion retractable that internals are caused in thermal stress through stuffing-box and housing activity with top outlet pipe 18.Adopt 51 flanges of end socket 52 and cylindrical shell to link sealing; Opening flange and end socket makes things convenient for internals to install or lift out tower; When distributive pipe and the many groups of collector pipe usefulness straight tube bobbin carriage; The one group of group of being more convenient for breaking the whole up into parts is installed, and has avoided the fixing welding of shell-and-tube reactor reaction tube and two ends tube sheet, improves structural reliability; The 2nd, catalyst is adorned cold pipe and is improved catalyst volume filling rate outward, significantly reduces reactor size.Reactor of the present invention in addition both can rationally utilize reactor by-product middle pressure steam, can improve production capacity again, and the device that especially suitably maximizes is produced 600000 ton large-scale reactors per year like top act.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.
More than cooling medium is representative with water in the explanation, but is not limited to water, when the need higher reaction temperatures, can be conduction oil or fused salt.
Claims (7)
1. heat-exchange catalytic reaction device; Mainly by having the top air inlet mouth of pipe (1); Dress catalyst manhole (2), gas multihole distributor (10), gas outlet, bottom (3) are with the compression shell (5) that unloads catalyst pores (4) and be supported on the water-cooled set of heat exchange tubes (7) on the housing bottom support plate (6); Water inlet pipe (14) and outlet pipe (18); Be supported on the catalyst (9) of bottom porous gas collection plate (8) or lower clapboard (22) or be loaded on housing (5) with set of heat exchange tubes (7) between slurry attitude bed catalyst (9) form, it is characterized in that set of heat exchange tubes (7) forms distributive pipe (11) and bottom communicating pipe (15) binding by distributive pipe (11) and collector pipe (12) and many row heat exchanging water pipes (13) binding that links between distributive pipe and the collector pipe; Bottom communicating pipe (15) links with bottom water inlet pipe (14); Collector pipe (12) linked with top communicating pipe (17), and top communicating pipe (17) links with water header (16), and water header (16) links with outlet pipe (18); Outlet pipe (18) is through housing upper end stuffing-box (19) movable sealing; Bottom water inlet pipe (14) and housing bottom stuffing-box (20) movable sealing, the cylindrical shell (51) of housing (5) and upper cover (52) are with lip weldering sealing between big flange (53), or upper cover (52) directly directly is connected with cylindrical shell (51).
2. a kind of catalysis heat transfer reaction unit according to claim 1 is characterized in that connecting distributive pipe (11) and the collector pipe (12) of organizing heat exchanging water pipe (13) is endless tube.
3. a kind of catalysis heat transfer reaction unit according to claim 1 is characterized in that connecting distributive pipe (11) and the collector pipe (12) of organizing heat exchanging water pipe (13) is the straight tube comb.
4. a kind of catalysis heat transfer reaction unit according to claim 1 is characterized in that from top to bottom becoming in the bed axial flow.
5. a kind of catalysis heat transfer reaction unit according to claim 1 is characterized in that becoming from inside to outside or from outside to inside in the bed Radial Flow.
6. a kind of catalysis heat transfer reaction unit according to claim 1, it is characterized in that in the bed by about to from a side direction opposite side lateral flow.
7. a kind of catalysis heat transfer reaction unit according to claim 1 is characterized in that the heat exchanging water pipe is the flat tube of water or heat exchange plate in the pipe.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100044324A CN101491751B (en) | 2008-01-23 | 2008-01-23 | Heat-exchange catalytic reaction device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100044324A CN101491751B (en) | 2008-01-23 | 2008-01-23 | Heat-exchange catalytic reaction device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101491751A CN101491751A (en) | 2009-07-29 |
| CN101491751B true CN101491751B (en) | 2012-04-25 |
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| CN2008100044324A Expired - Fee Related CN101491751B (en) | 2008-01-23 | 2008-01-23 | Heat-exchange catalytic reaction device |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102814149A (en) * | 2012-08-23 | 2012-12-12 | 上海蒙福陇化学工程有限公司 | Methanation furnace for producing methane from coal synthesis gas and production method of methanation furnace |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102059078B (en) * | 2010-11-19 | 2013-06-19 | 航天长征化学工程股份有限公司 | Isothermal radial converter |
| CN104399413B (en) * | 2014-11-18 | 2016-03-16 | 安徽新月化工设备有限公司 | One is controlled moves thermal reactor |
| CN111250000A (en) * | 2020-03-23 | 2020-06-09 | 江苏普格机械有限公司 | Central gas collecting pipe of shift converter |
| CN111514827B (en) * | 2020-04-26 | 2022-04-01 | 太原科技大学 | Processing device and processing method for preparing methane from synthesis gas |
| CN113509894B (en) * | 2021-07-22 | 2023-04-14 | 中冶赛迪工程技术股份有限公司 | Moving bed gas-solid radial reactor |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1857766A (en) * | 2005-04-30 | 2006-11-08 | 杭州林达化工技术工程有限公司 | Heat exchanging reactor |
| CN201171976Y (en) * | 2008-01-23 | 2008-12-31 | 杭州林达化工技术工程有限公司 | Heat-exchange catalytic reaction device |
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- 2008-01-23 CN CN2008100044324A patent/CN101491751B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1857766A (en) * | 2005-04-30 | 2006-11-08 | 杭州林达化工技术工程有限公司 | Heat exchanging reactor |
| CN201171976Y (en) * | 2008-01-23 | 2008-12-31 | 杭州林达化工技术工程有限公司 | Heat-exchange catalytic reaction device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102814149A (en) * | 2012-08-23 | 2012-12-12 | 上海蒙福陇化学工程有限公司 | Methanation furnace for producing methane from coal synthesis gas and production method of methanation furnace |
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| CN101491751A (en) | 2009-07-29 |
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