CN100386138C - 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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- CN100386138C CN100386138C CNB2003101219041A CN200310121904A CN100386138C CN 100386138 C CN100386138 C CN 100386138C CN B2003101219041 A CNB2003101219041 A CN B2003101219041A CN 200310121904 A CN200310121904 A CN 200310121904A CN 100386138 C CN100386138 C CN 100386138C
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Abstract
The present invention relates to a catalysis reactor for internal heat exchange, which is mainly composed of a pressure shell P with a top opening tube 1 and a bottom outlet tube 2, an internal heat exchange tube liner CR and a catalyst K outside the tube, wherein the bottom of the pressure shell P is provided with a catalyst discharge outlet 5; the internal heat exchange tube liner CR is supported on a supporting rack S arranged on the bottom of the shell; the catalyst K is supported on a multi-hole supporting board R, and the catalyst is arranged at the bottom of the multi-hole supporting board R. The air-cooling and water-cooling heat exchange or the air-cooling and water-cooling heat exchange is combined to be used for reaction of methanol, dimethyl ether, methylamine, etc. The present invention has the purposes to enhance the reaction efficiency and the production, save the power consumption and realize large-scale production.
Description
Technical 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.
Background technology
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 pipe apparatus with catalyst inside layer, lateral inflow between pipe.Reaction heat is managed outer boiled water and is moved heat continuously, produces steam and is gone out by the side pipe, and reaction gas goes out tower by the bottom escape pipe, and this tower has a narrow range of temperature, but the catalyst packing factor 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 content 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 heat exchanger tube courage C
RForm by the concentric circle footpath concentric suit of multiple cold tube bag that varies in size, 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, upper conduit A 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, fastening and use washer sealing between dividing plate F and little cylindrical shell E by little shell flange H, the cylindrical shell of housing P and upper cover I can weld sealing with lip between big flange Q, and upper cover I also can directly weld with straight tube.
In a better example of the present invention, each cold tube bag middle cooling pipe C of described reactor is that an end links the U-shaped pipe of going up another upper end open of endless tube B, unstripped gas is entered by the top mouth of pipe 1 and is distributed to the upper conduit A that draws dividing plate F, stuffing-box G in the little cylindrical shell E, is distributed to the cold pipe C of many rows U-shaped that endless tube B is gone up in binding through upper conduit A again in last endless tube B.
In another better example of the present invention, the cold pipe C of each cold tube bag of described reactor is by connecting the many rows lower cooling pipe C that goes up endless tube B and following endless tube D and linking the up cold pipe C of endless tube D upper end open down
1Form, gas advances endless tube D down through lower cooling pipe C, again through up cold pipe C
1Go out cold pipe and advance catalyst layer K reaction, go out tower through the bottom mouth of pipe 2 again.
In another better example of the present invention, the cold pipe C of each cold tube bag of described reactor 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, downcomer 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 bottom mouth of pipe 2 through house steward M, respectively arrange cold pipe C to connecting down on the endless tube through each 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 F and goes up stuffing-box 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 K for raw material gas inlet, and there is the mouth of pipe 4 bottom for the reaction gas outlet.
In another better example of the present invention, the catalyst layer K of described reactor only is contained in outside the cold pipe of cold tube bag layer, also can be by cold tube bag layer catalyst layer K
1With lower thermal barrier catalyst layer K
2Form.
In another better example of the present invention, cylindrical shape porous gas distributor T and porous gas gas collector V are arranged in the described reactor shell, gas is advancing to be among the catalyst layer K between tower distributor T and the gas collector V Radial Flow reaction.
In another better example of the present invention, the catalyst layer K of described reactor 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.
In another better example of the present invention, described reactor can be air cooling reactor RA and another axially or radially tubular type water-cooled reactor RB use of connecting in the pipe, the air cooling reactor RA top mouth of pipe 1 is communicated with tubular type water-cooled reactor RB upper orifice 3 in the pipe, air cooling reactor RA upper orifice 3 is communicated with the tubular type water-cooled reactor RB bottom mouth of pipe 4 in the pipe, the gas of air cooling reactor RA cold tube bag heating goes out tower to tubular type water-cooled reactor RB reaction through the top mouth of pipe 1 in managing, reaction gas is through the outer catalyst layer reaction of air cooling reactor RA pipe in the inlet pipe again of the tubular type water-cooled reactor RB bottom mouth of pipe 4, and the mouth of pipe 4 goes out tower bottom air cooling reactor RA in the pipe again.Tubular type water-cooled reactor RB can be a 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.
Description of drawings
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 reactor constitutional diagram in the pipe.
Fig. 6 is air cooling reactor and a shell-and-tube water-cooled reactor 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 passing through flange H and shell with the top mouth of pipe 1 little cylindrical shell E Body P upper cover I connects, is tightly connected with lip weldering between big flange Q between housing P top and the upper cover I, 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, raw gas pressure 5～13MPa, hydrogeneous, carbon oxide feed gas about 100 Advanced in the little cylindrical shell E of reactor by the top mouth of pipe 1 about ℃, enter the upper conduit A that is loaded on stuffing-box G and arrive each Upper endless tube B, cooling pipe courage CREach lower cooling pipe C and pipe outer catalyst layer K and flow heat exchange, arrive behind the lower endless tube D again through upper cooling pipe C1With the outer catalyst layer K countercurrent flow of pipe, go out upper cooling pipe C1Enter the outer catalyst of pipe Layer K reaction, reaction gas goes out the bottom mouth of pipe 2 through porous bearing plates R and goes out reactor, and there is outlet 5 bottom for stopping Car unloads catalyst and uses.
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 upper orifice 3 when methyl alcohol was syntheticROuter catalyst layer K reaction, reaction heat Absorbed by water in the cold pipe, go out catalyst layer K reaction gas and go out reactor through porous bearing plates R by the bottom mouth of pipe 4, Boiler water is diverted to each cold pipe C through each downcomer L to each time endless tube D by the bottom mouth of pipe 2, bottom manifold M, The reaction heat of the outer catalyst layer K of water absorption tube produces steam in the pipe, on flow on each endless tube B through upper conduit In the little cylindrical shell E of A to the dividing plate F, go out tower through the top mouth of pipe 1 again.
Fig. 3 is the reactor of the air cooling of cold pipe adverse current and adiabatic combination. Unstripped gas such as methyl alcohol synthetic raw gas are by upper Section's mouth of pipe 3 enters flow downward the same with Fig. 2 behind the catalyst layer K, earlier at cold tube bag CROuter catalyst layer K1Reaction, again adiabatic catalyst layer K outside lower guide tracheae L2Heat insulation layer is established in reaction, bottom can be fully sharp Fill catalyst with space reactor, improve and reactor product content, increase output. The air cooling reactor is by low The low-temp methanol synthetic raw gas bottom mouth of pipe 2 that temperature is about 100 ℃ advances house steward M, assigns to each downcomer L and advances Entering lower endless tube D upwards flows with more than the outer catalyst layer countercurrent flow to 200 of pipe ℃, again on each to cold pipe C Endless tube B exports between dividing plate F and little cylindrical shell E through upper conduit A and to go out tower by the top mouth of pipe 1.
Fig. 4 is water-cooled or air cooling radial flow reactors in the pipe, and unstrpped gas is advanced reactor by upper orifice 3, Cross catalyst layer K to porous gas gas collector V through porous gas distributor T radial flow, reaction gas is through catalysis Agent porous bearing plates R goes out reactor to the bottom mouth of pipe 4, and the cooling mediums such as cold air or water are at the cold pipe of cold tube bag Interior upwards mobile.
Fig. 2, Fig. 3, Fig. 4 respectively have two import mouths of pipe and two outlet mouths of pipe, can be used for two reactors Series combination.
Fig. 5 is air cooling reactor RA and pipe-type water-cooling reactor RB tandem compound figure in the pipe. For example methyl alcohol closes Become, about 100 ℃ of unstripped gas is entered by the air cooling reactor RA bottom mouth of pipe 2 in the pipe, through cold tube bag CRIn cold The pipe adverse current upwards flows, and the outer catalyst layer K reaction gas heat of absorption tube is heated to more than 200 ℃, through head tube Mouth 1 goes out tower catalyst layer K outside pipe-type water-cooling reactor RB pipe, 200～280 ℃ of reaction temperatures, reaction Heat is absorbed by the outer boiler water of reaction tube and produces steam recovery heat, goes out pipe-type water-cooling reactor RB gas and advances The outer catalyst layer K reaction of air cooling reactor RA pipe in the pipe, reaction heat is by cold raw material aspiration in the cold pipe of cold tube bag Receive, go out tower by the bottom mouth of pipe 4 then.
Fig. 6 is air cooling reactor RA and shell-and-tube water-cooled reactor RC constitutional diagram in the pipe. For example methyl alcohol closes Become, about 100 ℃ of unstripped gas is advanced by the inner heat transfer reactor RA of air cooling in the pipe bottom mouth of pipe 2, through cold tube bag CRThe middle cooling pipe adverse current upwards flows, and the outer catalyst layer K reaction gas heat of absorption tube is heated to more than 200 ℃ warp The top mouth of pipe 1 goes out tower to shell-and-tube water-cooled reactor RC pipe inner catalyst layer, 200～280 ℃ of reaction temperatures, Reaction heat is absorbed by the outer boiler water of reaction tube and produces steam recovery heat, goes out shell-and-tube water-cooled reactor RC gas Body returns the interior air cooling reactor RA of pipe and is entered by upper orifice 3, and boiler water is entered by the bottom mouth of pipe 2, Heat absorption produces steam between catalyst layer K pipe, by upper orifice 3 outlets, air cooling reactor RA in pipe Manage outer catalyst layer K reaction, reaction heat is absorbed by cold unstripped gas in the cold pipe of cold tube bag, then by the bottom mouth of pipe 4 go out tower.
Fig. 7 is that the interior water-cooled reactor of pipe and the interior air cooling reactor of pipe are combined into up and down the reactor schematic diagram in the same housing P, gas is by managing the interior air cooling reactor bottom mouth of pipe 2 through lower union M, catalyst layer K countercurrent flow outside the cold pipe C of cold tube bag and pipe, be communicated to behind the endless tube B on each on the central tube Y-direction to top exit, be introduced into water-cooled catalyst layer K in the upper tube1Air cooled lamp catalyst layer K in the lower tube is arrived in reaction again2Reaction, Reaction gas goes out tower by the bottom mouth of pipe 4, and boiler water is encircled to each time through total endless tube W, branch water conduit N by import 6 Pipe D is diverted to each water cooling tube C, and the outer catalyst layer reaction heat of absorption tube also produces steam, again by conduit A to Go out tower by the mouth of pipe 7 again in the little cylindrical shell E in top.
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 4 air inlets of the bottom mouth of pipe, and product goes out tower by upper orifice 3.Cooling medium water etc. equally by the bottom mouth of pipe 2 through house steward 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. goes out tower by the top mouth of pipe 1.
The present invention compared with the prior art, the one, realize optimal reaction temperature by the inside reactor heat exchange, avoided the dilution effect of cold shock formula reactor to product, improved synthetic ratio; The 2nd, the fixing welding of shell-and-tube reactor reaction tube and two ends tube sheet has been avoided in all heat exchanger tube courage and assemblings of housing space bar movable sealing in adopting, and improve structural reliability, and a difficult problem is installed and used in the manufacturing of adopting the little tube structure in upper end to solve large-scale reactor; The 3rd, 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 save into the investment of tower gas heat exchanger again, improved production capacity, especially adapted to the maximization device, as following institute act annual output 1650000 ton large-scale reactors.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.
Main embodiment
The present invention can illustrate by following examples:
Embodiment: with air cooling reactor RA in Fig. 3 pipe and Fig. 4 tubular type water-cooled reactor RB tandem compound such as Fig. 5, air cooling reactor RA internal diameter 4.6M in the pipe, dress NC307 catalyst for methanol 105M
34.6 meters of tubular type water-cooled reactor RB internal diameters, dress NC307 catalyst 100M
3Under synthesis pressure 9MPa, synthesis gas 88125Kmol/H contains H
267.18%, CO 10%, CO
21.5%, CH
4+ N
221%, H
2O 0.06%, CH
3OH 0.26%, 120 ℃ of temperature, the air cooling reactor RA bottom mouth of pipe 2 in the inlet pipe, reaction heat is warmed up to 220 ℃ outside the absorption tube in cold tube bag, goes out tower to tubular type water-cooled reactor RB reaction through the top mouth of pipe 1, water absorbed and produces steam in reaction heat was managed, go out 250 ℃ of tubular type water-cooled reactor RB gas temperatures, return the outer catalyst layer K reaction of air cooling reactor RA pipe in the pipe, go out tower by the air cooling reactor RA bottom mouth of pipe 4 in the pipe at last, reaction gas is 75073Kmol/H, contains H
260.80%, CO 3.74%, CO
21.1%, CH
4+ N
224.65%, H
2O 0.73%, CH
3OH 9.0%, 210 ℃ of temperature, methanol output 5000 ton per days.
Claims (10)
1. inner heat-exchange catalytic reaction device, by have the top mouth of pipe (1), the bottom mouth of pipe (2), bottom have catalyst unload outlet (5) compression shell (P), be supported on the internal heat exchange tubes courage (C on the housing bottom bearing support (S)
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
R) form by the concentric circle footpath concentric suit of multiple cold tube bag that varies in size, each cold tube bag is by upper conduit (A), last endless tube (B) and the cold pipe of many rows (C) that is attached on the endless tube (B) constitute, upper conduit (A) lower end is communicated with last endless tube (B), upper conduit (A) upper end open is also by the stuffing-box (G) on the dividing plate (F) in housing (P) the little cylindrical shell in upper end (E), fastening and use washer sealing between dividing plate (E) and little cylindrical shell (E) by little shell flange (H), the cylindrical shell of housing (P) and upper cover (I) seal with lip weldering between big flange (Q), or upper cover (I) directly welds with straight tube.
2. inner heat-exchange catalytic reaction device according to claim 1, it is characterized in that 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 (B), or the cold pipe (C) of each cold tube bag is by connecting many rows lower cooling pipe (C) of going up endless tube (B) and following endless tube (D) and linking the up cold pipe (C of many rows of the upper end open of endless tube (D) down
1) form.
3. inner heat-exchange catalytic reaction device according to claim 1, the cold pipe (C) that it is characterized in that each cold tube bag is all formed by connecting the cold pipe of many rows (C) of going up endless tube (B) and following endless tube (D), following endless tube (D) is communicated with downcomer (L), downcomer (L) is communicated with bottom manifold (M), the mouth of pipe (2) is arranged at house steward (M) bottom, other 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) to connecting down on the endless tube (D) through each time endless tube (D) again, upwards flow and absorb heat, endless tube (B) is communicated with upper conduit (A) on each again, upper conduit (A) passes stuffing-box (G) on the dividing plate (F) in the little cylindrical shell (E) and enters in the little cylindrical shell (E) and go out reactor through the top mouth of pipe (1) again, housing (P) top has the mouth of pipe (3) to be communicated to catalyst layer (K) for raw material gas inlet, and there is the mouth of pipe (4) bottom for the reaction gas outlet.
4. inner heat-exchange catalytic reaction device according to claim 1 is characterized in that catalyst layer (K) only is contained in outside the cold pipe of cold tube bag layer, and the endless tube bottom is fire-resistant pottery Ball support catalyst under the cold tube bag.
5. inner heat-exchange catalytic reaction device according to claim 1 is characterized in that catalyst layer (K) is by cold tube bag layer catalyst layer (K
1) and one deck adiabatic catalyst layer (K of bottom
2) form.
6. inner heat-exchange catalytic reaction device according to claim 1, it is characterized in that having in the housing cylindrical shape porous gas distributor (T) and porous gas gas collector (V), unstripped gas is crossed catalyst layer (K) through gas distributor (T) radial flow, is reacted to porous gas gas collector (V) and goes out reactor through porous bearing plates (R) to the bottom mouth of pipe (4).
7. inner heat-exchange catalytic reaction device according to claim 1, when it is characterized in that catalyst layer (K) for three-phase bed or slurry attitude bed, gas is advanced by the bottom mouth of pipe (4), flows to be reacted to upper orifice (3) outlet on the cold tube bag extroversion.
8. inner heat-exchange catalytic reaction device according to claim 3, it is characterized in that in this pipe that air cooling reactor (RA) the top mouth of pipe (1) is communicated with tubular type water-cooled reactor (RB) upper orifice (3) axially or radially, interior air cooling reactor (RA) upper orifice (3) of pipe mouth of pipe (4) bottom tubular type water-cooled reactor (RB) is communicated with.
9. inner heat-exchange catalytic reaction device according to claim 3, it is characterized in that air cooling reactor (RA) the top mouth of pipe (1) is communicated with shell-and-tube water-cooled reactor (RC) the top mouth of pipe (3) in this pipe, air cooling reactor (RA) upper orifice (3) is communicated with shell-and-tube water-cooled reactor (RC) the bottom mouth of pipe (4) in the pipe.
10. inner heat-exchange catalytic reaction device according to claim 3, the interior air cooling reactor of water-cooled reactor and pipe is combined into up and down in the same housing (P) in it is characterized in that managing, the air cooling reactor has the bottom mouth of pipe (2) to be communicated with house steward (M) in the lower tube, house steward (M) through the cold pipe of cold tube bag (C) with each on endless tube (B) be communicated to central tube (Y) upward to top exit, boiler water import (6) is communicated with total endless tube (W), total endless tube (W) is communicated to each water cooling tube (C) through a minute water conduit (N) and each time endless tube (D), and upper conduit (A) is communicated with the top mouth of pipe (1) of the little cylindrical shell in top (E).
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 |
Applications Claiming Priority (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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| Publication Number | Publication Date |
|---|---|
| CN1623644A CN1623644A (en) | 2005-06-08 |
| CN100386138C true CN100386138C (en) | 2008-05-07 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| 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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| CN (1) | CN100386138C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
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| 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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Citations (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 |
| 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 |
| WO2000002655A1 (en) * | 1998-07-09 | 2000-01-20 | Washington Group International, Inc. | Radial flow 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 |
| CN1413974A (en) * | 2002-08-29 | 2003-04-30 | 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 |
-
2003
- 2003-12-06 CN CNB2003101219041A patent/CN100386138C/en not_active Expired - Fee Related
Patent Citations (10)
| 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 |
| WO2000002655A1 (en) * | 1998-07-09 | 2000-01-20 | 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 |
| WO2001091894A1 (en) * | 2000-04-24 | 2001-12-06 | Ren Lou | A gas-solid phase exothermic catalytic reactor with low temperature difference and its process |
| CN1413974A (en) * | 2002-08-29 | 2003-04-30 | 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 |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| 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 |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1623644A (en) | 2005-06-08 |
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