CN201161185Y - Double-layer heat exchange plate-type reactor in parallel - Google Patents
Double-layer heat exchange plate-type reactor in parallel Download PDFInfo
- Publication number
- CN201161185Y CN201161185Y CNU2008200764250U CN200820076425U CN201161185Y CN 201161185 Y CN201161185 Y CN 201161185Y CN U2008200764250 U CNU2008200764250 U CN U2008200764250U CN 200820076425 U CN200820076425 U CN 200820076425U CN 201161185 Y CN201161185 Y CN 201161185Y
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- heat
- basket
- heat exchanger
- plates
- exchanger plates
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- 238000005192 partition Methods 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 51
- 239000007789 gas Substances 0.000 claims description 36
- 239000012530 fluid Substances 0.000 claims description 9
- 235000007164 Oryza sativa Nutrition 0.000 claims description 5
- 235000009566 rice Nutrition 0.000 claims description 5
- 230000005587 bubbling Effects 0.000 claims description 3
- 240000007594 Oryza sativa Species 0.000 claims 1
- 210000001503 joint Anatomy 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- 238000009434 installation Methods 0.000 abstract description 3
- 230000005611 electricity Effects 0.000 abstract 1
- 230000002093 peripheral effect Effects 0.000 abstract 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 15
- 241000209094 Oryza Species 0.000 description 4
- 230000002175 menstrual effect Effects 0.000 description 4
- 230000035939 shock Effects 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000002950 deficient Effects 0.000 description 2
- 230000032683 aging Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000002441 reversible effect Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
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- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The utility model relates to a parallel-connection double-deck heat-exchanging plate reactor which includes an inner cylinder arranged in an outer cylinder body, an accelerant basket and a central pipe provided with an electric heater are arranged in the inner cylinder, a horizontal partition board is arranged in the middle of the inner cylinder, the partition board partitions the inner cylinder into an upper accelerant basket and a lower accelerant basket which are separated from each other, an effective number of heat-exchanging plates are respectively arranged on connecting frames at the bottoms of the accelerant baskets, all the heat-exchanging plates are in parallel arranged in the inner cylinder; the upper end opening of the heat-exchanging plate is connected with the outlet of a general air-inlet loop pipe, and the lower end opening is connected with the inlet of a rising-air pipe. Each heat-exchanging plate consists of two plates with uniform impresses, and the peripheral edges of the two plates are fixedly connected. Since the heat is exchanged by heat-exchanging plates instead of by cool pipes, heat-exchanging plates with various impresses are assembled together to form a set of heat exchanger with ultrahigh heat transfer efficiency which can take the reaction heat away in time, the heat transfer coefficient can be increased by 3-5 times, the gas processing amount is increased, the yield is greatly increased, the operation is convenient and practicable, the manufacture and the installation are convenient and are not limited by the size of an obturating head at the top, additionally the reactor has the advantages of low resistance, low electricity consumption, and automatic accelerant loading and unloading.
Description
Technical field
The utility model relates to chemical industry equipment, is specifically related to the board-like gas-solid catalysis device of a kind of heat exchange.
Technical background
For guaranteeing carrying out continuously of heat-producing chemical reaction, need constantly shift out reaction heat, so that course of reaction is carried out along the optimum temperature curve.As the methyl alcohol reaction of formation is the mutually reversible catalytic exothermic reaction of gas-solid, its reaction heat shifted out multiple mode, wherein present industrial main employing cold-tube type reactor, be that the limit border ring is removed heat, to reach optimum response speed, obtain satisfied output and conversion ratio, and the reactor resistance is reached minimize.The characteristics of this cold-tube type reactor are, because catalyst is aging easily, service life is short, thereby adopt a large amount of catalyst of loading in actual production, strengthen reserve factor, with the prolongation catalyst replacement cycle, thereby increase equipment running resistance and power consumption greatly, reduced the disposal ability of tower.But not only its heat exchange efficiency is lower for the cooler tube bundle heat exchange mode that adopts at present, and catalyst utilizes the yarn number little, and simultaneously, the equipment running resistance is big, investment and production cost height, and have manufacturing, the inconvenient defective of installation.
Summary of the invention
The utility model provides a kind of heat exchange board-like gas-solid catalysis device, to overcome the defective that prior art exists.
The utility model purpose realizes in the following manner: it comprises the inner core that is assemblied in the outer cylinder body the double-deck heat exchange plate-type reactor of this parallel connection, be provided with basket and the central tube that is provided with electric heater in the inner core, it is characterized in that described inner core middle part is provided with a lateral partitions, described dividing plate is separated into upper and lower basket independently separately with inner core, be respectively fitted with the heat exchanger plates of effective quantity on the link of each basket bottom, the upper port of heat exchanger plates taps into the total endless tube outlet of gas, and the lower port of heat exchanger plates connects the riser inlet.
Described heat exchanger plates is made of the metallic plate of two identical impressions respectively, is connected between pairing each periphery of two metallic plates, and the slit between two metallic plates forms the fluid passage.
Impression on the described heat exchanger plates is corrugated, linear, polyline shaped or bubbling shape, when fluid flows through the heat exchanger plates of above-mentioned impression in the crankle mode, on the one hand accelerated rate of flow of fluid and big embankment height heat transfer yarn number, simultaneously prolonged the time that fluid passes through again, the reaction heat that not only can make the catalyst layer gathering makes the plate inner fluid obtain preheating in time by the fluid removal in this heat exchanging plate of heat exchanger simultaneously.
Described heat exchanger plates is arranged in parallel in cylindrical shell or fan-shaped array, or is designed to various forms of arrangements according to other technological requirements.
Described upward basket bottom is a taper porous plate gas collector, and the catalyst downstream line of its lower end joins with a catalyst outlet sleeve after passing down basket.Upper strata zero rice pressing plate is provided with the catalyst that communicates with the lower floor basket and loads pipe, reactor head is provided with the cold shock looped pipeline line that communicates with upper strata basket and lower floor's basket respectively, the upper strata heat exchanger plates connects a layer sub-air chamber through the air inlet pipe that air inlet total endless tube in upper strata communicates, upper strata heat exchanger plates gas vent connects a layer riser, stimulates the menstrual flow upward to go out the reactor lower part outlet through upper strata porous plate gas collector, sleeve pipe, top tank air outlet sleeve, outlet sleeve successively behind the catalyst layer; Lower floor heat exchanger plates gas access is worn layer zero a rice pressing plate, dividing plate, upper strata porous plate gas collector on successively, is gone up the lower floor's air inlet pipe that communicates with upper strata sub-air chamber behind the basket and join through the total endless tube of lower floor's air inlet, and lower floor's heat exchanger plates gas vent goes out reactor lower part through lower floor's porous plate gas collector and sleeve pipe successively and exports after lower floor's riser stimulates the menstrual flow down the basket catalyst layer.
The catalyst downstream line preferably is positioned at the inner core centre, be threaded between catalyst downstream line and catalyst outlet sleeve, contact cooperation between catalyst outlet sleeve and the outlet of lower floor porous plate gas collector lower end, when needs draw off catalyst, the catalyst outlet sleeve is screwed out, catalyst in each basket can be respectively through the outlet of catalyst downstream line and lower floor's taper porous plate gas collector lower end outlet outflow reactor, catalyst outlet sleeve bottom is provided with a gases at high pressure control valve, and this valve is used to regulate two-layer gas flow.
The technological progress that the utility model is obtained: 1. owing to the cold-tube type reactor of a large amount of catalyst of former filling is divided into the reaction tower of parallel connection about in the of two, promptly the former standby catalyst layer in tower bottom is used, making a tower make two towers uses, increase catalyst greatly and utilized the yarn number, significantly reduced the equipment running resistance, the equipment running resistance only is 1/8 of a former tower, greatly reduces investment and production cost simultaneously.2. because heat exchange element changes the heat exchanger plates heat exchange into by cold pipe heat exchange, the heat exchanger plates that is about to various impressions is bolted together and constitutes one group of heat exchanger that heat transfer efficiency is high, the reaction heat that can make the catalyst layer gathering is in time by the fluid removal in this heat exchanger, calculate through reality, its overall heat-transfer coefficient can increase 3～5 times, significantly increased the gas treatment amount, output is significantly increased.3. owing to have the function of automatic loading, unloading catalyst, when needs draw off catalyst, the catalyst outlet sleeve can be screwed out, thereby draw off catalyst fast, and easy to operate feasible, make easy for installation, be not subjected to top end socket size restriction, started new way for current methanol reactor maximizes.
Description of drawings
Below in conjunction with accompanying drawing the utility model is further described.
Fig. 1 is the utility model overall structure schematic diagram.
Fig. 2 is that the A-A of Fig. 1 is to generalized section.
The specific embodiment
As shown in Figure 1 and Figure 2, in existing methyl alcohol synthetic reactor inner core 15, be provided with basket and the central tube 16 that is provided with electric heater, inner core 15 middle parts are provided with a lateral partitions 11, dividing plate 11 is separated into upper and lower independently basket 22a, 22b separately with inner core 15, be respectively fitted with heat exchanger plates 5a, the 5b of effective quantity on the link 14,4 of each basket bottom, each heat exchanger plates 5a, 5b are arranged in parallel in inner core 15, fan-shaped array or be designed to various forms of arrangement modes according to other technological requirements.The upper port of heat exchanger plates 5a connects the outlet of the total endless tube 8a of layer air inlet, and heat exchanger plates 5a lower port connects a layer riser 17a inlet; The upper port of heat exchanger plates 5b connects the outlet of the total endless tube 8b of lower floor's air inlet, and the lower port of heat exchanger plates 5b connects the riser 17b of lower floor inlet. Heat exchanger plates 5a, 5b are made of the metallic plate of two identical overall dimensions and identical impression respectively, be welded to each other between pairing each periphery of two metallic plates and be connected, stay the slit of establishing to form the fluid passage between two metallic plates, stream socket is established at heat exchanger plates 5a, 5b two ends respectively, and the impression on heat exchanger plates 5a, the 5b is corrugated (or linear or polyline shaped or bubbling shape).
Last basket 22a bottom is a taper porous plate gas collector 12, and the catalyst downstream line 6 of its lower end joins with a catalyst outlet sleeve 25 after passing down basket 22b.Catalyst downstream line 6 is positioned at inner core 15 centres, catalyst downstream line 6 adopts with catalyst outlet sleeve 25 and is threaded, contact cooperation between catalyst outlet sleeve 25 and the outlet of lower floor porous plate gas collector 2 lower ends, catalyst outlet sleeve 25 is provided with a gases at high pressure control valve 26.On the zero rice pressing plate 9a of upper strata a catalyst that communicates with the basket 24b of lower floor is set and loads pipe 23, the cold shock looped pipeline line 21b that urceolus 1 top is provided with the cold shock looped pipeline line 21a that communicates with upper strata basket 22a respectively and communicates with the lower floor basket, the air inlet pipe 19 of upper strata heat exchanger plates 5a through communicating with the total endless tube 8a of upper strata air inlet connects layer sub-air chamber 20, and upper strata heat exchanger plates 5a gas vent stimulates the menstrual flow to go up via tedge 17a and goes out the reactor lower part gas vent successively behind upper strata porous plate gas collector 12, top tank air outlet sleeve 7, gas outlet tube 3 after basket 22a goes into catalyst layer; Lower floor heat exchanger plates 5b gas access through the total endless tube 8b of lower floor's air inlet with successively on wear layer zero a rice pressing plate 9b, dividing plate 11, upper strata porous plate gas collector 12, go up the inlet manifold of lower floor 18 who communicates with upper strata sub-air chamber 20 behind the basket 22a and join, the heat exchanger plates 5b of lower floor gas vent goes out reactor lower part gas vent 26 through lower floor's porous plate gas collector 2 and sleeve pipe 25 after going into lower floor's catalyst layer by the riser 17b of lower floor, sub-air chamber of lower floor 10, the basket 22b that stimulates the menstrual flow down successively successively.
Catalyst downstream line 6 is positioned at the centre of inner core 15, catalyst downstream line 6 is threaded with 25 of catalyst outlet sleeves, contact cooperation between catalyst outlet sleeve 25 and the outlet of lower floor porous plate gas collector 2 lower ends, when needs draw off catalyst, catalyst outlet sleeve 25 is screwed out, catalyst in each basket can be respectively through 25 outlets of catalyst downstream line and lower floor's taper porous plate gas collector 2 lower ends outlet outflow reactor, catalyst outlet sleeve 25 bottoms are provided with a gases at high pressure control valve 26, and this valve is used to regulate two-layer gas flow.
During the equipment operation, cold air is gone into reactor by the upper gas import of urceolus 1, through inner core 15, after the annular space preheating that urceolus is 1 by entering upper strata sub-air chamber 20 behind the central tube 16 heated air heating reduction catalyst of cold air air inlet pipe 13 through electric heater is housed, flow into upper strata inlet manifold 19 and the inlet manifold of lower floor 18 then respectively, again respectively through endless tube 8a, 8b enters the heat exchanger plates 5a of each layer, 5b, after cold air and the bed heat exchange, heat exchanger plates 5a, cold air temperature raises in the 5b, again respectively through last, go into catalyst layer behind riser 17a of lower floor and the 17b, reacted methyl alcohol gas is successively respectively via gas collector 12 and 2, sleeve pipe 7 and 25, gas outlet tube 3 and sleeve pipe 25 back outflow reactors.
Except that above-mentioned methyl alcohol synthetic reactor embodiment, those skilled in the art or those skilled in the art also can be used for the utility model other any form cold-tube type reactor, this should understand is in scope of the present utility model, is subjected to the restriction of the utility model claim.
Claims (6)
1. double-deck heat exchange plate-type reactor of parallel connection, it comprises the inner core (15) that is assemblied in the outer cylinder body (1), be provided with basket and the central tube (16) that is provided with electric heater in the inner core (15), it is characterized in that described inner core (15) middle part is provided with a lateral partitions (11), described dividing plate (11) is separated into inner core (15), following basket (22a independently separately, 22b), the link (14 of each basket bottom, 4) be respectively fitted with the heat exchanger plates (5a of effective quantity on, 5b), and heat exchanger plates (5a, upper port 5b) taps into the total endless tube outlet of gas, (5a, lower port 5b) connects the riser inlet to heat exchanger plates.
2. the double-deck heat exchange plate-type reactor of parallel connection according to claim 1, it is characterized in that described heat exchanger plates (5a, 5b) be made of the butt joint of the metallic plate of two identical impressions respectively, be connected between each periphery that two metallic plates are docked, the slit between two metallic plates forms the fluid passage.
3. the double-deck heat exchange plate-type reactor of parallel connection according to claim 2 is characterized in that (5a, 5b) impression on is corrugated, linear, polyline shaped or bubbling shape to described heat exchanger plates.
4. according to claim 1, the double-deck heat exchange plate-type reactor of 2 or 3 described parallel connections, (5a 5b) is arranged in parallel or fan-shaped array in cylindrical shell (1) to it is characterized in that described heat exchanger plates.
5. the double-deck heat exchange plate-type reactor of parallel connection according to claim 4, it is characterized in that described upward basket (22a) bottom is a taper porous plate gas collector (12), the catalyst downstream line (6) of its lower end passes down basket (22b) back and joins with a catalyst outlet sleeve (25), and upper strata zero rice plate (9a) is provided with the catalyst that communicates with lower floor basket (22b) and loads pipe ().
6. the double-deck heat exchange plate-type reactor of parallel connection according to claim 5 is characterized in that cylindrical shell (1) bottom is equipped with gases at high pressure control valve (26).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200764250U CN201161185Y (en) | 2008-03-07 | 2008-03-07 | Double-layer heat exchange plate-type reactor in parallel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200764250U CN201161185Y (en) | 2008-03-07 | 2008-03-07 | Double-layer heat exchange plate-type reactor in parallel |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201161185Y true CN201161185Y (en) | 2008-12-10 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008200764250U Expired - Lifetime CN201161185Y (en) | 2008-03-07 | 2008-03-07 | Double-layer heat exchange plate-type reactor in parallel |
Country Status (1)
| Country | Link |
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| CN (1) | CN201161185Y (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101966440A (en) * | 2010-10-19 | 2011-02-09 | 西北大学 | Cambered plate type gas-solid phase reactor |
| CN102872767A (en) * | 2012-10-23 | 2013-01-16 | 上海戊正工程技术有限公司 | Industrialized plate type reactor for carbonylating and coupling to synthesize ester |
| CN102895922A (en) * | 2012-10-23 | 2013-01-30 | 上海戊正工程技术有限公司 | Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester |
-
2008
- 2008-03-07 CN CNU2008200764250U patent/CN201161185Y/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101966440A (en) * | 2010-10-19 | 2011-02-09 | 西北大学 | Cambered plate type gas-solid phase reactor |
| CN101966440B (en) * | 2010-10-19 | 2012-11-07 | 西北大学 | Cambered plate type gas-solid phase reactor |
| CN102872767A (en) * | 2012-10-23 | 2013-01-16 | 上海戊正工程技术有限公司 | Industrialized plate type reactor for carbonylating and coupling to synthesize ester |
| CN102895922A (en) * | 2012-10-23 | 2013-01-30 | 上海戊正工程技术有限公司 | Industrial plate type reactor for preparing glycol by hydrogenating oxalate or preparing alcohol by hydrogenating ester |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Shijiazhuang Zhengyuan Towers Equipment Co., Ltd. Assignor: Qian Jinhua Contract fulfillment period: 2009.9.25 to 2014.9.25 Contract record no.: 2009130000185 Denomination of utility model: Double-layer heat exchange plate-type reactor in parallel Granted publication date: 20081210 License type: Exclusive license Record date: 20091012 |
|
| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.9.25 TO 2014.9.25; CHANGE OF CONTRACT Name of requester: SHIJIAZHUANG ZHENGYUAN TOWERS EQUIPMENT CO., LTD. Effective date: 20091012 |
|
| CX01 | Expiry of patent term |
Granted publication date: 20081210 |
|
| CX01 | Expiry of patent term |