CN201161186Y - Low-pressure double-layer heat exchange plate-type reactor in parallel - Google Patents
Low-pressure double-layer heat exchange plate-type reactor in parallel Download PDFInfo
- Publication number
- CN201161186Y CN201161186Y CNU2008200764265U CN200820076426U CN201161186Y CN 201161186 Y CN201161186 Y CN 201161186Y CN U2008200764265 U CNU2008200764265 U CN U2008200764265U CN 200820076426 U CN200820076426 U CN 200820076426U CN 201161186 Y CN201161186 Y CN 201161186Y
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- Prior art keywords
- basket
- heat exchange
- heat exchanger
- heat
- parallel
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- 238000005192 partition Methods 0.000 claims abstract description 6
- 239000003054 catalyst Substances 0.000 claims description 33
- 239000012530 fluid Substances 0.000 claims description 9
- 235000007164 Oryza sativa Nutrition 0.000 claims description 6
- 235000009566 rice Nutrition 0.000 claims description 6
- 230000035939 shock Effects 0.000 claims description 4
- 230000005587 bubbling Effects 0.000 claims description 3
- 238000007789 sealing Methods 0.000 claims description 3
- 240000007594 Oryza sativa Species 0.000 claims 1
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 abstract description 12
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 11
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- 239000007788 liquid Substances 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 10
- 241000209094 Oryza Species 0.000 description 5
- 239000007787 solid Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000012495 reaction gas Substances 0.000 description 2
- 230000032683 aging Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 210000001503 joint Anatomy 0.000 description 1
- 238000012856 packing Methods 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
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
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Abstract
The utility model relates to a lower-voltage parallel-connection double-deck heat-exchanging plate reactor which includes an accelerant basket, a heat exchanger, and a central air and water inlet pipe which are arranged in a cylinder body; wherein, a horizontal partition board is arranged in the middle of the cylinder body, the partition board partitions the cylinder body into an upper accelerant basket and a lower accelerant basket which are separated from each other, heat-exchanging plate type heat exchangers are arranged in the accelerant baskets, and the heat-exchanging plates are in parallel arranged in the cylinder body. The reactor has the advantages that one tower can be used as two towers, the potential of the accelerant can be fully tapped, the utilization coefficient of the accelerant is greatly increased, the operational resistance of the equipment is only one eighth of the prior tower, cool pipe type heat exchange is changed into heat-exchanging plate type heat exchange, namely, the heat-exchanging plates with various impresses form a set of heat exchanger with ultrahigh heat transfer efficiency, the total heat transfer coefficient of which is far lager than that of the common cool pipe type heat exchange; with the property of low resistance, the heat-exchanging plate type heat exchange can greatly increase the yield, and intermediate-pressure steam can be produced when the cold liquid in the heat-exchanging plates is water. The reactor has convenient and feasible production, not only greatly lowers the investment and the production cost, but also has the function for automatically loading and unloading the accelerant, and opens up a new way for upsizing the prior methanol reactor.
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 in practice and load catalyst in a large number, to strengthen reserve factor, prolong the catalyst replacement cycle, but too big standby yarn number has increased the catalyst bed layer height, thereby has increased equipment running resistance and power consumption greatly.
Summary of the invention
The utility model provides a kind of increases the catalyst usage factor, significantly reduce equipment running resistance and can improve the board-like gas-solid catalysis device of low pressure parallel heat exchanging of production capacity greatly.
For realizing the utility model purpose, this low pressure double-deck heat exchange plate-type reactor in parallel comprises basket, heat exchanger and the central tube that is installed in the cylindrical shell, it is characterized in that described cylindrical shell middle part is provided with a lateral partitions, described dividing plate is separated into upper and lower basket independently separately with cylindrical shell, be equiped with the heat exchange plate type heat exchanger in each basket, the upper port of heat exchanger plates is joined with the heat transferring medium house steward respectively, the lower port of upper strata heat exchanger plates connects a layer riser, and the lower port of lower floor's heat exchanger plates connects lower floor's riser.
The outlet of described riser communicates with catalyst layer respectively, and to the byproduct steam type of reactor, then extend neck is external respectively in its outlet.
Described heat exchanger plates is made of the metallic plate butt joint of two identical impressions respectively, the sealing that is connected between each periphery that two metallic plates are docked, thus between the slit between two metallic plates, form the fluid passage.
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.
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, accelerated rate of flow of fluid on the one hand, greatly improve total heat transfer yarn number, and prolonged the time that fluid passes through, 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 exchanger simultaneously.
Described to go up the basket bottom is a taper porous plate gas collector, and the catalyst downstream line of its lower end, the upper strata escape pipe that passes down basket direct reach tower bottom; Upper strata zero rice pressing plate is provided with the catalyst that communicates with the lower floor basket and loads pipe, and the cylindrical shell top is provided with the cold shock looped pipeline line that communicates with upper strata basket and lower floor's basket respectively.
The technological progress that the utility model is obtained: because the cold-tube type reactor of a large amount of catalyst of former filling is divided into reaction tower in parallel about in the of two, promptly the former standby catalyst layer in tower bottom being used parallel connection is a new tower, making a tower make two towers uses, the potentiality of catalyst have fully been excavated, increase catalyst greatly and utilized the yarn number, the equipment running resistance only is 1/8 of a former tower, heat exchange element changes the heat exchanger plates heat exchange into by cold pipe heat exchange simultaneously, 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, can arrange according to selected shape and be assemblied in the cylindrical shell, be not subjected to top end socket size restriction, its total heat transfer yarn number is more many greatly than general cold-tube type heat exchange, the reaction heat that can make the catalyst layer gathering is in time by the fluid removal in this heat exchanger, have under the characteristic of lower resistance, use the heat exchanger plates heat exchange can significantly increase output, easy to make feasible, not only can reduce investment and production cost greatly, but also because of having automatic dress, the function of unloading catalyst, start new way for current methanol reactor maximizes, had promotion prospect and economic benefit preferably.
Description of drawings
Below in conjunction with accompanying drawing the utility model is further described.
Fig. 1 is the utility model structural representation.
Fig. 2 is that the A-A of Fig. 1 is to generalized section.
Fig. 3 is the another kind of embodiment structural representation of Fig. 1.
The specific embodiment
Embodiment 1: as shown in Figure 1, installing basket, heat exchanger and water inlet central tube in existing low-pressure methanol synthesis tower cylindrical shell 2, cylindrical shell 2 middle parts are provided with a lateral partitions 19, dividing plate 19 is separated into upper and lower independently basket 3a, 3b separately with cylindrical shell 2, last basket 3a bottom is a taper porous plate gas collector 18, and the upper strata escape pipe 22 that the catalyst downstream line 23 of its lower end passes down basket 3b directes reach tower bottom.Upper strata zero rice pressing plate 7 is provided with the catalyst that communicates with the basket 3b of lower floor and loads pipe 4, be equiped with the heat exchange plate type heat exchanger in each basket, heat exchanger plates 14a, 14b are made of the metallic plate of two identical overall dimensions and identical impression respectively, be welded to connect the space that forms sealing between pairing each periphery of two metallic plates, stay the slit of establishing to form the fluid passage between two metallic plates, stream socket is established at heat exchanger plates 14a, 14b two ends respectively, and the impression on heat exchanger plates 14a, the 14b is corrugated (or linear or polyline shaped or bubbling shape). Heat exchanger plates 14a, 14b are arranged in parallel (as shown in Figure 2) in cylindrical shell 1, or according to other technological requirement fan-shaped array or be designed to various forms of arrangement modes. Heat exchanger plates 14a, 14b upper port are joined with heat transferring medium house steward 15 respectively, and the lower port of heat exchanger plates 14a connects layer riser 13, and the lower port of heat exchanger plates 14b connects lower floor's riser 21, and the outlet of riser 13,21 is extend neck body 2 exterior pressure vessels respectively.
It is heat transferring medium that present embodiment adopts water, boiler feedwater is from cylindrical shell 2 outside upper and lower layer water inlet pipe 10a, 10b, enter upper strata outlet manifold 16, lower floor's outlet manifold 24 via upper and lower layer riser 13,21 respectively, be diverted to again among upper strata heat exchanger plates 14a and the heat exchanger plates 14b of lower floor, after water among the heat exchanger plates 14a and the catalyst layer heat exchange, the temperature vaporization that raises, water vapour through the outlet of heat exchanger plates 14a upper end successively on the upper strata dry pipe 12, upper strata distributive pipe 11 enter the straight-through top of tower 9 of water outlet central tube and go out tower; Another road is assigned to through lower floor's outlet manifold 24 and is flowed down among the floor heat exchanger plates 14b, after heat exchanger plates 14b and catalyst layer heat exchange, water temperature raises in the heat exchanger plates 14b, the steam that produces is from heat exchanger plates 14b upper end outlet dry pipe 20, lower floor's distributive pipe 17, water outlet central tube in lower floor successively, 9 go out tower from the top, and the water vapour that goes out tower is gone into pressure vessel.Reacting gas after the preheating enters upper and lower layer gas distributor respectively through cylindrical shell 2 top upper strata air inlet 8a, the air inlet 8b of lower floor, make gas can evenly enter each catalyst layer, reacted top tank air goes out tower through top tank air gatherer 18, upper strata escape pipe 22, communicating pipe 25 through tower bottom outlet 27 successively; Reacted lower floor gas directly goes out tower from tower lower part outlet 26.
Embodiment 2: as shown in Figure 3, the present embodiment difference from Example 1 is the logical respectively place of the outlet catalyst layer of upper strata riser 13 and lower floor's riser 21, it is heat transferring medium that present embodiment adopts reaction gas, reaction gas enters house steward 15 after on upper strata gas-distributing pipe 11 and lower floor's gas-distributing pipe 17 go into respectively from cylindrical shell 2 top air inlets 9, discharge 12 in the lower floor, 20, through last, the heat exchanger plates 14a of lower floor, after 14b and the catalyst layer heat exchange, successively through upper strata heat exchanger plates 14a outlet at bottom, upper strata outlet manifold 16, enter cylindrical shell 2 top gas distributors behind the upper strata riser 13, reenter catalyst layer and react; Behind the heat exchanger plates 14b of lower floor outlet at bottom, lower floor's outlet manifold 24, lower floor's riser 21, enter lower floor's gas distributor successively through the lower floor's gas after lower floor's catalyst layer heat exchange, reenter down catalyst layer and react, the reacted gas warp gas outlet tube 26 of basket 3b bottom down goes out tower.
Above embodiment middle cylinder body 2 tops all are provided with the upper and lower layer cold shock looped pipeline line 6 that communicates with upper strata basket 3a and the basket 3b of lower floor, lower floor's cold shock by-pass pipe links to each other with top by-pass mouth, and pass upper strata zero rice pressing plate 7, go up basket 3a, gas collector 18, dividing plate 19 backs be to basket 3b down.The utility model also is provided with automatic loading and unloading catalyst function, and the filling of lower floor's catalyst is by packing in the filling pipe 4 that is located between upper strata zero rice plate 7 and the lower floor's zero rice plate 5.Drawing off of upper strata catalyst can be unloaded to tower bottom by the catalyst downstream line 23 of gas collector 18 bottoms, opens manhole 1 and can draw off full tower catalyst.
Claims (7)
1. a low pressure double-deck heat exchange plate-type reactor in parallel, comprise the basket that is installed in the cylindrical shell (2), heat exchanger and central tube, it is characterized in that described cylindrical shell (2) middle part is provided with a lateral partitions (19), described dividing plate (19) is separated into cylindrical shell (2), following basket (3a independently separately, 3b), be equiped with the heat exchange plate type heat exchanger in each basket, heat exchanger plates (14a, upper port 14b) is joined with heat transferring medium house steward (15) respectively, the lower port of heat exchanger plates (14a) connects a layer riser (13), and the lower port of heat exchanger plates (14b) connects lower floor's riser (21).
2. low pressure according to claim 1 double-deck heat exchange plate-type reactor in parallel is characterized in that outside the outlet difference extend neck body (2) of described riser (13,21).
3. low pressure according to claim 1 double-deck heat exchange plate-type reactor in parallel is characterized in that the outlet of described riser (13,21) communicates with catalyst layer respectively.
4. according to claim 1,2 or 3 described low pressure double-deck heat exchange plate-type reactor in parallel, it is characterized in that described heat exchanger plates (14a, 14b) respectively the metallic plate by two identical impressions constitute, the sealing that is connected between pairing each periphery of two metallic plates, the slit between two metallic plates forms the fluid passage.
5. low pressure according to claim 4 double-deck heat exchange plate-type reactor in parallel is characterized in that described heat exchanger plates (14a, 14b) is arranged in parallel or fan-shaped array in cylindrical shell (2).
6. low pressure according to claim 5 double-deck heat exchange plate-type reactor in parallel is characterized in that the impression on the described heat exchanger plates (14a, 14b) is corrugated, linear, polyline shaped or bubbling shape.
7. low pressure according to claim 6 double-deck heat exchange plate-type reactor in parallel, it is characterized in that described upward basket (3a) bottom is a taper porous plate gas collector (18), the upper strata escape pipe (22) that the catalyst downstream line (23) of its lower end passes down basket (3b) directes reach the tower bottom; Upper strata zero rice pressing plate (7) is provided with the catalyst that communicates with lower floor basket (3b) and loads pipe (4), and cylindrical shell (2) top is provided with the cold shock looped pipeline line (6) that communicates with upper strata basket (3a) and lower floor's basket (3b) respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200764265U CN201161186Y (en) | 2008-03-07 | 2008-03-07 | Low-pressure double-layer heat exchange plate-type reactor in parallel |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008200764265U CN201161186Y (en) | 2008-03-07 | 2008-03-07 | Low-pressure double-layer heat exchange plate-type reactor in parallel |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201161186Y true CN201161186Y (en) | 2008-12-10 |
Family
ID=40182130
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2008200764265U Expired - Lifetime CN201161186Y (en) | 2008-03-07 | 2008-03-07 | Low-pressure double-layer heat exchange plate-type reactor in parallel |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201161186Y (en) |
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2008
- 2008-03-07 CN CNU2008200764265U patent/CN201161186Y/en not_active Expired - Lifetime
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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: Lin Meili Contract fulfillment period: 2009.9.25 to 2014.9.25 Contract record no.: 2009130000184 Denomination of utility model: Low-pressure 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 |