CN2477267Y - Isothermal efficiency self-discharging carbinol synthetic tower inner element - Google Patents
Isothermal efficiency self-discharging carbinol synthetic tower inner element Download PDFInfo
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- CN2477267Y CN2477267Y CN 00262874 CN00262874U CN2477267Y CN 2477267 Y CN2477267 Y CN 2477267Y CN 00262874 CN00262874 CN 00262874 CN 00262874 U CN00262874 U CN 00262874U CN 2477267 Y CN2477267 Y CN 2477267Y
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- Prior art keywords
- basket
- cold
- methyl alcohol
- pipe
- cold pipe
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Abstract
The utility model relaters to an inner part of isothermal and efficient self discharging methanol synthesizing tower. Catalyzer basket adopts cold pipe bag with upper and lower circular canals in pairs which combines gas first and allocates and collect gas reversely under even stress, having no heat-insulating layer generally. The heat exchanger adopts multicenter helix board structure with low flow rate, low resistance, great recurrent air flow and strong production intensity; the cover board of the catalyzer basket and the bottom of unload pipe adopts demountable structure convenient for catalyzer filling and self discharging. The inner part has the advantages of good isothermy of catalyzer bed, high heat transferring efficiency, high composition rate, low resistance, large production, great catalyzer filling amount, long service life, convenient load and unload, easy operation, simple structure, good security, reliability, etc.
Description
The utility model belongs to the cold-tube type gas solid catalytic reactor, is mainly used in methyl alcohol synthetic reaction and ammonia synthesis reaction, is particularly useful for joining the occasion of alcohol or single alcohol production.
Before the utility model was made, the traditional cold cast ammonia converter internals that general synthesis ammonia plant uses mainly contained two sleeve pipes and flows three sleeve pipes, single tube adverse current, single tube and stream and U type tubular type etc., and was many with single tube dicyclo pipe parallel type internals.Ammonia converter internals is made of basket and heat exchanger two big parts.Cold pipe is set in the basket, and cold pipe is loaded catalyst outward.The difference of various cold-tube type synthetic towers mainly is the difference of cold-tube type formula.The bottom heat exchanger utilizes out the high-temperature gas preheating inlet tower gas body of basket bed, and the gas reaction liberated heat relies on the Continuous Heat Transfer of cold pipe to shift out in the bed.The cold pipe of different types and quantity all is provided with round the bed temperature best distribution.
Many traditional methyl alcohol synthetic reactor internals are to continue to use synthetic ammonia tower inner parts.Because the methyl alcohol and the characteristics of ammonia synthesis reaction and the catalyst performance of use have bigger difference: the methyl alcohol synthesising reacting heat is big, the reaction speed methyl alcohol of bed top, bottom differs greatly not as ammonia synthesis, catalyst for methanol is especially responsive to heat, overheated very easily inactivation and aggravation side reaction.Therefore ammonia convertor designing requirement bed temperature is as far as possible near the optimal temperature curve distribution, and to obtain maximum ammonia net value, methyl alcohol synthetic reactor then requires the bed axial temperature difference as far as possible little, and promptly isothermal requires higher.For the cold Guan Yire hyperenergia in the reverse-flow cold pipe of single tube bottom, the cold pipe of single tube parallel type is then opposite, the cold Guan Yire hyperenergia in top, all incompatible with the methyl alcohol synthetic reaction, thereby the bed axial temperature difference all (is generally 40 ℃～60 ℃ greatly, reach as high as 100 ℃), be unfavorable for reaction, life of catalyst is also short.The easy drawing crack of weld seam of the cold pipe of dicyclo tubular construction.Two sleeve pipes and the actual operating position of U type tubular type are also undesirable.Existing many ammonia converter internalses adopt the binary channels spiral-plate heat exchanger, because passage is little, flow velocity is high, resistance is prone to obstruction greatly, shrivel problem.
The isothermal methyl alcohol synthetic reactor of Germany Lurgi company adopts tube shell type structure, loads catalyst in the pipe, carries out gas-solid phase reaction, uses water shifting heat between pipe.This tower bed has a narrow range of temperature, but catalyst loading and unloading trouble, loadings is few again, and cost is also high.
In addition, catalyst for methanol is also very easily poisoned by trace sulfide except that easy overheated aging, is subjected to the general producer of makings condition restriction life of catalyst only 3 to 4 months, changes more frequent.And traditional methyl alcohol synthetic reactor is because basket and heat exchanger take welding fixing, and catalyst can only treat that internals hang out the back and open basket lid back with gas cutting and pour out from the top, and is time-consuming and labour intensity is big.
The purpose of this utility model is the drawback that overcomes prior art, provide a kind of bed temperature distribute even more ideal, reaction efficiency is high, catalyst life is long, structure is reliable more, load and unload more convenient isothermal self-unloading methyl alcohol synthetic reactor internals efficiently.
Fig. 1 is the efficient self-tipping type methyl alcohol synthetic reactor of an isothermal inner parts structure schematic diagram:
Wherein 1-interior endless tube, 2-beds, 3-central tube, 4-basket cylindrical shell, 5-and flow cold pipe, 6-basket muff, the cold pipe of 7-adverse current, 8-outer endless tube, 9-temperature-measuring casing, 10-cold looped pipeline, 11-collector box, 12-air entraining pipe, 13-seal washer, 14-basket cover plate, 15-taper card, 16-spiral-plate heat exchanger, 17-discharge duct.
The utility model is made up of basket and heat exchanger two big parts.Basket comprises: 1-interior endless tube, 2-beds, 3-central tube, 4-basket cylindrical shell, 5-and flow cold pipe, 6-basket muff, the cold pipe of 7-adverse current, 8-outer endless tube, 9-temperature-measuring casing, 10-cold looped pipeline, 11-collector box, 12-air entraining pipe, 13-seal washer, 14-basket cover plate, 15-taper card, 17-discharge duct etc.By air entraining pipe-12, adverse current cold pipe-7 and flow cold pipe-5 and in endless tube-1, outer endless tube-8 assembly welding form cold tube bag, and the cold pipe of adverse current and and flow cold pipe and be spaced.Air entraining pipe-12, central tube-3 upper end adopt stuffing box structure to seal on basket cover plate-14, can allow again to stretch.Be connected by concavo-convex flange between 4-basket cylindrical shell and 14-basket cover plate, the 11-collector box, bolted adopts the expanded graphite washer sealing.Heat exchanger adopts spiral plate type efficiently.For reducing the resistance of spiral plate, the utility model adopts 6～12 passages (hot and cold passage half and half), and 3～8m/s hangs down operated in flow rate, high turbulent heat transfer.Basket is arranged on the top of spiral-plate heat exchanger.Take welding between the parts.The internals material is 1Cr18Ni9Ti or 0Cr18Ni10Ti stainless steel.
Main line gas enters the cold passage preheating of spiral-plate heat exchanger-16 through the annular space of methyl alcohol synthetic reactor urceolus and methyl alcohol synthetic reactor internals, rise to collector box-11 from central tube-3 then, baffling enters air entraining pipe-12 again, through last endless tube-1,8 with distribution of gas to each also flow cold pipe-5, gas is managed the further preheating of outer reaction gas in the pipe, removes the reaction heat of bed simultaneously.Baffling was to each adverse current cold pipe-7 again behind the endless tube-1,8 under gas flowed from top to bottom in pipe and comes together in, and gas is mobile from bottom to top once more by reaction gas preheating outside the pipe in pipe, removes the reaction heat of bed simultaneously again.The gas that goes out adverse current cold pipe-7 enters beds from the top, and oxycarbide in the gas and hydrogen constantly synthesize methyl alcohol.Reaction gas flows from top to bottom, leaves the passage of heat that basket enters spiral-plate heat exchanger-16 from taper card-15, and heat is passed to main line gas in the cold passage, and cooled reaction gas goes out synthetic tower from the bottom of methyl alcohol synthetic reactor urceolus.By-pass gas enters collector box-11 from the cold looped pipeline-10 at basket top, and the main line gas merging of the preliminary preheating in the cold passage of spiral-plate heat exchanger of fork-like farm tool used in ancient China enters air entraining pipe-12 with rising from central tube-3, is used to regulate the temperature of bed.
Bed gas reaction liberated heat is also flowed the cold air through preliminary preheating in the cold passage of spiral-plate heat exchanger-16 of fork-like farm tool used in ancient China in the cold pipe of cold pipe and adverse current and is suitably removed behind the countercurrent flow earlier and behind the stream.Thereby unique cold tubular construction and rational design parameter guarantee the isothermal of beds.For strengthening the reliability of cool pipe welding line structure, the utility model adopts ring structure (i.e. two outer endless tubes, two interior endless tubes) in pairs.Open the basket cover plate, in catalyst can be packed basket into from the basket top, more during catalyst changeout, only needing to open catalyst to the seal of discharge duct bottom can draw off voluntarily.
The cold pipe of the utility model basket is 18～25 meters than heat transfer area
2/ rice
3Catalyst, wherein the cold pipe of adverse current accounts for 30～45%, and does not have upper thermal insulating layer, and lower thermal insulating layer accounts for total bed height＜5%.Spiral-plate heat exchanger is 8～20 meters than heat transfer area
2/ rice
3Catalyst.
The utility model compared with prior art has following remarkable advantage:
1, cold tubular construction and Rational Parameters, the bed isothermal is good, helps the methyl alcohol synthetic reaction, the conversion ratio height, side reaction is few, helps prolonging internals and catalyst life again.
2, adopt the high-efficiency helical sheet heat exchanger, loaded catalyst is big, the heat transfer efficiency height, and production capacity is big.
3, take 6～12 multichannel spiral-plate heat exchangers, flow velocity is low, and resistance is little, and circulating flow rate is big, the production intensity height.
4, take the upper and lower structure of endless tube in pairs, the distribution of gas, compile and stressed evenly, increased security and the reliability used.
5, take the self-unloading structure of basket cover plate expanded graphite washer sealing and discharge duct bottom, be beneficial to the loading and unloading of catalyst.
Claims (7)
1, a kind of isothermal self-tipping type methyl alcohol synthetic reactor internals is characterized in that: be made up of basket and heat exchanger two big parts; Basket comprises: 1-interior endless tube, 2-beds, 3-central tube, 4-basket cylindrical shell, 5-and flow cold pipe, 6-basket muff, the cold pipe of 7-adverse current, 8-outer endless tube, 9-temperature-measuring casing, 10-cold looped pipeline, 11-collector box, 12-air entraining pipe, 13-seal washer, 14-basket cover plate, 15-taper card, 17-discharge duct etc.; By air entraining pipe-12, adverse current cold pipe-7 and flow cold pipe-5 and in endless tube-1, outer endless tube-8 assembly welding form cold tube bag, and the cold pipe of adverse current and and flow cold pipe and be spaced; Air entraining pipe-12, central tube-3 upper end adopt stuffing box structure to seal on basket cover plate-14; Basket is arranged on the top of spiral-plate heat exchanger-16; Catalyst filling is in basket.
2, methyl alcohol synthetic reactor internals as claimed in claim 1 is characterized in that: spiral-plate heat exchanger is 6～12 passage spiral plates (hot and cold passages half and half), adopts low flow velocity 3～8m/s, is 8～20 meters than heat transfer area
2/ rice
3Catalyst.
3, methyl alcohol synthetic reactor internals as claimed in claim 1 is characterized in that: cold pipe recuperated gas flows to and adopts baffling (also flowing the back adverse current earlier); Cold pipe is 18～25 meters than heat transfer area always
2/ rice
3Catalyst, wherein the cold pipe of adverse current accounts for 30～45%.
4, methyl alcohol synthetic reactor internals as claimed in claim 1 is characterized in that: no upper thermal insulating layer in the basket, lower thermal insulating layer accounts for total bed height＜5%.
5, methyl alcohol synthetic reactor internals as claimed in claim 1 is characterized in that: the endless tube in the basket adopts up and down endless tube structure in pairs.
6, methyl alcohol synthetic reactor internals as claimed in claim 1, it is characterized in that: be connected by concavo-convex flange between basket cylindrical shell-4 and basket cover plate-14, the collector box-11, bolted adopts expanded graphite washer sealing structure and bottom that the discharge duct-17 of detachable seal configuration is arranged.
7, methyl alcohol synthetic reactor internals as claimed in claim 1 is characterized in that: methyl alcohol synthetic reactor internals material is 1Cr18Ni9Ti or 0Cr18Ni10Ti stainless steel.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00262874 CN2477267Y (en) | 2000-11-25 | 2000-11-25 | Isothermal efficiency self-discharging carbinol synthetic tower inner element |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00262874 CN2477267Y (en) | 2000-11-25 | 2000-11-25 | Isothermal efficiency self-discharging carbinol synthetic tower inner element |
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| Publication Number | Publication Date |
|---|---|
| CN2477267Y true CN2477267Y (en) | 2002-02-20 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 00262874 Expired - Fee Related CN2477267Y (en) | 2000-11-25 | 2000-11-25 | Isothermal efficiency self-discharging carbinol synthetic tower inner element |
Country Status (1)
| Country | Link |
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| CN (1) | CN2477267Y (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003055586A1 (en) * | 2001-12-28 | 2003-07-10 | Ren Lou | A method and apparatus for optimizing the gas-solid phase catalytic reaction |
| CN105967976A (en) * | 2016-05-09 | 2016-09-28 | 山西阳煤化工机械（集团）有限公司 | Methanol synthetic tower with high efficiency and high pressure |
| CN106629775A (en) * | 2017-01-18 | 2017-05-10 | 山东科技大学 | Multitube-type ultra-low-pressure isothermal ammonia converter |
| CN106698470A (en) * | 2017-01-18 | 2017-05-24 | 山东科技大学 | Helical plate type ultralow-pressure isothermal ammonia synthesizing tower |
| CN106732204A (en) * | 2017-02-04 | 2017-05-31 | 济南承乾工程技术有限公司 | One kind segmentation spiral plate type ultralow pressure isothermal ammonia convertor |
-
2000
- 2000-11-25 CN CN 00262874 patent/CN2477267Y/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2003055586A1 (en) * | 2001-12-28 | 2003-07-10 | Ren Lou | A method and apparatus for optimizing the gas-solid phase catalytic reaction |
| CN105967976A (en) * | 2016-05-09 | 2016-09-28 | 山西阳煤化工机械（集团）有限公司 | Methanol synthetic tower with high efficiency and high pressure |
| CN106629775A (en) * | 2017-01-18 | 2017-05-10 | 山东科技大学 | Multitube-type ultra-low-pressure isothermal ammonia converter |
| CN106698470A (en) * | 2017-01-18 | 2017-05-24 | 山东科技大学 | Helical plate type ultralow-pressure isothermal ammonia synthesizing tower |
| CN106732204A (en) * | 2017-02-04 | 2017-05-31 | 济南承乾工程技术有限公司 | One kind segmentation spiral plate type ultralow pressure isothermal ammonia convertor |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C19 | Lapse of patent right due to non-payment of the annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |