CN2280087Y - Reactor for conversion sulfur oxides by use of heat pipe heat-exchange - Google Patents
Reactor for conversion sulfur oxides by use of heat pipe heat-exchange Download PDFInfo
- Publication number
- CN2280087Y CN2280087Y CN96247229U CN96247229U CN2280087Y CN 2280087 Y CN2280087 Y CN 2280087Y CN 96247229 U CN96247229 U CN 96247229U CN 96247229 U CN96247229 U CN 96247229U CN 2280087 Y CN2280087 Y CN 2280087Y
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- CN
- China
- Prior art keywords
- heat
- conversion reactor
- heat pipe
- reactor
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- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The utility model relates to sulphuric acid production equipment, which is especially an SO< 2 > catalystic reactor or a conversion reactor. Hot SO< 3 > and cool SO< 2 > can exchange heat through a heat exchanger which is composed of heat pipes; the heating section of the heat pipe exchanger is arranged among each catalyzer of the conversion reactor; the cooling section of the heat pipe exchanger is arranged at the outside of the conversion reactor. Because the heat pipes adopt finned pipes to carry out enhanced heat transfer, the number of the heat pipe is less than the ordinary light pipe under the same heat transfer area. The utility model has the advantages of high heat-transfer efficiency, small resistance, compact structure, small flow path and little heat dissipation.
Description
The utility model relates to a kind of gas washing in SA production equipment, especially is SO
2Catalyticreactor is commonly called as conversion reactor.
At present, traditional conversion reactor flow process (see figure 1) is from the next cold SO of purification section
2Gas at first enters between the pipe of the 3rd interchanger 3, with the 3rd section hot SO that comes out
3Gas converting heat (walk pipe in) heat exchange is heated to first section catalyst that comes out that the required temperature (about 400 ℃) of reaction enters conversion reactor 5 and carries out conversion reaction.From first section reacted SO that comes out
3Enter in the pipe of the 3rd interchanger 1 and SO from first interchanger 3
2Heat exchange enters second section catalyst reaction after the cooling.The SO that behind second section catalyst internal reaction, comes out
3Gas enters in the pipe of second interchanger 2, with the SO from the 4th interchanger 4
2Enter the 3rd section catalyst after the heat exchange cooling, enter after the reaction in the pipe of the 3rd interchanger 3 with from induced draft fan SO
3Enter first absorption tower 6 after the heat exchange cooling.Eject next SO from the absorption tower
2Gas enters between the pipe of the 4th interchanger 4 and the SO that comes from the 4th section catalyst
3After heating up, heat exchange enters again between the pipe of second interchanger 2 and SO from two sections catalyst
3Heat exchange enters second absorption tower after heating up.This flow process pipeline turnover is various, fluid resistance increases, and heat waste is also considerable, generally can reach 17% of reaction heat, leaks in often having between shell and tube heat exchanger pipe and tube sheet and takes place.
The purpose of this utility model is exactly to provide a kind of SO of making for the above-mentioned defective that solves prior art
2Catalytic oxidation process follow the SO that optimum temperature curve carries out as much as possible with heat pipe heat exchanging
2Conversion reactor.
Technical solution of the present utility model is as follows:
A kind of SO with heat pipe heat exchanging
2Conversion reactor is characterized in that at it hot SO between each section
3Gas and cold SO
2The interchanger heat exchange that gas adopts heat pipe to form; The heating zone of hot tube heat exchanger be arranged in each catalyst in the conversion reactor between, it is external that the cooling section of hot tube heat exchanger then can be arranged in conversion reactor.
Advantage of the present utility model is to have satisfied wishes to obtain the purpose of maximum economic benefits with minimum investment, minimum working cost to the requirement of industrial production conversion reactor, utilizes heat pipe heat exchanging, makes SO
2Catalytic oxidation process realize optimization, make the multistage catalyzed oxidation as far as possible near the optimum pilot wire, because heat pipe adopts the finned tube enhancement of heat transfer, therefore under same heat transfer area, the used pipe number of heat pipe lacks than common light pipe, and its heat transfer efficiency height, resistance drop are little; Compact construction, flow process reduces, and heat lost by radiation is few.
Below in conjunction with accompanying drawing the utility model is further described:
Fig. 1 is the prior art constructions synoptic diagram.
Fig. 2 is a structural representation of the present utility model.
Fig. 3 is the another synoptic diagram of structure of the present utility model.
Fig. 4 is another synoptic diagram of structure of the present utility model.
Hot tube heat exchanger of the present utility model also can all be arranged in outer each section gas inlet and outlet of conversion reactor and connect with conduit.Heat pipe can horizontal positioned (heat pipe that wick is arranged), also can become a pitch angle (greater than 7 degree, to use gravity type heat pipe with horizontal plane.It is applicable to the fixed-bed conversion interchanger; Ebullated bed transforms interchanger; Also can in ebullated bed, fixed bed combined process flow, use simultaneously.When the utility model being four sections fixed bed heat pipe conversion reactors, with the heating zone of hot tube heat exchanger be arranged in each catalyst in the conversion reactor 5 between, it is external that the cooling section of hot tube heat exchanger then can be arranged in conversion reactor 5.Because heat pipe adopts the finned tube enhancement of heat transfer, therefore under same heat transfer area, the used pipe number of heat pipe lacks than common light pipe.SO from clean-up stage
2Cooling section through hot tube heat exchanger 9 and 7 is heated to one section catalyst that temperature of reaction enters conversion reactor, pass through the heating zone of hot tube heat exchanger 7 then, enter second section catalyst after the cooling, enter the 3rd section catalyst after the heating section cooling through hot tube heat exchanger 8 again, go to first absorption tower after the cooling of being heated through the 3rd hot tube heat exchanger again.The SO that comes out by first absorption tower
2Gas at first is heated back to the cooling section of second hot tube heat exchanger through the cooling section of hot tube heat exchanger 10 and is heated once more and enters the 4th section catalyst reaction after go to second absorption tower after the heating section cooling of superheater tube interchanger 10.Because this conversion can directly be arranged in the heating section of heat pipe in the conversion reactor, has saved a large amount of import and export pipelines, has reduced resistance to flow, heat waste, investment and process cost, the more important thing is the reliability height, the danger of leaking in not having.
When utility model is ebullated bed conversion reactor (Fig. 3), temperature is the SO of 50-60C
2Gas the heat that ebullated bed reactor one side roof part absorbs heat pipe from top to bottom and derives from each section fluidized bed be heated to 300-350 ℃ of first section ebullated bed in bottom that enters the ebullated bed conversion reactor from top to bottom through four sections reactions after transformation efficiency reach 95-98%, do not have SO in the ebullated bed outside
3Water cooler reclaims heat and produces steam.
When the utility model is that heat pipe-type ebullated bed and heat pipe-type fixed bed are united (Fig. 4) when using, ebullated bed can be with one section, also can be with the fixed bed of second-stage reaction, realization double conversion double absorption.Because the simple thermosteresis of flow process is few, can directly reclaim heat in ebullated bed.
Claims (4)
1. SO with heat pipe heat exchanging
2Conversion reactor is characterized in that at it hot SO between each section
3Gas and cold SO
2The interchanger heat exchange that gas adopts heat pipe to form; The heating zone of hot tube heat exchanger be arranged in each catalyst of conversion reactor between, it is external that the cooling section of hot tube heat exchanger then can be arranged in conversion reactor.
2. the SO with heat pipe heat exchanging according to claim 1
2Conversion reactor is characterized in that hot tube heat exchanger also can all be arranged in outer each section gas inlet and outlet of conversion reactor and connects with conduit.
3. the SO with heat pipe heat exchanging according to claim 1
2Conversion reactor is characterized in that heat pipe can horizontal positioned, also can become a pitch angle with horizontal plane.
4. the SO with heat pipe heat exchanging according to claim 1
2Conversion reactor is characterized in that it is applicable to the fixed-bed conversion interchanger; Ebullated bed transforms interchanger; Also can in ebullated bed, fixed bed combined process flow, use simultaneously.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96247229U CN2280087Y (en) | 1996-12-20 | 1996-12-20 | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN96247229U CN2280087Y (en) | 1996-12-20 | 1996-12-20 | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2280087Y true CN2280087Y (en) | 1998-04-29 |
Family
ID=33919480
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN96247229U Expired - Fee Related CN2280087Y (en) | 1996-12-20 | 1996-12-20 | Reactor for conversion sulfur oxides by use of heat pipe heat-exchange |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2280087Y (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101143716B (en) * | 2006-09-15 | 2010-05-12 | 南化集团研究院 | Low concentration sulphur dioxide flue gas acid preparing heat using method |
| CN102303848A (en) * | 2011-04-02 | 2012-01-04 | 中冶焦耐(大连)工程技术有限公司 | Method for exchanging heat between high-temperature process gas and low-temperature process gas in acid production process |
| CN102336396A (en) * | 2011-09-27 | 2012-02-01 | 宜兴市化工成套设备有限公司 | Continuous heat transfer sulfur dioxide conversion process |
| CN102336397A (en) * | 2011-09-27 | 2012-02-01 | 宜兴市化工成套设备有限公司 | Continuous heat transfer sulfur dioxide converter |
| CN102910592A (en) * | 2012-10-31 | 2013-02-06 | 宜兴市化工成套设备有限公司 | Quasi-isothermal venturi converter for heat energy substitution |
| CN104379503A (en) * | 2012-06-06 | 2015-02-25 | 赫多特普索化工设备公司 | Process for the oxidation of SO2 to SO3 |
-
1996
- 1996-12-20 CN CN96247229U patent/CN2280087Y/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101143716B (en) * | 2006-09-15 | 2010-05-12 | 南化集团研究院 | Low concentration sulphur dioxide flue gas acid preparing heat using method |
| CN102303848A (en) * | 2011-04-02 | 2012-01-04 | 中冶焦耐(大连)工程技术有限公司 | Method for exchanging heat between high-temperature process gas and low-temperature process gas in acid production process |
| CN102303848B (en) * | 2011-04-02 | 2013-04-10 | 中冶焦耐(大连)工程技术有限公司 | Method for exchanging heat between high-temperature process gas and low-temperature process gas in acid production process |
| CN102336396A (en) * | 2011-09-27 | 2012-02-01 | 宜兴市化工成套设备有限公司 | Continuous heat transfer sulfur dioxide conversion process |
| CN102336397A (en) * | 2011-09-27 | 2012-02-01 | 宜兴市化工成套设备有限公司 | Continuous heat transfer sulfur dioxide converter |
| CN102336396B (en) * | 2011-09-27 | 2013-04-10 | 宜兴市化工成套设备有限公司 | Continuous heat transfer sulfur dioxide conversion process |
| CN104379503A (en) * | 2012-06-06 | 2015-02-25 | 赫多特普索化工设备公司 | Process for the oxidation of SO2 to SO3 |
| US9487401B2 (en) | 2012-06-06 | 2016-11-08 | Haldor Topsoe A/S | Process for the oxidation of SO2 to SO3 |
| CN104379503B (en) * | 2012-06-06 | 2017-08-18 | 托普索公司 | For by SO2It is oxidized to SO3Technique |
| CN102910592A (en) * | 2012-10-31 | 2013-02-06 | 宜兴市化工成套设备有限公司 | Quasi-isothermal venturi converter for heat energy substitution |
| CN102910592B (en) * | 2012-10-31 | 2014-04-09 | 宜兴市化工成套设备有限公司 | Quasi-isothermal venturi converter for heat energy substitution |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C53 | Correction of patent for invention or patent application | ||
| CB03 | Change of inventor or designer information |
Designer after: Zhuang Jun Designer after: Zhang Hong Designer after: Yu Bin Designer after: Xu Jianren Designer after: Zhang Weihua Designer before: Zhuang Jun Designer before: Zhang Hong Designer before: Yu Bin Designer before: Xu Jianren Designer before: Zhang Weihua |
|
| COR | Change of bibliographic data |
Free format text: CORRECT: DESIGNER; FROM: ZHUANG JUN; ZHANG HONG; YU BIN; XU JIANREN; ZHANG WEIHUA TO: ZHUANG JUN; ZHANG HONG; YU BIN; XU JIANREN; ZHANG WEIHUA |
|
| 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 |