CN203359975U - Self-heat-exchange deaerator - Google Patents
Self-heat-exchange deaerator Download PDFInfo
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- CN203359975U CN203359975U CN 201320305935 CN201320305935U CN203359975U CN 203359975 U CN203359975 U CN 203359975U CN 201320305935 CN201320305935 CN 201320305935 CN 201320305935 U CN201320305935 U CN 201320305935U CN 203359975 U CN203359975 U CN 203359975U
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Abstract
The utility model discloses a self-heat-exchange deaerator, which comprises an upper barrel body and a lower barrel body, wherein a shell and tube heat exchanger is arranged inside the barrel bodies; the upper barrel body is directly welded onto the upper tube plate of the shell and tube heat exchanger, and the lower barrel body is directly welded onto the lower tube plate of the shell and tube heat exchanger so as to form an integral, the structure is compact, and the flowing path of the gas is short. The shell and tube heat exchanger comprises baffle plates and heat exchanging tubes; process gas enters the space among the heat exchanging tubes, and performs heat exchanging with the first section reaction heat gas inside the heat exchanging tubes to ensure that the gas at the inlet is dried, so that the first section palladium catalyst is prevented from being wetted by the moisture contained in the gas, and the deoxygenation efficiency of the deaerator and the long-term stable operation are guaranteed; the process gas subject to heat exchange and cooling then enters the second section palladium contact agent for oxidation reaction; the second section and a third section are arranged in case that the gas takes a short passage; the distribution of the process gas in the second section palladium contact agent and the third section palladium contact agent are rearranged; thorough deoxygenation reaction is performed in the third section. The purpose of self-heat-exchange deoxidization is realized.
Description
Technical field
The utility model relates to a kind of deoxygenator, especially a kind of from the heat exchange type deoxygenator, and while specifically being applied to undivided cell production oxymuriate, by-product electrolysis tail gas is deviate from oxygen recovery hydrogen.
Background technology
Containing a large amount of hydrogen in the electrolyzer emptying gas, is precious resources, directly discharges not only polluted air, and the waste precious resources.Because wherein contain the foreign gases such as oxygen, chlorine, carbonic acid gas, not only make hydrogen purity inadequate, also, because oxygen, chlorine bring unsafe factor to hydrogen recovery, can not directly recycle.Therefore, deoxygenator need to be set all removes oxygen in hydrogen.
When current deoxygenator uses, temperature is uncontrollable, and when oxygen level is high, temperature is up to 500～600 ℃, and the deoxygenator appearance is rubescent, more dangerous, stops for some time, then drives.At the driving initial stage, because catalyst activity is good, overheating problem is also arranged.After using for some time, one section entrance gas at normal temperature, due to the dipping of steam, make the catalyst inactivation gradually from top to bottom.Uncontrollable because of temperature, the catalyst addition is restricted, and the exit gas oxygen level is higher, and after especially applicable for some time, the bottom catalyst is flooded inactivation by steam, and effectively the catalyst amount reduces, and oxygen level is higher, is forced to parking maintenance.
The utility model content
The technical problems to be solved in the utility model be to provide a kind of safe, deoxidation efficiency is high, easy control of temperature from the heat exchange type deoxygenator.
For solving the problems of the technologies described above, technical solution adopted in the utility model is: a kind of from the heat exchange type deoxygenator, its gordian technique is: it comprises upper shell, is positioned at shell and tube heat exchanger and the lower shell at middle part, be provided with to be connected between upper shell and shell and tube heat exchanger and use upper tubesheet, be provided with to be connected between shell and tube heat exchanger and lower shell and use lower tubesheet, be provided with heat-exchanger rig in described shell and tube heat exchanger, the top of shell and tube heat exchanger is provided with inlet mouth, described shell and tube heat exchanger was communicated with lower shell by communicating pipe, and described upper shell top is provided with air outlet.
Described heat-exchanger rig comprises at least two highly different traverse baffles that are installed on the shell and tube heat exchanger inwall, be equipped with a plurality of heat transfer tubes on described traverse baffle, the upper/lower terminal of described heat transfer tube is positioned respectively on upper tubesheet and lower tubesheet, and upper shell and lower shell are communicated with by heat transfer tube.Highly different traverse baffles is crisscross arranged on the inwall of shell and tube heat exchanger, forms the circulation passage of continuous bending, to increase heat exchange distance and heat-exchange time, improves heat exchange efficiency.
Described upper and lower tube sheet and traverse baffle are rectangle structure, are provided with through hole above it.
Described inlet mouth is communicated with communicating pipe by the pipeline with valve.
Be provided with the first barrier in described lower shell, described barrier top is provided with first paragraph palladium catalyst; Be provided with from top to bottom the 3rd barrier, the second barrier in described upper shell, be filled with second segment catalyst, the 3rd section catalyst on described the second barrier, the 3rd barrier.
The upper portion side wall of described lower shell is provided with the first hand hole, and the upper portion side wall of described upper shell is provided with the second hand hole.
Principle of work of the present utility model is: the process gas that need to remove oxygen is introduced between the tubular heat exchange pipe, and carry out heat exchange with the first paragraph reaction heat gas entered in the tubular heat exchange pipe, be heated to more than 100 ℃, make inlet gas all the time in " dry gas " state, prevent from gas carrying secretly steam and soaked the first paragraph palladium catalyst, guaranteed deoxygenator deoxidation efficiency and operation steady in a long-term.The process gas of lowering the temperature through heat exchange enters second segment palladium catalyst place again and carries out oxidizing reaction, for preventing gas, walks short circuit, and second, third section palladium catalyst is set, and between second, third section palladium catalyst, the process gas redistribution, enter three sections and carry out thorough deoxygenation.Reach the deoxidation design from the 3rd section process gas that the palladium catalyst exports away.Thereby realize the purpose from the heat exchange deoxygenation.
The beneficial effect that adopts technique scheme to produce is:
1, be provided with heat-exchanger rig in the utility model shell and tube heat exchanger, the gas that temperature is higher enters upper shell by heat transfer tube from lower shell, in the gas communication process, heat transfer tube utilizes hydrogen deoxygenation liberated heat, can be by more than the gas heating to 100 at deoxygenator inlet mouth place ℃, higher than dew point, make inlet gas all the time in " dry gas " state, prevented in gas that carrying steam secretly soaks palladium catalyst, make it to lose activity, thereby guarantee deoxygenator deoxidation efficiency and operation steady in a long-term.Otherwise carry steam in gas secretly after the certain period, palladium catalyst is soaked, so-called catalyst " is had a bath ", catalyst surface is covered, lose activity, reload rear use after catalyzer need to being taken out to oven dry, increase the equipment stop frequency, increased unsafe factor.
2, the utility model is provided with the cold shock interface on communicating pipe, inlet mouth is by being with valvular pipeline to be communicated with the cold shock interface, can open as required valve, the gas that temperature is low is directly sent in lower shell, by controlling the quench gas scale of construction, controlling the deoxygenation temperature of reaction can not infinitely raise, and reaches oxidizing reaction temperature controlled, thereby guarantees the deoxygenator safe operation.
3, the utility model rationally utilizes the reaction heat of deoxidation, controls deoxygenation and reacts under optimum temps, guarantees after deoxidation that in hydrogen, oxygen content is lower, can realize degree of depth deoxidation, and after deoxidation, hydrogen purity can reach more than 99.9%.
The accompanying drawing explanation
Fig. 1 is structural representation of the present utility model;
Fig. 2 is the structural representation (upper tubesheet and lower tubesheet) of tube sheet;
Fig. 3 is the B-B diagrammatic cross-section in Fig. 2;
Fig. 4 is the schematic diagram of traverse baffle;
Fig. 5 is the schematic diagram of barrier;
Fig. 6 is the A-A schematic diagram in Fig. 1;
Wherein, 1, handle; 2, leg; 3, base plate; 4, gusset; 5, the first pipe flange; 6, short tube; 7, communicating pipe; 8, cold shock interface; 9, lower shell; 10, the installation of TC base; 11, lower tubesheet; 12, angle steel; 13, spacing tube; 14, traverse baffle; 15, heat transfer tube; 16, shell and tube heat exchanger; 17, upper tubesheet; 18, double threaded screw; 19, thermometer mounting seat; 20, upper shell; 21, support; 22-1, the first barrier, 22-2, the second barrier, 22-3, the 3rd barrier; 23, the first hand hole; 24, top board; 25, inlet mouth; 26, pipe flange; 27, the second hand hole; 28, the second pipe flange; 29, blind flange; 30, air outlet; 31, left cutting wires; 32, right cutting wires.
Embodiment
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail.
Referring to accompanying drawing 1 and accompanying drawing 6, the utility model comprises upper shell 20, shell and tube heat exchanger 16 and lower shell 9 three parts, be provided with the upper tubesheet 17 that is connected use between upper shell 20 and shell and tube heat exchanger 16, be provided with the lower tubesheet 11 that is connected use between shell and tube heat exchanger 16 and lower shell 9, be provided with heat-exchanger rig in described shell and tube heat exchanger 16, the top of shell and tube heat exchanger 16 is provided with inlet mouth 25, described shell and tube heat exchanger 16 is by being communicated with lower shell 9 communicating pipe 7, and described upper shell 20 tops are provided with air outlet 30.The upper shell 20 of the present embodiment directly is welded on the upper tubesheet 17 of shell and tube heat exchanger 16, and lower shell 9 directly is welded on the lower tubesheet 11 of shell and tube heat exchanger 16, forms an integral body, compact construction, and the gas flow process is short.
Referring to accompanying drawing 1, accompanying drawing 2, accompanying drawing 3 and accompanying drawing 4, described heat-exchanger rig comprises at least two highly different traverse baffles 14 and the heat transfer tube 15 be installed on shell and tube heat exchanger 16 inwalls, described traverse baffle 14 is provided with through hole, be equipped with several heat transfer tubes 15 in this through hole, 50 left and right heat transfer tubes of operated by rotary motion can meet service requirements, the upper/lower terminal of described heat transfer tube 15 is positioned respectively on upper tubesheet 17 and lower tubesheet 11, upper shell 20 and lower shell 9 are communicated with by heat transfer tube 15, and gas enters upper shell 20 by heat transfer tube 15 from lower shell 9.Highly different traverse baffles 14 is crisscross arranged on the inwall of shell and tube heat exchanger 16, form the circulation passage of continuous bending, two traverse baffles of operated by rotary motion get final product, referring to accompanying drawing 1, on two traverse baffles 14 1, once arrange, the traverse baffle on top is arranged on the inwall of right side, lower baffle is arranged on left side wall, the other end of traverse baffle does not contact with the inwall of shell and tube heat exchanger 16, so just formed the circulation passage of S type, make the gas of coming in from inlet mouth 25 descending along the circulation passage of bending, extended the currency.Referring to accompanying drawing 4, traverse baffle 14 is rectangle structure, the traverse baffle on top is shaped as square plate in Fig. 4 and dismisses remaining part after left part along left cutting wires, and the traverse baffle of bottom is shaped as square plate in Fig. 4 and dismisses remaining left part after the part of right side along right cutting wires.Referring to accompanying drawing 2, upper tubesheet 17, lower tubesheet 11 are square structure, and the above is provided with through hole.
The middle part vertical pipe of described communicating pipe 7 is provided with cold shock interface 8, and described inlet mouth 25 is communicated with cold shock interface 8 by the pipeline with valve, can make the gas that portion temperature is lower directly enter in lower shell 9.
Referring to accompanying drawing 1 and accompanying drawing 5, be provided with the first barrier 22-1 in described lower shell 9, described the first barrier 22-1 top is provided with first paragraph palladium catalyst; Be provided with from top to bottom the 3rd barrier 22-3, the second barrier 22-2 in described upper shell 20, be filled with respectively second segment catalyst, the 3rd section catalyst on described the second barrier 22-2, the 3rd barrier 22-3.The structure iron that accompanying drawing 5 is first, second, third barrier, 3 barriers of every layer of placement of the present embodiment, be filled with the palladium catalyst above barrier.
Referring to accompanying drawing 1, the upper portion side wall of described lower shell 9 is provided with the first hand hole 23, and the upper portion side wall of described upper shell 20 is provided with the second hand hole 27, by hand hole, barrier and square palladium catalyst is put into to deoxygenator, handled easily.Be provided with thermopair on lower shell 9.
The flow process of the utility model gas: gas first enters shell and tube heat exchanger 16 from inlet mouth 25, enter again lower shell 9, during beginning, normal temperature palladium catalyst just has the active temperature rise that starts, make the gas temperature after first paragraph palladium catalyst reach 360 ℃, also reach 100 ℃ by the heat exchange inlet gas, realized from heat exchange, later by control, enter the quench gas scale of constructions in cold shock interface 8 and make bulk temperature reach normal design to get final product.Gas again from bottom by entering upper shell 20 through heat transfer tube 15, make gas successively by second segment palladium catalyst, the 3rd section palladium catalyst, finally from air outlet, 30 go out deoxygenator.
The higher reaction of oxygen content at first paragraph palladium catalyst place is violent, and thermal discharge is large, by filling thickness, controls the deoxidation degree, by heat exchange by the partial reaction thermal exchange to inlet gas; Inlet mouth 25 was communicated with communicating pipe 7, and communicating pipe 7 is passages of gas after heat exchange, and when gasinlet temperature surpasses 150 ℃, available cold shock gas reduces gasinlet temperature.Second and third section palladium catalyst place is lower because of oxygen level, and it is limited that temperature raises, and just guarantee the oxygen content after deoxidation, and favourable gas distributes again.
Claims (7)
1. one kind from the heat exchange type deoxygenator, it is characterized in that: it comprises upper shell (20), be positioned at shell and tube heat exchanger (16) and the lower shell (9) at middle part, be provided with between upper shell (20) and shell and tube heat exchanger (16) and be connected with upper tubesheet (17), be provided with between shell and tube heat exchanger (16) and lower shell (9) and be connected with lower tubesheet (11), described shell and tube heat exchanger is provided with heat-exchanger rig in (16), the top of shell and tube heat exchanger (16) is provided with inlet mouth (25), described shell and tube heat exchanger (16) is by being communicated with lower shell (9) communicating pipe (7), described upper shell (20) top is provided with air outlet (30).
2. according to claim 1 from the heat exchange type deoxygenator, it is characterized in that: described heat-exchanger rig comprises at least two the highly different traverse baffles (14) that are installed on shell and tube heat exchanger (16) inwall, be equipped with a plurality of heat transfer tubes (15) on described traverse baffle (14), the upper/lower terminal of described heat transfer tube (15) is positioned respectively upper tubesheet (17) and lower tubesheet (11) is upper, and upper shell (20) and lower shell (9) are communicated with by heat transfer tube (15).
3. according to claim 2 from the heat exchange type deoxygenator, it is characterized in that: described traverse baffle (14) arranges two, and upper baffle and lower baffle are crisscross arranged on the inwall of shell and tube heat exchanger (16), forms the circulation passage of continuous bending.
4. according to claim 3 from the heat exchange type deoxygenator, it is characterized in that: described upper and lower tube sheet and traverse baffle (14) are rectangle structure, are provided with through hole above it.
5. according to claim 4 from the heat exchange type deoxygenator, it is characterized in that: described inlet mouth (25) is communicated with the cold shock interface (8) of being located on communicating pipe (7) by the pipeline with valve.
6. described from the heat exchange type deoxygenator according to claim 1～5 any one, it is characterized in that: be provided with the first barrier (22-1) in described lower shell (9), described the first barrier (22-1) top is provided with first paragraph palladium catalyst; Be provided with from top to bottom the 3rd barrier (22-3), the second barrier (22-2) in described upper shell (20), be filled with respectively second segment catalyst, the 3rd section catalyst on described the second barrier (22-2), the 3rd barrier (22-3).
7. according to claim 6 from the heat exchange type deoxygenator, it is characterized in that: the upper portion side wall of described lower shell (9) is provided with the first hand hole (23), and the upper portion side wall of described upper shell (20) is provided with the second hand hole (27).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320305935 CN203359975U (en) | 2013-05-31 | 2013-05-31 | Self-heat-exchange deaerator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201320305935 CN203359975U (en) | 2013-05-31 | 2013-05-31 | Self-heat-exchange deaerator |
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| Publication Number | Publication Date |
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| CN203359975U true CN203359975U (en) | 2013-12-25 |
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| CN 201320305935 Expired - Fee Related CN203359975U (en) | 2013-05-31 | 2013-05-31 | Self-heat-exchange deaerator |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103941763A (en) * | 2014-01-07 | 2014-07-23 | 广州粤能电力科技开发有限公司 | Boiler water supply de-aerator temperature rise automatic control method and system |
| CN107244657A (en) * | 2017-08-09 | 2017-10-13 | 沈阳东方钛业股份有限公司 | A kind of multipipe structure ozone generator and its manufacture method |
| CN111717891A (en) * | 2020-06-23 | 2020-09-29 | 广东鑫国源能源有限公司 | Novel hydrogen deoxygenator |
| CN112174090A (en) * | 2020-10-20 | 2021-01-05 | 湖南恒光科技股份有限公司 | Hydrogen deoxidization process system and method |
| CN114456848A (en) * | 2022-02-23 | 2022-05-10 | 山西沃能化工科技有限公司 | Device and method for deoxidizing and desulfurizing converter gas |
-
2013
- 2013-05-31 CN CN 201320305935 patent/CN203359975U/en not_active Expired - Fee Related
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103941763A (en) * | 2014-01-07 | 2014-07-23 | 广州粤能电力科技开发有限公司 | Boiler water supply de-aerator temperature rise automatic control method and system |
| CN103941763B (en) * | 2014-01-07 | 2016-04-13 | 广州粤能电力科技开发有限公司 | The intensification autocontrol method of boiler feed deaerator and system |
| CN107244657A (en) * | 2017-08-09 | 2017-10-13 | 沈阳东方钛业股份有限公司 | A kind of multipipe structure ozone generator and its manufacture method |
| CN107244657B (en) * | 2017-08-09 | 2023-03-31 | 沈阳东方钛业股份有限公司 | Ozone generator with multi-tube structure and manufacturing method thereof |
| CN111717891A (en) * | 2020-06-23 | 2020-09-29 | 广东鑫国源能源有限公司 | Novel hydrogen deoxygenator |
| CN112174090A (en) * | 2020-10-20 | 2021-01-05 | 湖南恒光科技股份有限公司 | Hydrogen deoxidization process system and method |
| CN112174090B (en) * | 2020-10-20 | 2021-11-16 | 湖南恒光科技股份有限公司 | Hydrogen deoxidization process system and method |
| CN114456848A (en) * | 2022-02-23 | 2022-05-10 | 山西沃能化工科技有限公司 | Device and method for deoxidizing and desulfurizing converter gas |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20131225 Termination date: 20160531 |