CN2350120Y - Thermal balance high-pressure energy-saving reactor - Google Patents
Thermal balance high-pressure energy-saving reactor Download PDFInfo
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- CN2350120Y CN2350120Y CN 98240557 CN98240557U CN2350120Y CN 2350120 Y CN2350120 Y CN 2350120Y CN 98240557 CN98240557 CN 98240557 CN 98240557 U CN98240557 U CN 98240557U CN 2350120 Y CN2350120 Y CN 2350120Y
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Abstract
The utility model relates to an energy-saving reactor for pressurization gas-solidoid catalytic reaction. After unreacted gas and reaction gas carry out heat exchange and temperature rise in a heat exchanger in a reactor tower, the temperature of the unreacted gas is raised further by external hot gas, and the unreacted gas enters a catalyst layer to react. The utility model is suitable for the case that reaction heat is insufficient to maintenance reaction self-heating to proceed, such as methanation reactor with hydrocarbon of low concentration can make use of the residual heat of the factory fluid reasonably to implement the heat balance operation of the reactor, and a normally open electric heater is not needed to compensate heat to maintain production operation, so the economic effects of electricity saving and energy saving are achieved.
Description
The utility model is a kind of gas-solid-phase catalytic reaction device, is used for fluid catalytic reaction and diabatic process, belongs to field of chemical engineering, is specially adapted to the methanation under low reaction pneumatolytic part, also can be used for the building-up process of other low reaction heat.
As everyone knows, synthesizing methanol, methyl ether and methanation reaction all are strong exothermal reactions under hydrogen, nitrogen synthetic ammonia or the gas pressurized such as hydrogen, carbon monoxide.Under the general technology condition, the problem that this class reactor designing institute will solve emphatically is in time to remove reaction heat to cross heat inactivation to prevent catalyst.This class reaction can utilize basket pyroreaction gas to heat into, and the cryogenic gas of reactor carries out to keep reaction self-heating.But reaction heat is how much relevant with the effective ingredient of participation reaction in the reaction gas.For example in Ammonia Production, make with extra care syngas for synthetic ammonia with methanation, per 1% (volume ratio) carbon monoxide and H-H reaction generate the reaction heat of methane and water generates in the unstripped gas, temperature rise is 69 ℃ under thermal insulation, at present ammonia factory controls generally that carbon monoxide gas can satisfy the self-heating of reaction and carry out in the methanation inlet gas about 0.6%.In the middle pressure methyl alcohol methanation process that occurs in recent years, methanation import carbon monoxide is 0.3～0.6%, adopts preheating to advance method such as tower gas and still can reach high pressure self-heating methanation reaction.Carry out but under low CO content more, just be difficult to self-heating, need often drive electric heater and keep operation, thereby cause the power consumption power consumption.
Task of the present utility model is to solve the problem that prior art exists according to the fuel factor of gas-solid-phase catalytic reaction and HEAT TRANSFER LAW, seeks the energy-conservation reactor that can reach the thermal balance successive reaction under a kind of low reaction heat.
A kind of energy-saving reactor of the gas-solid-phase catalytic reaction that is used to pressurize down has reactor pressure-bearing urceolus P, the internals that basket R and heat exchanger E form, and basket R has cover plate H, cylindrical shell S, the catalyst K of bottom card J and interior dress, register C and C
b, heat exchangers in towers has tubular type or plate type heat exchanger E
1, or E
1And E
2, mainly be that reactor is provided with pipe b
2And b
3The unreacting gas passage or the high temperature of UNICOM's cryogenic heat exchanger and high-temperature heat-exchanging are worn hot gas path, and the unreacting gas 1 that advances urceolus P is through heat exchangers in towers E
1It is again through high-temperature heat-exchanging E behind the unreacting gas 2 that heat exchange heats up
2Wear the further heat exchange of hot gas with external high temperature and heat up, advance basket R again and react to unreacting gas 3.Above-mentioned high-temperature heat-exchanging E
2Can be located in the urceolus P, at this moment high temperature is worn hot gas 6 by pipe b
2Enter heat exchanger E
2, at cryogenic heat exchanger E
1Unreacting gas 2 after heat exchange heats up is through high-temperature heat-exchanging E
2Wear the further heat exchange of hot gas 6 and heat up and react with external for unreacting gas 3 advances basket R again.High-temperature heat-exchanging also can be located at outside the urceolus P, at this moment advances urceolus P through cryogenic heat exchanger E
1The unreacting gas 2 that heat exchange heats up is by pipe b
2It is outer through high-temperature heat-exchanging E to guide to tower
2With wear the further heat exchange of hot gas and heat up and react for unreacting gas 3 advances basket R again.The operating pressure of reactor is 3.0～32MPa, and wearing hot gas pressure is 0.5～32MPa.The operating pressure of wearing hot gas can be lower than the operating pressure of reactor, also can equate, wears hot gas and can be ammonia synthesis and go out tower hot gas.Wear hot gas and also can be conversion hot gas.
Below in conjunction with accompanying drawing, be described further.
Fig. 1 be high-temperature heat-exchanging be located at urceolus outer by urceolus P basket R and cryogenic heat exchanger E
1The reactor schematic diagram of forming.
In Fig. 1, in outer pressure carriage P, top basket R is by cover plate H, simplified S, bottom card J and interior dress catalyst K.Heat exchanger tube courage C is arranged in the catalyst layer
b, collection chamber D is arranged, bottom heat exchanger E on the cover plate
1Be shell and tube, unreacting gas 1 enters urceolus at lower columns heat exchange of heat pipe E
1Pipe between be gas 2 from reaction hot gas 4 heat temperature raisings of basket R, then through pipe b
2Going out tower, to go tower external heat exchanger to be worn the hot gas heat temperature raising by high temperature be gas 3, again by managing b among Fig. 1
3Advance tower to the catalyst layer reaction, go out catalyst layer gas 4 at heat exchangers in towers E
1Intraductal heat transfer gives pipe outer gas 2, and be cooled to temperature for example 100 ℃ gas 5 go out tower.
Be the heat transfer relation schematic diagram of this reactor heat exchanger among Fig. 2.Cryogenic heat exchanger E in tower
1Middle unreacting gas is heated by reaction gas, and temperature is by T
1Be elevated to T
2, the reaction gas temperature is by T
4Be reduced to T
5, then unreacting gas in high-temperature heat-exchanging by high temperature wear hot gas for example the heating of ammonia convertor exhaust gas or high temperature shift gas by T
2Be warming up to T
3, wear hot gas by T
6Cool to T
7, unreacting gas advances basket, finishes reaction and is reaction gas.Because reaction heat is little and have heat radiation, reaction temperature T
4Be lower than unreacted temperature T
3Therefore can not heat unreacting gas with reaction gas makes by T
2Be warmed up to T
3, must wear hot gas with other high temperature and heat.
Fig. 3 is high-temperature heat-exchanging E
2Be located in the high pressure urceolus P (by urceolus P, basket R and high cryogenic heat exchanger E
1, E
2Form) the reactor schematic diagram.Figure middle and upper part basket R has cold air distributor C by cover plate H, cylindrical shell S, bottom card J and interior dress catalyst K in the catalyst layer, regulate the catalyst layer temperature with cold air 9, figure middle and lower part cryogenic heat exchanger E
1With high-temperature heat-exchanging E
2Be spiral heat exchanger.Unreacting gas 1 enters the laggard cryogenic heat exchanger E of urceolus P
1Cold air path thermal response gas 4 heat temperature raisings that gone out basket R be gas 2, then at high-temperature heat-exchanging E
2Cold air path in by by the pipe b
3The high temperature of introducing is worn hot gas 6 and is further heated, and is warmed up to gas 3 and goes the basket reaction, and wearing the hot gas cooling is that gas 7 is by pipe b
2Go out tower, the reaction gas 4 that goes out basket R is at cryogenic heat exchanger E
1It is that gas 5 is after pipe b that hot gas path conducts heat to cooling behind the unreacting gas
1Go out tower, lower end b
4 Middle gas 8 is that conditioned reaction device catalyst temperature is used.
Embodiment produces 100000 tons of high pressure methyl alcohol methanation devices such as synthetic ammonia installation employing per year.Refining syngas for synthetic ammonia Alloy instead of Copper is washed method eliminating minute CO, and the high-pressure methanation tower adopts Fig. 3 pattern, and diameter is with φ 1000, in adorn Ni-based methanation catalyst 5M
3, inlet tower gas amount 40000 NM
3/ h advances methanator CO 0.05%, CO
20.001%, CH
40.5%, H
274.589%, N
224.86%, 80 ℃ of temperature advance methanator cryogenic heat exchanger E
1After be warmed up to 270 ℃, again at high-temperature heat-exchanging E
2In with through the pipe b
3Introduce, go out tower hot gas 6 temperature by synthetic ammonia and wear the hot gas heat exchange for 360 ℃, the latter cools to 300 ℃ gas 7 through pipe b
2Go out tower, unreacting gas is warmed up to 330 ℃ and advances basket reaction, goes out 310 ℃ of basket temperature, and at E
1In with the inlet tower gas heat exchange after cool to 120 ℃ and go out tower.
The utility model reasonably utilizes the thermal balance operation of the rich process gas waste heat realization response device of factory, does not need typical electric heater to compensate heat and keeps production run, has reached the economic effect of power and energy saving.
Claims (8)
1. the energy-saving reactor of the gas-solid-phase catalytic reaction that is used to pressurize down has reactor pressure-bearing urceolus P, the internals that basket R and heat exchanger E form, and basket R has cover plate H, cylindrical shell S, the catalyst K of bottom card J and interior dress, register C and C
b, heat exchangers in towers has tubular type or plate type heat exchanger E
1, or E
1And E
2, it is characterized in that reactor is provided with pipe b
2And b
3The unreacting gas passage or the high temperature of UNICOM's cryogenic heat exchanger and high-temperature heat-exchanging are worn hot gas path, advance unreacting gas 1 cryogenic heat exchanger E in tower of urceolus P
1It is again through high-temperature heat-exchanging E behind the unreacting gas 2 that heat exchange heats up
2Wear the further heat exchange of hot gas with external high temperature and heat up, advance basket R again and react to unreacting gas 3.
2. energy-saving reactor according to claim 1 is characterized in that high-temperature heat-exchanging E
2Be located in the urceolus P, high temperature is worn hot gas 6 by pipe b
2Enter heat exchanger E
2, at cryogenic heat exchanger E
1Unreacting gas 2 after heat exchange heats up is through high-temperature heat-exchanging E
2Wear the further heat exchange of hot gas 6 and heat up and react with external for unreacting gas 3 advances basket R again.
3. energy-saving reactor according to claim 1 is characterized in that high-temperature heat-exchanging is located at outside the tower, advances urceolus P through cryogenic heat exchanger E
1The unreacting gas 2 that heat exchange heats up is by pipe b
2It is outer through high-temperature heat-exchanging E to guide to tower
2With wearing the further heat exchange intensification of hot gas is that unreacting gas 3 is again by pipe b
3Advancing basket R reacts.
4. energy-saving reactor according to claim 1, the operating pressure that it is characterized in that reactor is 3.0～32MPa.
5. energy-saving reactor according to claim 1, it is characterized in that wearing hot gas pressure is 0.5～32MPa.
6. energy-saving reactor according to claim 1, it is characterized in that wearing hot gas is that ammonia synthesis goes out tower hot gas.
7. energy-saving reactor according to claim 1, it is characterized in that wearing hot gas is conversion hot gas.
8. energy-saving reactor according to claim 1, the pressure that it is characterized in that wearing hot gas is lower than the operating pressure of reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98240557 CN2350120Y (en) | 1998-09-14 | 1998-09-14 | Thermal balance high-pressure energy-saving reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 98240557 CN2350120Y (en) | 1998-09-14 | 1998-09-14 | Thermal balance high-pressure energy-saving reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2350120Y true CN2350120Y (en) | 1999-11-24 |
Family
ID=33987533
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 98240557 Expired - Lifetime CN2350120Y (en) | 1998-09-14 | 1998-09-14 | Thermal balance high-pressure energy-saving reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2350120Y (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100386138C (en) * | 2003-12-06 | 2008-05-07 | 杭州林达化工科技有限公司 | Process and equipment for internal heat exchanging catalytic reaction |
| CN101966440A (en) * | 2010-10-19 | 2011-02-09 | 西北大学 | Cambered plate type gas-solid phase reactor |
-
1998
- 1998-09-14 CN CN 98240557 patent/CN2350120Y/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100386138C (en) * | 2003-12-06 | 2008-05-07 | 杭州林达化工科技有限公司 | Process and equipment for internal heat exchanging catalytic reaction |
| 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 |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |