CN101559342A - Gas-solid catalytic reaction heat exchange device and reaction heat exchange process - Google Patents
Gas-solid catalytic reaction heat exchange device and reaction heat exchange process Download PDFInfo
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- CN101559342A CN101559342A CNA2009100743323A CN200910074332A CN101559342A CN 101559342 A CN101559342 A CN 101559342A CN A2009100743323 A CNA2009100743323 A CN A2009100743323A CN 200910074332 A CN200910074332 A CN 200910074332A CN 101559342 A CN101559342 A CN 101559342A
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Abstract
The invention relates to a gas-solid catalytic reaction heat exchange device and a reaction heat exchange process. The gas-solid catalytic reaction heat exchange device comprises a reactor filled with a catalyst, and a heat exchanger connected with the outside of the reactor. Feed gas undergoes reaction under the action of the catalyst after entering the reactor, materials after the reaction are discharged from the reactor, a heat transferring medium exchanges heat with reactant, and steam or condensate liquid after the heat exchange is discharged from the reactor; the steam or condensate liquid out of the reactor enters the heat exchanger, exchanges heat with cooling water or water vapor introduced from the other side of the heat exchanger, and condensate liquid or steam after the heat exchange is discharged from the heat exchanger and enters the reactor; and the cooling water or the steam is heated into water vapor or condensed into condensed water which is discharged from the heat exchanger. Because a waste heat recoverer or a reboiler is arranged outside the reaction device, reaction heat in the catalytic reaction can be removed in time or the reaction heat heats endothermic catalytic reaction; and simultaneously, the differential pressure of double-sided operation of the reactor is greatly reduced, the design and manufacture difficulties of the reactor are reduced, the operation of the reaction device is more reliable and safe, and the manufacturing cost of the device is greatly reduced.
Description
Technical field
The present invention relates to reacting replacing heat device and reacting replacing heat technology, relate in particular to cooling or heat air solid catalysis reacting replacing heat device reaction heat-exchanging process.
Background technology
The cooling or the heating process process of existing gas-solid catalysis are as follows: reactor adopts shell-and-tube, unreacted unstripped gas enters the reaction side that reactor is equipped with catalyst, the heat release or the endothermic reaction take place under the effect of catalyst, heat transferring medium water or steam enter the heat exchange side of reactor, boiling generation steam by water is removed reaction heat very soon, or adopts steam to make reaction continue to carry out for reaction provides heat.Because the water of boiling or the steam of heating are when adapting with reaction temperature, it is bigger that the pressure of reactor both sides often differs, thereby make that the operation pressure reduction of reactor is bigger, and manufacturing expense is higher, and security, the less stable of reactor operation.Fig. 1 is the methanol reactor structure and the heat-exchanging process schematic diagram of existing low-pressure process byproduct steam, methanol reactor adopts the shell-and-tube synthetic tower, unreacted unstripped gas 1 enters in the pipe that methanol reactor C is equipped with catalyst, exothermic reaction takes place under the effect of catalyst, operating pressure 5.0～6.0MPa, 220～280 ℃ of reaction temperatures, the reacted material 2 that contains methyl alcohol goes out reactor C, cooling water 10 enters between the pipe of methanol reactor C, reaction heat is removed very soon by the water generates steam of managing outer boiling, and the by-product temperature is 200～260 ℃, and the water vapour of pressure 1.5～4.8MPa enters drum D to carry out after carbonated drink separates, steam 6 goes out drum, supplementing water 5 mends drum, 200,000 tons/year methanol synthesis reactor, and device diameters needs 4.8 meters, tube sheet 9a, 320 millimeters of 9b thickness, it manufactures and designs obviously very big difficulty.
Summary of the invention
The invention provides a kind of gas and solid phase catalyzing heat release or endothermic reaction heat-exchanging process,, and make the operation of reactor reliable more, safe, stable with reduction gas solid catalytic reactor manufacture difficulty and manufacturing expense.
The present invention seeks to realize like this: this gas and solid phase catalyzing heat exchange reaction unit comprises the reactor that is filled with catalyst, it is characterized in that the outer heat exchanger that connects of described reactor, described heat exchanger heat transferring medium goes out reactor outlet successively after reactor inlet, catalytic bed heat exchange, the heat transferring medium that goes out reactor outlet is gone into heat exchanger entrance, and the heat transferring medium that goes out heat exchanger reenters reactor inlet and recycles.
Described heat exchanger is waste heat recoverer or reboiler.
Above-mentioned heat transferring medium can be a kind of simple substance, also can be mixture, under the active operating temperature of different catalysts, can adjust the composition of heat transferring medium, with the more approaching requirement of the pressure differential that satisfies the reactor both sides, thereby reduces the operation pressure reduction of reactor both sides.
The reacting replacing heat technology of described gas-solid catalysis heat-exchanger rig may further comprise the steps:
A. unstripped gas reacts under the effect of catalyst after entering reactor, and reacted material goes out reactor through the bottom;
B. heat transferring medium enters reactor and reactant carries out heat exchange, and the steam of heat transferring medium or condensate liquid go out reactor after the heat exchange;
C. the steam or the condensate liquid that go out the reactor heat transferring medium enter in the heat exchanger, and the cooling water or the water vapour that feed with the heat exchanger opposite side carry out heat exchange, and the condensate liquid of heat transferring medium or steam enter reactor after going out heat exchanger after the heat exchange, so circulation;
D. cooling water is heated to form and goes out heat exchanger after water vapour or water vapour are condensed into condensed water.
The technological progress that the present invention obtains: because heat exchanger is set in the gas-solid catalysis device is waste heat recoverer or reboiler and employing heat transferring medium, remove reaction heat or in the endothermic catalytic reaction heating in catalytic reaction, reactor bilateral operation pressure reduction is reduced greatly, therefore reduced DESIGN OF REACTOR, manufacture difficulty, made consersion unit move reliable more, safety, stable.The low pressure methanol reactor heat-exchanging process of aforementioned existing byproduct steam for example, heat transferring medium adopts methanol aqueous solution, can make the pressure of reactor both sides equate, consider the fluctuating factor of operation, when desirable design pressure difference 1.0MPa, 4.8 meters of reactor diameters, the thickness of tube sheet can be reduced to 150 millimeters, not only improve the safety in operation of reactor, greatly reduced the equipment making cost simultaneously.
Description of drawings
Fig. 1 is the low-pressure process methanol reactor structure and the heat-exchanging process schematic diagram of existing byproduct steam.
Fig. 2 is the gas-solid catalysis heat-releasing device and the reacting replacing heat process schematic representation of byproduct steam of the present invention.
Fig. 3 is steam-heated gas-solid catalysis heat sink structure and reacting replacing heat process schematic representation for the present invention adopts.
The specific embodiment
Embodiment 1: as shown in Figure 2, the outer waste heat recoverer B that connects of reactor A, heat transferring medium goes out the reactor A top exit successively in the waste heat recoverer B after reactor A bottom inlet 3, catalytic bed heat exchange, the heat transferring medium 4 that goes out the reactor A top exit is gone into waste heat recoverer B inlet, the heat transferring medium that goes out waste heat recoverer B reenters reactor A bottom inlet 3 and recycles, and cooling water 5 goes out waste heat recoverer B after being heated to form water vapour 6.With the synthesizing methanol is example, and unreacted unstripped gas 1 enters the catalyst reaction side is housed in the methanol synthesis reactor A, and unstripped gas 1 contains CO11.2%, CO
24.7%, H
248.5%, its pressure is 5.5MPa, and 220 ℃ of temperature react under the effect of catalyst, the portion gas synthesizing methanol, and reaction temperature is 245 ℃, the reacted gas 2 that contains 5.6% methyl alcohol goes out reactor A.Heat transferring medium is that the methanol aqueous solution of weight content about 90% is through the 3 heat exchange sides that enter methanol synthesis reactor A that enter the mouth, reactant heat exchange evaporation with the reaction side, 220 ℃ of its evaporating temperatures, pressure are 5.5MPa, and the heat transferring medium 4 after the heat exchange goes out methanol synthesis reactor A through top exit.The heat transferring medium 4 that goes out methanol synthesis reactor A enters in the pipe of waste heat recoverer B, and with the outer cooling water heat exchange of pipe, the heat transferring medium of heat exchange condensation goes out waste heat recoverer B and 3 enters reactor A, so circulation after enter the mouth.Temperature is that 80 ℃ cooling water 5 enters between waste heat recoverer B pipe, and the steam 6 that is produced pressure 1.9MPa by heat transferring medium 4 heating goes out waste heat recoverer B.
Embodiment 2: as shown in Figure 3, the present embodiment difference from Example 1 is, the outer reboiler B1 that connects of reactor A, heat transferring medium goes out the reactor A lower part outlet successively in the reboiler B1 behind reactor A top inlet, catalytic bed indirect heat exchange, the heat transferring medium 41 that goes out the reactor A lower part outlet is gone into reboiler B1 inlet, the heat transferring medium 31 that goes out reboiler B1 reenters reactor A top inlet and recycles, and water vapour 51 goes out reboiler B1 after being condensed into condensed water 61.With the methanol conversion hydrogen is example, and its pressure is 1.5MPa, and the raw material vapour 1 of the first alcohol and water that temperature is 220 ℃ enters outside the pipe of methanol conversion A, and pipe is outer to be equipped with the catalyst that is used for methanol conversion hydrogen manufacturing, under the effect of catalyst, and methyl alcohol and H
2O reacts and generates H
2, reaction temperature is 230 ℃, contains H after the reaction
2Gas 2 go out methanol conversion A outlet at bottom.Isoamyl alcohol 31 as heat transferring medium is housed in the pipe of conversion reactor A, its temperature is 240 ℃, pressure is 1.57MPa, the steam of this heat transferring medium enters in the pipe of conversion reactor A, provide condensation behind the heat for managing outer methanol conversion reaction, condensed heat transferring medium 41 goes out in the pipe that conversion reactor A enters reboiler B1, is evaporated to isoamyl alcohol gas with the water vapour heat exchange of pipe external pressure 4.45MPa and goes out reboiler B1, is entered in the pipe of conversion reactor A by top then to recycle.
Claims (4)
1. gas-solid catalysis heat-exchanger rig, it comprises the reactor that is filled with catalyst, it is characterized in that the outer heat exchanger that connects of described reactor, described heat exchanger heat transferring medium goes out reactor outlet successively after reactor inlet, catalytic bed heat exchange, the heat transferring medium that goes out reactor outlet is gone into heat exchanger entrance, and the heat transferring medium that goes out heat exchanger reenters reactor inlet and recycles.
2. gas-solid catalysis heat-exchanger rig according to claim 1 is characterized in that described heat exchanger is waste heat recoverer or reboiler.
3. the reacting replacing heat technology of a gas-solid catalysis heat-exchanger rig as claimed in claim 1 is characterized in that it may further comprise the steps:
A. unstripped gas reacts under the effect of catalyst after entering reactor, and reacted material goes out reactor through the bottom;
B. heat transferring medium enters reactor and reactant carries out heat exchange, and the steam or the condensate liquid of the heat transferring medium after the heat exchange go out reactor;
C. the steam or the condensate liquid that go out the reactor heat transferring medium enter in the heat exchanger, and the cooling water or the water vapour that feed with the heat exchanger opposite side carry out heat exchange, and the condensate liquid of heat transferring medium or steam enter reactor after going out heat exchanger after the heat exchange, so circulation;
D. cooling water is heated to form and goes out heat exchanger after water vapour or water vapour are condensed into condensed water.
4. according to the reacting replacing heat technology of claim 1,2 or 3 described gas-solid catalysis heat-exchanger rigs, it is characterized in that described heat exchanger is waste heat recoverer or reboiler.
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| CNA2009100743323A CN101559342A (en) | 2009-05-12 | 2009-05-12 | Gas-solid catalytic reaction heat exchange device and reaction heat exchange process |
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|---|---|---|---|
| CNA2009100743323A CN101559342A (en) | 2009-05-12 | 2009-05-12 | Gas-solid catalytic reaction heat exchange device and reaction heat exchange process |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104368293A (en) * | 2014-11-07 | 2015-02-25 | 长兴三伟热熔胶有限公司 | Reaction kettle capable of reducing reaction time |
| CN104383861A (en) * | 2014-11-07 | 2015-03-04 | 长兴三伟热熔胶有限公司 | Cooling water circulation system of reaction kettle |
| CN107032300A (en) * | 2017-05-05 | 2017-08-11 | 金澳科技（湖北）化工有限公司 | A kind of hydrogen production by methanol system of reactor feed temperature stabilization |
| CN109225072A (en) * | 2018-09-14 | 2019-01-18 | 新奥科技发展有限公司 | A kind of synthesis reaction system and synthetic reaction method |
| CN114163468A (en) * | 2021-12-08 | 2022-03-11 | 昆明理工大学 | Preparation method and equipment of organic silicon monomer |
-
2009
- 2009-05-12 CN CNA2009100743323A patent/CN101559342A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104368293A (en) * | 2014-11-07 | 2015-02-25 | 长兴三伟热熔胶有限公司 | Reaction kettle capable of reducing reaction time |
| CN104383861A (en) * | 2014-11-07 | 2015-03-04 | 长兴三伟热熔胶有限公司 | Cooling water circulation system of reaction kettle |
| CN107032300A (en) * | 2017-05-05 | 2017-08-11 | 金澳科技（湖北）化工有限公司 | A kind of hydrogen production by methanol system of reactor feed temperature stabilization |
| CN107032300B (en) * | 2017-05-05 | 2019-04-26 | 金澳科技（湖北）化工有限公司 | A kind of hydrogen production by methanol system that reactor feed temperature is stable |
| CN109225072A (en) * | 2018-09-14 | 2019-01-18 | 新奥科技发展有限公司 | A kind of synthesis reaction system and synthetic reaction method |
| CN114163468A (en) * | 2021-12-08 | 2022-03-11 | 昆明理工大学 | Preparation method and equipment of organic silicon monomer |
| CN114163468B (en) * | 2021-12-08 | 2024-03-15 | 昆明理工大学 | Preparation method and equipment of organic silicon monomer |
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Open date: 20091021 |