CN104399413B - One is controlled moves thermal reactor - Google Patents
One is controlled moves thermal reactor Download PDFInfo
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- CN104399413B CN104399413B CN201410662794.8A CN201410662794A CN104399413B CN 104399413 B CN104399413 B CN 104399413B CN 201410662794 A CN201410662794 A CN 201410662794A CN 104399413 B CN104399413 B CN 104399413B
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- gas
- heat exchanger
- endless tube
- aqueduct
- distributing cylinder
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/0285—Heating or cooling the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
- C01B2203/02—Processes for making hydrogen or synthesis gas
- C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
- C01B2203/0227—Processes for making hydrogen or synthesis gas containing a reforming step containing a catalytic reforming step
Abstract
The invention discloses and a kind of controlledly move thermal reactor, move heat pipe bundle and comprise outfall sewer, water inlet manifold, endless tube, dividing plate, caecum formula heat exchanger tube and aqueduct; Described dividing plate is arranged at the middle part of endless tube, the upper and lower of endless tube is divided into diversion box and header tank, water inlet manifold is communicated with the diversion box on endless tube top, outfall sewer is communicated with the header tank of endless tube bottom, aqueduct is set in caecum formula heat exchanger tube, the one end open other end of caecum formula heat exchanger tube is closed, the openend of caecum formula heat exchanger tube is communicated with the header tank of endless tube bottom, aqueduct both ends open, the top of aqueduct is communicated with the diversion box on endless tube top, and the bottom of aqueduct is positioned on the blind end of caecum formula heat exchanger tube.Catalyst frame of the present invention, move heat pipe bundle and be separated with pressure-bearing shell, easy access, catalyst self-unloading, Catalyst packing; Hot-water line will be moved be embedded in beds inside and beds internal-response heat can be removed in time.
Description
Technical field
The present invention relates to a kind of fixed-bed catalytic reactor, in particular a kind ofly controlledly move thermal reactor.
Background technology
After CO transformationreation, device is as a kind of extensive use reactor of chemical industry, therebetween, people have carried out improvement repeatedly to shift-converter, by original holoaxial to change into overall diameter to, very good effect is obtained in catalyst bed layer resistance, but beds is still adiabatic reaction, and beds is divided into some beds, takes indirect heat exchange or use Technology Quenched with Water between every bed.It is low that this indirect heat exchange reclaims transformation system heat quality, reclaims sensible heat and latent heat efficiency is low, the easy overtemperature of catalyst, convert and be also mixed with the defects such as side reaction such as methanation simultaneously.
The carbonylation synthesis reactor of coal-ethylene glycol, loading catalyst in the pipe of current employing ф 25X2, pipe external application water shifting heat, a shell-and-tube reactor is made up of to ф 21 cylinder shape catalyst bed thousands of holoaxial, distribution of gas is uneven, side reaction thing is many, catalyst bed layer resistance is large, thermal stress is large, equipment leakage, the carbonylation synthesis reactor of glycol unit of a set of 200,000 tons/year need the parallel running of 6 shell reactors, the defects such as construction investment is large.
The esterification hydrogenation reactor of coal-ethylene glycol, loading catalyst in the pipe of current employing ф 38X2, pipe external application water shifting heat, the defects such as a shell-and-tube reactor is made up of to ф 34 cylinder shape catalyst bed thousands of holoaxial, and distribution of gas is uneven, side reaction thing is many, catalyst bed layer resistance is large, thermal stress large, equipment leakage, construction investment are large.
The reaction of coal preparing natural gas adopts: n adiabatic bed coordinates the heat-removing way of n useless overheated boiler, and need to increase reactants water steam to suppress first, second adiabatic bed reaction, configuration cycles gas simultaneously, otherwise there is first, second adiabatic bed temperature runaway phenomenon, the defects such as operation energy consumption is high, plant investment is large, SR is large.
The Fischer-Tropsch synthesis of coal liquifaction, coal paraffin is not also at the maximization device of operation, the small-sized F-T synthesis device reaction device that part is being run also is shell and tube reactor, Fe (or Co) series catalysts is seated in ф 76X4 pipe, still has that distribution of gas is uneven, overtemperature, carbon distribution, Long carbon chain alkane yield are low, resistance is large, equipment leakage, is difficult to the defects such as maximization.
Summary of the invention
The object of the invention is to overcome the deficiencies in the prior art, provide and a kind of controlledly move thermal reactor, be converted into steam generation decalescence by water in heat exchanger tube and remove heat of reaction in beds in time.
The present invention is achieved by the following technical solutions, and what the present invention includes pressure-bearing shell and be arranged at sealed catalyst frame in pressure-bearing shell and water route self-loopa moves heat pipe bundle, moves outside heat pipe bundle described in sealed catalyst frame is coated on; Described heat pipe bundle of moving comprises outfall sewer, water inlet manifold, endless tube, dividing plate, caecum formula heat exchanger tube and aqueduct; Described dividing plate is arranged at the middle part of endless tube, the upper and lower of endless tube is divided into diversion box and header tank, water inlet manifold is communicated with the diversion box on endless tube top, outfall sewer is communicated with the header tank of endless tube bottom, aqueduct is set in caecum formula heat exchanger tube, the one end open other end of caecum formula heat exchanger tube is closed, the openend of caecum formula heat exchanger tube is communicated with the header tank of endless tube bottom, aqueduct both ends open, the top of aqueduct is communicated with the diversion box on endless tube top, and the bottom of aqueduct is positioned on the blind end of caecum formula heat exchanger tube.
Described sealed catalyst frame comprises sealing plate, gas distributing cylinder, gas collecting jar with ground-on cover plate; Described gas distributing cylinder is arranged in pressure-bearing shell, sealing plate is fixed on the top of gas distributing cylinder, gap between gas distributing cylinder and pressure-bearing shell is formed radially distribution of gas room along pressure-bearing shell, gas collecting jar with ground-on cover plate is arranged in gas distributing cylinder along the radial direction of gas distributing cylinder, loading catalyst in gas distributing cylinder, described endless tube, caecum formula heat exchanger tube and aqueduct lay respectively in gas distributing cylinder.
Described pressure-bearing shell comprises upper cover, enclosure body, low head; Described upper cover by Flange joint in enclosure body, enclosure body and low head one-body molded; Upper cover being offered respectively the water inlet for connecting water inlet manifold, for connecting delivery port and the air inlet of outfall sewer, low head being offered respectively catalyst self-unloading short circuit and the gas outlet for being connected gas collecting jar with ground-on cover plate.
Be provided with supporting seat and gripper shoe in described enclosure body, described supporting seat is fixed on the inwall of enclosure body, and the two ends of gripper shoe are supported on supporting seat, and gas distributing cylinder, endless tube and gas collecting jar with ground-on cover plate support on the supporting plate successively.
Described sealing plate and be respectively equipped with the first seal between outfall sewer and water inlet manifold, is provided with the second seal, is provided with the 3rd seal between gas outlet and the escape pipe of gas collecting jar with ground-on cover plate between the bottom of gas distributing cylinder and low head.
The inner side of described gas distributing cylinder and the outside of gas collecting jar with ground-on cover plate arrange gas distribution grid respectively, and described gas distribution grid evenly offers multiple passage.
Gas enters upper cover inside from air inlet, then enters distribution of gas room, then enters in catalyst by the even radial direction of gas distributing cylinder, is having Co-Mo, pd/AI
2o
3, Cu, Ni, Cu-Zn, Fe, Co series catalysts completes the exothermic reactions such as conversion, synthesis, hydrogenation under catalytic condition, reacted gas enters escape pipe by gas collecting jar with ground-on cover plate, then flows out controlledly to move thermal reactor.Conversion, synthesis or the exothermic reaction liberated heat such as hydrogenation are converted into steam by the water be embedded in the caecum formula heat exchanger tube of catalytic inner and remove heat of reaction in beds in time, and by-product goes out the saturated vapor under different pressures.
Unsaturated water enters diversion box by water inlet manifold, aqueduct is assigned to by diversion box, unsaturated water flows out in aqueduct lower end, then the blind end of caecum formula heat exchanger tube is entered, flow from bottom to top, and complete the absorption to catalyst bed heat in caecum formula heat exchanger tube inside, and become supersaturation water, then enter header tank, be then discharged in the controlled drum moving thermal reactor periphery by outfall sewer and flash off saturated vapor.
The present invention is suitable for the reactors such as CO transformationreation, carbonylation reaction, esterification hydrogenation reaction, methanation reaction, methanol-fueled CLC reaction, Fischer-Tropsch synthesis.
The present invention is directed to CO transformationreation reactor existing problems and deficiency, and present high water/gas, high CO Water gas shift/WGS demand, have developed and controlledly move thermal reactor, caecum formula heat exchanger tube is embedded in beds, water in caecum formula heat exchanger tube is utilized to be converted into the principle of steam generation decalescence, by CO+H
2o → H
2+ CO
2+ Q
puttransformationreation liberated heat shifts out beds in time, guarantees reaction bed temperature≤380 DEG C, and the saturated vapor of by-product 0.8 ~ 9.0MPa, is beneficial to catalyst self-unloading and is convenient to move the maintenance of hot water tube bundle sections.Efficiently solve existing shift-converter reclaim heat quality low, reclaim low, the easy overtemperature of catalyst of heat energy efficiency, methanation side reaction, the difficult self-unloading of catalyst and the large defect of construction investment.
The present invention is directed to filling Pd/AI
2o
3the carbonylation shell and tube synthesis reactor existing problems of series catalysts, ethylene glycol and deficiency, have developed and controlledly move hot carbonylation synthesis reactor, caecum formula heat exchanger tube is embedded in beds, utilizes water in caecum formula heat exchanger tube to be converted into the principle of steam generation decalescence, by CO+CH
3oNO → (COOCH
3)
2+ NO+Q
putreaction liberated heat shifts out beds in time, guarantees reaction bed temperature≤140 DEG C, and the saturated vapor of by-product 0.2 ~ 0.3MPa, beds adopts full radial structure.Efficiently solve existing carbonylation synthesis reactor catalyst easy overtemperature, side reaction be large, bed resistance is large, be difficult to maximize, catalyst difficulty self-unloading and the large defect of construction investment.
The present invention is directed to filling Cu series catalysts, the esterification hydrogenation shell and tube synthesis reactor existing problems of ethylene glycol and not enough, have developed and controlledly move hot carbonylation synthesis reactor, caecum formula heat exchanger tube is embedded in beds, water in caecum formula heat exchanger tube is utilized to be converted into the principle of steam generation decalescence, by CH
3oNO adds H
2reaction (4H
2+ (COOCH
3)
2→ (OHCH
2cH
2oH)
2+ 2CH
3oH+Q
put) liberated heat shifts out beds in time, guarantees reaction bed temperature≤250 DEG C, and the saturated vapor of by-product 2.0 ~ 3.2MPa, beds adopts full radial structure.Efficiently solve the easy overtemperature of existing esterification hydrogenation reactor catalyst, side reaction is large, bed resistance is large, be difficult to maximization, the difficult self-unloading of catalyst and the large defect of construction investment.
The present invention is directed to the Ni series catalysts 320 ~ 420 DEG C of serviceability temperatures, develop and controlledly move hot methane synthesis reactor, caecum formula heat exchanger tube is embedded in beds, utilizes water in caecum formula heat exchanger tube to be converted into the principle of steam generation decalescence, by CO and H
2methanation reaction (CO+H
2→ CH
4+ H
2o+Q
put) liberated heat shifts out beds in time, guarantees reaction bed temperature≤420 DEG C, and the saturated vapor of by-product 3.8 ~ 12.0MPa, beds adopts full radial structure.The defect such as efficiently solve the easy overtemperature of existing methane synthesis reactor catalyst, bed resistance is large, operation energy consumption is high, plant investment is large, SR is large.
The present invention is directed to Fischer-Tropsch shell and tube synthesis reactor existing problems and the deficiency of filling Fe (or Co) series catalysts, have developed and controlledly move hot Fischer-Tropsch synthesis device, employing caecum formula heat exchanger tube is embedded in beds, water in caecum formula heat exchanger tube is utilized to be converted into the principle of steam generation decalescence, by CO and H
2fischer-Tropsch synthesis (nCO+ (2n+1) H
2→ C
nh
2n+2+ nH
2o+Q
put) liberated heat shifts out beds in time, guarantees Co reaction bed temperature≤240 DEG C, and the saturated vapor of by-product 1.8 ~ 2.8MPa; Fe reaction bed temperature≤260 DEG C, and the saturated vapor of by-product 2.0 ~ 3.8MPa, beds adopts full radial structure.Efficiently solve the defect that existing Fischer-Tropsch synthesis device exists.
The present invention has the following advantages compared to existing technology: (1) catalyst frame of the present invention, move heat pipe bundle and be separated with pressure-bearing shell, easy access, catalyst self-unloading, Catalyst packing;
(2) hot-water line will be moved be embedded in beds inside and beds internal-response heat can be removed in time, avoid original conversion, synthesis and hydrogenation catalyst to be sintered phenomenon to occur, efficiently solve catalyst short, the easy overtemperatures in service life such as existing conversion, synthesis and hydrogenation, side reaction thing is many, bed temperature is wayward, the driving time is long, be difficult to defects such as maximizing, operation energy consumption is high, construction investment is large;
(3) temperature of beds is regulated by byproduct steam pressure, guarantees that adjustment aspect is flexible, easy to control; When also guaranteeing to drive simultaneously, take to add steam to water circulation system, move thermal reactor temperature rise, with restart up by controlled rapidly;
(4) Natural Circulation is taked in water route, during unexpected parking, the controlled reactant moving thermal reactor internal residual part continues reaction, water route also still keeps circulation, and beds internal heat is shifted out, guarantee also can not surpass at the controlled bed temperature moving thermal reactor of unexpected dead ship condition, available protecting catalyst service life;
(5) controlled move thermal reactor gas distributor and gas collecting jar with ground-on cover plate realize inside and outside two items compensation, make radial gas distribution error≤5.0%, guarantee that distribution of gas is even; Controlledly move thermal reactor bed overall resistance≤0.01MPa;
(6) adopt overall diameter to beds, be easy to larger-scale unit, not only solve a transport difficult problem, reduce construction investment simultaneously.
Accompanying drawing explanation
figure1 is analysing and observe of reactor of the present invention
figure;
figure2 is structural representations of pressure-bearing shell
figure;
figure3 is the structural representations moving heat pipe bundle
figure.
Detailed description of the invention
Elaborate to embodiments of the invention below, the present embodiment is implemented under premised on technical solution of the present invention, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
Embodiment 1
As
figure1,
figure2 Hes
figureshown in 3, the present embodiment comprise pressure-bearing shell 1 and the sealed catalyst frame 2 that is arranged in pressure-bearing shell 1 and water route self-loopa move heat pipe bundle 3, move described in sealed catalyst frame 2 is coated on outside heat pipe bundle 3, move heat pipe bundle 3 and comprise outfall sewer 31, water inlet manifold 32, endless tube 33, dividing plate 34, caecum formula heat exchanger tube 35 and aqueduct 36, described dividing plate 34 is arranged at the middle part of endless tube 33, the upper and lower of endless tube 33 is divided into diversion box 37 and header tank 38, water inlet manifold 32 is communicated with the diversion box 37 on endless tube 33 top, outfall sewer 31 is communicated with the header tank 38 of endless tube 33 bottom, aqueduct 36 is set in caecum formula heat exchanger tube 35, the one end open other end of caecum formula heat exchanger tube 35 is closed, the openend of caecum formula heat exchanger tube 35 is communicated with the header tank 38 of endless tube 33 bottom, aqueduct 36 both ends open, the top of aqueduct 36 is communicated with the diversion box 37 on endless tube 33 top, the bottom of aqueduct 36 is positioned on the blind end of caecum formula heat exchanger tube 35, sealed catalyst frame 2 comprises sealing plate 21, gas distributing cylinder 22, gas collecting jar with ground-on cover plate 23, described gas distributing cylinder 22 is arranged in pressure-bearing shell 1, sealing plate 21 is fixed on the top of gas distributing cylinder 22, gap between gas distributing cylinder 22 and pressure-bearing shell 1 is formed radially distribution of gas room 24 along pressure-bearing shell 1, gas collecting jar with ground-on cover plate 23 is arranged in gas distributing cylinder 22 along the radial direction of gas distributing cylinder 22, loading catalyst in gas distributing cylinder 22, described endless tube 33, caecum formula heat exchanger tube 35 and aqueduct 36 lay respectively in gas distributing cylinder 22, pressure-bearing shell 1 comprises upper cover 11, enclosure body 12, low head 13, described upper cover 11 is connected in enclosure body 12 by flange 14, enclosure body 12 and low head 13 one-body molded, upper cover 11 being offered respectively the water inlet 15 for connecting water inlet manifold 32, for connecting delivery port 16 and the air inlet 17 of outfall sewer 31, low head 13 being offered respectively catalyst self-unloading short circuit 18 and the gas outlet 19 for being connected gas collecting jar with ground-on cover plate 23.
Supporting seat 121 and gripper shoe 122 is provided with in enclosure body 12, described supporting seat 121 is fixed on the inwall of enclosure body 12, the two ends of gripper shoe 122 are supported on supporting seat 121, and gas distributing cylinder 22, endless tube 33 and gas collecting jar with ground-on cover plate 23 are bearing in gripper shoe 122 successively.
Sealing plate 21 and be respectively equipped with the first seal 25 between outfall sewer 31 and water inlet manifold 32, is provided with the second seal 26, is provided with the 3rd seal 27 between the escape pipe of gas outlet 19 and gas collecting jar with ground-on cover plate 23 between the bottom of gas distributing cylinder 22 and low head 13.
The inner side of gas distributing cylinder 22 and the outside of gas collecting jar with ground-on cover plate 23 arrange gas distribution grid respectively, and gas distribution grid evenly offers multiple passage.Entering in catalyst frame 2 and the collection of reacted gas uniform being discharged of gas uniform can be facilitated.
The reactor of the present embodiment is applied to 220,000 tons/year of synthetic ammonia installation high water/gas than device:
1, design condition and requirement:
Water-gas gas componant:
2, transformation series
system is mainwant economic indicator list
| Sequence number | Major economic indicators title | Major economic indicators |
| 1 | Byproduct steam amount (2.5 ~ 3.8MPa) | 1063.5g/tNH 3 |
| 2 | Byproduct steam amount (1.0 ~ 1.27MPa) | 247.8kg/tNH 3 |
| 3 | The heating deoxygenation water yield (3.0MPa) | 1311.313kg/tNH 3 |
| 4 | Add hot desalinized water amount (directly removing thermal de-aeration) | 6388.78kg/tNH 3 |
| 5 | Deaerated water heater condensate liquid | 95.2kg/tNH 3 |
| 6 | Desalted water heater condensate liquid | 440.64kg/tNH 3 |
| 7 | Detoxification groove (becoming in advance) conversion ratio | ≤13％ |
| One becomes conversion ratio | ≥85％ | |
| Two become conversion ratio | ≥98.14％ | |
| 8 | System outlet CO content (butt) | ≤0.75％ |
| 9 | Transformation system resistance MPa | ≤0.05 |
Embodiment 2
The present embodiment is applied to 400,000 tons/year of low water/gas of synthetic ammonia installation than device, and other embodiments are identical with embodiment 1.
1, design condition and requirement:
Conversion tolerance: 160273Nm
3/ h
Operating pressure: 2.1MPa
Operating temperature: 35 ~ 40 DEG C
Gas componant is:
| Sequence number | Title | CO 2％ | CO％ | H 2％ | O 2％ | N 2％ | CH 4％ |
| 1 | Semiwater gas | 7.87 | 29.3 | 46.03 | 0.3 | 15.19 | 1.02 |
| 2 | Conversion gas | 24.00 | 4～8 | 55.40 | 0 | 12.60 | 0.85 |
2, the present invention is compared with traditional total-low process heat-insulating shift-converter, can bring following energy-conservation:
。
Claims (6)
1. one kind is controlledly moved thermal reactor, it is characterized in that, the sealed catalyst frame (2) comprising pressure-bearing shell (1) and be arranged in pressure-bearing shell (1) and water route self-loopa move heat pipe bundle (3), move described in sealed catalyst frame (2) is coated on outside heat pipe bundle (3), described heat pipe bundle (3) of moving comprises outfall sewer (31), water inlet manifold (32), endless tube (33), dividing plate (34), caecum formula heat exchanger tube (35) and aqueduct (36), described dividing plate (34) is arranged at the middle part of endless tube (33), the upper and lower of endless tube (33) is divided into diversion box (37) and header tank (38), water inlet manifold (32) is communicated with the diversion box (37) on endless tube (33) top, outfall sewer (31) is communicated with the header tank (38) of endless tube (33) bottom, aqueduct (36) is set in caecum formula heat exchanger tube (35), the one end open other end of caecum formula heat exchanger tube (35) is closed, the openend of caecum formula heat exchanger tube (35) is communicated with the header tank (38) of endless tube (33) bottom, aqueduct (36) both ends open, the top of aqueduct (36) is communicated with the diversion box (37) on endless tube (33) top, the bottom of aqueduct (36) is positioned on the blind end of caecum formula heat exchanger tube (35).
2. one according to claim 1 is controlled moves thermal reactor, it is characterized in that, described sealed catalyst frame (2) comprises sealing plate (21), gas distributing cylinder (22), gas collecting jar with ground-on cover plate (23), described gas distributing cylinder (22) is arranged in pressure-bearing shell (1), sealing plate (21) is fixed on the top of gas distributing cylinder (22), gap between gas distributing cylinder (22) and pressure-bearing shell (1) is formed radially distribution of gas room (24) along pressure-bearing shell (1), gas collecting jar with ground-on cover plate (23) is arranged in gas distributing cylinder (22) along the radial direction of gas distributing cylinder (22), gas distributing cylinder (22) interior loading catalyst, described endless tube (33), caecum formula heat exchanger tube (35) and aqueduct (36) lay respectively in gas distributing cylinder (22).
3. one according to claim 2 is controlled moves thermal reactor, it is characterized in that, described pressure-bearing shell (1) comprises upper cover (11), enclosure body (12), low head (13); Described upper cover (11) is connected in enclosure body (12) by flange (14), enclosure body (12) and low head (13) one-body molded; Upper cover (11) being offered respectively the water inlet (15) for connecting water inlet manifold (32), for connecting delivery port (16) and the air inlet (17) of outfall sewer (31), low head (13) being offered respectively catalyst self-unloading short circuit (18) and the gas outlet (19) for being connected gas collecting jar with ground-on cover plate (23).
4. one according to claim 3 is controlled moves thermal reactor, it is characterized in that, supporting seat (121) and gripper shoe (122) is provided with in described enclosure body (12), described supporting seat (121) is fixed on the inwall of enclosure body (12), the two ends of gripper shoe (122) are supported on supporting seat (121), and gas distributing cylinder (22), endless tube (33) and gas collecting jar with ground-on cover plate (23) are bearing in gripper shoe (122) successively.
5. one according to claim 3 is controlled moves thermal reactor, it is characterized in that, described sealing plate (21) and be respectively equipped with the first seal (25) between outfall sewer (31) and water inlet manifold (32), be provided with the second seal (26) between the bottom of gas distributing cylinder (22) and low head (13), between the escape pipe of gas outlet (19) and gas collecting jar with ground-on cover plate (23), be provided with the 3rd seal (27).
6. one according to claim 3 is controlled moves thermal reactor, it is characterized in that, the inner side of described gas distributing cylinder (22) and the outside of gas collecting jar with ground-on cover plate (23) arrange gas distribution grid respectively, and described gas distribution grid evenly offers multiple passage.
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| CN108212027B (en) * | 2017-12-21 | 2021-03-16 | 海南汉地阳光石油化工有限公司 | Catalytic system of refining reactor |
| CN109052318B (en) * | 2018-09-30 | 2022-04-08 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN109173936B (en) * | 2018-09-30 | 2021-10-08 | 中石化宁波工程有限公司 | Methanol synthesis water-cooling reactor |
| CN113757700B (en) * | 2021-09-01 | 2022-08-16 | 武汉氢能与燃料电池产业技术研究院有限公司 | Hydrogen catalytic combustion hydrogen eliminating device |
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| CN102814149A (en) * | 2012-08-23 | 2012-12-12 | 上海蒙福陇化学工程有限公司 | Methanation furnace for producing methane from coal synthesis gas and production method of methanation furnace |
| CN104069777B (en) * | 2014-07-14 | 2015-12-16 | 南京博扬化工科技有限公司 | A kind of isothermal adiabatic radial compound formula reactor |
| CN204261651U (en) * | 2014-11-18 | 2015-04-15 | 安徽新月化工设备有限公司 | One is controlled moves thermal reactor |
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