CN1853766A - Reactor of fixed bed for strong exothermal reaction - Google Patents
Reactor of fixed bed for strong exothermal reaction Download PDFInfo
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- CN1853766A CN1853766A CN 200510049691 CN200510049691A CN1853766A CN 1853766 A CN1853766 A CN 1853766A CN 200510049691 CN200510049691 CN 200510049691 CN 200510049691 A CN200510049691 A CN 200510049691A CN 1853766 A CN1853766 A CN 1853766A
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- fused salt
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- heat exchange
- fixed bed
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- 238000006243 chemical reaction Methods 0.000 title claims abstract description 116
- 150000003839 salts Chemical class 0.000 claims abstract description 103
- 238000010438 heat treatment Methods 0.000 claims abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000011261 inert gas Substances 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 15
- 238000005485 electric heating Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- 239000003054 catalyst Substances 0.000 description 8
- 238000007254 oxidation reaction Methods 0.000 description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 6
- JFDZBHWFFUWGJE-UHFFFAOYSA-N benzonitrile Chemical compound N#CC1=CC=CC=C1 JFDZBHWFFUWGJE-UHFFFAOYSA-N 0.000 description 6
- 230000003647 oxidation Effects 0.000 description 6
- 238000000034 method Methods 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- ITQTTZVARXURQS-UHFFFAOYSA-N 3-methylpyridine Chemical compound CC1=CC=CN=C1 ITQTTZVARXURQS-UHFFFAOYSA-N 0.000 description 4
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- WGQKYBSKWIADBV-UHFFFAOYSA-N benzylamine Chemical compound NCC1=CC=CC=C1 WGQKYBSKWIADBV-UHFFFAOYSA-N 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005243 fluidization Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 230000011218 segmentation Effects 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- LGRFSURHDFAFJT-UHFFFAOYSA-N Phthalic anhydride Natural products C1=CC=C2C(=O)OC(=O)C2=C1 LGRFSURHDFAFJT-UHFFFAOYSA-N 0.000 description 1
- 230000003321 amplification Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 235000010233 benzoic acid Nutrition 0.000 description 1
- 150000001559 benzoic acids Chemical class 0.000 description 1
- JHIWVOJDXOSYLW-UHFFFAOYSA-N butyl 2,2-difluorocyclopropane-1-carboxylate Chemical compound CCCCOC(=O)C1CC1(F)F JHIWVOJDXOSYLW-UHFFFAOYSA-N 0.000 description 1
- 235000019504 cigarettes Nutrition 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 238000013467 fragmentation Methods 0.000 description 1
- 238000006062 fragmentation reaction Methods 0.000 description 1
- 239000008187 granular material Substances 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- FPYJFEHAWHCUMM-UHFFFAOYSA-N maleic anhydride Chemical compound O=C1OC(=O)C=C1 FPYJFEHAWHCUMM-UHFFFAOYSA-N 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- 238000003199 nucleic acid amplification method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000005245 sintering Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 229910000314 transition metal oxide Inorganic materials 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
A fixed-bed reactor suitable for the strong heat-releasing reaction is composed of main reaction cylinder, baffle plates, reacting tubes passing through said baffle plates, fused salt cavity surrounding said reacting tubes, circulating heat-exchanging cylinder containing fused salt, upper and lower guide tube between main reaction cylinder and said heat-exchanging cylinder, and the upper coiled tube for cooling fused salt, lower heating tube and inertial gas nozzle, all of which are installed in said heat-exchanging cylinder.
Description
(1) technical field
The present invention relates to a kind of chemical industry equipment, relate in particular to a kind of fixed bed reactors that are applicable to strong exothermal reaction.
(2) background technology
Some industrial strong exothermal reactions, as toluene oxidation synthesizing benzoic acids, the synthetic benzonitrile of amino toluene oxidation, the synthetic phthalic anhydride of o xylene oxidation, oxidation of propane system cis-butenedioic anhydride etc., carrying out along with reaction, a large amount of reaction heat of constantly emitting are as can not in time removing, reaction bed temperature is constantly risen, if technological operation is improper, will cause the bed part " focus " and the diameter of axle to excessive temperature differentials, thereby cause complete oxidation, reduce productive rate, secondly catalyst granules is in operation under the high temperature for a long time, can cause its sintering and inactivation.Therefore for improving reaction efficiency, need constantly shift out the heat that produces, to keep the stable of reaction bed temperature.For this type of strong exothermal reaction, people have designed the reactor of many patterns industrial, to satisfy above-mentioned requirements.Can specifically be summarized as follows:
(1) adopts fluidized-bed reactor, this reaction unit can be taken away the heat that produces by material pneumatic, substantially the temperature difference and part " focus " of bed have been eliminated, dense-phase circulating fluidized bed reactor as Chinese patent CN1214959 design, realized the reaction rate and the reaction temperature of gas-solid strong exothermal reaction process are effectively controlled, reaction temperature fluctuation and " temperature runaway " phenomenon have been avoided, fine reaction selection, the problem such as anticorrosion, explosion-proof of having solved.But this reactor requires the catalyst mechanical strength higher, and transition metal oxide is (as V
2O
5, Mo-Bi-O etc.) and catalyst easily fragmentation in this system, active specy easily runs off.
(2) adopting calandria type fixed bed reactor, is to reduce the tubulation caliber for eliminating " focus " the simplest method, improve heat exchanger effectiveness, but this method has increased the reactor bed pressure drop, has improved running cost; As patent US3801634, JP53-30688B, JP85485 is described in addition, with inert particle segmentation dilute catalyst (adopting different thinner ratios), controls catalyst activity with this at beds, eliminates " focus ".But common this method has increased the catalyst bed layer height, has reduced the production capacity of whole device; Be to increase the heat transfer coefficient of tube wall, Chinese patent CN2415831 proposes to add the hot fin of superconduction in beds, heat can be rapidly by the hot fin of superconduction export to reaction tube outward move thermal medium, exchange capability of heat exceeds 5 times of shell and tube reactors.But, still can't solve the part " focus " and the axial temperature difference of bed because conducting strip has only been removed its peripheral part heat.
(3) fixed bed reactors of shell side fused salt outer circulation heat-exchange system are present industrial the most frequently used methods, and it flows by fused salt and takes away a large amount of heat of tube side internal reaction generation.For increasing the heat transfer coefficient of fused salt, patent US4256783 and US3147084 are by being provided with many deflection plates and baffle plate around reaction tube, the runner of managing outer fused salt has been carried out distribution design, this reactor can be eliminated the bed layer shaft radial temperature difference substantially, but for main equipment, the reactor operation is very complicated, and the reaction influence factor is many.The reactor that US4256783 invents is provided with a plurality of suspension type pump for liquid salts for the circulation of segmentation fused salt, therefore for keeping the good circulation of fused salt, to the very high requirement of design proposition of pump for liquid salts and runner.Pump for liquid salts favorable mechanical design is its basic prerequisite that turn round for a long time and reposefully, and the dingus pump for liquid salts adopts the base bearing structure usually, axle stressed better, the diameter of axle and thin, but the bottom wearing and tearing are big, need frequently to overhaul.The bigger device pump for liquid salts adopts suspended structure, because of not establishing base bearing, but must often not overhaul and long-term operation, but price and running funds costliness comparatively.No matter be that all the requirement of condition is all very harsh to external world for dingus pump for liquid salts or bigger device pump for liquid salts, the impurity that brings in the variation of temperature of molten salt and the cyclic process makes troubles all can for the running of pump for liquid salts, in order to adapt to the running requirements of pump for liquid salts, just need often to change.The long-term dependence on import of domestic manufacturer is not grasped the key technology of this type of reactor all the time, and is very passive in actual production and operation.
(3) summary of the invention
The deficiency of the pump for liquid salts of palpus service firing condition harshness when removing the heat that strong exothermal reaction produced that in fixed bed reactors, carries out in order to overcome the circulation of available technology adopting fused salt, the present invention
The fixed bed reactors that are applicable to strong exothermal reaction of a kind of simple and reliable for structure, not outer circulation of fused salt, handling safety, reduced investment are provided.
The technical scheme that the present invention solves its technical problem is:
A kind of fixed bed reactors that are applicable to strong exothermal reaction, comprise main reaction cylinder, has vertically arranged reaction tube in the described main reaction cylinder, the reaction tube periphery is the fused salt chamber, described fused salt chamber is horizontally disposed deflection plate, described reaction tube passes through described deflection plate, described reaction tube lower end is equipped with gripper shoe, described main reaction cylinder top has upper conduit, the bottom has downcomer, the fused salt chamber of described main reaction cylinder is by on described, downcomer is communicated with fused salt cycle heat exchange tube, described fused salt cycle heat exchange tube upper end has the hot gas gas outlet, the lower end has the fused salt discharge port, and described fused salt heat exchanging tube has the extension that is higher than upper conduit that is enough to make the hot gas smooth discharge; In the described fused salt cycle heat exchange tube: top is equipped with the fused salt cooling coil, and the bottom is equipped with heating tube, is provided with inert gas nozzle at the downcomer position, and the jet hole of described inert gas nozzle stretches in the described downcomer.
Further, described heating tube is positioned at described cycle heat exchange tube below.
Described inert gas nozzle is through the fused salt preheating, concrete way can be: described inert gas nozzle has introduction segment, described introduction segment is close to described fused salt cycle heat exchange drum outer wall and affixed with it, and described inert gas preheating device is a fused salt cycle heat exchange tube.
Further, offer aperture on the described deflection plate, percent opening is 10% ~ 70%.
Further, pass through the place of passing through of deflection plate, leave the space of 0.5 ~ 5mm between the two at reaction tube.
Further, described fused salt cycle heat exchange tube has a plurality of, and each fused salt cycle heat exchange tube cooperates with described main reaction cylinder.
Further, described heating tube is an electric heating tube.
The course of work of the present invention is: the fused salt that will dissolve joins in the fused salt cycle heat exchange tube earlier, and makes the height of fused salt be higher than the upper conduit position, and also be full of fused salt in the main reaction cylinder this moment.Start heating tube then and again fused salt is heated, make temperature of molten salt be substantially equal to reaction temperature required in the reaction tube.Start the inert gas injection cock, nozzle sprays inert gas at a high speed, and (described inert gas is at fused salt, promptly this gas can not react with fused salt), rush at the reaction tube bottom, thereby driving peripheral fused salt flows in the main reaction chamber tube, and form a large amount of bubbles, make the violent turbulence of fused salt.The fused salt of entrained air bubbles upwards flows with S shape through deflection plate, has eliminated the mobile dead band of reaction tube outward, and the fused salt of a spot of entrained air bubbles can be by the Clearance Flow of deflection plate aperture and deflection plate cross section and reaction tube outer wall simultaneously.The gas-liquid fluidisation fused salt of a large amount of high speed turbulences flow to the napex of main reaction chamber, by the upper guide siphunculus, enter the fused salt circulation and move hot cylindrical shell, gas-liquid separation this moment, bubble is by the discharging of hot gas gas outlet, fused salt flows downward after the heat exchange of water vapour cooling coil, reenters the main reaction chamber cylindrical shell through the bottom conduction pipe.Under the drive of the air-flow that inert gas nozzle ejected, fused salt constantly circulates.
Beneficial effect of the present invention is: 1. spray power by inert gas, the industrial pump for liquid salts commonly used that defaulted has reduced the unsafe factor that brings because of fused salt corrosion and leakage, has also saved production cost greatly.2. because equipment there is no special harsh requirement to operating condition, so fused salt need not be changed.3. can come the outer fused salt fluidized state of adjustable pipe by regulating the inert gas injection flow, improve the outer fused salt convection heat transfer' heat-transfer by convection effect of pipe, the inert gas bubble also can be taken away the part heat simultaneously.4. can regulate temperature of molten salt at any time, to adapt to the reaction of different temperatures by regulating cooler pan and the heating tube in the fused salt heat exchanging cylindrical shell.
(4) description of drawings
Fig. 1 is the fixed bed reactors structural representation that the present invention is applicable to strong exothermal reaction.
Fig. 2 is that deflection plate and reaction tube are provided with schematic diagram.
Fig. 3 is that the deflection plate and the reaction tube of side-looking is provided with schematic diagram.
Fig. 4 is the inert gas nozzle lateral plan.
Fig. 5 is the inert gas nozzle front view.
(5) specific embodiment
Below in conjunction with the drawings and specific embodiments the present invention is described in further detail.
Embodiment one
With reference to Fig. 1,2,3,4,5, a kind of fixed bed reactors that are applicable to strong exothermal reaction comprise main reaction cylinder 1, and main reaction cylinder 1 is of a size of Φ 15cm * 150cm, fused salt cycle heat exchange tube 2 is of a size of: Φ 10cm * 200cm has been arranged vertically 5 reaction tubes 3 in main reaction cylinder 1.Reaction tube 3 peripheries are the fused salt chamber, and horizontally disposed in the fused salt chamber have 5 deflection plates 4, and described reaction tube 3 passes through described deflection plate 4.Described reaction tube lower end is equipped with gripper shoe 5, is used for supporting the fused salt of main reaction cylinder 1.The top of main reaction cylinder 1 has upper conduit 6, the bottom has downcomer 7, the fused salt chamber of main reaction cylinder 1 is communicated with fused salt cycle heat exchange tube 2 by described upper and lower conduit, described fused salt cycle heat exchange tube upper end has hot gas gas outlet 8, the lower end has fused salt discharge port 9, and described fused salt cycle heat exchange tube 2 has the extension that is higher than upper conduit that is enough to make the hot gas smooth discharge;
In the described fused salt cycle heat exchange tube 2: top is equipped with fused salt cooling coil 10, the bottom is equipped with electric heating tube 11, being provided with the jet hole diameter at the downcomer position is the inert gas nozzle 12 of 2mm, the size of the size of this inert gas nozzle 12 and main reaction cylinder and fused salt cycle heat exchange tube adapts, with reaction tube and the corresponding amplification of fused salt cycle heat exchange tube or dwindle, in suitable scope, adjust.The jet hole of this inert gas nozzle 12 stretches in the described downcomer and by inert gas nozzle support ring 13 and supports, and described electric heating tube 11 is positioned at described inert gas nozzle 12 belows.Certainly the electric heating tube here also can be other forms of heating tube.
Above reactor can use in the synthetic benzonitrile catalytic reaction of amino toluene oxidation.Load vpo catalyst in the reaction tube, inert gas is a nitrogen.Reactor feed gas consists of: toluene/ammonia/air=1/4/25 (mol), reaction result sees Table 1.
Table 1
| Reaction temperature ℃ | Reaction volume air speed h -1 | Nitrogen jet amount m 3/h | Reaction yield % (mol) |
| 400 420 440 | 4500 4500 4500 | 0.5 0.5 0.7 | 78％ 86％ 81％ |
Above reactor can use in the synthetic cigarette nitrile catalytic reaction of 3-picoline ammoxidation.Load vpo catalyst in the reaction tube, inert gas is a nitrogen.Reactor feed gas consists of: 3-picoline/ammonia/air=1/4/25 (mol), reaction result sees Table 2.
Table 2
| Reaction temperature ℃ | Reaction volume air speed h -1 | Nitrogen jet amount m 3/h | Reaction yield % (mol) |
| 380 400 420 | 4500 4500 4500 | 0.5 0.5 0.7 | 77％ 82％ 75％ |
From above table data as can be seen, fixed bed reactors of the present invention, after nozzle begins to spray nitrogen, fused salt begins the fluidisation circulation, it is consistent that temperature of molten salt in the entire reaction tube fused salt chamber tends to rapidly, can obviously reduce and eliminate beds " focus ", and improve the bed axial temperature difference, improve the productive rate of strong exothermic oxidation reaction target product.
Embodiment two
As embodiment one described reactor, described inert gas nozzle has introduction segment, described introduction segment is close to described fused salt cycle heat exchange drum outer wall and affixed with it, the barrel of fused salt cycle heat exchange tube is the preheating device of inert gas nozzle, be used for the inert gas preheating, make the gas that inert gas nozzle ejects and the temperature of fused salt be unlikely to differ too big.
Embodiment three
As embodiment 1 described reactor, also offer aperture on the described deflection plate, percent opening is 10%.Fused salt can also produce by aperture and flow after offering aperture on the deflection plate, promotes heat exchange.All the other structures are identical with embodiment one with embodiment.
Embodiment four
As embodiment 1 described reactor, also offer aperture on the described deflection plate, percent opening is 30%, pass through the place of passing through of deflection plate at reaction tube, leave the space of 0.5mm between reaction tube outer wall and the deflection plate cross section, the existence in this space can promote flowing of fused salt equally, thereby promotes that all the other structures of heat exchange are identical with embodiment one with embodiment.
Embodiment five
As embodiment 1 described reactor, also offer aperture on the described deflection plate, percent opening is 45%, passes through the place of passing through of deflection plate at reaction tube, leaves the space of 1mm between reaction tube outer wall and the deflection plate cross section.All the other structures are identical with embodiment one with embodiment.
Embodiment six
As embodiment 1 described reactor, also offer aperture on the described deflection plate, percent opening is 60%, passes through the place of passing through of deflection plate at reaction tube, leaves the space of 2.5mm between reaction tube outer wall and the deflection plate cross section.All the other structures are identical with embodiment one with embodiment.
Embodiment seven
Main reaction cylinder is of a size of: Φ 40cm * 400cm, fused salt cycle heat exchange tube is of a size of: Φ 30cm * 400cm, the jet hole diameter of inert gas nozzle is 7mm, be furnished with 67 reaction tubes, 15 deflection plates in the main reaction cylinder, also offer aperture on the described deflection plate, percent opening is 70%, passes through the place of passing through of deflection plate at reaction tube, leaves the space of 4mm between reaction tube outer wall and the deflection plate cross section.Described fused salt cycle heat exchange tube has two, the both sides with main reaction cylinder of distributing symmetrically, and each fused salt cycle heat exchange tube cooperates with described main reaction cylinder.For large-sized main reaction cylinder, the number that increases fused salt cycle heat exchange tube can obtain better heat exchange effect.All the other structures are identical with embodiment one with embodiment.
Embodiment eight
Main reaction cylinder is of a size of: Φ 50cm * 500cm, fused salt cycle heat exchange tube is of a size of: Φ 40cm * 570cm, the jet hole diameter of inert gas nozzle is 10mm, be furnished with 81 reaction tubes, 19 deflection plates in the main reaction cylinder, also offer aperture on the described deflection plate, percent opening is 70%, passes through the place of passing through of deflection plate at reaction tube, leaves the space of 5mm between reaction tube outer wall and the deflection plate cross section.Described fused salt cycle heat exchange tube has three, is evenly distributed on around the main reaction cylinder, and each fused salt cycle heat exchange tube cooperates with described main reaction cylinder.For large-sized main reaction cylinder, the number that increases fused salt cycle heat exchange tube can obtain better heat exchange effect.All the other structures are identical with embodiment one with embodiment.
Embodiment nine
As embodiment eight described reactors, described fused salt heat exchanging tube has four, is evenly distributed on around the main reaction cylinder, and each fused salt cycle heat exchange tube cooperates with described main reaction cylinder.All the other structures are identical with embodiment eight with embodiment.
Claims (8)
1. fixed bed reactors that are applicable to strong exothermal reaction, comprise main reaction cylinder, has vertically arranged reaction tube in the described main reaction cylinder, the reaction tube periphery is the fused salt chamber, described fused salt chamber is horizontally disposed deflection plate, described reaction tube passes through described deflection plate, described reaction tube lower end is equipped with gripper shoe, it is characterized in that: described main reaction cylinder top has upper conduit, the bottom has downcomer, the fused salt chamber of described main reaction cylinder is by on described, downcomer is communicated with fused salt cycle heat exchange tube, described fused salt cycle heat exchange tube upper end has the hot gas gas outlet, the lower end has the fused salt discharge port, and described fused salt heat exchanging tube has the extension that is higher than upper conduit that is enough to make the hot gas smooth discharge;
In the described fused salt cycle heat exchange tube: top is equipped with the fused salt cooling coil, and the bottom is equipped with heating tube, is provided with inert gas nozzle at the downcomer position, and the jet hole of described inert gas nozzle stretches in the described downcomer.
2. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 1 is characterized in that: described heating tube is positioned at described inert gas nozzle below.
3. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 1 is characterized in that: described inert gas nozzle has preheating device.
4. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 3, it is characterized in that: described inert gas nozzle has introduction segment, described introduction segment is close to described fused salt cycle heat exchange drum outer wall and affixed with it, and described nozzle preheating device is a fused salt cycle heat exchange tube.
5. as the described fixed bed reactors that are applicable to strong exothermal reaction of one of claim 4, it is characterized in that: also offer aperture on the described deflection plate, percent opening is 10%～70%.
6. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 5 is characterized in that: pass through the place of passing through of deflection plate at reaction tube, leave the space of 0.5～5mm between reaction tube outer wall and the deflection plate cross section.
7. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 6 is characterized in that: described fused salt cycle heat exchange tube has a plurality of, and each fused salt cycle heat exchange tube cooperates with described main reaction cylinder.
8. the fixed bed reactors that are applicable to strong exothermal reaction as claimed in claim 7 is characterized in that: described heating tube is an electric heating tube.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100496915A CN100393404C (en) | 2005-04-28 | 2005-04-28 | Reactor of fixed bed for strong exothermal reaction |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100496915A CN100393404C (en) | 2005-04-28 | 2005-04-28 | Reactor of fixed bed for strong exothermal reaction |
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| CN1853766A true CN1853766A (en) | 2006-11-01 |
| CN100393404C CN100393404C (en) | 2008-06-11 |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101491752B (en) * | 2008-01-23 | 2011-09-21 | 中国石油化工股份有限公司 | Endothermic reaction method |
| CN101941879B (en) * | 2009-07-06 | 2013-12-04 | 中国石油化工股份有限公司 | Method for preparing ethylene by dehydrating ethanol |
| CN108043332A (en) * | 2018-01-17 | 2018-05-18 | 北京国能中林科技开发有限公司 | A kind of efficient dehydrogenation reactor applied to liquid hydrogen source material |
| CN109489022A (en) * | 2017-09-11 | 2019-03-19 | 甘肃光热发电有限公司 | Steam purge formula photo-thermal electricity steam generating system |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4203906A (en) * | 1977-07-13 | 1980-05-20 | Nippon Shokubai Kagaku Kogyo Co., Ltd. | Process for catalytic vapor phase oxidation |
| BG40018A1 (en) * | 1983-07-01 | 1986-10-15 | Nikolov | Reactor for carrying out high exothermic and endothermic catalytic processes |
| TW527218B (en) * | 1999-03-16 | 2003-04-11 | Basf Ag | Multitube reactor, especially for catalytic gas-phase reactions |
| CN1603310A (en) * | 2003-09-29 | 2005-04-06 | 上海子能高科股份有限公司 | Method for making 3-cyanopyridine in reactor |
| CN2782209Y (en) * | 2005-04-28 | 2006-05-24 | 浙江工业大学 | Fixed bed reactors suitable for strong exothermic reaction |
-
2005
- 2005-04-28 CN CNB2005100496915A patent/CN100393404C/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101491752B (en) * | 2008-01-23 | 2011-09-21 | 中国石油化工股份有限公司 | Endothermic reaction method |
| CN101941879B (en) * | 2009-07-06 | 2013-12-04 | 中国石油化工股份有限公司 | Method for preparing ethylene by dehydrating ethanol |
| CN109489022A (en) * | 2017-09-11 | 2019-03-19 | 甘肃光热发电有限公司 | Steam purge formula photo-thermal electricity steam generating system |
| CN108043332A (en) * | 2018-01-17 | 2018-05-18 | 北京国能中林科技开发有限公司 | A kind of efficient dehydrogenation reactor applied to liquid hydrogen source material |
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| CN100393404C (en) | 2008-06-11 |
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