CN205235936U - Modular fixed bed reactor reaches device by its formation - Google Patents
Modular fixed bed reactor reaches device by its formation Download PDFInfo
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- CN205235936U CN205235936U CN201521062555.5U CN201521062555U CN205235936U CN 205235936 U CN205235936 U CN 205235936U CN 201521062555 U CN201521062555 U CN 201521062555U CN 205235936 U CN205235936 U CN 205235936U
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Abstract
The utility model provides a modular fixed bed reactor reaches device by its formation, include, casing, isothermal reaction bed, adiabatic reaction bed and air distributor, air distributor, isothermal reaction bed, adiabatic reaction bed overlap in proper order to be established, and is equipped with the clearance each other, be provided with the heat transfer structure in the isothermal reaction bed, it includes and runs through along the axial a plurality of heat transfer pieces of isothermal reaction bed, still include the air guide structure. After making technology gas get into the catalyst bed, along radial flow, this kind of flow pattern who expands the formula outward, the reaction that increases to the quantity of gas and, avoided the improvement of gas flow rate, has lengthened technology gas and at the intraformational dwell time of catalyst bed, has promoted the reaction to go on totally, improved the utilization ratio of catalyst. Because the setting of adiabatic reaction bed in the outside of isothermal reaction bed, is favorable to absorbing the heat of isothermal reaction bed, reduced the heat transfer volume on the one hand simultaneously, on the other hand has promoted going on of adiabatic reaction.
Description
Technical field
The utility model relates to technical field of chemical, is specifically related to a kind of combined type fixed bed reactionDevice.
Background technology
Fixed bed reactors claim again packed bed reactor, are filled with solid catalyst or solid reactant and useTo realize a kind of reactor of heterogeneous reaction process. Solids is graininess conventionally, particle diameter 2～15mm left sideThe right side, is piled into the bed of certain altitude (or thickness). Bed transfixion, fluid enters by bedRow reaction. Fixed bed reactors are mainly used in realizing gas-solid catalysis, as ammonia convertor, dioxyChange sulphur contact oxidation device, hydrocarbon steam converting furnace etc., be widely used in petroleum refining industry, inorganicizationWork industry, the fields such as organic chemical industry's industry.
In actual use, for complicated reaction of high order, they generally need to be by multiple fixed bedsReactor series connection is used, to meet the requirement in differential responses stage, but the appliance arrangement portion of plural serial stagePart is many, floor space is large and cost of investment is high. For this reason, Chinese patent literature CN104069777A is openThe adiabatic radial compound formula of a kind of isothermal reactor, it is made up of housing and internals, wherein, housing byShell upper end socket is connected with outer casing underpart cylindrical shell; Internals comprise isothermal radial section beds,Upper atmolysis cylinder, upper gas collecting jar with ground-on cover plate, heat exchanger tube, heat exchanger tube import bobbin carriage, heat exchanger tube outlet bobbin carriage, cold shockDevice; Cold shock vaporization layer, beds, lower atmolysis cylinder and the lower gas collecting jar with ground-on cover plate of adiabatic radial section; InternalsFor radially arranging, wherein the top of internals is provided with the beds of isothermal radial section, this isothermal radialThe catalyst layer of section is located between atmolysis cylinder and upper gas collecting jar with ground-on cover plate and outside heat exchanger tube; The bottom of internalsBe provided with the beds of adiabatic radial section, this catalyst layer is located between lower atmolysis cylinder and lower gas collecting jar with ground-on cover plate.
But in upper this device, the set-up mode of heat exchanger, on the one hand, makes isothermal bed still have temperatureProblem pockety, it not only affects reaction effect, and there is temperature runaway in part even, serious shadowRing use activity and the life-span of the selective and catalyst of reaction; On the other hand, the gas in bed is metAfter heat exchanger tube, can change the flow direction of gas, cause the flow direction confusion of gas at bed,CONCENTRATION DISTRIBUTION is inhomogeneous, and the time of staying inequality in bed easily occurs " back-mixing ". Back-mixing can affectAlong the CONCENTRATION DISTRIBUTION on main flow direction and Temperature Distribution, make concentration trend towards exit concentration. For mass transferProcess, such change in concentration reduces concentration motive force, thereby has reduced transmission speed. For insteadAnswer process, such change in concentration reduces reactant concentration, and production concentration increases, thereby makes main anti-Answer Speed Reduction and series winding side reaction speed to increase, reaction selectivity declines. Another process gas may beBed internal short-circuit, affects the utilization rate (being that air speed reduces) of bed inner catalyst and the heat exchange of heat exchangerEffect.
Due to heat exchanger poor effect in above-mentioned patent documentation, it must arrange chiller, and Quench liquid existsWhen process for cooling gas vaporizing in reactor, diluted the concentration of process gas, and change in concentration makes concentrationMotive force reduces, and reaction selectivity declines, and further, Quench gas also can participate in subsequent reactions, orCause the total tolerance that enters adiabatic bed to increase, increased the load of catalyst, reduce reaction efficiency.
Finally, in said apparatus reaction bed, gas is by export-oriented center flow, increases for gas flowReaction, the fluid circulation area of this reactor bed reduces gradually, rate of flow of fluid increases gradually, workThe skill gas time of staying shortens, and catalyst utilization reduces, and reaction not exclusively.
Utility model content
Therefore, the technical problems to be solved in the utility model is to overcome isothermal bed of the prior artThe defects such as temperature distributing disproportionation is even, process gas is easy " back-mixing ", catalyst utilization reduction, therebyA kind of combined type fixed bed reactors are provided.
For this reason, the technical scheme that the application takes is,
A kind of combined type fixed bed reactors, comprise, top is provided with the housing that generates gas outlet, andBe arranged at isothermal reaction bed, adiabatic reaction bed and the gas distributor of described enclosure interior, described inIsothermal reaction bed is set in the outside of described gas distributor, and and described gas distributor between arrangeGapped, described adiabatic reaction bed is set in the outside of described isothermal reaction bed, and described isothermalBetween reaction bed and described adiabatic reaction bed, be provided with gap; Described gas distributor be arranged at instituteThe process gas import of stating on housing is connected, and is provided with pore on the perisporium of described gas distributor;In described isothermal reaction bed, be provided with heat exchange structure, it comprises and runs through vertically described isothermal reaction bedSome heat exchanging piece of layer, described some heat exchanging piece circumferentially evenly arrange along described isothermal reaction bed;Also comprise gas-guiding structure, it comprises the porous structure that is arranged at the inside and outside perisporium of described isothermal reaction bedWith the porous structure that is arranged at the inside and outside perisporium of described adiabatic reaction bed, and it is anti-to be sheathed on described thermal insulationAnswer the gas guide board of bed outside, between described gas guide board and described adiabatic reaction bed periphery wallBe provided with gap.
Preferably, combinations thereof formula fixed bed reactors, described isothermal reaction bed, described thermal insulation are anti-Length is consistent in the axial direction with described heat exchange structure to answer bed.
Preferably, combinations thereof formula fixed bed reactors, heat exchanging piece is heat exchanger plates, or, heat-exchanging component,Described heat-exchanging component is made up of some heat exchanger tubes along the arranged radially of described isothermal reaction bed.
Preferably, combinations thereof formula fixed bed reactors, described heat exchanger tube is extended surface tube.
Preferably, combinations thereof formula fixed bed reactors, multiple described isothermal reaction beds are sheathed successivelyForm isothermal reaction bed group, between each described isothermal reaction bed, be formed with gap; And/or,
Multiple described adiabatic reaction beds are sheathed formation adiabatic reaction bed group successively, and each described thermal insulation is anti-Answer and between bed, be formed with gap.
Preferably, combinations thereof formula fixed bed reactors, the upper/lower terminal of described isothermal reaction bedBe respectively arranged with the upper and lower tube sheet of fixing described heat exchange structure, on described upper and lower tube sheet, arrange respectivelyThere are Catalyst packing mouth and catalyst discharge port.
Preferably, combinations thereof formula fixed bed reactors, described lower perforated plate is away from described isothermal reactionThe side of bed is connected with lower tube box, is provided with heat transferring medium entrance pipe on described lower tube box,The outside that described heat transferring medium entrance pipe one end extends to described housing forms heat transferring medium entrance, changesThermal medium enters described lower tube box from described heat transferring medium entrance through heat transferring medium entrance pipe, then under warpTube sheet enters heat exchange structure, realizes heat exchange with described isothermal reaction bed;
Described upper perforated plate is being connected with upper tube box away from the side of described isothermal reaction bed, described inThe top of upper tube box is provided with heat transferring medium export pipeline, and extend described heat transferring medium export pipeline one endForm heat transferring medium outlet to the outside of described housing, the heat transferring medium that completes heat exchange is by under describedTube sheet enters described lower tube box, and finally through heat transferring medium export pipeline, is discharged by heat transferring medium outlet.
Preferably, combinations thereof formula fixed bed reactors, described upper, lower tube case comprises upper and lower bobbin carriageBody and be separately positioned on the upper and lower maintenance flange on described upper and lower bobbin carriage body, described heat exchange is situated betweenMatter export pipeline and heat transferring medium entrance pipe are separately positioned on upper and lower maintenance flange.
Preferably, combinations thereof formula fixed bed reactors, the upper/lower terminal of described adiabatic reaction bedBe respectively arranged with upper and lower plate, on described upper and lower plate, be respectively arranged with the second Catalyst packing mouth andTwo catalyst discharge ports.
Preferably, combinations thereof formula fixed bed reactors, the inside and outside perisporium of described isothermal reaction bedPorous structure and to be arranged at the percent opening of porous structure of the inside and outside perisporium of described adiabatic reaction bed littleIn 30%; And/or,
The perforate size of the pore arranging on the perisporium of described gas distributor is 1-10mm, and percent opening is1-10%; And/or, the porous structure of described adiabatic reaction bed periphery wall and described gas guide boardGap is not more than 500mm.
Preferably, combinations thereof formula fixed bed reactors, the thickness of bed layer of described adiabatic reaction bed withThe ratio that is layed in the particle diameter of described bed is not more than 100.
The invention also discloses a kind of combined type fixed-bed reactor, comprise in the axial direction multipleThe combined type fixed bed reactors described above that connect.
Technical solutions of the utility model, tool has the following advantages:
1,, in the combined type fixed bed reactors that the utility model provides, described isothermal reaction bed is sheathedIn the outside of described gas distributor, and and described gas distributor between be provided with gap, described thermal insulationReaction bed is set in the outside of described isothermal reaction bed, and described isothermal reaction bed and described exhaustedBetween thermal response bed, be provided with gap, above-mentioned gas distributor, isothermal reaction bed and adiabatic reaction bedThe layer mode of sheathed connection successively diametrically, enters after beds, radially process gasFlow, this type of flow that extends out formula, for gas flow increase reaction and, avoided gas flowThe raising of speed, has extended the time of staying of technique in beds, promotes reaction to enter completelyOK, improved the utilization rate of catalyst. Simultaneously because adiabatic reaction bed is arranged on isothermal reaction bedOutside, be conducive to absorb the heat of isothermal reaction bed, reduced on the one hand the consumption of heat transferring medium,Promote on the other hand the carrying out of adiabatic reaction.
In described isothermal reaction bed, be provided with heat exchange structure, it comprises that to run through vertically described isothermal anti-Answer some heat exchanging piece of bed, described some heat exchanging piece circumferentially evenly establishing along described isothermal reaction bedPut; This setup is further regular radially mobile gas, makes its journey laminar flow state,The back-mixing of having avoided reaction in bed, has improved reaction efficiency. Meanwhile, above-mentioned set-up mode heat exchange is equalEven, efficiency is high, avoids occurring " temperature runaway ", and has reduced the use of chiller, has saved equipment cost.
2, in the combined type fixed bed reactors that the utility model provides, described isothermal reaction bed, instituteLength is consistent in the axial direction with described heat exchange structure to state adiabatic reaction bed, is conducive to regular process gas and existsFootpath upwards flow, avoid back-mixing, be more conducive to the steady diffusion of gas, keep reaction stability.
3,, in the combined type fixed bed reactors that the utility model provides, heat exchanger tube adopts extended surface tube, finSheet pipe has high voltage bearing feature, and its fin can effectively increase heat exchange area again, many extended surface tubesFin is connected to form pipe row, and regular process gas flows.
4, in the combined type fixed bed reactors that the utility model provides, described adiabatic reaction bed peripheryThe porous structure of wall and the gap of described gas guide board are not more than 500mm, are preferably 10-100mm,Its effect is to prevent the flow field of gas flow to adiabatic bed inside of outside porous structure and temperature fieldDisturb, ensure that the gas flow in bed is laminar flow, avoid back-mixing. Last reaction generate gas fromBottom, the gap outflow of outside porous structure and gas guide board, then prolong reactor shell upwards, from insteadAnswer the generation gas outlet at device top to flow out, enter into subsequent processing.
5, in the combined type fixed bed reactors that the utility model provides, multiple described isothermal reaction bedsSheathed formation isothermal reaction bed group, is formed with gap between each described isothermal reaction bed successively; And/or,Multiple described adiabatic reaction beds are sheathed formation adiabatic reaction bed group successively, each described adiabatic reaction bedInterlayer is formed with gap. Thereby realize the multistage control to reaction, meet the condition in differential responses stageDemand, for example, can effectively control respectively the temperature of each section of reaction, the time of staying of reaction, or controlThe conversion ratio of process gas in bed processed, the consumption of minimizing catalyst. And process gas is by each reactionWhen bed, all can distribute again, improve the uniformity of gas distribution, improve reaction efficiency.
Brief description of the drawings
In order to be illustrated more clearly in the utility model detailed description of the invention or technical side of the prior artCase, does the accompanying drawing to required use in detailed description of the invention or description of the Prior Art simply belowIntroduce, apparently, the accompanying drawing in the following describes is embodiments more of the present utility model, rightIn those of ordinary skill in the art, do not paying under the prerequisite of creative work, can also basisThese accompanying drawings obtain other accompanying drawing.
Fig. 1 is a kind of combined type fixed bed reactors of the present utility model;
Fig. 2 is the sectional view of combined type fixed bed reactors shown in Fig. 1;
Fig. 3 is the sectional view with the combined type fixed bed reactors of various heat exchange structure;
Fig. 4 is the structural representation with the sectional view of the combined type fixed bed reactors of reaction bed;
Fig. 5 is a kind of combined type fixed-bed reactor of the utility model.
Description of reference numerals:
1-housing, the import of 11-process gas, 12-generates gas outlet, 13-heat transferring medium entrance, 14-Heat transferring medium outlet, 2-isothermal reaction bed, 3-adiabatic reaction bed, 4-gas distributor, 5-Heat exchange structure, 51-heat exchanger plates, 52-extended surface tube, 6-lower perforated plate, 61-catalyst discharge port, 611-The second catalyst discharge port, 62-lower tube box, overhauls flange under 63-, 7-upper perforated plate, 71-catalysisAgent filler, 711-the second Catalyst packing mouth, 72-upper tube box, the upper maintenance of 73-flange, 8-is manyHole wall plate, 9-gas guide board.
Detailed description of the invention
Below in conjunction with accompanying drawing, the technical solution of the utility model is clearly and completely described, aobviousSo, described embodiment is the utility model part embodiment, instead of whole embodiment.Based on the embodiment in the utility model, those of ordinary skill in the art are not making creative workThe every other embodiment obtaining under prerequisite, belongs to the scope that the utility model is protected.
In description of the present utility model, it should be noted that term " first ", " second ", "Three " only for describing object, and can not be interpreted as instruction or hint relative importance. Unless separately had brightTrue regulation and restriction, term " installation ", " being connected ", " connection " should be interpreted broadly, exampleAs, can be to be fixedly connected with, can be also to removably connect, or connect integratedly; Can be machineryConnecting, can be also electrical connection; Can be to be directly connected, also can indirectly be connected by intermediary,It can be the connection of two element internals. For the ordinary skill in the art, can be concreteSituation is understood the concrete meaning of above-mentioned term in the utility model.
In addition related technical characterictic in the different embodiments of described the utility model,The conflict of will not forming each other just can mutually combine.
As illustrated in fig. 1 and 2, a kind of combined type fixed bed reactors of the present utility model, comprise, topPortion is provided with the housing 1 that generates gas outlet 12, and is arranged at the isothermal reaction bed of described housing 1 insideLayer 2, adiabatic reaction bed 3 and gas distributor 4, wherein, described isothermal reaction bed 2 is set inThe outside of described gas distributor 4, and and described gas distributor 4 between be provided with gap, described absolutelyThermal response bed 3 is set in the outside of described isothermal reaction bed 2, and described isothermal reaction bed 2And be provided with gap between described adiabatic reaction bed 3; Described gas distributor 4 be arranged at described shellProcess gas import 11 on body 1 is connected, and is provided with pore on the perisporium of described gas distributor 4;In described isothermal reaction bed 2, be provided with heat exchange structure 5, as shown in Figure 2, it comprises vertically and running throughSome heat exchanging piece of described isothermal reaction bed 2, described some heat exchanging piece are along described isothermal reaction bedCircumferentially evenly arrange, process gas is carried out after reaction bed, uniform by the gap between heat exchanging pieceRadial Flow, journey laminar flow state, avoids the back mixing of reaction in reaction bed, improves reaction efficiency;Also comprise gas-guiding structure, it comprises the porous structure 8 that is arranged at the inside and outside perisporium of described isothermal reaction bedWith the porous structure 8 that is arranged at the inside and outside perisporium of described adiabatic reaction bed, and it is anti-to be sheathed on described thermal insulationAnswer the gas guide board 9 of bed outside, described gas guide board 9 and described adiabatic reaction bed periphery wallBetween be provided with gap.
On the basis of above-mentioned embodiment, described isothermal reaction bed 2, described adiabatic reaction bed 3Length is consistent in the axial direction with described heat exchange structure 5.
On the basis of above-mentioned embodiment, as shown in Figure 2, heat exchanging piece is heat-exchanging component, described in changeHot assembly is made up of some heat exchanger tubes along described isothermal reaction bed 2 arranged radiallys, present embodimentIn be extended surface tube 52. In the time carrying out exothermic reaction in isothermal reaction bed, can be by controlling extended surface tubeThe flow of 52 interior heat transferring mediums and rate of gasification, move heat to reaction bed, and control reaction bedTemperature. Heat transferring medium can adopt water at atmospheric pressure (being less than 373K), pressure (hydraulic) water (373-573K), the raw liquid (connection in roadThe mixture of benzene and Biphenyl Ether, 473-623K), fused salt (sodium nitrate, potassium nitrate and natrium nitrosum mixedCompound, 573K-773K) or flue gas (873-1073K). There is stable in properties, corrosion-free, hot meltGreatly, the feature such as cheap, can be according to selections such as operation temperature range and fuel factor sizes.
As alternative embodiment, as shown in Figure 3, in the less demanding situation of pressure, changeWarmware can also be heat exchanger plates 51, and it has easy to make and self-cleaning feature.
As disposable embodiment, as shown in Figure 4, described isothermal reaction bed 2 can be provided withMultiple, multiple described isothermal reaction beds 2 are sheathed formation isothermal reaction bed group successively, each described etc.Between temperature reaction bed, be formed with gap.
As disposable embodiment, as shown in Figure 4, described adiabatic reaction bed 3 can be provided withMultiple, multiple described adiabatic reaction beds 3 are sheathed formation adiabatic reaction bed group successively, each described exhaustedBetween thermal response bed, be formed with gap.
Above-mentioned mapping mode is conducive to realize the multistage control to reaction, meets differential responses stagesCondition demand, for example, can effectively control respectively the temperature of each section of reaction, the time of staying of reaction,Or the conversion ratio of the interior process gas of control bed, the consumption of minimizing catalyst. And process gas is by eachWhen reaction bed, all can distribute again, improve the uniformity of gas distribution, improve reaction efficiency.
On the basis of above-mentioned embodiment, the upper/lower terminal of described isothermal reaction bed arranges respectivelyThere are upper perforated plate 7 and the lower perforated plate 6 of fixing described heat exchange structure 5, on described upper perforated plate 7, lower perforated plate 6Be respectively arranged with Catalyst packing mouth 71 and catalyst discharge port 61.
On the basis of above-mentioned embodiment, described lower perforated plate 6 is away from described isothermal reaction bedSide is connected with lower tube box 62, on described lower tube box 62, is provided with heat transferring medium entrance pipe,The outside that described heat transferring medium entrance pipe one end extends to described housing 1 forms heat transferring medium entrance 13,Heat transferring medium enters described lower tube box 62 from described heat transferring medium entrance 13 through heat transferring medium entrance pipe,Enter heat exchange structure 5 through lower perforated plate 6 again, realize heat exchange with described isothermal reaction bed 2; On describedTube sheet 7 is being connected with upper tube box 72 away from the side of described isothermal reaction bed 2, described upper pipeThe top of case 72 is provided with heat transferring medium export pipeline, and described heat transferring medium export pipeline one end extends toThe outside of described housing forms heat transferring medium outlet 14, completes the heat transferring medium of heat exchange by described upper pipePlate 7 enters described upper tube box 72, and finally through heat transferring medium export pipeline, by heat transferring medium outlet 14Discharge.
On the basis of above-mentioned embodiment, described upper, lower tube case comprises upper and lower bobbin carriage body and dividesBe not arranged on upper maintenance flange 73 and lower maintenance flange 63 on described upper and lower bobbin carriage body, described in changeThermal medium export pipeline and heat transferring medium entrance pipe are separately positioned on maintenance flange 73 and lower maintenance methodOn blue 63, be mainly used in the handling of maintenance, cleaning and the catalyst of heat exchanger.
On the basis of above-mentioned embodiment, the upper/lower terminal of described adiabatic reaction bed 3 is established respectivelyBe equipped with upper and lower plate, on described upper and lower plate, be respectively arranged with the second Catalyst packing mouth 711 and second and urgeAgent discharge port 611. In the application's adiabatic reaction bed, heat-exchanger rig can be set, its bed is adoptedUse thin bed structure, what in bed, mainly carry out is the endothermic reaction, its heat mainly by process gas andThe heat radiation of isothermal reaction bed provides. Bed is thin, and gas flow rate is very low, and in bed, flowing of gas isDesirable displacement is flowed, and therefore reaction density is high, and reaction speed is fast, while completing same production task, and instituteWith catalyst amount and the small volume of reactor.
Preferably, on the basis of above-mentioned embodiment, the inside and outside perisporium of described isothermal reaction bedPorous structure 8 and be arranged at the percent opening of the porous structure 8 of the inside and outside perisporium of described adiabatic reaction bedBe not more than 30%; The perforate size of the pore arranging on the perisporium of described gas distributor is 1-10mm,Percent opening is 1-10%.
Preferably, on the basis of above-mentioned embodiment, described adiabatic reaction bed 3 periphery walls manyThe gap of hole wall plate 8 and described gas guide board 9 is not more than 500mm.
The invention also discloses a kind of combined type fixed-bed reactor as shown in Figure 5, comprise manyThe individual above-mentioned arbitrary combined type fixed bed reactors that connect in the axial direction.
In the application, process gas enters into the gas distributor 4 of reactor from process gas import 11, ventilationPore on its perisporium is discharged, thereby realizes being uniformly distributed in the axial direction, is then entered by porous structureEnter isothermal reaction bed 2. Process gas is dispersed in whole bed cross section, and the catalyst granules gap of flowing through, entersRow mass transfer and reaction, generate gaseous product, and after heat exchange structure 5 moves heat drop temperature, from outside porousThe tapping of wallboard is discharged. Again through and adiabatic reaction bed 3 gap, entered by porous structureEnter to adiabatic reactor reaction bed 3. After adiabatic bed 3 has reacted, last reaction generates gas from itFlow out the porous structure in outside and bottom, the gap of gas guide board 9, then prolong housing upwards, from reactionThe generation gas outlet 12 at device top is flowed out, and enters into subsequent processing. This reactor can be according to reaction processRequirement, arranges multistage bed (as Fig. 4) diametrically. Also can be according to the requirement of production capacity,Axially many combination of reactors (as Fig. 5) are in parallel uses, and has solved the maximization problem of equipment. AndIn the time that catalyst activates, upper and lower two can also switch use. This reactor is applicable to have and putsHeat and heat absorption reaction of high order technique, can more effective control reaction bed temperature, improves reaction efficiency,Reduce circulating flow rate. Utilize heat exchange structure to reclaim reaction heat, by-product high-quality steam. Heat exchanger tube (plate)Employing radial circumference is uniform, and the pressure drop of system is little, and can not cause back-mixing. Single device has multistageReaction, has reduced number of devices and investment. A for example reaction for Methanol hydro carbons, just can adoptCombined type gas-liquid-solid fixed bed reaction gas in the present embodiment. By the hybrid technique of gas-phase methanol and recycle gaseous componentsGas enters the reactor that the utility model provides, and can directly obtain hydrocarbon products. Process gas is firstIn one section of bed-isothermal reaction bed 2, dewater, the reaction such as hydrocarbonylation, and emit amount of heat. ?In second layer bed-adiabatic reaction bed 3, reform, disproportionation, building-up reactions, and absorption portion heat,The final hydrocarbon products that generates.
Obviously, above-described embodiment is only for example is clearly described, and not to the side of enforcementThe restriction of formula. For those of ordinary skill in the field, also can on the basis of the above descriptionTo make other changes in different forms. Here without also giving all embodimentsWith exhaustive. And the apparent variation of being extended out thus or the still guarantor in the invention of variationProtect among scope.
Claims (12)
1. combined type fixed bed reactors, comprise, top is provided with the housing that generates gas outlet,With the isothermal reaction bed, adiabatic reaction bed and the gas distributor that are arranged at described enclosure interior, itsBe characterised in that,
Described isothermal reaction bed is set in the outside of described gas distributor, and with described distribution of gasBetween device, be provided with gap, described adiabatic reaction bed is set in the outside of described isothermal reaction bed, andBetween described isothermal reaction bed and described adiabatic reaction bed, be provided with gap;
Described gas distributor is connected with the process gas import being arranged on described housing, and described gasOn the perisporium of body distributor, be provided with pore;
In described isothermal reaction bed, be provided with heat exchange structure, it comprises that to run through vertically described isothermal anti-Answer some heat exchanging piece of bed, described some heat exchanging piece circumferentially evenly establishing along described isothermal reaction bedPut;
Also comprise gas-guiding structure, it comprises the porous that is arranged at the inside and outside perisporium of described isothermal reaction bedWallboard and be arranged at the porous structure of the inside and outside perisporium of described adiabatic reaction bed, and be sheathed on described absolutelyThe gas guide board of thermal response bed outside, described gas guide board and described adiabatic reaction bed peripheryBetween wall, be provided with gap.
2. combined type fixed bed reactors according to claim 1, is characterized in that, described etc.Temperature reaction bed, length is consistent in the axial direction with described heat exchange structure for described adiabatic reaction bed.
3. combined type fixed bed reactors according to claim 1 and 2, is characterized in that, changeWarmware is heat exchanger plates, or,
Heat-exchanging component, described heat-exchanging component is by some heat exchange along the arranged radially of described isothermal reaction bedPipe composition.
4. combined type fixed bed reactors according to claim 3, is characterized in that, described in changeHeat pipe is extended surface tube.
5. according to the combined type fixed bed reactors described in claim 1,2 or 4, it is characterized in that,Multiple described isothermal reaction beds are sheathed formation isothermal reaction bed group successively, each described isothermal reaction bedInterlayer is formed with gap; And/or,
Multiple described adiabatic reaction beds are sheathed formation adiabatic reaction bed group successively, and each described thermal insulation is anti-Answer and between bed, be formed with gap.
6. combined type fixed bed reactors according to claim 5, is characterized in that, described etc.The upper/lower terminal of temperature reaction bed is respectively arranged with the upper and lower tube sheet of fixing described heat exchange structure, instituteState and on upper and lower tube sheet, be respectively arranged with Catalyst packing mouth and catalyst discharge port.
7. combined type fixed bed reactors according to claim 6, is characterized in that,
Described lower perforated plate is being connected with lower tube box away from the side of described isothermal reaction bed, described inOn lower tube box, be provided with heat transferring medium entrance pipe, described heat transferring medium entrance pipe one end extends to instituteThe outside of stating housing forms heat transferring medium entrance, and heat transferring medium is situated between through heat exchange from described heat transferring medium entranceMatter entrance pipe enters described lower tube box, then enters heat exchange structure through lower perforated plate, with described isothermal reactionBed is realized heat exchange;
Described upper perforated plate is being connected with upper tube box away from the side of described isothermal reaction bed, described inThe top of upper tube box is provided with heat transferring medium export pipeline, and extend described heat transferring medium export pipeline one endForm heat transferring medium outlet to the outside of described housing, the heat transferring medium that completes heat exchange is by under describedTube sheet enters described lower tube box, and finally through heat transferring medium export pipeline, is discharged by heat transferring medium outlet.
8. combined type fixed bed reactors according to claim 7, is characterized in that, described upper,Lower tube box comprises upper and lower bobbin carriage body and is separately positioned on upper and lower on described upper and lower bobbin carriage bodyMaintenance flange, described heat transferring medium export pipeline and heat transferring medium entrance pipe are separately positioned on upper and lowerOn maintenance flange.
9. according to the arbitrary described combined type fixed bed reactors of claim 6-8, it is characterized in that,The upper/lower terminal of described adiabatic reaction bed is respectively arranged with upper and lower plate, on described upper and lower plate, dividesBe not provided with the second Catalyst packing mouth and the second catalyst discharge port.
10. combined type fixed bed reactors according to claim 9, is characterized in that,
The porous structure of the inside and outside perisporium of described isothermal reaction bed and be arranged at described adiabatic reaction bedThe percent opening of the porous structure of inside and outside perisporium is not more than 30%; And/or,
The perforate size of the pore arranging on the perisporium of described gas distributor is 1-10mm, and percent opening is1-10％；
And/or,
The porous structure of described adiabatic reaction bed periphery wall and the gap of described gas guide board are not more than500mm。
11. combined type fixed bed reactors according to claim 10, is characterized in that,
The thickness of bed layer of described adiabatic reaction bed be layed in described bed particle diameter ratio notBe greater than 100.
12. 1 kinds of combined type fixed-bed reactors, is characterized in that, comprise multiplely connecting in the axial directionThe arbitrary described combined type fixed bed reactors of claim 1-11 that connect.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521062555.5U CN205235936U (en) | 2015-12-17 | 2015-12-17 | Modular fixed bed reactor reaches device by its formation |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201521062555.5U CN205235936U (en) | 2015-12-17 | 2015-12-17 | Modular fixed bed reactor reaches device by its formation |
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| CN205235936U true CN205235936U (en) | 2016-05-18 |
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| CN201521062555.5U Withdrawn - After Issue CN205235936U (en) | 2015-12-17 | 2015-12-17 | Modular fixed bed reactor reaches device by its formation |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413592A (en) * | 2015-12-17 | 2016-03-23 | 北京烨晶科技有限公司 | Combined type fixed bed reactor and device formed thereby |
| CN111701538B (en) * | 2020-06-19 | 2021-03-09 | 宁波巨化化工科技有限公司 | Perturbator structure for gas-phase aldehyde hydrogenation reactor |
-
2015
- 2015-12-17 CN CN201521062555.5U patent/CN205235936U/en not_active Withdrawn - After Issue
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413592A (en) * | 2015-12-17 | 2016-03-23 | 北京烨晶科技有限公司 | Combined type fixed bed reactor and device formed thereby |
| CN111701538B (en) * | 2020-06-19 | 2021-03-09 | 宁波巨化化工科技有限公司 | Perturbator structure for gas-phase aldehyde hydrogenation reactor |
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