CN103816840A - Fixed-bed reactor - Google Patents

Fixed-bed reactor Download PDF

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Publication number
CN103816840A
CN103816840A CN201310575072.4A CN201310575072A CN103816840A CN 103816840 A CN103816840 A CN 103816840A CN 201310575072 A CN201310575072 A CN 201310575072A CN 103816840 A CN103816840 A CN 103816840A
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China
Prior art keywords
heat
reactor
tube
catalyst
reaction
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Pending
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CN201310575072.4A
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Chinese (zh)
Inventor
曼弗雷德·莱尔
沃尔夫冈·舒斯特
埃德蒙德·伯姆
约阿希姆·恩格尔曼
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CHEMIEANLAGENBAU CHEMNITZ GmbH
MAN Energy Solutions SE
Original Assignee
CHEMIEANLAGENBAU CHEMNITZ GmbH
MAN Diesel and Turbo SE
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Publication of CN103816840A publication Critical patent/CN103816840A/en
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • F28D7/163—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
    • F28D7/1669—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing the conduit assemblies having an annular shape; the conduits being assembled around a central distribution tube
    • 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
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • 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
    • B01J8/0207—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 the fluid flow within the bed being predominantly horizontal
    • B01J8/0214—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 the fluid flow within the bed being predominantly horizontal in a cylindrical annular shaped bed
    • 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
    • B01J8/0278—Feeding reactive fluids
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0041—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for only one medium being tubes having parts touching each other or tubes assembled in panel form
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/005—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits for only one medium being tubes having bent portions or being assembled from bent tubes or being tubes having a toroidal configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
    • F28F9/00—Casings; Header boxes; Auxiliary supports for elements; Auxiliary members within casings
    • F28F9/007—Auxiliary supports for elements
    • F28F9/013—Auxiliary supports for elements for tubes or tube-assemblies
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
    • B01J2208/00132—Tubes
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00752—Feeding
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00761—Discharging
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00823—Mixing elements
    • B01J2208/00831—Stationary elements
    • B01J2208/0084—Stationary elements inside the bed, e.g. baffles
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00893—Feeding means for the reactants
    • B01J2208/00911—Sparger-type feeding elements
    • 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
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Geometry (AREA)
  • Fluid Mechanics (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)

Abstract

The invention relates to a radial-flow reactor (1) for carrying out chemically catalytic reactions with an isothermal reaction regime. According to the invention, the reaction space (7) of the reactor (1) is penetrated by a plurality of heat exchange tubes (9), the heat exchange tubes (9) being arranged as parallel to the centre axis (6) as possible and in a plurality of groups, such that the groups form full rows (38) which are arranged in the radial direction in the reaction space (7), the outer contours of adjacent heat exchange tubes (9) of a row (38, 39) are so close to one another that radial flow ducts (40) are formed. The present invention also relates to the use of the reactor to obtain an approximate isothermal reaction mechanism. The present invention also relates to the use of the reactor, wherein the reactor is used to carry out the reaction possessing a heat effect by utilzing fused salt as heating agents in the heat exchange tubes by the approximate isothermal reaction mechanism. The present invention also relates to the use of the reactor used for gas-phase reaction. The present invention also relates to the use of the reactor used for oxidation reaction, hydrogenation reaction, dehydrogenation reaction, nitration, hydrocarbylation reaction or used for manufacturing hydrocarbon via alcohol or dimethyl ether.

Description

Fixed bed reactors
Technical field
The present invention relates to the fixed bed reactors that a kind of radial flow is crossed.
Background technology
Fixed bed reactors are the reactors for carrying out chemical reaction, wherein flow axis to or radially flow through the catalyst being in fixed bed.
Prior art is known to very different fixed bed reactors.What have special interest at this is the fixed bed reactors that radial flow is crossed.Utilize this structure type likely, create the large face that flows through with the little pressure loss.In reactor, be often provided with heat-exchange device at this, to input or output heat, to create identical reaction condition in reaction heat release or heat absorption.
Therefore in EP2165755A1, describe and have a kind of isothermal chemical reactor, it has the heat exchange elements with multiple heat exchange elements of arranging around reactor axis, and described heat exchange elements is made up of each radial oriented row (it is made up of multiple axially extended hot switching paths abreast).The passage of heat exchange elements is connected respectively on the distributor tube or collection tube with continually varying cross section.At this, hot switching path has longitudinal cross-section (it has the shape of about ellipse or rectangle) and different lateral orientation in heat exchange elements inside.Have the each independent passage of non-circular cross section and perpendicular to the distributor tube of described passage or collection tube to be connected in technical requirement very high, and be also therefore expensive.In addition depend on design ground, only can reach a limited heat-exchange surface density.
In document DE10031347A1, introduced a kind of reactor of cylinder shape of the heat exchanger plate with radial arrangement, wherein heat exchanger plate also can the design of wedge shape ground.Depend on design ground, the maintenance of this equipment expends huge.Heat exchange medium is evenly distributed to and in heat exchanger plate, needs SC.Especially the in the situation that of required pressure stability or in the case of variable plate thickness, the manufacture of heat exchanger plate is complicated and is therefore expensive.
In EP2363203A1, also disclose a kind of reactor with heat exchanger plate, described heat exchanger plate has multiple adjacent passages, for transmitting heat-carrying agent.Due to its complicated structure, described heat exchanger plate is expensive in the mill, and due to the structure of its rapid wear, described heat exchanger plate is with respect to mechanical load, and especially pressure load is fragile.
DE102009031765A1 discloses a kind of converter of cylinder shape, and for carrying out the catalytic reaction of heat release, wherein the hot panel of wedge shape is for output-response heat.Hot panel is matched with the cooling system with evaporative medium especially.In this system, by it, at self, the heat in the heat exchanger in converter sends the heat-carrying agent of secondary heat-carrying agent closed circuit to the heat-carrying agent of evaporation.Described hot panel due to its complexity, be expensive in the mill for guaranteeing the structure of pressure stability.
Summary of the invention
Task of the present invention is to propose fixed bed reactors that a kind of radial flow is crossed, that react for having the chemical catalysis of fuel factor under the pressure improving, these fixed bed reactors are cheap in the mill, and the heat of reaction that can discharge or absorb from different courses of reaction with different amounts very is simply coordinated, for creating the reaction condition of isothermal as far as possible.
According to the present invention, the reactor of the feature of this task by having independent claims solves.The preferred design of the present invention is the theme of dependent claims.
Reactor according to the present invention is applicable to carry out the chemical catalysis reaction with fuel factor with the reaction condition of isothermal as far as possible, although the adiabatic region of reactor reacts and is favourable and therefore the invention still further relates to and have the reactor of the conversion zone of isothermal substantially for some, it has adiabatic region.In adiabatic region, do not carry out the cooling of reacting gas or heating.
The shape of reactor is cylinder shape in principle, has as far as possible circular cross section, thereby this shape defines axially (along the longitudinal direction of cylinder) and the direction of (in circular cross section therefrom mind-set outside) radially.In circular cross section, be in axial direction medially furnished with the central axis of reactor.Reactor is upright in use, that is to say that axial direction is orientated vertically.
Reactor has the reactor cover of cylinder shape of arranging around central axis, its preferred pressure stably implement and thereon end place seal by upper cap portion and seal by lower cap portion in its lower end.Reactor cover and upper cap portion and lower cap portion are totally called as pressure shield in scope herein.
Substantially the reative cell of annular is positioned at reactor cover inside, and this reative cell surrounds the central tube of perforation.Utilize expression " substantially " to show that circular shape is preferred, but for example can allow little error by manufacturing tolerance.
The reative cell of annular is surrounded by external cavity, and wherein external cavity and reative cell are separated by the outer wall of local perforations at least.In order to use reactor, catalyst filling is filled in reative cell.Inside at central tube limits internal cavity.
Whether external cavity and central tube are provided for input and use gas and for output products gas, wherein input and export or depend in contrast concrete pending reaction via external cavity via central tube.Undertaken by the region of the perforation of the inner and outer wall of gauge reative cell with the input of gas or the output of product gas.Can realize gas flow radially by input and output.
What " perforation " expressed is the gas permeability of outer wall and the central tube (inwall of reative cell) of reative cell, thereby reacting gas can pass described outer wall and central tube, but the catalyst being in reative cell is maintained original place.Perforation can be with very different modes and method, for example, for example, guarantee by the tool wall components jaggy form of hole or gap or metal gate (with).Hole size must be coordinated with the granular size of catalyst to be filled at this.In addition must guarantee as follows, that is, catalyst granules does not stop up perforation.The wall components of multilayer can be set for this reason if desired, and the layer of this wall components is advantageously arranged by spacing retainer compartment of terrain in addition.
According to the size of reactor of the present invention not especially output limited and that depend on corresponding requirements determine.In business is used, people are devoted to reactor to determine as wide as possible specification conventionally based on economic cause.The size that reative cell is radial and axial is determined in requirement based on reaction technology in first step.Then by corresponding, for the space requirement of the part of appliance of directing reaction gas and heat-carrying agent and carry out to obtain out reactor size by designing requirement.
The overall diameter of this reactor is usually located at 2m in the region between 9m, is preferably placed at 3m in the region between 5m.Total height is usually located at 3m in the region between 30m, is preferably placed at 15m in the region between 25m.But for example for distributed solution or for test objective, the reactor with less size is also so possible.Central tube has 0.3m conventionally to the diameter between 1.5m.Preferred diameter at 0.6m in the region between 0.9m.Therefore central tube is convenient to assembling, is safeguarded or maintenance.The flowing through evenly and radially of gas via the wall surface of porous can be realized in the length ground that depends on the wall of porous on central tube and porous.The radial dimension of external cavity is preferably placed at 0.05m in the region between 0.5m, more preferably at 0.1m in the region between 0.3m.
In addition, reative cell is passed by multiple heat-exchange tubes, and wherein heat-exchange tube is parallel to central axis and to organize layout as far as possible.At this, each group is formed on the row completely that are radially orientated in reative cell.The outline of the adjacent heat exchanging tube of row so mutually near, to form flow channel radially by row completely.Be listed in this completely and mean, described row radially almost pass through whole reative cell.Radial flow channels can be regarded as lower channel at this, and in the time that reaction is carried out, catalyst is in described passage, and described passage is divided into reative cell radially portion's section of extending, and wherein pipe row prevent the crossing current of adjacent catheter as far as possible as passage gauge part.Although this stream causes by the pressure differential between central tube and external cavity substantially diametrically, crossing current can be due to poor the causing of reacting gas mass density that closes on the region of heat-exchange tube and cause away from the temperature difference between the region of heat-exchange tube.Crossing current can make reaction efficiency reduce, because that it causes is uncertain, reacting gas rests on the time period in reactor.By placing adjacent heat-exchange tube and form row completely to above said closing on each other like that, crossing current is advantageously dropped to minimum.
Flow channel or the completely radial direction of row not only can be regarded as the accurate radial direction from central shaft alignment in context.Can be advantageously for definite reaction, reative cell is not crossed with the shortest path by reacting gas, but for example a little obliquely or snakelike wire cross.
Express " reactor radially flow through " and represent radially to flow through flowing of reactor, describedly flow but also can point to a little obliquely, that is to say and there is axial component.
Large spacing between heat-exchange tube causes the Temperature Distribution between the central authorities of adjacent heat exchanging tube and the outer surface of heat-exchange tube in row, and this Temperature Distribution causes pressure differential and crossing current.The outline of adjacent heat exchanging tube of row preferably has the 5mm of being less than, and is preferably less than the spacing of 3mm, is preferably less than in addition 2mm and is particularly preferably less than the spacing of 1mm, and wherein being directly arranged side by side of contact is particularly advantageous.Providing spacing is for the condition that provides is provided.
The input of the discharge of product gas or use gas can be laterally by reactor cover or in its axial end region at this, that is to say in upper cap portion and lower cap portion region, and especially in the region of central axis, carries out there.
The shape of cross section of heat-exchange tube is unrestricted in principle.But circular pipe is preferred, this is because described pipe easily obtains at an easy rate as semi-finished product, and is convenient to process, and cheap, automated method can be used for welded pipe in addition.In addition,, under given pressure differential, the cross section of annular can be realized minimum wall thickness.
The overall diameter of heat-exchange tube and wall thickness depended on the main points of range request and flow technique and selected.Flow cross section is selected so bigly to reach a flowing velocity of medium, this flowing velocity is guaranteed enough heat transmission in neither endothermic nor exothermic reaction, this means that heat of reaction can be exported reliably in exothermic reaction or input for reacting required heat in the endothermic reaction, and the pressure loss is remained in economic scope.The common overall diameter of this heat-exchange tube in the region between 40mm, is preferably placed at 20mm at 15mm in the region between 30mm.Wall thickness is usually located at 1.0mm between 4.0mm, is preferably placed at 1.5mm between 2.5mm.Maximum temperature and chemical tolerance level that first material depends on during whole service are selected.Conventionally use boiler tube steel alloy-free or few alloy, and also use under special circumstances stainless steel.
Spacing each other of row and its mutual layout depend on the specified criteria of the reaction technology of expectation completely.Therefore, the design dependency of the layout of the heat exchange array in reative cell is in the amount of the course of reaction on flow direction and fuel factor.The layout that is matched with reaction by heat exchange array is guaranteed the isothermal in reative cell.Heat-exchange surface density is matched with the specified criteria of reaction technology at this.By placing middle column or using different pipe diameters can increase heat-exchange surface density.
Heat-exchange tube is suitable for flowing through different heat-carrying agents, for example water, oil, steam or fused salt, and circulate at the heat exchanger of reactor cover outside with other preferred arrangements.
Reaction process depends on multiple influence factors at this.This reaction process is by the pressure of reacting gas, temperature and composition, and the time of staying of reacting gas in catalyst bed and composition, the size and shape of catalyst affect fatefully.At this, the time of staying depends on the volume flow of reacting gas and the cross section of the passage flowing through.Temperature determined by the heat transmission on conduit wall, and wherein heat transmission depends on again flowing velocity in passage and the type of wall surface.That is to say, by suitably determining according to the size of heat-exchange tube of the present invention and arranging that capable of regulating goes out best reaction process.
Therefore can advantageously create following reactor, it can be matched with the essential reaction condition of differential responses especially neatly.Therefore only must adjust the layout of heat-exchange tube in reative cell.Therefore, heat-exchange surface density also can adjust neatly and simply.In addition, produce the eddy current of reacting gas in this region by the structurized surface of the radial flow channels that forms, described eddy current advantageously promotes heat exchange.In addition advantageously, (especially circular) pipe is pressure stability, thereby also meets this requirement with cheap mode and method.
Professional can carry out the design of reactor no problemly, especially makes above-mentioned key element be matched with the reaction condition of informing for definite reaction.
Preferably, at least one heat-exchange tube of group is at least one tube end place single ground or be preferably bent doubly, and is fixed at least unilaterally in tube sheet.Pipe is preferably dual to be oppositely bent, thereby this bend causes axial offset, and need not change to the angle that enters of tube sheet, thereby the connection in this external tube sheet in axial direction realizes.
Heat-exchange tube is through the boring in tube sheet, and tube end and tube sheet couple together hermetically, especially welds.Being welded on this is preferably undertaken by arc-welding process or method of laser welding with automated method.Therefore heat-exchange tube is fixed in tube sheet in its position and orientation.
Preferably, all heat-exchange tubes are fixed in tube sheet unilaterally, and particularly preferably its each end is fixed in each tube sheet.Preferably be provided with two tube sheets.
The side direction dislocation forming due to bend by tube end, described tube end can be connected to heat-carrying agent closed circuit in tube sheet, although and can not hindered in the case of the very little spacing of outline that has heat-exchange tube.There are various possibilities in the design of bend, therefore the pipe of group can alternately be bent to the right or left, or (or to the right) is bent and (without bend ground) design point-blank alternately left.
Another favourable effect of bend is the stability of the lifting of tube sheet.Therefore fixedly causing cutting apart by the boring end without the heat-exchange tube of bend.Advantageously be achieved as follows by bend, that is, boring is spaced apart, and therefore tube sheet need not be divided, and boring also need not be together interlaced and and then form the gap of comb shape.
Although pipe is preferably fixed in unique tube sheet in its each end, but as what for example introduce in DE202007006812U1, this tube sheet of not getting rid of each side can be also multi-piece type.
In the design of alternative, pipe also can have in its end less pipe diameter, thereby between outline, has spacing, and this spacing can realize professional connectivity.
In addition preferably, heat-exchange tube between row, be furnished with other heat-exchange tube groups completely, described heat-exchange tube group forms shorter middle column.Preferably, middle column starts and extends to outer wall on the radius between central tube and outer wall.Can advantageously promote the heat exchange effect in the exterior domain of reactor by middle column.
In preferred design of the present invention, the multiple of heat-exchange tube are listed as around the starlike ground of central tube completely and arrange symmetrically.Said row completely preferably extend to outer wall from central tube.
In the region of central tube and/or in the region of outer wall, can be provided with adiabatic zone, not arrange heat-exchange tube in the scope of described adiabatic zone, wherein catalyst volume share depends on process in this adiabatic zone.As an alternative or the adiabatic zone line of the zone line that is arranged in circlewise reative cell additionally also can be set.Catalyst share in catalyst share in adiabatic zone in central tube region and annular adiabatic zone line always should be preferably no more than 5% with respect to whole catalyst cumulative volume, in adiabatic zone in outer wall area, it is maximum 10% corresponsively that this catalyst share can depend on.
Preferably, heat-exchange tube has the cross section of general circle.This class pipe is cheapness and very easy to use as semi-finished product.In the design of alternative, heat-exchange tube has circular cross section and in zone line, has (for example oval or polygonal) cross section of micro-length in its end.Therefore the connection in tube sheet and fixing can carrying out as above-described by the cross section based on circular.The cross section of the micro-length of heat-exchange tube in zone line is applicable to definite process very well.If described pipe axis of pitch is radially enough large, in straight tube, the tube pitch in tube sheet can be very large so, to such an extent as to the weld seam of adjacent tubes no longer influences each other.Can cancel in this case the bend of pipe.
In addition preferably, organize the inner vicissitudinous cross section of heat-exchange tube tool.There are different alternative schemes at this, the selection of described alternative scheme is undertaken by the specified criteria depending on process, for example: alternately occur at the inner large round diameter of group and small circular diameter, or in the exterior domain of reative cell, occur larger diameter and occur less diameter in inner region at reative cell.
By arranging that heat exchange array (row and middle column completely) carrys out the geometry in intended radial flow channel (the catalyst gap that gas flow is crossed).
Preferably, the spacing between the outline of adjacent row completely or adjacent row completely and the outline of middle column outwards increases from central tube.It is synthetic that this class design is specially adapted to gasoline.
Have in the course of reaction (for example, by methyl alcohol or dimethylether/carbinol mixture or the synthetic hydrocarbon of alcohols mixture) of the conversion of minimizing at streamwise, flow channel radially designs as follows,, described flow channel streamwise becomes more and more wider.The cooling effect entering in region of gas preferably and along the flow direction towards leaving reduces thus.In the reaction of the type, discontinuity on the inside beginning of middle column (at the less pipe diameter of the beginning of middle column) plays a part favourable, and this is because the space between row is best for settling heat-exchange surface completely.
Other reactions, for example, have the parallel flow channel of reaction (for example, by synthesis gas synthesizing methanol) needs that streamwise has the course of reaction of constant conversion amount.Described flow channel for example obtains by outwards becoming larger pipe cross section.Cooling effect is constant on the flow direction of reacting gas thus.
Therefore make the thermal output in the region of each reative cell be matched with course of reaction by the heat-exchange surface that suitably distributes.Draw thus following advantage:
-prevent the infringement due to the overheated catalyst causing;
-avoid the less desirable side reaction that causes due to the hot-spot in reative cell;
-intermediate regeneration cycle in reproducible catalyst becomes longer;
Obtain significant prolongation the service life of-catalyst;
-product selectivity and product yield are mentioned.
In order to realize the fillable of the reactor with catalyst, the minimum spacing minimum between two (row or middle column completely) row is 15mm, preferably 20mm.
Preferably, at least one is listed as or the axis of the heat-exchange tube of middle column is positioned on the straight line radially outward pointing to completely.
In the design of alternative, at least one is listed as completely or the axis of the heat-exchange tube of middle column forms serpentine.Promote the mobile share of the turbulence state in the region of heat-exchange tube by this layout.
For lift gas is through the flow turbulence of reative cell, heat-exchange tube can have turbulent flow generator at its outline.This turbulent flow generator is only arranged in outline region at this, thereby turbulent flow generator stretches into flow channel.Turbulent flow generator is not set between heat-exchange tube.For in the time that heat-carrying agent flows through, promote turbulent flow and thereby also promote heat exchange, also can be provided with turbulent flow generator in heat-exchange tube inside.
Heat-exchange tube utilizes at least one, and preferably two ends are connected with distribution apparatus or gathering-device.Heat-carrying agent and distribution apparatus that heat-exchange tube is left in gathering-device collection are distributed to heat-carrying agent in heat-exchange tube.Wherein, heat-exchange tube is fixed on described tube sheet, described cap portion inclusion tube sheet.
Gathering-device (be also referred to as heat-carrying agent collector or collect cap portion) is connected with heat exchanger mostly, and this heat exchanger preferred arrangements is in reactor outside.Advantageously, the heat exchange circulation loop so forming can be for cooling and heating.Therefore there is following possibility, that is, for example, in the time of starting reactor, input heat, so that reach more quickly process temperature.Reaction start time proceed to subsequently cooling so that keep best process temperature for exothermic reaction.
Heat-carrying agent is imported in reactor or by heat-carrying agent and exports to heat exchanger and preferably undertaken by ring duct from reactor from heat exchanger, and this ring duct is preferably positioned at reactor outside equally.Ring duct has multiple connecting portions for distribution apparatus or gathering-device.Preferably be provided with four connecting portions.
Alternatively, distribution apparatus also can have the device for the homogenising that flows, for example orifice plate before tube sheet.
The concrete design of distribution apparatus or gathering-device, ring duct and heat exchanger especially depends on the heat-carrying agent of use.Reactor according to the present invention is applicable to most heat-carrying agent, and this is water, oil, steam and fused salt especially.
For example be used as heat-carrying agent for being provided with fused salt for the synthetic reactor of gasoline, this fused salt has following composition: potassium nitrate (53 % by weight), natrium nitrosum (40 % by weight), sodium nitrate (7 % by weight).
Occur reactor cover and be in the different thermal expansion of heat-exchange system wherein at run duration, this heat-exchange system is made up of heat-exchange tube, distributor and collector and the corresponding path that carrys out autoreactor.For fear of the unallowed stress between equipment group, preferably on the heat-carrying agent of reactor, in enforcement division, compensator is set.Preferably corrugated expansion joint.Compensator can be positioned at inside reactor or outside in principle, wherein the preferred layout in reactor outside.
Preferably, the perforation of central tube and/or reacting outdoor wall can change by the axial length of reactor, makes it to meet following target,, use gas uniform is distributed in reative cell, will uses gas uniform to be distributed on the each axial position of catalyst filling.
Between heat-exchange tube in reative cell, be filled with the catalyst of preferred particulates form of bio-carrier.In gasoline is synthetic, at this, the radial flow direction (from central tube to external cavity) along reacting gas preferably reduces the ratio of the heat-exchange surface of heat-exchange tube and catalyst volume.In methyl alcohol is synthetic, this preferably keeps constant than the flow direction along reacting gas.The ratio of the heat-exchange surface of heat-exchange tube and catalyst volume is generally such as 10m 2/ m 3to 200m 2/ m 3, be preferably such as 50m 2/ m 3to 110m 2/ m 3.
Catalyst volume is determined the whole space of being filled by catalyst granules, comprises the space between catalyst granules, does not comprise the volume of heat-exchange tube.And reaction compartment is determined the whole space between central tube and external cavity and is therefore the volume sum of catalyst volume and heat-exchange tube.
Preferably, in the upper region of reative cell and lower area, be filled with inert material, this inert material is by providing high flow resistance to prevent the reaction in described region and avoiding the by-pass flow of reacting gas.In the case of the tube end being bent, in this region, the structure portion of being bent of flow channel disturbs, thereby the reaction process limiting may occur hardly in described region.In addition heat-exchange tube axially protrudes from catalyst filling mostly, thereby is configured with dead band in the region of the topmost of reative cell.In the region in inert material and dead band, central tube and outer wall are not preferably bored a hole.Because catalyst granules is tending towards stopping in the time using reactor, dead band comprises deposit catalyst granules, the volume that the catalyst granules that its compensation causes due to stop loses.Preferably avoid gas not pass through the possibility of reactor with the hollow area that catalyst granules is filled between central tube and the outer wall of boring a hole contact catalyst.Deposit catalyst granules is favourable in dead band.Therefore, catalyst volume declines in use.But the impact of ratio on above-mentioned heat exchange surface and catalyst volume is inapparent and negligible.
Preferably, catalyst to be filled is extrudate, its have diameter be 1mm to the particle diameter between 2mm, there is 3mm to the length between 15mm, and then preferably there is 3mm to the length between 6mm.The particularly preferably particle of almost spherical, it has the diameter of 1mm to 3mm, preferably has the diameter of 1.5mm to 2mm.Therefore advantageously, can reduce by the higher packed density of catalyst the necessary sized of reactor, this is accompanied by, and material is saved and energy is saved.In addition due to very little granular size, become easily and also advantageously make Just because of this gas flow homogenising with the filling reactor of catalyst.
Preferably, be furnished with at least one and keep grid on the heat-exchange tube between upper end and bottom, this maintenance grid stationary pipes orientation and the orientation of stationary pipes in reactor each other, that is to say the width that also adjusts flow channel.These maintenance grid are made up of annular radial system.Particularly preferably, keep grid to be formed by least two concentric rings, be connected with the bar as far as possible radially extending thus by being parallel to pipe row, thereby form the closed casket box around heat exchange array, wherein, can change for the spacing of spoke of the heat-exchange tube that keeps different-diameter.Bar is particularly preferably band iron at this, and by being welded to connect.Band iron can have embedded groove at this, so that make assembling become easy.Particularly preferably, band iron has upper seamed edge inclination and/or rounding and lower seamed edge, so that do not hinder filling and the taking-up of catalyst, and avoid consequent dead zone.Advantageously, the heat insulation layer of annular can and keep the ring of grid to cross at zone line.
Preferably, for maintenance work, reactor is that appearance is accessible.This can be especially by the manhole in one or more upper cap portions in pressure shield and/or lower cap portion or also realize by the input pipe of reacting gas or the conduit that leaves of product gas.For this reason particularly preferably, be provided with dismountable connecting portion at input pipe or in leaving conduit, for example flange part, so that open conduit in order to enter.
Preferably, the filling device that the useful catalyst of reacting appliance is filled.
Particularly preferred filling device is described and is had at least one catalyst dispenser and a filling tube multiple and that described catalyst dispenser is connected in claim 15.Filling device this be arranged in reative cell above.At least one catalyst dispenser is arranged in the outside of heat-exchange tube bundle.Multiple filling tubes (described filling tube is with corresponding at least one catalyst dispenser that passes into of tube end on it) extend in the dead band being formed by the region of the top of reative cell, and pass in this dead band with its lower tube end, wherein in dead band, the extension of all filling tubes is coordinated with each other as follows,, the overall distribution of its lower tube end is to the whole cross section of catalyst case.
Filling device utilization is familiar with as follows,, in the time utilizing catalyst granules catalyst filling chamber, the temporal spacing colliding between two catalyst in same area on the one hand should be enough large, thereby not crooked (verkanten) and block mutually of the catalyst granules of collision, but there is time enough to turn to or slide in homeostasis position separately, and described catalyst granules is feeded thus as far as possible hermetically, on the other hand, described temporal spacing should be even as far as possible, to obtain the in height charging of homogeneous.Utilize and preferably can construct static filling device with the filling tube of bouquet (Strau β) arranged in form, rotatablely move and vertical motion although lack, this filling device is catalyst filling material as follows,, the catalyst filling forming is feeded in heterogeneity and at this hermetically along level and vertical direction, described filling tube extends to the intermediate space between heat-exchange tube from catalyst dispenser, extends to the dead band (that is to say the reative cell not being filled) of the catalyst-free between the downside of upper perforated plate and the upside of catalyst filling to be filled.Extension by all filling tubes in dead band is coordinated with each other as follows, that is, the overall distribution of its lower tube end, to the whole cross section of catalyst case, is guaranteed catalyst material uniform filling to the cross section of catalyst case.
The upper end of filling tube passes into catalyst dispenser, thus guarantee catalyst material without interruptedly evenly flow into each filling tube and and then catalyst material on certain hour, evenly leave the bottom of filling tube, be below also referred to as trickling speed.Each time quantum is determined by the size that enters opening at the size of the open cross-section of filling tube or the upper tube end place of filling tube through the amount of the catalyst material of filling tube.That can determine filling tube according to the trickling speed of expecting enters opening or inside dimension.Catalyst dispenser is arranged in the outside of heat-exchange tube group, thereby this catalyst dispenser can freely design and place on the one hand, and convenient approaching on the other hand, therefore during catalyst filling chamber, catalyst dispenser can be filled with catalyst material without any problems again by operator.Filling device according to the present invention is preferably mounted in fixed bed reactors, and preferably after end filling process, can again from these fixed bed reactors, not remove, thereby design freedom is not limited to dismounting possibility to be arranged yet.
After end-of-fill, the upside of catalyst filling abuts in the lower tube end of filling tube.Because filling device preferably remains in fixed bed reactors, so state that filling tube and catalyst dispenser can keep catalyzed agent material to fill, thereby at reactor run duration, in the time there is possible sedimentation in catalyst filling, other catalyst materials trickle in catalyst case automatically, until again reach the operational height of catalyst filling, that is to say, until the upside of catalyst filling reaches the lower tube end of filling tube again.Therefore also guarantee all the time the maintenance of the optimum height of catalyst filling.
The size of the capacity of filling device and relevant part of appliance and spacing are preferably determined specification as follows, that is, even in the time there is sedimentation, the upside of catalyst filling is always positioned on predetermined minimum catalyst height reliably.In order to be limited in by-pass flow in the upper area of catalyst filling and to this meaningfully, give the additional inert filler of area filling of the minimum constructive height top of catalyst filling.In the time that the amount of catalyst is enough, inert filler can be inputted by filling device equally, or intermediate space through heat-carrying agent collector and reactor cover or input through the opening in heat-carrying agent collector.For example can remove the air-locked upper closure of central tube for this reason.For this filling process, can in the not transparent region in the outer wall of reative cell, create opening equally.Dead band below heat-carrying agent collector can minimize effectively by the upper inert filler of manufacture like this.
Preferably, reactor cover arrangement goes out catalyst holding device.Can avoid thus keeping for level the additional member of catalyst filling.
The present invention other equally preferred embodiment in, heat-exchange tube group and catalyst filling are configured with circlewise without internal cavity pipe and catalyst-free, wherein catalyst filling is kept by catalyst holding device radially outer and inner radial, and is furnished with external cavity between the catalyst holding device of reactor cover and radially outer.Internal cavity and external cavity can use gas or derive product gas for importing.In addition avoid the reaction in the fringe region of fixed bed reactors, in described reaction, reaction condition may suffer interference effect.
Advantageously, catalyst bracket (Katalysatorauflage) is the surface of the filler in lower reactor cap portion.The design of fixed bed reactors is simplified thus, and this is because do not have special member must be set to catalyst bracket.
Preferably, catalyst dispenser is flatly arranged in the outside of heat-exchange tube group.With which, the chamber above heat-exchange tube can be for other members vertically, for example heat-carrying agent distributor or heat-carrying agent collector.
Only in the favourable improvement project of the present invention, be configured with a catalyst dispenser and it extends on whole periphery along the inner side of reactor cover circlewise.Utilize this measure, catalyst dispenser is not only saved spatially and is arranged, and is easily closely arranged in fixed bed reactors.
At this, catalyst dispenser is preferably with the cross-sectional configurations of basin form, and filling tube passes at the end of this catalyst dispenser, and the wall of catalyst dispenser extends to the entrance of filling tube obliquely.In other embodiments, wall also can vertically extend.With which, catalyst dispenser can construct and guarantee as follows in design simply, that is, all the catalyst material in basin arrives the entrance of filling tube.
In the preferred embodiment of the present invention, heat-carrying agent distributor or heat-carrying agent collector (according to the flow direction of heat-carrying agent) are arranged on the cross section of heat-exchange tube group (row or middle column completely), and catalyst dispenser is arranged on the dead band between heat-carrying agent distributor or heat-carrying agent collector and reactor cover.Utilize this layout of heat-carrying agent distributor or heat-carrying agent collector and catalyst dispenser, the space above heat-exchange tube is saved spatially and is utilized.
At this advantageously, the upper tube end of heat-exchange tube is welded on running through in boring of each upper perforated plate hermetically, and tube sheet is the end of heat-carrying agent distributor or heat-carrying agent collector, and heat-exchange tube passes in this heat-carrying agent distributor or heat-carrying agent collector.Therefore, can also manufacture at an easy rate according to fixed bed reactors of the present invention, this is because cancelled the independent member for the end of heat-carrying agent distributor or heat-carrying agent collector.
At this particularly preferably, filling tube has the first section and the second section separately, this first section is from catalyst dispenser, between heat-carrying agent distributor or heat-carrying agent collector and reactor cover, extend to straight down in dead band, this second section extends radially inwardly from the first section.In this design, the first section of filling tube is saved spatially, between heat-carrying agent distributor or heat-carrying agent collector (that is to say upper perforated plate) and reactor cover, extend bunchy, and on catalyst case, distribute with its second section with bouquet form subsequently.
Multi-piece type in the heat-carrying agent distributor and/or heat-carrying agent collector implemented, filling tube also can be passed between two heat-carrying agent distributors or heat-carrying agent collector.Also possible that, filling tube is through heat-carrying agent distributor or heat-carrying agent collector.
In the favourable design of the present invention, the lower tube end of filling tube distributes as follows, that is, it is the identical volume content of catalyst filling filler always.Therefore, reach the density as far as possible uniformly through whole cross section of catalyst filling.Catalyst filling vertically preferably only extends on all heat-exchange tubes have the region of linear section, that is to say and does not extend to radially further in the region being bent of external heat-exchange tube.
Preferably, filling tube has oval-shaped cross section.The filling tube being shaped so also can be utilized without any problems less cross sectional dimensions and extend in intermediate space narrow, between heat-exchange tube, although and due to larger cross sectional dimensions for this reason vertically, described filling tube has enough large pipe cross section, so that obtain enough trickling speed and/or avoid blockage.
Advantageously, under the running status of fixed bed reactors, catalyst case is filled pipe and each catalyst dispenser is filled with catalyst material.Therefore, at lasting reactor run duration, occur may sedimentation time at catalyst filling, catalyst material also can trickle in catalyst case automatically, and catalyst filling filler once more.Therefore reactor operation keeps the optimum height of catalyst filling constant.
Preferably, each filling tube has restriction.With which, the inside dimension of filling tube can be selected as follows,, get rid of the situation that the catalyzed agent material of filling tube stops up, and by restriction, can rotate as follows for the channel cross-section of each filling tube,, can obtain the trickling speed of expectation.
At this particularly preferably, the size of restriction opening is adjustable.Therefore during lasting filling process, the size of restriction opening and and then trickling speed also can be matched with without any problems the specified criteria of change.
The present invention also relates to reactor, in order to obtain nearly quasi-isothermal reaction mechanism (Reaktionsregime) purposes, described reactor is with the heat-exchange tube being as far as possible directly arranged side by side with the form of group, this heat-exchange tube forms radial flow channels, also with the fused salt as heat-carrying agent.Nearly quasi-isothermal reaction mechanism can be regarded as following reaction mechanism, that is, this reaction mechanism have approximately constant, have and be 10 ℃ to the maximum, be preferably 5 ℃ to the maximum, be particularly preferably the temperature of the temperature fluctuation of 2 ℃ to the maximum.
Particularly preferably, utilize the nearly quasi-isothermal reaction mechanism with the fused salt as heat-carrying agent in heat-exchange tube, reactor according to the present invention is used for carrying out neither endothermic nor exothermic reaction.
In addition preferably, be used for gas-phase reaction, the reaction of preferably putting thermocatalytic or endothermic catalytic according to reactor of the present invention.
Particularly preferably, according to reactor of the present invention for oxidation reaction, hydrogenation reaction, dehydrogenation reaction, nitration reaction, alkylation reaction or for manufacturing hydrocarbon by alcohols or dimethylether, be particularly useful for by methanol synthesized gasoline, and for by synthesis gas synthesizing methanol.
Preferably when for the synthesis of gasoline, product is inputted by central tube and reactor product is exported by external cavity.Preferably fused salt is as heat-carrying agent, and described fused salt by the heat-carrying agent distributor below being arranged in, is pressed in the heat-carrying agent collector that is arranged in top through heat-exchange tube in heat-carrying agent closed circuit, and from collector is transported to heat exchanger.
Accompanying drawing explanation
Set forth the present invention by embodiment and Tu Lai below, wherein:
Fig. 1 illustrates through according to the longitudinal section of reactor of the present invention,
Fig. 2 illustrates through according to the cross-sectional view of reactor of the present invention,
Fig. 3 a, 3b illustrate the difference layout of pipe row,
Fig. 4 illustrates the fragment figure that keeps grid,
Fig. 5 a, 5b illustrate the connection of the pipe being bent and be not bent in tube sheet with two cutaway views,
Fig. 6 illustrates the longitudinal section of the isothermal fixed bed reactors of crossing through axial flow, have catalyst according to the invention filling device,
Fig. 7 illustrates the longitudinal section of the isothermal fixed bed reactors of crossing through radial flow, have catalyst according to the invention filling device, and
Fig. 8 a, 8b illustrate through according to two of filling device of the present invention sectional views.
The specific embodiment
Fig. 1 illustrates according to isothermal reactor 1 of the present invention with longitudinal section.This isothermal reacting appliance has the pressure shield 2 being made up of the reactor cover 3 of cylinder shape, and this pressure shield thereon end is sealed by upper reactor cap portion 4 and sealed by lower reactor cap portion 5 in its bottom.Reactor 1 is orientated vertically, that is to say, central axis or reactor axis 6 are extended vertically.Reative cell 7 is in reactor cover 3 inside, this reative cell by perforation outer wall 10 and carry out gauge around the central tube 13 of internal cavity 11.The outer wall 10 of perforation separates reative cell 7 and external cavity 12.In reative cell 7, be filled with catalyst filling 8.Reative cell 7 (that is to say in the direction of central axis 6) by multiple heat-exchange tubes 9 and passes in the axial direction.
The axis of ventilative central tube 13 is central axis 6.That is to say that catalyst filling 8 extends circlewise between the outer wall 10 of reative cell and central tube 13.
In the embodiment shown in fig. 1, reactor 1 at its lower area until the beginning of catalyst filling 8 with under inert filler 14a fill, the catalyst granules of catalyst filling 8 is positioned on this lower area.Upper inert filler 14b is in the top of catalyst filling 8.
Depend on reacting gas is in what place of reactor 1 inside, the reacting gas 15 to be indicated conventionally of the reactor 1 of flowing through has other compositions, and is correspondingly differently indicated.Use gas 16 to enter conduit 17 and enter reactor 1 by being in the gas at lower reactor cap portion 5 centers as fresh, unreacted gas.Adjust best according to special program at this with pressure, temperature and the composition of gas 16.Use gas 16 to enter the central tube 13 that conduit 17 flows to directly connected perforation from gas.Use gas be passed in therefrom in center tube wall by the opening 18 that forms of perforation and enter the catalyst filling 8 being in annular reative cell 7, use gas radially to pass catalyst filling 8 and be reacted into the product of expectation at this as reacting gas 15.After this, described product is as product gas 19 through the ventilative outer wall 10 of reative cell and enter in external cavity 12, and described product gas flows in reaction cap portion 4 and leaves conduit 20 via the gas that passes upper reaction cap portion 4 therefrom and leave reactor 1 from this external cavity.
Constant radially rate of departure from central tube 13 to reative cell 7 is by carefully designing and regulating mutually the mobile section of all generation pressure losses to reach.Can provide as follows as conclusive design size at this: the ratio of the flow cross section of central tube 13 and total face that flows through of center tube wall, the axial porous of center tube wall distribute and the pressure drop coefficient of the ventilative outer wall 10 of catalyst filling 8 and reative cell.To consider the sedimentation of catalyst filling 8 at run duration.For fear of the by-pass flow in the upper region of catalyst filling 8, central tube 13 has airtight region 21 up, and same outer wall 10 has airtight region 22 up.In addition, catalyst is filled in reactor 1 with enough amounts, thereby the full level of catalyst can not drop to below 21 and not transparent region that can not drop to outer wall 10, not transparent region of central tube 13 below 22.
Reaction temperature in catalyst filling 8 is controlled by multiple heat-exchange tubes that flow through by heat-carrying agent 25 9.At this, heat-exchange tube 9 is incorporated in upper perforated plate 23 or in lower perforated plate 24 in its end, and welds hermetically with described tube sheet there.At this, the heat-carrying agent 25 that flows through heat-exchange tube 9 imports in heat-carrying agent distributor 28 by heat-carrying agent input pipe 26.Dispenser cap portion 27 is connected with lower perforated plate 24 hermetically at this.Before entering heat-exchange tube 9, the uniforming device 29 that heat-carrying agent 25 is implemented as orifice plate in the interior utilization of distributor 28 at this is evenly distributed on flow cross section.After flowing through heat-exchange tube 9, heat-carrying agent 25 arrives heat-carrying agent collector 30.This heat-carrying agent collector and heat-carrying agent distributor 28 are built same or similarly.This collector 30 is corresponding has collector cover portion 31.Heat-carrying agent 25 is discharged to conduit 32 output-response devices 1 and flowed at this unshowned cooling device by heat-carrying agent.For maintenance work, collector 30 can approach by collector manhole 33.To the passage of the inside of reactor 1 for example by leaving dismountable connecting portion 34 in conduit 20 at gas or by realizing at this unshowned manhole in upper reactor cap portion 4.The different heat expansion of all elements that are in inside reactor of reactor cover 3 and heat-exchange system is all absorbed by compensator 35, and described compensator is formed as being arranged in the corrugated expansion joint of reactor cover portion 4 outsides at this.
According to the present invention, be placed on heat-exchange tube 9 in catalyst filling 8 and be parallel to as far as possible central axis and arrange to organize 36 form (referring to Fig. 2).In order to manufacture and in order to transport tube bank, heat-exchange tube 9 is fixed in its position by the maintenance grid 37 of multiple levels.
Fig. 2 illustrates the cross-sectional view of reactor, its diagram of distribution with the heat-exchange tube 9 in catalyst filling 8 inside.Heat-exchange tube 9 can be grouped into the group of row 38 and the group of middle column 39 completely, and these set constructors go out radial flow channels 40.If the radial dimension of middle column 39 does not reach the size of the outermost of row 38 completely, will produce so the radial flow channels 40 of the flow cross section with increase.Therefore can create when needed the radial flow channels 41 of the cooling surface density with minimizing.In addition,, without the catalyst area of cooling device, that is to say that adiabatic conversion zone 42 is arranged on the radially outer in heat-exchange tube region.The conversion zone of described thermal insulation can be radially inwardly, that is to say towards reactor axis arrange, also can be radially outwardly, that is to say away from reactor axis arrange.
Two Fig. 3 a and 3b illustrate the design of the alternative that heat-exchange tube 9 is listed as.In Fig. 3 a, heat exchange array is with its axis arranged on straight line, and wherein the heat-exchange tube 9 of different-diameter alternately occurs.
Fig. 3 b illustrates the snakelike layout of the axis of heat-exchange tube 9, and therefore described heat-exchange tube forms snakelike radial flow channels 40.
Maintenance grid 37 for (unshowned at Fig. 4) heat-exchange tube shown in Figure 4.These maintenance grid are substantially by radially holding element 43 and circular holding element 44 form.In addition, keep grid 37 to reinforce by extra cross bar 45.Holding element 43,44,45 is preferably made up of the semi-finished product of rectangle.In addition they have upside and the downside of preferred rounding, to filling reative cell 7(referring to Fig. 1 with catalyst) Shi Buhui hinders the whereabouts of catalyst and to avoids dead band.At this, holding element 43 radially keeps the row of heat-exchange tube 9 on both sides, and wherein band iron is for example changed and is matched with different pipe diameters by thickness.Therefore, described band iron is fixed to one another a row heat-exchange tube 9.Circular holding element 44 is fixed to one another different pipe row again, and its method is that the holding element 44 of described circle is connected with holding element 43 radially.
Fig. 5 a illustrates that the heat-exchange tube 9 being bent lines up the sectional views of the layout of two pipe row in tube sheet 23.Directly be positioned at abreast row at this pipe 9.01,9.02 and 9.03.Pipe 9.01 is dually oppositely bent to the right at this, and arranges in the position that dextrad staggers through tube sheet 23 at the line with respect to straight.Pipe 9.02 directly guides through tube sheet 23.Being positioned at pipe 9.03 below, to be similar to pipe 9.01 bending equally doubly, but be bending left, and also left-hand staggers and guides through tube sheet 23.The pipe row side by side with pipe 9.11,9.12,9.13 on side are correspondingly processed exactly.
Fig. 5 b illustrate have in Fig. 5 a, describe from above the top view of tube sheet of visible tube end.The circle of dotted line shows the position of the pipe being bent that is in tube sheet 23 belows.
In the embodiment shown in fig. 6, catalyst case 49 or be filled on catalyst filling 8 along continuous straight runs in the catalyst case whole cross section in reactor cover 3 extends, that is to say, are discs through the level cross-sectionn of catalyst filling 8, and the inwall of reactor cover 3 forms its edge.
Correspondingly, the heat-exchange tube 9 in catalyst filling 8 is distributed on disc equally, that is to say, the level cross-sectionn of restrainting through heat-exchange tube 9 is a disc substantially equally.At this, radially inner most heat-exchange tube 9 circular ground around reactor axis 6 arrange and radially outmost heat-exchange tube 9 circular the pitch arrangement to reactor cover 3 inwalls to be scheduled to.
Concept " substantially " and " approximately " should mean, radially inner most and radially outmost heat-exchange tube 9 depends on that design ground may lie loosely on circumference, but radially staggers each other with maximum two tubular axis distance between centers of tracks.
Catalyst filling 8 abuts on the outside of heat-exchange tube 9, and is flow through by reacting gas 15 under the running status of reactor 1.
In this embodiment, reacting gas 15 and heat-carrying agent 25 flow with reverse flow in catalyst filling 8, and reacting gas 15 flows from top to bottom and heat-carrying agent 25 flows from the bottom up.
Enter gas in reactor 1 and be called as and use gas 16, flow through that gas catalyst filling 8, that react is called as reacting gas 15 and the gas that leaves reactor 1 is called as product gas 19.
Use gas 16 to enter in the upper reactor cap of conduit 17 importing portion 4 by gas in this embodiment, and product gas 19 leave the lower reactor cap of conduit 20 derivation portion 5 by gas.
The bottom of heat-exchange tube 9 lower perforated plate 24 run through boring in weld hermetically and pass into heat-carrying agent distributor 28, lower perforated plate 24 forms the bottom of these heat-carrying agent distributors.
The upper end of heat-exchange tube 9 upper perforated plate 23 run through boring in weld hermetically and pass into heat-carrying agent collector 30, upper perforated plate 23 forms the bottom of these heat-carrying agent collectors.
Lower reactor cap portion 5 covers heat-carrying agent distributor 28, and upper reactor cap portion 4 covers heat-carrying agent collector 30.
In unshowned embodiment, heat-carrying agent distributor 28 and/or heat-carrying agent collector 30 also can be implemented on multi-piece type ground.
In the illustrated embodiment, heat-carrying agent distributor 28 and heat-carrying agent collector 30 are constructed circlewise, and wherein reactor axis 6 is corresponding extends through ring center.At this, the interior diameter of ring is selected as follows, that is, radially inner most heat-exchange tube 9 can extend point-blank between heat-carrying agent distributor 28 and heat-carrying agent collector 30.The overall diameter of ring is less than the overall diameter that heat-exchange tube 9 is restrainted, and has the tube end being bent, to can pass in heat-carrying agent distributor 28 or heat-carrying agent collector 30 thereby be radially further in outside heat-exchange tube 9.On the height of the half between heat-carrying agent distributor 28 and heat-carrying agent collector 30, heat-exchange tube 9 keeps grid 37 through level, and this level keeps grid steady heat exchanging tube 9 in the horizontal direction.
In unshowned embodiment, also can vertically arrange multiple maintenance grid 37.
Heat-carrying agent distributor 28 connects at least one heat-carrying agent input pipe 26.Two heat-carrying agent input pipes 26 in the embodiment shown, its outside from reactor 1 vertically through reactor cap portion 5 extend.
Heat-carrying agent collector 30 connects at least one heat-carrying agent and discharges conduit 32.Be that two heat-carrying agents are discharged conduit 32 in the embodiment shown, it flatly stretches out through reactor cover 3.
Catalyst filling 8 vertically only extends on as lower area, and in this region, all heat-exchange tubes 9 have straight section, that is to say, catalyst filling 8 does not extend to as in lower area, in this region, is radially further in outside heat-exchange tube 9 and is bent.
In the arranged beneath of catalyst filling 8 by the filler being formed by inert material (being also referred to as below lower inert filler 14a), lower inert filler fills up the lower area of this filler filling reactor 1, that is to say the lower part of lower reactor cap portion 5 and filling reactor cover 3, until the beginning of the directly-heated exchanging tube section in the heat-exchange tube 9 being bent, and therefore until the beginning of catalyst filling 8.Therefore, the upside of inert filler 14a forms catalyst bracket, for spreading vertically catalyst filling 8 and therefore for the downward gauge of catalyst filling.
The coboundary of catalyst case 49 and the thus operational height of catalyst filling 8, that is to say that the upside of catalyst filling and the downside of upper perforated plate 23 or heat-carrying agent collector 30 exist predetermined spacing.The space being formed by this spacing is called as dead band 50.
Filling device 51 is arranged in the top of catalyst case 49 and has catalyst dispenser 52 and multiple filling tube 48/53.
Catalyst dispenser 52 is constructed circlewise and is arranged in above heat-carrying agent collector 30 in reactor 1.The cross section of catalyst dispenser 52 is peviforms, has the end 54 and wall 55, and described wall 55 narrowed towards the end 54 taperedly.
Filling tube 48/53 utilizes its upper end hermetically in the end 54 of running through boring 56(and be fixed in a) referring to Fig. 8 catalyst dispenser 52 and pass into this catalyst dispenser, referring to the details diagram in Fig. 8 a.Filling tube is extended from catalyst dispenser 52, and first pencil ground, to the direction of outer reactor cover 3, extends downwardly in dead band 50 subsequently between the outward flange of heat-carrying agent collector 30 and the inwall of reactor cover 3.Filling tube is bifurcated there, and extends and extend in the intermediate space between heat-exchange tube 9 with different length along different directions, and wherein all of the lower tube end of filling tube 48/53 is evenly distributed on total cross section of catalyst case 49 substantially.Filling tube 48/53 has minimal tilt degree on its total length, and it guarantees the perfectly mobile or trickling of the catalyst material in filling tube 48/53.
In unshowned embodiment, filling tube 48/53 multi-piece type can between two heat-carrying agent distributors 28 or heat-carrying agent collector 30, pass in the heat-carrying agent distributor 28 implemented and/or heat-carrying agent collector 30.Also possible that, filling tube 48 is through heat-carrying agent distributor 28 or heat-carrying agent collector 30.
The inside dimension of filling tube 48/53 designs as follows, that is, in each chronomere, only the catalyst material of a scheduled volume can pass each filling tube 48/53, that is to say, produces predetermined trickling speed.
Filling device 51 is forever retained in reactor 1.Therefore heat-carrying agent distributor 28 and heat-carrying agent collector 30 can be for example about approaching more like a cork heat-exchange tube 9 and need not considering to dismantle possibility and more freely design.
Upper reactor cap portion 4 has catalyst and fills sleeve pipe 57, fills sleeve pipe can utilize catalyst material to carry out catalyst filling distributor 52 by suitable facility by this catalyst.
Lower reactor cap portion 5 has the emptying sleeve pipe 58 of catalyst, can and be gone up inert filler 14b if desired and again clear out of reactor 1 lower inert filler 14a, catalyst filling 8 by the emptying sleeve pipe of this catalyst.
In addition, in upper reactor cap portion 4, be also configured with manhole 59, for maintenance work, assembler can enter upper region by this manhole, that is to say the top that enters heat-carrying agent collector 30.This manhole 59 can be used for carrying catalyst equally.
In addition, heat-carrying agent input pipe 26 and/or heat-carrying agent are discharged conduit 32 and can be designed as follows, that is, discharge conduit can realize and lead to inside reactor through described heat-carrying agent input pipe and heat-carrying agent.
Hereinafter, as long as no other explanation,, according to the embodiment of Fig. 7 corresponding to according to the embodiment of Fig. 6.
In the embodiment shown in Fig. 7 of reactor 1 according to the present invention, catalyst case 49 or catalyst filling 8 are constructed along reactor cover 3 inwalls circlewise with the internal cavity 11 of catalyst-free and the external cavity 12 of catalyst-free.At its radial outside, catalyst filling 8 is surrounded by the ventilative outer wall 10 of cylinder shape.For fear of by-pass flow, not transparent region 22 is connected on ventilative outer wall 10.Between outer wall 10 and the inwall of reactor cover 3, be configured with external cavity 12.In its radially built-in side, catalyst filling 8 abuts on ventilative central tube 13 or by this central tube and carrys out gauge, and the axis of this central tube is reactor axis 6.
Corresponding to structure catalyst filler 8 circlewise, heat-exchange tube 9 is restrainted also structure circlewise.At this, radially inner most heat-exchange tube 9 is sentenced predetermined spacing apart from the inside gauge in footpath of catalyst filling 8 and is arranged, and radially outmost heat-exchange tube 9 is sentenced predetermined spacing apart from the outside gauge in footpath of catalyst filling 8 and arranged.
In this embodiment, gas flows from the bottom up, wherein said gas as use gas 16 to import that gas enters the bottom of conduit 17 and in the region of catalyst filling 8 through the ventilative wall there of central tube 13 in inflow catalyst filler 8, leave conduit 20 so this use gas substantially radially flows through as reacting gas 15 and upwards flow to vertically gas in external cavity 12, and leave this gas as product gas 19 and leave conduit.
Because heat-carrying agent 25 flows equally from the bottom up, there is in this embodiment thus the concurrent of heat-carrying agent 25 and gas.
In this embodiment, all heat-exchange tubes 9 extend point-blank on its total length.As according in the embodiment of Fig. 6, the bottom of heat-exchange tube 9 lower perforated plate 24 run through boring in fixing and pass into heat-carrying agent distributor 28 hermetically, lower perforated plate 24 forms the end of described heat-carrying agent distributor.In addition, heat-carrying agent distributor 28 has dispenser cap portion 27, and it covers lower perforated plate 24, and is connected hermetically with this lower perforated plate.
The upper end of heat-exchange tube 9 upper perforated plate 23 run through boring in fixing hermetically, and pass into heat-carrying agent collector 30, upper perforated plate 23 forms the end of described heat-carrying agent collector, in addition, heat-carrying agent collector 30 has in this embodiment spherical collector cap portion 31, it covers upper perforated plate 23, and is connected hermetically with this upper perforated plate.
In collector cap portion 31, be configured with collector manhole 33, to be passed into heat-exchange tube 9 for maintenance work can realize for assembler.
Heat-carrying agent distributor 28 and heat-carrying agent collector 30 are constructed circlewise, they are corresponding has center and runs through opening, the in the situation that of heat-carrying agent distributor 28, central tube 13 runs through opening through this center, the in the situation that of heat-carrying agent collector 30, central tube 13 extends to this center within a predetermined distance to be run through in opening.
The radially outward edge of heat-carrying agent distributor 28 and heat-carrying agent collector 30 is between outside gauge place, the footpath of radially outmost heat-exchange tube 9 and catalyst filling 8, thereby 28(also has heat-carrying agent collector 30 at heat-carrying agent distributor) radial outer wall and the inwall of reactor cover 3 between be configured with annular gap, radially the extending and be greater than the radially extension of external cavity 12 of this annular gap.
Heat-carrying agent distributor 28 is connected at least one heat-carrying agent input pipe 26.Two heat-carrying agent input pipes 26 shown in Figure 7, its extend vertically and by lower reactor cap portion 5 to downward-extension.
Heat-carrying agent collector 30 is connected at least one heat-carrying agent and discharges conduit 32.Two heat-carrying agents shown in Figure 7 are discharged conduit 32, and it stretches out vertically through upper reactor cap portion 4 and their this side is connected to heat-carrying agent collector 60 outside, annular.Outside heat-carrying agent collector 60 is connected to again the heat-carrying agent of level and discharges conduit 61.
Be in vertical heat-carrying agent between heat-carrying agent collector 30 in reactor cap portion 4 and outside heat-carrying agent collector 60 and discharge conduit 32 and there is each compensator 35 in upper reactor cap portion 4 inside, for compensating different temperature expansions.
For steady heat exchanging tube 9 flatly, on half height between lower perforated plate 24 and upper perforated plate 23 or be furnished with the maintenance grid 37 of level between heat-carrying agent distributor 28 and heat-carrying agent collector 30, it passes through heat-exchange tube 9.
Central tube 13 extends through lower reactor cap portion 5 downwards and stretches out via this lower reactor cap portion, and is formed for using the gas of gas 16 to enter conduit 17.From this bottom, that is to say from use gas 16 enter opening until catalyst filling 8 beginning airtight construct central tube 13 walls.
On end, central tube 13 extends in the central opening of annular heat-carrying agent collector 30 thereon.In region, end, central tube 13 is configured with air-locked wall 21 equally thereon, and described air-locked wall extends to catalyst filling 8 within a predetermined distance from the upper end of central tube 13.The upper end air seal ground sealing of central tube 13.
At this, the lower part of reactor 1 (that is to say lower reactor cap portion 5 and until the lower part of the reactor cover 3 of the bottom of catalyst filling 8) is also filled with lower inert filler 14a.That is to say, the upside of this lower inert filler 14a is formed for lower gauge place and the vertical rack of catalyst filling 8.
In the embodiment shown in fig. 7, the catalyst dispenser 52 of filling device 51, along the inner side of reactor cover 3, extends circlewise on total periphery of reactor cover.This catalyst dispenser is arranged on the intermediate space or annular gap between the outside of heat-carrying agent collector 30 and the inner side of reactor cover 3, thereby filling tube 53 extends to the below of upper perforated plate 23 or heat-carrying agent collector 30 vertically from the 54s, the end of catalyst dispenser 52, and then, as according in the embodiment of Fig. 6, be branched to heat-exchange tube 9 with bouquet form intrafascicular
State after catalyst material is filled into catalyst case 49 completely shown in Figure 7, that is to say, the upside of catalyst filling 8 abuts on the lower tube end of filling tube 53.In addition, fill filling tube 53 and catalyst dispenser 52 with catalyst material, thereby the in the situation that of catalyst filling 8 sedimentation, even be also automatically again filled in catalyst case 49 at reactor run duration catalyst material.In addition in this embodiment, upper inert filler 14b is in catalyst filling 8 tops.
As according in the embodiment of Fig. 6, upper reactor cap portion 4 has catalyst and fills sleeve pipe 57 and manhole 59.
Similarly, as according in the embodiment of Fig. 6, lower reactor cap portion 5 has the emptying sleeve pipe 58 of catalyst.
Reactor 1 shown in Figure 7 also has fluidizer 62, for emptying reactor 1.Distribution conduit 63 for fluidizing gas belongs to this fluidizer, and described distribution conduit, between catalyst filling 8 and heat-carrying agent distributor 28, is extended in lower inert filler 14a.Described distribution conduit 63 has ring duct 64, and this ring duct extends and is connected on gas input pipe 65 around heat-exchange tube 9 bundles, and this gas input pipe is through the outside horizontal-extending of reactor cover 3 and have compressor 66 in the outside of reactor cover 3.Gas can be under the state of dehumidifying, in the case of the pressure improving, and continuously or utilize compression shock pulsed and carry.In addition, distribution conduit 63 also has bifurcated catheter 67 radially, and described bifurcated catheter is suitable for being fluidly connected with ring duct 64, and it is intrafascicular to extend to heat-exchange tube 9 in lower inert filler 14a inside, and fluidizing gas leaves this bifurcated catheter.Also exist alternatively other, the preferred lower bifurcation conduit 68 that can operate separately, it is arranged in the below that heat-exchange tube 9 is restrainted.
The connection at the upper tube end of filling tube 53 and the end 54 of catalyst dispenser 52 is shown with the size increasing in Fig. 8 a.The upper tube end of filling tube 53 has the shoulder section 69 of radial expansion, and it was connected hermetically with the end 54 of catalyst dispenser 52.The end 54, has the ramp for the entrance of filling tube 53, thereby catalyst material guides to entrance from the territory, lateral areas of catalyst dispenser 52.The restriction 70 with restriction opening 71 is arranged in the shoulder section 69 at upper tube end place of filling tube 53, determine that by this restriction each time quantum enters the amount of the catalyst material of filling tube 53, and therefore determine the trickling speed of the catalyst material that leaves filling tube 53.
Filling tube 53 has oval-shaped cross section, and (Fig. 8 b).Less cross sectional dimensions 72 determines by the size of the intermediate space between adjacent heat-exchange tube 9, and filling tube 53 is extended through this intermediate space.The size of larger cross sectional dimensions 73 determines as follows, that is, filling tube 53 freely pass through cross section 74 with respect to the size of catalyst granules enough greatly, to avoid blocking catalyst granules and therefore stop up filling tube 53.
Reference numerals list
1 reactor
2 pressure shield
3 reactor covers
Reactor cap portion on 4
5 times reactor cap portions
6 central axis/reactor axis
7 reative cells
8 catalyst fillings
9 heat-exchange tubes
The outer wall of 10 reative cells
11 internal cavities
12 external cavities
The inwall of 13 central tubes/reative cell
Inert filler under 14a
The upper inert filler of 14b
15 reacting gas
16 use gas
17 gases enter conduit
Opening in 18 central tubes
19 product gas
20 gases leave conduit
Not transparent region in 21 central tubes
Not transparent region in the outer wall of 22 reative cells
23 upper perforated plates
24 lower perforated plates
25 heat-carrying agents
26 heat-carrying agent input pipes
27 dispenser cap portions
28 heat-carrying agent distributors
29 uniforming devices
30 heat-carrying agent collectors
31 collector cap portions
32 heat-carrying agents are discharged conduit
33 collector manholes
34 dismountable connecting portions
35 compensators
36 heat-exchange tube groups
37 keep grid
38 are listed as completely
39 middle column
40 radial flow channels
41 have the radial flow channels of the cooling surface density of minimizing
The conversion zone of 42 thermal insulation
43 holding elements radially
The holding element of 44 circles
45 cross bars
48 filling tubes through heat-carrying agent collector
49 catalyst cases
50 dead bands
51 filling devices
52 catalyst dispensers
53 filling tubes
The end of 54 catalyst dispensers
The wall of 55 catalyst dispensers
56 run through boring
57 catalyst are filled sleeve pipe
The emptying sleeve pipe of 58 catalyst
59 manholes
The heat-carrying agent collector of 60 annulars
The heat-carrying agent of 61 levels is discharged conduit
62 fluidizers
63 distribution conduit
64 ring ducts
65 gas input pipes
66 compressors
67 bifurcated catheter
68 lower bifurcation conduits
69 shoulder sections
70 restriction
71 restriction openings
72 less cross sectional dimensions
73 larger cross sectional dimensions
74 pass through cross section

Claims (19)

1. the reactor (1) that radial flow is crossed, it is for utilizing the reaction mechanism of isothermal substantially to carry out chemical catalysis reaction, described reactor has the cover (3) of the cylinder shape of substantially arranging around central axis (6), substantially the reative cell (7) of annular is formed in described cover, described reative cell surrounds the central tube (13) of perforation, and surrounded by external cavity (12), wherein said external cavity (12) and described reative cell (7) are separated by the outer wall (10) of perforation, and external cavity (12) and central tube (13) are for inputting reacting gas (15) and for output products gas (19), it is characterized in that, described reative cell (7) is passed by multiple heat-exchange tubes (9), wherein said heat-exchange tube (9) is parallel to described central axis (6) and as far as possible with multiple groups of layouts, thereby described group forms the row completely (38) that are radially arranged in described reative cell (7), wherein row (38, 39) outline of adjacent heat exchanging tube (9) mutually near, thereby form flow channel (40) radially.
2. reactor according to claim 1 (1), is characterized in that, at least one heat-exchange tube (9) of group at least one tube end place single ground or preferably twice be bent, and be fixed on tube sheet at least unilaterally in (23,24).
3. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, be furnished with other heat-exchange tubes (9) group between the row completely (38) of heat-exchange tube (9), described heat-exchange tube group forms shorter middle column (39).
4. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, between outer wall (10) between central tube (13) and the row completely (38) of heat-exchange tube (9) of perforation and/or perforation and the row completely (38) of heat-exchange tube (9), the conversion zone (42) of thermal insulation lays respectively in annular space, and/or is listed as completely or middle column is interrupted by the adiabatic zone line of at least one annular.
5. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, described heat-exchange tube (9) has circular continuously cross section, or on its end, has circular cross section and have elongated cross section at zone line.
6. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, described heat-exchange tube (9) is at the vicissitudinous cross section of the inner tool of group.
7. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, outwards increase or remain unchanged as far as possible from described central tube (13) in spacing between the outline of adjacent row (38) completely or between adjacent row completely and the outline of middle column (39).
8. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, at least one is listed as completely or the axis of the heat-exchange tube (9) of middle column is positioned on the straight line radially outward pointing to.
9. according to the reactor described in any one in claim 1 to 7 (1), it is characterized in that, at least one is listed as completely or the axis of the heat-exchange tube (9) of middle column is positioned on serpentine.
10. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, at least one end of (9) of heat-exchange tube, preferably two ends are furnished with distributor (28) or the collector (30) for heat-carrying agent (25).
11. reactors according to claim 10 (1), it is characterized in that, described heat-carrying agent ingress pipe (26) and/or described heat-carrying agent delivery line (32) are connected by compensator (35) and reactor cover (3) or upper reactor cap portion (4) or lower reactor cap portion (5).
12. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, the perforation of the outer wall (10) of described central tube (13) and/or described reative cell (7) changes along the axial direction of reactor (1).
13. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, between heat-exchange tube (9) in described reative cell (7), be filled with the catalyst (8) of granular filler form, and the heat-exchange surface of described heat-exchange tube (9) and the ratio of catalyst volume radially flow direction reduce or keep constant, and are such as 10m 2/ m 3to 200m 2/ m 3, be preferably such as 50m 2/ m 3to 110m 2/ m 3.
14. reactors according to claim 13 (1), it is characterized in that, the granular size that described catalyst to be filled (8) has is, 1mm is to the diameter between 2mm, 3mm is to the length between 15mm, and preferably 3mm is to the length between 6mm, or particularly preferably, have diameter and be 1mm to 3mm, preferably diameter is the spherical particle of 1.5mm to 2mm.
15. according to the reactor one of aforementioned claim Suo Shu (1), it is characterized in that, in described reactor (1), for being arranged in reative cell (7) top to the filling device (51) of described reative cell (7) catalyst filling filler (8), described filling device has:
At least one catalyst dispenser (52), described at least one catalyst dispenser is arranged in the outside of heat-exchange tube (9) bundle, and
Multiple filling tubes (53), described filling tube passes into respectively in described at least one catalyst dispenser (52) with pipe end on it, extend in the dead band (50) being formed by the uppermost region of reative cell (7), and pass in described dead band with its lower tube end, wherein in described dead band (50), the extension of all filling tubes (53) is coordinated with each other, thereby the overall distribution of its lower tube end is to the whole cross section of catalyst case (49).
16. according to reactor in any one of the preceding claims wherein in order to obtain nearly quasi-isothermal reaction mechanism purposes, described reactor is with the heat-exchange tube being as far as possible directly arranged side by side and the fused salt as heat-carrying agent in heat-exchange tube, and described heat-exchange tube forms flow channel radially.
17. according to the purposes of the reactor described in any one in claim 1 to 15, and described reactor is for utilizing the fused salt as heat-carrying agent in heat-exchange tube to carry out the reaction with fuel factor with nearly quasi-isothermal reaction mechanism.
18. according to the purposes of the reactor described in any one in claim 1 to 15, and described reactor is for gas-phase reaction, the reaction of preferably putting thermocatalytic or endothermic catalytic.
19. according to the purposes of the reactor described in any one in claim 1 to 15, described reactor is for oxidation reaction, hydrogenation reaction, dehydrogenation reaction, nitration reaction, alkylation reaction or for manufacturing hydrocarbon by alcohols or dimethylether, be particularly useful for by methanol synthesized gasoline, and for by synthesis gas synthesizing methanol.
CN201310575072.4A 2012-11-15 2013-11-15 Fixed-bed reactor Pending CN103816840A (en)

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CN106922133A (en) * 2014-10-30 2017-07-04 赛贝克环球科技公司 The reactor and its application method of the coldplate put including radial direction
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Application publication date: 20140528