CN105080433A - Novel plate-type axial reactor - Google Patents
Novel plate-type axial reactor Download PDFInfo
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- CN105080433A CN105080433A CN201510555379.7A CN201510555379A CN105080433A CN 105080433 A CN105080433 A CN 105080433A CN 201510555379 A CN201510555379 A CN 201510555379A CN 105080433 A CN105080433 A CN 105080433A
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Abstract
The invention relates to a novel plate-type axial reactor. The novel plate-type axial reactor comprises a reactor housing (5), a heat exchange plate halved tie (6), heat transfer medium distribution manifolds (10), heat transfer medium distribution branch pipes (11), heat transfer medium collection manifolds (3) and heat transfer medium collection branch pipes (4), wherein the reactor housing (5) is provided with a reaction mass inlet (1), a reaction mass outlet (8), heat transfer medium inlets (9) and heat transfer medium outlets (2); the heat exchange plate halved tie (6) consists of a plurality of sets of subsidiary heat exchange plate halved ties; one end of each set of subsidiary heat exchange plate halved tie is connected with the heat transfer medium inlets (9) through the heat transfer medium distribution branch pipes (11) and the corresponding heat transfer medium distribution manifolds (10), and the other end of each set of subsidiary heat exchange plate halved tie is connected with the heat transfer medium outlets (2) through the heat transfer medium collection branch pipes (4) and the corresponding heat transfer medium collection manifolds (3). Compared with the prior art, the novel plate-type axial reactor has the advantages of being small in size, convenient to loading and unloading of a catalyst, flexible in structure and capable of multi-section reaction.
Description
Technical field
The present invention relates to a kind of axial flow reactor, especially relate to a kind of New-type plate axial flow reactor.
Background technology
For industrial production, great majority reaction all will have catalyst to participate in, and catalyst is generally solid, and reaction relates to heterogeneous, comprises gas-solid phase, liquid-solid phase is gentle liquid-solid equal, can adopt the reactor of the types such as fixed bed, fluid bed, moving bed and slurry bed system.Wherein, fixed bed reactors are the most common, the simplest reactor types of structure.Often with heat release or endothermic thermal event in chemical reaction process, for keeping reaction temperature in rational scope, usually direct or indirect heat exchange mode is taked, and direct heat transfer form can reduce the treating capacity of reaction mass and cause burden, so indirect heat exchange mode is comparatively common to subsequent products separation and purification.And adopt tubulation to form calandria type fixed bed reactor as indirect heat exchange element, be the current modal heat exchange type fixed bed reactors form of chemical industry.Catalyst packing is in pipe or outside pipe, and heat transferring medium adopts gas, water, saturation water, fused salt or heat conduction wet goods mode.In most cases, because two ends exist tube sheet, catalyst is inconvenient to be seated in outside pipe, and Catalyst packing is relatively simple in pipe; Heat transferring medium walks shell side usually, because shell side deflection plate can strengthen Hydrodynamic turbulence effect, is conducive to improving heat transfer coefficient, and if walk tube side, because of straight tube and wall is smooth, boundary layer is laminar flow, and heat-transfer effect is poor.
And for being usually used in the ion exchange resin solid acid base catalysator of the reaction such as etherificate and ehter bond cracking reaction, hydration reaction, esterification, condensation and cyclisation, in many reaction mediums, polymer backbone can occur swelling, if and it fills in tubulation, owing to managing interior limited space, Severe blockage in pipe can be caused, pressure drop is suddenly risen, and even can cause tube wall deformation, there is potential safety hazard; If it fills in outside pipe, heat transferring medium is walked in pipe, and heat transfer coefficient is low, moves heat not in time, product performance and catalyst activity all effected, and therefore this reaction type is not suitable for adopting shell and tube reactor.
Some gas-liquid-solids are reacted, gas-liquid charging respectively, mix after charging, due to incorporation time and limited space, when causing entering beds, material is uneven, and according to shell and tube reactor, uneven material is subdivided into thousands of junior units immediately, response situation in every root pipe is all different, has a strong impact on properties of product.
In calandria type fixed bed reactor, because the heat transfer coefficient of tubulation is not high, need more heat exchange area, and due to limiting factors such as tube pitches, reactor volume is larger; Catalyst packing is in tubulation, and in a usual reactor, tubulation quantity has thousands of, and catalyst loading and unloading workload is large, and leak detection maintenance waits comparatively complicated; When improving single device output, shell and tube reactor often faces that pressure drop is large, hot(test)-spot temperature is high and the problem such as volume is excessive.
Summary of the invention
Object of the present invention is exactly providing that a kind of volume is little to overcome defect that above-mentioned prior art exists, catalyst loading and unloading convenience, flexible structure, can carry out the New-type plate axial flow reactor of multistage reaction.
Object of the present invention can be achieved through the following technical solutions:
A kind of New-type plate axial flow reactor, comprise shell of reactor, heat exchanger plates halved tie, heat transferring medium distribution header, heat transferring medium dispensing branch, heat transferring medium collects house steward and heat transferring medium collects arm, described shell of reactor is provided with reacting material inlet, reacting material outlet, heat transferring medium import and heat transferring medium outlet, it is characterized in that, described heat exchanger plates halved tie forms by organizing sub-heat exchanger plates halved tie more, often organize sub-heat exchanger plates halved tie one end and be connected heat transferring medium import by heat transferring medium dispensing branch with corresponding heat transferring medium distribution header, the other end is collected arm by heat transferring medium and is connected heat transferring medium outlet with corresponding heat transferring medium collection house steward.
Heat exchanger plates halved tie is divided into bisection structure, quartering structure, many repetitional structure or concentric structure by described many groups sub-heat exchanger plates halved ties in the horizontal direction.
Described bisection structure is two groups of sub-heat exchanger plates halved ties in the semicolumn bodily form, and one group of sub-heat exchanger plates organizes sub-heat exchanger plates to intrafascicular heat exchanger plates to parallel to intrafascicular heat exchanger plates pair with another;
Described quartering structure is that four groups of sub-heat exchanger plates halved ties in segment are arranged around reactor center axle, the sub-heat exchanger plates of different group to intrafascicular heat exchanger plates to be parallel to each other or vertically;
Described many repetitional structure are that the sub-heat exchanger plates halved tie in segment of more than five groups is arranged around reactor center axle;
Described concentric structure is that the sub-heat exchanger plates halved tie of many groups is formed with concentric circles arrangement, and heat transferring medium distribution header and the heat transferring medium of the corresponding varying number of sub-heat exchanger plates halved tie of different group collect house steward.
In described bisection structure, quartering structure and many repetitional structure, it is circular arc that heat transferring medium distribution header and heat transferring medium collect house steward; In described concentric structure, heat transferring medium distribution header and heat transferring medium collect house steward's linearly section shape, along reactor radial distribution.
Described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, for the circulation passage of heat transferring medium, heat exchanger plates is to arranging many places welding between upper two plates, welding manner is one or both in the welding of a some shape or bar shaped welding, welding position is crisscross arranged, and makes plate effects on surface form concaveconvex shape; Each heat exchanger plates is connected to heat transferring medium distribution header to bottom port by heat transferring medium dispensing branch, and top port is collected arm by heat transferring medium and is connected to heat transferring medium collection house steward.Heat exchanger plates is opened to hundreds of generally there being tens, and conversion zone is divided into tens or hundreds of part, and after reaction mass enters beds, after the strong flow-disturbing of catalyst, reaction mass can mix.
When reactor is higher or have multiply input and output material, described heat transferring medium import and heat transferring medium outlet are respectively equipped with at least one, and concrete quantity can be arranged according to reaction needed.
Described heat exchanger plates halved tie axially can be divided into multistage at reactor, the heat exchanger plates of each section of heat exchanger plates halved tie is separate and adjustable to quantity, spacing and shape, required heat exchange area can be adjusted according to the difference of differing heights region exothermic heat of reaction amount in reactor, and this multi-segment structure can improve separate unit treating capacity, remove heat of reaction in time, prevent accumulation of heat; Different section can load different catalysts, realizes multiple reaction series connection in separate unit reactor.
What arrange in material inlet, material outlet, quench gas import, circulating air import, manhole and gas distributor between described multistage heat exchanger plates halved tie is one or more, realizes multiple reaction series connection to coordinate.
Described each heat exchanger plates is internally plate journey, adjacent heat exchanger plates between be shell side, shell side loading catalyst, heat transferring medium limp journey, shell side walked by reaction mass.
Described reactor also comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet and product gas outlet.
Described heat exchanger plates halved tie lifts into reactor shell from upper cover, is fixed by supports support, and reactor can Assembling; Catalyst directly loads one by one from reactor upper cover or manhole between heat exchanger plates pair, draws off from low head discharge port; Heat transferring medium can be gas, water, conduction oil or fused salt.
Described heat exchanger plates arranges support member to bottom, and top is provided with and controls each heat exchanger plates to the heat exchanger plates distance pieces of spacing, and plate is 10 ~ 200mm to spacing, and preferred plate is 20 ~ 80mm to spacing.
Preferably, when reactor diameter is less than or equal to 2m, heat exchanger plates halved tie is bisection structure; When reactor diameter is between 2 ~ 4m, heat exchanger plates halved tie is quartering structure; By that analogy, when reacting diameter and continuing to increase, correspondingly, heat exchanger plates halved tie is many repetitional structure, manufactures to facilitate and installs heat exchanger plates pair.
Compared with prior art, the present invention has the following advantages:
(1) volume is little, is beneficial to equipment enlarging:
Owing to not having the requirements such as similar tube pitch, the Catalyst packing rate of this novel reactor is between 60% ~ 90%., plate identical at same loaded catalyst, height for reactor is when to spacing, catalyst thickness is identical at once mutually with caliber, ensure enough heat exchange areas, the diameter of this novel reactor is approximately about 60 ~ 80% of shell-and-tube reactor diameter, volume is about about 40 ~ 60% of shell-and-tube reactor, reactor volume reduces greatly, reactor has expansion space, can load more multi-catalyst, is conducive to improving separate unit reactor output and equipment enlarging.
(2) good effect of heat exchange:
Compared with the halved tie of original monolithic devices heat exchanger plates, in repetitional structure, often organize the corresponding heat transferring medium distribution header of sub-heat exchanger plates halved tie and a heat transferring medium collects house steward, heat exchanger plates is to can be parallel or vertical; In concentric structure, its heat exchanger plates away from reactor center axle is collected house steward's quantity to the heat transferring medium distribution header of upper connection and heat transferring medium and is collected house steward's quantity more than the heat exchanger plates near catalyst housing to the heat transferring medium distribution header of upper connection and heat transferring medium; Can avoid thus due to plate to width or circumferential lengths excessive, make the phenomenon of heat transferring medium maldistribution, therefore heat exchange evenly.Simultaneously, the staggered Type of Welding that heat exchanger plates is right and the rough surface peening disturbance of two side liquids, enhance heat exchange efficiency, reaction heat is removed in time, adjacent panels between temperature distribute gently, closer to isothermal reaction, be conducive to reducing the generation of side reaction, improve reaction selectivity and yield, the service life of extending catalyst.
(3) flexible structure, can multisection type reaction be carried out:
This New-type plate axial flow reactor, when it is divided into multistage at vertical direction, can the inner multiply input and output material of realization response device or cascade reaction.Being interconnected between every section of plate halved tie and separate, by arranging corresponding supplementary structure between different section, multiply input and output material can being realized; In the different section of reactor, different catalyst can be loaded, thus realize cascade reaction, save equipment and space; At the differing heights of reactor, reaction severe degree is different, can adjust the flow of heat transferring medium, heat exchange area and heat exchanger plates parameter etc. according to this.
(5) separate unit treating capacity is large:
This novel reactor can be divided into 2 deciles, 4 deciles or more deciles diametrically, and therefore reactor diameter does not limit by strip width, thus is adapted to the large reactor assembly of production capacity better.
This reactor can adopt axially multisection type, beds is divided into multistage, heat exchanger plates halved tie is also divided into multistage to inlay wherein, reacting material inlet and cooling medium import and export are provided with between every two-stage catalytic agent bed, therefore the treating capacity of separate unit reactor feedstocks increases, and heat of reaction is evenly distributed in each section, and cooled medium is removed in time, hot(test)-spot temperature is low, and reaction conversion ratio is high.
(6) Catalyst packing is easy:
Catalyst packing at this novel reactor shell side, plate pair and plate between, plate between without hindrance, be convenient to filling, between plate to be opened to hundreds of tens usually to quantity, far fewer than tubulation quantity, it is little to load workload.
(7) be easy to install, transport and maintenance:
As a whole, can directly lift into reactor, plate have tube sheet to both sides in heat exchanger plates halved tie, and reactor can Assembling, and reduce cost of transportation, plate is few to quantity; Because heat exchanger plates halved tie entirety can be divided into the sub-heat exchanger plates halved tie of many groups, when with sub-heat exchanger plates halved tie form transport, transportation clearance is little, is convenient to transport; The right quantity of heat exchanger plates is less relative to tubulation number in shell and tube reactor, and welding position is less, and inspection and maintenance work is simple.
Accompanying drawing explanation
Fig. 1 is a kind of New-type plate axial flow reactor of the present invention structural representation;
Fig. 2 is structure schematic top plan view that heat exchanger plates halved tie horizontal direction of the present invention halves;
Fig. 3 is that in heat exchanger plates halved tie horizontal direction of the present invention, quartering structure vertical arranges schematic top plan view;
Fig. 4 is that in heat exchanger plates halved tie horizontal direction of the present invention, quartering parallelism structural arranges schematic top plan view;
Fig. 5 is heat exchanger plates halved tie concentric structure schematic top plan view of the present invention;
Fig. 6, in New-type plate axial flow reactor of the present invention, vertical direction is divided into multi-segment structure schematic diagram;
Reference numeral: 1 is reacting material inlet, 2 is heat transferring medium outlet, and 3 is heat transferring medium collection house steward, 4 is heat transferring medium collection arm, and 5 is shell of reactor, and 6 is heat exchanger plates halved tie, 7 is catalyst discharge port, and 8 is reacting material outlet, and 9 is heat transferring medium import, 10 is heat transferring medium distribution header, and 11 is heat transferring medium dispensing branch, and 12 is distance pieces, 13 is support member, 14 is recycle stock entrance, and 15 is cold shock material inlet, and 16 is gas-liquid distributor or collector.
Detailed description of the invention
Below in conjunction with the drawings and specific embodiments, the present invention is described in detail.The present embodiment is implemented premised on technical solution of the present invention, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following embodiment.
Embodiment 1
As shown in Figure 1, a kind of New-type plate axial flow reactor, comprise shell of reactor 5, heat exchanger plates halved tie 6, heat transferring medium distribution header 10, heat transferring medium dispensing branch 11, heat transferring medium collects house steward 3 and heat transferring medium collects arm 4, described shell of reactor 5 is provided with reacting material inlet 1, reacting material outlet 8, heat transferring medium import 9 and heat transferring medium outlet 2, described heat exchanger plates halved tie 6 forms by organizing sub-heat exchanger plates halved tie more, often organize sub-heat exchanger plates halved tie one end by the heat transferring medium entrance of heat transferring medium dispensing branch 11 with corresponding heat transferring medium distribution header 10 coupled reaction device shell 5, the other end collects the heat transferring medium outlet 2 of arm 4 and corresponding heat transferring medium collection house steward 3 coupled reaction device shell 5 by heat transferring medium, described heat exchanger plates halved tie 6 entirety is in cylindrical shape.
As shown in Figure 2, in the present embodiment, heat exchanger plates halved tie 6 is divided into bisection structure by many groups of sub-heat exchanger plates halved ties in the horizontal direction, described bisection structure is two groups of sub-heat exchanger plates halved ties in the semicolumn bodily form, one group of sub-heat exchanger plates organizes sub-heat exchanger plates to intrafascicular heat exchanger plates to parallel to intrafascicular heat exchanger plates pair with another, and heat transferring medium distribution header 10 and heat transferring medium collect house steward 3 in circular arc; Because sub-heat exchanger plates halved tie connects respective heat transferring medium distribution header 10 and heat transferring medium collection house steward 3 respectively, thus reduce heat exchanger plates centering heat transferring medium flowing stroke in the horizontal direction, make horizontal direction heat exchange even.
Described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, for the circulation passage of heat transferring medium, each heat exchanger plates is connected to heat transferring medium distribution header 10 to bottom port by heat transferring medium dispensing branch 11, and top port is collected arm 4 by heat transferring medium and is connected to heat transferring medium collection house steward 3.
Described each heat exchanger plates is internally plate journey, adjacent heat exchanger plates between be shell side, shell side loading catalyst, heat transferring medium limp journey, shell side walked by reaction mass.
Described reactor also comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet and product gas outlet.
As shown in Figure 2, described heat exchanger plates arranges support member 13 to bottom, and this support member 13 is a strip draw-in groove; Heat exchanger plates is provided with top and controls each heat exchanger plates to the heat exchanger plates distance pieces 12 of spacing, by adjustment heat exchanger plates to the clamped position of bottom on support member 13 and top distance pieces 12, regulates the spacing that heat exchanger plates is right.
Described heat exchanger plates halved tie 6 lifts into reactor shell from upper cover, supports fixing by support member 13, and reactor can Assembling; Catalyst directly loads one by one from reactor upper cover or manhole between heat exchanger plates pair, draws off from low head discharge port; Heat transferring medium can be gas, water, conduction oil or fused salt.
This enforcement reactor is not owing to having the requirements such as similar tube pitch, and Catalyst packing rate is between 60% ~ 90%., plate identical at same loaded catalyst, height for reactor is when to spacing, catalyst thickness is identical at once mutually with caliber, enough heat exchange areas can be ensured, and reactor diameter is about 60 ~ 80% of shell-and-tube reactor diameter, volume is about 40 ~ 60% of shell-and-tube reactor, reactor volume reduces greatly, reactor has expansion space, can load more multi-catalyst, is conducive to improving separate unit reactor output and equipment enlarging.
As a whole, can directly lift into reactor, plate have tube sheet to both sides to plate-type heat-exchange assembly, and reactor can Assembling, and reduce cost of transportation, plate is few to quantity; When heat exchanger plates halved tie by organize more sub-heat exchanger plates halved tie form time, it is more easily installed, and inspection and maintenance work is simple.
Embodiment 2
As shown in Figure 3, in the present embodiment, heat exchanger plates halved tie 6 is divided into quartering structure by many groups of sub-heat exchanger plates halved ties in the horizontal direction, this quartering structure is that four groups of sub-heat exchanger plates halved ties in segment are arranged around reactor center axle, each sub-heat exchanger plates is to intrafascicular heat exchanger plates to being parallel to each other, and heat transferring medium distribution header 10 and heat transferring medium collect house steward 3 equally in circular arc.In the present embodiment, the heat transferring medium of heat transferring medium import 9 and correspondence exports 2 quantity and can be between 1 ~ 4, needs to arrange according to heat transferring medium flow.
All the other are identical with embodiment 1.
The present embodiment reactor is used for hydration reaction, there is catalyst not easily broken, catalyst activity is high, advantage that the life-span is long.The catalyst of hydration reaction is generally resin type catalyst, and the phenomenons such as the swelling and heat expansion of chemistry can occur.In common shell and tube reactor, Catalyst packing is in pipe, for swellable catalyst narrow space (caliber 20 ~ 40mm), under lower expansion rate (2 ~ 7%), catalyst will be squeezed broken, cause tubulation inner catalyst resistance drop suddenly to increase and catalyst activity reduction, cannot run well.And in this New-type plate reactor, Catalyst packing is between plate pair, space between plate pair is a larger similar rectangular parallelepiped space (200 ~ 4000mm*20 ~ 60mm*H), and the swelling space of 10% ~ 30% can be reserved, therefore the expansion space of catalyst is more abundant, catalyst is not easily broken, and service life can reach more than 8000 hours.
Embodiment 3
As shown in Figure 4, in the present embodiment, heat exchanger plates halved tie 6 is divided into quartering structure by many groups of sub-heat exchanger plates halved ties in the horizontal direction, this quartering structure is that four groups of sub-heat exchanger plates halved ties in segment are arranged around reactor center axle, as different from Example 2, each sub-heat exchanger plates to intrafascicular, adjacent sub-heat exchanger plates to intrafascicular heat exchanger plates to mutually vertical.
All the other are identical with embodiment 2.
When reactor diameter is between 2 ~ 4m, preferably use the quartering structure of embodiment 2 or embodiment 3, to reduce the right manufacturing cost of heat exchanger plates, convenient installation; When reacting diameter and continuing to increase, consider equally, correspondingly, can use many repetitional structure from manufacture and setting angle, described many repetitional structure are that the sub-heat exchanger plates halved tie in segment of more than five groups is arranged around reactor center axle.
Embodiment 4
As shown in Figure 5, in the present embodiment, heat exchanger plates halved tie 6 is divided into concentric structure by many groups of sub-heat exchanger plates halved ties in the horizontal direction, described concentric structure is that the sub-heat exchanger plates halved tie of many groups is formed with concentric circles arrangement, heat transferring medium distribution header 10 and heat transferring medium collect house steward 3 linearly section shape, along reactor radial distribution, heat exchanger plates near reactor center axle is collected house steward 3 quantity to the heat transferring medium distribution header 10 of upper connection and heat transferring medium and is less than the heat exchanger plates of close catalyst housing to the heat transferring medium distribution header 10 of upper connection and heat transferring medium collection house steward 3 quantity.Similar with repetitional structure, this structure connects respective heat transferring medium distribution header 10 due to sub-heat exchanger plates halved tie and heat transferring medium collects house steward 3, and heat exchanger plates is larger to girth, it is more that the heat transferring medium distribution header 10 that sub-heat exchanger plates halved tie connects and heat transferring medium collect house steward 3 quantity, meet the heat transferring medium flow requirement in all regions of reaction compartment thus, to make heat exchange even.In the present embodiment concentric structure, heat transferring medium import 9 and heat transferring medium export 2 quantity and heat exchanger plates to spacing with reactor diameter and concrete exothermic heat of reaction speed and Flux modulation.
All the other are identical with embodiment 1.
Embodiment 5
As shown in Figure 6, described heat exchanger plates halved tie 6 is axially divided into multistage at reactor, the heat exchanger plates of each section of heat exchanger plates halved tie 6 is separate and adjustable to quantity, spacing and shape, specifically adjusts required heat exchange area according to the difference of differing heights region exothermic heat of reaction amount in reactor; Different section can load different catalysts, realizes multiple reaction series connection in separate unit reactor.Beds is divided into multistage, heat exchanger plates halved tie is also divided into multistage to inlay wherein, reacting material inlet and cooling medium import and export are provided with between every two-stage catalytic agent bed, therefore the treating capacity of separate unit reactor feedstocks increases, heat of reaction is evenly distributed in each section, and cooled medium is removed in time, hot(test)-spot temperature is low, and reaction conversion ratio is high.
In the present embodiment, what arrange in material inlet, material outlet, cold shock material inlet 15, recycle stock entrance 14, manhole, gas distributor or collector 16 between multistage heat exchanger plates halved tie 6 is one or more, realizes multiple reaction series connection to coordinate.All the other are identical with embodiment 1.
The present embodiment reactor is used for dimethyl ether C4, C5 olefine reaction, 5 sections can be divided into, every section of catalyst bed floor height 1.5m ~ 2.5m, reactor upper end is provided with hot dimethyl ether import, lower end is provided with reacting product outlet, be provided with cold dimethyl ether entrance and circulating air entrance between section and section, fully mixed with material before by gas distributor, then enter lower end bed continuation reaction.Every section of bed is all embedded with contour heat exchanger plates halved tie, and cooling medium circulation duct and import and export.The mode of moving heat in this reactor is divided into 3: saturation water heat absorption boiling process, the heat absorption of cold dimethyl ether become gaseous dimethyl process and circulating air endothermic process.Cold dimethyl ether both raw materials as a supplement, again as direct cooling medium, realize the reaction of multistage feeding multistage, can produce 30000 tons of C4, C5 alkene per year.
Embodiment 6
Embodiment 5 reactor is applied to and realizes indirect one-step method coal derived DME, reactor is divided into two sections, the catalyst of epimere filling synthesising gas systeming carbinol, the catalyst of hypomere filling preparing dimethyl ether from methanol, every section all arranges heat exchanger plates to the temperature of area, shape, heat transferring medium and flow etc. according to thermal discharge and reaction temperature.These two reactions are arranged in same reactor the cost of material and energy consumption that effectively can reduce dimethyl ether production.
Claims (10)
1. a New-type plate axial flow reactor, comprise shell of reactor (5), heat exchanger plates halved tie (6), heat transferring medium distribution header (10), heat transferring medium dispensing branch (11), heat transferring medium collects house steward (3) and heat transferring medium collects arm (4), described shell of reactor (5) is provided with reacting material inlet (1), reacting material outlet (8), heat transferring medium import (9) and heat transferring medium outlet (2), it is characterized in that, described heat exchanger plates halved tie (6) forms by organizing sub-heat exchanger plates halved tie more, often organize sub-heat exchanger plates halved tie one end and be connected heat transferring medium import (9) by heat transferring medium dispensing branch (11) with corresponding heat transferring medium distribution header (10), the other end is collected arm (4) by heat transferring medium and is connected heat transferring medium outlet (2) with corresponding heat transferring medium collection house steward (3).
2. a kind of New-type plate axial flow reactor according to claim 1, it is characterized in that, heat exchanger plates halved tie (6) is divided into bisection structure, quartering structure, many repetitional structure or concentric structure by described many groups sub-heat exchanger plates halved ties in the horizontal direction.
3. a kind of New-type plate axial flow reactor according to claim 2, it is characterized in that, described bisection structure is two groups of sub-heat exchanger plates halved ties in the semicolumn bodily form, and one group of sub-heat exchanger plates organizes sub-heat exchanger plates to intrafascicular heat exchanger plates to parallel to intrafascicular heat exchanger plates pair with another;
Described quartering structure is that four groups of sub-heat exchanger plates halved ties in segment are arranged around reactor center axle, the sub-heat exchanger plates of different group to intrafascicular heat exchanger plates to be parallel to each other or vertically;
Described many repetitional structure are that the sub-heat exchanger plates halved tie in segment of more than five groups is arranged around reactor center axle;
Described concentric structure is that the sub-heat exchanger plates halved tie of many groups is formed with concentric circles arrangement, and heat transferring medium distribution header (10) and the heat transferring medium of the corresponding varying number of sub-heat exchanger plates halved tie of different group collect house steward (3).
4. a kind of New-type plate axial flow reactor according to Claims 2 or 3, it is characterized in that, in described bisection structure, quartering structure and many repetitional structure, heat transferring medium distribution header (10) and heat transferring medium collect house steward (3) in circular arc; In described concentric structure, heat transferring medium distribution header (10) and heat transferring medium collect house steward (3) linearly section shape, along reactor radial distribution.
5. a kind of New-type plate axial flow reactor according to claim 3, it is characterized in that, described heat exchanger plates forms an airtight plate journey cavity to by two metal sheets by welding, only respectively stay a port at two ends, heat exchanger plates is to arranging many places welding between upper two plates, welding manner is one or both in the welding of a some shape or bar shaped welding, and welding position is crisscross arranged, and makes plate effects on surface form concaveconvex shape; Each heat exchanger plates is connected to heat transferring medium distribution header (10) to bottom port by heat transferring medium dispensing branch (11), and top port is collected arm (4) by heat transferring medium and is connected to heat transferring medium collection house steward (3).
6. a kind of New-type plate axial flow reactor according to claim 3, it is characterized in that, described heat exchanger plates is in concentric structure, and the heat exchanger plates near reactor center axle is collected house steward (3) quantity to the heat transferring medium distribution header (10) of upper connection and heat transferring medium and is less than the heat exchanger plates of close catalyst housing to the heat transferring medium distribution header (10) of upper connection and heat transferring medium collection house steward (3) quantity.
7. a kind of New-type plate axial flow reactor according to claim 1, is characterized in that, described heat transferring medium import (9) and heat transferring medium outlet (2) are respectively equipped with at least one.
8. according to the arbitrary described a kind of New-type plate axial flow reactor of claim 1 ~ 7, it is characterized in that, described heat exchanger plates halved tie (6) axially can be divided into multistage at reactor, the heat exchanger plates of each section of heat exchanger plates halved tie (6) is separate and adjustable to quantity, spacing and shape, in order to load different catalysts, realize multiple reaction series connection in separate unit reactor.
9. a kind of New-type plate axial flow reactor according to claim 8, it is characterized in that, what arrange in material inlet, material outlet, quench gas import, circulating air import, manhole and gas distributor between described multistage heat exchanger plates halved tie (6) is one or more, realizes multiple reaction series connection to coordinate.
10. a kind of New-type plate axial flow reactor according to claim 1, is characterized in that, described each heat exchanger plates is internally plate journey, adjacent heat exchanger plates between be shell side, shell side loading catalyst, heat transferring medium limp journey, shell side walked by reaction mass; Described reactor also comprises cylindrical shell, upper cover, manhole, low head, reacting gas inlet and product gas outlet; Described heat exchanger plates halved tie (6) lifts into reactor shell from upper cover, is fixed by supports support, and reactor can Assembling; Catalyst directly loads one by one from reactor upper cover or manhole between heat exchanger plates pair, draws off from low head discharge port; Heat transferring medium can be gas, water, conduction oil or fused salt.
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| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN108176335A (en) * | 2018-03-07 | 2018-06-19 | 厦门大学 | Tandem microreactor with hole-groove combined microchannel porous metals reaction carriers |
| WO2018205943A1 (en) * | 2017-05-09 | 2018-11-15 | 德艾柯工程技术（上海）有限公司 | Modularized temperature control reactor |
| CN109759000A (en) * | 2019-01-18 | 2019-05-17 | 山东诺为制药流体系统有限公司 | A kind of multithreading baffling bobbin carriage and reactor |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
| CN117466839A (en) * | 2023-10-07 | 2024-01-30 | 中建安装集团有限公司 | Process for preparing propylene oxide by directly oxidizing propylene with hydrogen peroxide by using flat-plate membrane reactor |
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| CN109759000B (en) * | 2019-01-18 | 2024-04-12 | 山东诺为制药流体系统有限公司 | Multithread baffle box and reactor |
| CN112044363A (en) * | 2020-08-31 | 2020-12-08 | 江苏永大化工机械有限公司 | Coupling reactor for producing ethylene glycol from coal |
| CN117466839A (en) * | 2023-10-07 | 2024-01-30 | 中建安装集团有限公司 | Process for preparing propylene oxide by directly oxidizing propylene with hydrogen peroxide by using flat-plate membrane reactor |
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