CN105107434A - Novel reactor for preparing epoxy propane by oxidizing propylene with hydrogen peroxide - Google Patents
Novel reactor for preparing epoxy propane by oxidizing propylene with hydrogen peroxide Download PDFInfo
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- CN105107434A CN105107434A CN201510556469.8A CN201510556469A CN105107434A CN 105107434 A CN105107434 A CN 105107434A CN 201510556469 A CN201510556469 A CN 201510556469A CN 105107434 A CN105107434 A CN 105107434A
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
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- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
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Abstract
The invention relates to a novel reactor for preparing epoxy propane by oxidizing propylene with hydrogen peroxide. The novel reactor comprises a reactor shell (5), a heat transfer plate pair bundle (6), a heat transfer medium distribution main pipe (10), a heat transfer medium distribution branch pipe (11), a heat transfer medium collecting main pipe (3) and a heat transfer medium collecting branch pipe (4), wherein the reactor shell (5) is provided with a reaction material inlet (1), a reaction material outlet (8), a heat transfer medium inlet (9) and a heat transfer medium outlet (2), the heat transfer plate pair bundle (6) consists of multiple sets of sub-heat transfer plate pair bundles, one end of each set of sub-heat transfer plate pair bundle is connected with the heat transfer medium inlet (9) through the heat transfer medium distribution branch pipe (11) and the corresponding heat transfer medium distribution main pipe (10), and the other end of each set of sub-heat transfer plate pair bundle is connected with the heat transfer medium outlet (2) through the heat transfer medium collecting branch pipe (4) and the corresponding heat transfer medium collecting main pipe (3). Compared with the prior art, the novel reactor provided by the invention has the advantages of small volume, convenience in catalyst loading, high heat transfer efficiency and flexibility in structure.
Description
Technical field
The present invention relates to a kind of axial flow reactor, especially relate to a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane.
Background technology
Expoxy propane is the important source material of producing polyethers, propane diols, isopropanolamine, propenyl, non-polyether polyalcohol etc., and the production method of current expoxy propane mainly contains chlorohydrination, indirect oxidation method (conjugated oxidation), cumene method and hydrogen peroxide oxidation propylene propylene oxide method.Chlorohydrination major defect uses poisonous chlorine, the serious also contaminated environment of equipment corrosion; Indirect oxidation method is high to feed quality requirements, and technique is tediously long, and scale of investment is large; Cumene method essence is still a kind of conjugated oxidation.Hydrogen peroxide oxidation propylene expoxy propane rule is that a kind of flow process is simple, accessory substance is few and the new technology of the direct oxidation method of green non-pollution production expoxy propane, and this technique in methanol solvate, produces expoxy propane with hydrogen peroxide catalyzed epoxidation of propylene under middle temperature, low pressure and liquid-phase condition.
What the novel reactor of this hydrogen peroxide legal system expoxy propane was conventional at present is shell and tube reactor, and Catalyst packing is in pipe, and cooling water walks reactor shell side.Because exothermic heat of reaction is many, the heat transfer coefficient of tubulation is not high, needs 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.
The charging of hydrogen peroxide legal system propylene oxide reaction device has the gentle liquid phase feeding of liquid phase two kinds of situations, namely has feed pre-mixer close and close two kinds of feeding manners without feed pre-mixer.Especially for liquid phase charging respectively, feed pre-mixer is not had to close, owing to entering incorporation time and limited space after reactor, when causing entering beds, material is uneven, according to shell and tube reactor, uneven material is subdivided into thousands of junior units immediately, and the response situation in every root pipe is all different, has a strong impact on properties of product.
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 novel reactor for hydrogen peroxide oxidation propylene expoxy propane that many reactions connect.
Object of the present invention can be achieved through the following technical solutions:
A kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane, 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, at least one heat transferring medium import and the outlet of at least one heat transferring medium, 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 by the heat transferring medium import of heat transferring medium dispensing branch with corresponding heat transferring medium distribution header coupled reaction device shell, the other end collects the heat transferring medium outlet of arm and corresponding heat transferring medium collection house steward coupled reaction device shell by heat transferring medium, described heat exchanger plates halved tie axially at least comprises one section at reactor, and the heat exchanger plates of each section of heat exchanger plates halved tie is separate and adjustable to quantity, spacing and shape.Due to sub-heat exchanger plates halved tie corresponding respective heat transferring medium distribution header and heat transferring medium collection house steward 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 halved tie entirety is in cylindrical shape, 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, sub-heat exchanger plates to intrafascicular heat exchanger plates to being formed by multi-point welding by two pieces of metallic plates.
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.
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.
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, solder joint density range is 100 ~ 5000 Ge/㎡, 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 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, conversion zone is divided into tens or hundreds of part, and the quantity (thousands of) of pipe in shell and tube reactor, after reaction mass enters beds, after the strong flow-disturbing of catalyst, reaction mass can mix.
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 ~ 60mm to spacing.
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, material inlet and product exit.
Described catalyst in reactor bed can be one section or multistage.When beds is one section, reactor only has a reacting material inlet, and a reacting product outlet and one group of cooling medium are imported and exported.When beds is multistage, reactor has multiple material inlet, and a product exit and many group cooling mediums are imported and exported
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 and water, is preferably water.
Preferably, when reactor diameter is less than or equal to 2m, heat exchanger plates halved tie is preferably halved structure, and the orientation of the plate halved tie of 2 deciles is parallel, have 2 heat transferring medium distribution headers and 2 heat transferring mediums collection house stewards, 1 or 2 heat transferring mediums import and export can be set as required respectively; And when reactor diameter is between 2 ~ 4m, the preferred quartering structure of heat exchanger plates halved tie, the orientation of the plate halved tie of 4 deciles can be parallel, also can be vertical, have 4 heat transferring medium distribution headers and 4 heat transferring mediums collection house stewards, 1 or 2 heat transferring mediums import and export can be set as required respectively; By that analogy, when reacting diameter and continuing to increase, consider from manufacture and setting angle, correspondingly, the preferred many repetitional structure of heat exchanger plates halved tie.
The present invention is used in the novel reactor of hydrogen peroxide expoxy propane, Catalyst packing heat exchanger plates pair and heat exchanger plates between, i.e. reactor shell side, be the space of reaction mass and catalyst, reaction mass vertically laminar flow passes through beds; It is plate journey that heat transferring medium is entered in heat exchanger plates by distribution header and dispensing branch, discharges reactor after being gathered by collection arm and house steward.
Heat exchanger plates of the present invention is staggered to upper some welding, and make the violent disturbance of cooling medium internal fluid, medium fluid is in turbulence state always, is forced-convection heat transfer.Reaction side material, near heat exchange element wall place, often forms liquid film, and the thermal resistance that this liquid film produces accounting in the entire thermal resistance of reaction side is heavy very large.And at this new type of plate effects on surface, because its shape is uneven, the positive perturbation action to liquid film forming, is made liquid film renewal speed accelerate, thus reduce its thermal resistance, improve the heat transfer coefficient of reaction side entirety.
Because the Suitable ranges of hydrogen peroxide oxidation propylene legal system expoxy propane is 30 ~ 60 degree, general cooling water is as cooling medium, temperature range is 30 ~ 40 degree, temperature difference is little, and this exothermic heat of reaction is violent, is about 200 ~ 250KJ/mol, the volume flow of required cooling water is nearly about 8 ~ 14 times of reaction mass volume flow, and when increasing material treating capacity, cold side is difficult to heat to be removed in time, causes the treating capacity of separate unit reactor limited.When therefore adopting multistage bed layered type reactor, just repeatedly charging can be set, to in each section of beds, all be provided with heat exchanger plates halved tie, be provided with heat transferring medium between every section of bed to import and export, the heat that every section of reaction produces is removed by every section of cooling medium just, and therefore sectional feeding form can increase the treating capacity of separate unit reactor, there will not be again heat to accumulate in a large number, the too high phenomenon of focus.
Because this novel reactor does not have the structures such as tube sheet, but adopting house steward and manifold configuration, its arrangement form is flexible, and can not hinder the handling of catalyst, reactor can be divided into arbitrarily several module in the horizontal direction, and its physical dimension is by decisions such as material distribution, manufacture and installations.
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, plate is comparatively flexible to the adjustment of spacing, and the Catalyst packing rate of this novel reactor is between 60% ~ 90% usually., 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) heat exchange efficiency is high:
Compared with the halved tie of original monolithic devices heat exchanger plates, many groups of sub-heat exchanger plates of repetitional structure are to intrafascicular, often organize the corresponding heat transferring medium distribution header of sub-heat exchanger plates halved tie and a heat transferring medium collection house steward, heat exchanger plates is to can be parallel or vertical, can avoid thus because plate is excessive to width, make the phenomenon of heat transferring medium maldistribution, therefore heat-obtaining evenly; 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 the generation reducing side reaction, improve reaction selectivity and yield, in the service life of extending catalyst, be applicable to the hydrogen peroxide legal system propylene oxide reaction that heat release is violent.
(3) structure of reactor is conducive to the mixing of inlet feed:
When inlet gas liquid phase material does not have premixed, due to Reactor inlet limited space, so before entering reactor bed, liquid phase can not mix completely, if it is divided into thousands of part immediately, every a material is inevitable inconsistent, the performance of all even product of impact reaction; And heat exchanger plates is opened to hundreds of generally there being tens in reactor of the present invention, 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.
(4) 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.
(5) 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, plate is to quantity usually tens or hundreds of, and far fewer than tubulation quantity, filling workload is little.
(6) be easy to install, transport and maintenance:
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, reduces cost of transportation; 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 tubulation thing reactor, and welding position is less, and inspection and maintenance work is simple.
Accompanying drawing explanation
Fig. 1 is a kind of novel reactor structural representation for hydrogen peroxide oxidation propylene expoxy propane of the present invention;
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 that the present invention, in the novel reactor of hydrogen peroxide oxidation propylene expoxy propane, 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, 11 is heat transferring medium dispensing branch, and 12 is distance pieces, and 13 is support member, 14 is fresh material entrance, and 15 is feed distributor.
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 novel reactor for hydrogen peroxide oxidation propylene expoxy propane, 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, the outlet of at least one heat transferring medium import at least one and heat transferring medium, 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, reaction compartment is split by described many groups sub-heat exchanger plates halved ties in the horizontal direction, described heat exchanger plates halved tie axially at least comprises one section at reactor, and the heat exchanger plates of each section of heat exchanger plates halved tie is separate and adjustable to quantity, spacing and shape.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, 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 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.
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 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, material inlet and product exit.
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 and water.
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.
The present embodiment reactor is used for hydrogen peroxide legal system propylene oxide unit, according to the difference of loading catalyst type, when separate unit reactor charge amount is in 100m3 catalyst left and right, thermal discharge is 16 ~ 24MW, inlet temperature controls at 25 ~ 33 DEG C, outlet temperature is no more than 60 DEG C, use cooling water cool, heat exchanger plates to spacing at 10 ~ 60mm, the conversion ratio of hydrogen peroxide is about 100%, hot(test)-spot temperature is about 55 DEG C-60 DEG C, meets technological requirement, and remarkable benefit.
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.Heat exchanger plates is 10 ~ 60mm to spacing.All the other are identical with embodiment 1.
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.Heat exchanger plates is 10 ~ 60mm to spacing.All the other are identical with embodiment 2.
When reactor diameter is less than or equal to 2m, preferably use the bisection structure of embodiment 1; 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.
Embodiment 4
As shown in Figure 5, beds is multistage, and reactor has multiple material inlet, and a product exit and many group cooling mediums are imported and exported.In the present embodiment, between each section of reactor, be provided with fresh material entrance 14 and feed distributor 15.In each section of beds, all be provided with heat exchanger plates halved tie 6, be provided with heat transferring medium between every section of bed to import and export, the heat of every section of reaction generation is removed by every section of cooling medium just, therefore sectional feeding form can increase the treating capacity of separate unit reactor, there will not be again heat to accumulate in a large number, the too high phenomenon of focus.
Claims (10)
1. the novel reactor for hydrogen peroxide oxidation propylene expoxy propane, 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), at least one heat transferring medium import (9) and at least one 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 the heat transferring medium import (9) of sub-heat exchanger plates halved tie one end by heat transferring medium dispensing branch (11) and corresponding heat transferring medium distribution header (10) coupled reaction device shell (5), the other end collects 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) axially at least comprises one section at reactor, and the heat exchanger plates of each section of heat exchanger plates halved tie (6) is separate and adjustable to quantity, spacing and shape.
2. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 1, it is characterized in that, heat exchanger plates halved tie (6) is divided into bisection structure, quartering structure or many repetitional structure by described many groups sub-heat exchanger plates halved ties in the horizontal direction, sub-heat exchanger plates to intrafascicular heat exchanger plates to being formed by multi-point welding by two pieces of metallic plates.
3. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane 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.
4. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 3, is characterized in that, described heat transferring medium distribution header (10) and heat transferring medium collect house steward (3) in circular arc.
5. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 1, 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, 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, solder joint density range is 100 ~ 5000 Ge/㎡, 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 novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 1, it is characterized in that, 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 ~ 60mm to spacing.
7. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane 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.
8. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 1, it is characterized in that, described reactor also comprises cylindrical shell, upper cover, manhole, low head, material inlet and product exit.
9. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 1, it is characterized in that, described catalyst in reactor bed can be one section or multistage, when beds is one section, reactor only has a reacting material inlet, and a reacting product outlet and one group of cooling medium are imported and exported, when beds is multistage, reactor has multiple material inlet, and a product exit and many group cooling mediums are imported and exported.
10. a kind of novel reactor for hydrogen peroxide oxidation propylene expoxy propane according to claim 6, it is characterized in that, 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 and water, is preferably water.
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| CN201510556469.8A CN105107434A (en) | 2015-09-02 | 2015-09-02 | Novel reactor for preparing epoxy propane by oxidizing propylene with hydrogen peroxide |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN107243298A (en) * | 2017-07-26 | 2017-10-13 | 德艾柯工程技术（上海）有限公司 | A kind of temperature control gas-solid horizontal reactor for having special distributor |
| CN109382045A (en) * | 2018-04-03 | 2019-02-26 | 青岛科大隆腾科技发展有限公司 | A kind of spiral plate fixed bed reactors of gas-solid contact catalysis reaction |
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| US20010006102A1 (en) * | 1999-12-28 | 2001-07-05 | Takeshi Nishimura | Shell and tube type heat exchanger |
| CN104801240A (en) * | 2015-03-24 | 2015-07-29 | 德艾柯工程技术（上海）有限公司 | Plate type heat exchange reactor |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| US20010006102A1 (en) * | 1999-12-28 | 2001-07-05 | Takeshi Nishimura | Shell and tube type heat exchanger |
| CN104801240A (en) * | 2015-03-24 | 2015-07-29 | 德艾柯工程技术（上海）有限公司 | Plate type heat exchange reactor |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105879790A (en) * | 2016-06-06 | 2016-08-24 | 江苏怡达化学股份有限公司 | Novel HPPO reactor |
| CN107243298A (en) * | 2017-07-26 | 2017-10-13 | 德艾柯工程技术（上海）有限公司 | A kind of temperature control gas-solid horizontal reactor for having special distributor |
| CN109382045A (en) * | 2018-04-03 | 2019-02-26 | 青岛科大隆腾科技发展有限公司 | A kind of spiral plate fixed bed reactors of gas-solid contact catalysis reaction |
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Application publication date: 20151202 |