CN202893319U - Shell side structure and tubular vinyl acetate synthesis reactor comprising same - Google Patents
Shell side structure and tubular vinyl acetate synthesis reactor comprising same Download PDFInfo
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- CN202893319U CN202893319U CN 201220336835 CN201220336835U CN202893319U CN 202893319 U CN202893319 U CN 202893319U CN 201220336835 CN201220336835 CN 201220336835 CN 201220336835 U CN201220336835 U CN 201220336835U CN 202893319 U CN202893319 U CN 202893319U
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Abstract
The utility model relates to a novel shell side structure for a vinyl acetate synthesis reactor. The shell side structure is characterized in that the upper and lower ends of the shell side structure are respectively uniformly provided with an upper ring-shaped distributor with at least two discharge ports and a low ring-shaped distributor with at least two inlet ports along the circumferential direction, wherein at least two discharge ports in the at least two discharge ports are communicated with a fluid through a ring-shaped channel of the upper ring-shaped distributor and at least two inlets in the at least two inlets are communicated with the fluid through a ring-shaped channel in the low ring-shaped distributor. The utility model also relates to a tubular vinyl acetate synthesis reactor comprising the shell side structure. The shell side structure provided by the utility model is capable of realizing uniform flow and uniform heat radiation in a shell side when water-steam is used as a heat radiation medium and reducing the radial temperature difference of the reactor, so that the whole performance of the tubular vinyl acetate synthesis reactor is improved; the synthesizing reaction heat is reasonably applied; and the operating cost is reduced, and investment and operating cost of the equipment such as heat-conducting media circulating pumps are reduced.
Description
Technical field
The utility model relates generally to the vinyl acetate synthesis reactor.Particularly, the utility model relates to a kind of water-water vapour of can realizing as removing the even distribution of thermal medium and evenly removing heat and can reach the novel shell side structure that is used for the vinyl acetate synthesis reactor that reduces vinyl acetate synthesis reactor radial direction temperature difference purpose and the shell and tube vinyl acetate synthesis reactor that comprises this novel shell side structure.
Background technology
The ethylene method is a kind of process for the synthesis of vinyl acetate in industrial main employing.Owing to adopt the reaction heat effect of ethylene method production vinyl acetate larger, so calandria type fixed bed reactor is present comparatively ideal consersion unit.Because therefore the reaction temperature general control generally needs to utilize the thermal medium of removing that comes from the outside to remove reaction heat such as conduction oil, fused salt etc. at 160 ℃-220 ℃ in the technique that adopts ethylene method production vinyl acetate.
Remove the mobile shunting that can be divided into upper and lower circle distributor in of thermal medium in the fixed bed reactors shell side and flow with the interflow, and interbank flowing.Use conduction oil, fused salt to have following shortcoming as removing thermal medium: it is poor that (1) reactor is removed thermal effect, and the impurity content of thick vinyl acetate raises; (2) synthesising reacting heat of vinyl acetate only is used for warm-up cycle gas and is rationally utilized.In addition, for the vinyl acetate synthetic reaction process, the temperature difference that reduces the conduction oil import and export can reduce the generation of byproduct of reaction, but conduction oil is imported and exported the internal circulating load that the temperature difference reduces greatly to increase conduction oil, increases Heat-transfer Oil Pump equipment investment and operating cost.Therefore, should under the prerequisite that satisfies the reaction process requirement, reduce the internal circulating load of conduction oil or fused salt in the design as far as possible.But the minimizing of conduction oil or flow rate of molten salt will increase the outer heat transmission resistance of pipe, also may increase the weight of the inhomogeneities that reactor temperature distributes.
Removing thermal medium Uniform Flow in the fixed bed reactors shell side is the key factor of steadily carrying out that is conducive to the vinyl acetate synthetic reaction with evenly distributing.
Circle distributor is to realize removing thermal medium equally distributed critical component in the fixed bed reactors shell side.The circle distributor of prior art only comprises that generally removing thermal medium for one enters hole (inlet port) or one and remove thermal medium tap (outlet).For example, utility model patent CN201684582U(Granted publication day: on December 29th, 2010) disclosed a kind of reactor for vinyl acetate production, this reactor adopts conduction oil as removing thermal medium.In this utility model patent CN201684582U, as Fig. 2 and shown in Figure 4 and such as [0033] section in specification record ground, in the oil-feed cavity and be provided with dividing plate with two heat conductive oil inlet equidistant; In fuel-displaced cavity and be provided with dividing plate with two conduction oils outlet equidistant.This shows that in this vinyl acetate reactor, oil-feed cavity and fuel-displaced cavity that conduction oil carries out annularly flow therein are divided into two parts by dividing plate separately.In each part, only be provided with a heat conductive oil inlet or a conduction oil outlet.The shortcoming of this layout of prior art is: constantly shunting or interflow when removing thermal medium and flowing along sprue in circle distributor, remove thermal medium and be the mobile state of variable mass, so that the pressure in the circle distributor gradually changes along fluid flow direction, rely on fluid to run into problem here by the uniform method of pressure drop realization of distribution hole.Therefore, domestic and international many scholars have launched research to the pressure distribution of circle distributor endometamorphism amount stream, and purpose is by seeking the rule of inhomogeneous perforate, to realize the uniform of Variable Mass Flow.Yet pressure distribution may change along with the variation of operation operating mode, and inhomogeneous perforate may be not suitable with the variation of pressure.Therefore, for the variable mass of tackling in the circle distributor flows, the method for offering the tap hole that differs in the aperture is not a good method.
The utility model content
The purpose of this utility model is to provide a kind of shell side structure take water-water vapour as the vinyl acetate synthesis reactor of removing thermal medium, by this structure can realize coming from the outside remove thermal medium in the calandria type fixed bed reactor shell side with thermal siphon mode Uniform Flow, uniform in the radial direction of temperature, thus the overall performance of reactor improved.
The utility model utilizes water to remove reaction heat in the latent heat of vaporization of calandria type fixed bed reactor shell side.Relative conduction oil, the heat-conducting mediums such as fused salt, it is higher that water-water vapour is removed the thermal efficiency as heat-conducting medium, not only is conducive to improve the thermal effect of removing of reactor, reduces the reactor temperature difference radially; Can also the by-product water vapour, thus make the vinyl acetate synthesising reacting heat obtain more reasonably utilizing; Can move in the thermal siphon mode, thereby can cut operating costs, cut down investment and the operating cost of the equipment such as heat-conducting medium circulating pump.
It is to realize the equally distributed key point of temperature in the calandria type fixed bed reactor shell side of the present utility model that setting, stringing mode and the deflection plate set-up modes etc. of the circle distributor in the calandria type fixed bed reactor shell side affect water and steam mobile factor in shell side.
The utility model provides a kind of shell side structure of shell and tube vinyl acetate synthesis reactor, it is characterized in that, at the upper/lower terminal of described shell side structure the upper circle distributor with at least two outlets and the lower circle distributor with at least two inlet ports are set evenly along the circumferential direction respectively, at least two outlets in described at least two outlets by the circular passage fluid communication with each other in the described upper circle distributor and described at least two at least two inlet ports that enter the mouth by the circular passage fluid communication with each other in the described lower circle distributor.
According to an aspect of the present utility model, described shell and tube vinyl acetate synthesis reactor can make water-water vapour as removing thermal medium and moving in the thermal siphon mode, and the number of described inlet port is preferably 4-16, and the number of described outlet is preferably 4-12.
According to another aspect of the present utility model, the diameter of described inlet port can be in the scope of DN150-DN350, and the diameter of described outlet can be in the scope of DN100-DN300.
According to another aspect of the present utility model, the inboard of circle distributor along the circumferential direction is provided with 50-100 and evenly distributes distribution hole of the same size on described.Described distribution hole is rounded, bar shaped or square, and its hydraulic diameter scope is preferably 40mm-300mm.
According to another aspect of the present utility model, along the circumferential direction preferably be provided with 15-30 distribution hole equally distributed, of the same size in the inboard of described lower circle distributor.Described distribution hole is rounded, bar shaped or square, and its hydraulic diameter scope is preferably 30mm-100mm.
For circle distributor, only depend on the even distribution of inlet port, what the even collection of outlet can't guarantee to come from the outside fully removes thermal medium at the Uniform Flow of reactor shell side.Especially reaction tube quantity is a lot of when reactor diameter is larger, produces easily flow dead.These flow dead usually concentrate on the center and peripheral zone of reactor.In order to improve the flow velocity of removing thermal medium, strengthen the shell-side fluid turbulence and improve heat-transfer effect, need to add deflection plate at the shell side of reactor.Except above-mentioned effect, deflection plate also has the tube bank of support to strengthen its rigidity, prevents the effects such as tube vibration.Traditional arrangement of baffles mode often can not satisfy water-equally distributed requirement of water vapour two phase flow.
According to another aspect of the present utility model, along continuous straight runs arranges deflection plate between circle distributor and the described lower circle distributor on described, described deflection plate comprise at least nose-circle ring baffle plate, bottom annular deflection plate and/or be arranged on described nose-circle ring baffle plate and described bottom annular deflection plate between annular deflection plate and disc deflection plate, thereby form the buffering flow region of removing thermal medium between circle distributor and the described lower circle distributor on described.
According to another aspect of the present utility model, axially make progress along described reactor, the center resection rate of described annular deflection plate increases gradually.
According to another aspect of the present utility model, the center resection rate of described nose-circle ring baffle plate is 1.5-3 times of described bottom annular deflection plate.
According to another aspect of the present utility model, reaction tube is not arranged in the central area in described shell and tube vinyl acetate synthesis reactor shell side.
According to another aspect of the present utility model, the fringe region in described shell and tube vinyl acetate synthesis reactor shell side is not arranged reaction tube.
The utility model also provides a kind of shell and tube vinyl acetate synthesis reactor that comprises above-mentioned shell side structure.
Setting, stringing mode and the deflection plate set-up mode that above-mentioned three aspects are circle distributor is to realize removing thermal medium key with thermal siphon mode Uniform Flow in the calandria type fixed bed reactor shell side, and the even distribution that therefore wants temperature in the realization response device must reasonably design the structure of these three aspects.
Vinyl acetate synthesis reactor shell side structure described in the utility model comprises the upper circle distributor of removing thermal medium, lower circle distributor, the arrangement of stringing mode and deflection plate.Upper and lower circle distributor arranges respectively a plurality of outlets and a plurality of inlet port above the outside.The characteristics of stringing mode are that central area and fringe region arrange not stringing zone.Deflection plate adopts annular, disc-shaped structure, and characteristics are for axially to make progress along reactor, and the center resection rate of annular deflection plate increases gradually.In the utility model, the center resection rate of annular deflection plate is defined as the rate value of annular deflection plate internal diameter and external diameter.
By described in the utility model distributor is arranged a plurality of inlet ports, can realize well the pre-distribution of water in circle distributor, can utilize better the even perforate of distributor to realize the uniform of fluid thereby can also reduce the mobile degree of variable mass, design and the machine-building difficulty of avoiding inhomogeneous perforate to cause.In vinyl acetate reactor center zone and fringe region reaction tube is not set by described in the utility model, can reduces the flow resistance in these two zones, be conducive to promote that the two-phase flow of water and steam evenly distributes.The mode that adopts disc and donut internal diameter described in the utility model to enlarge can adapt to better water vapor and become the flow condition that fluid volume increases behind the water vapour.
Compare with the shell side structure of present prior art shell and tube vinyl acetate synthesis reactor, novel shell side structure of the present utility model has the following advantages: (1) utilizes the latent heat of vaporization of water to remove heat, has improved the thermal effect of removing of shell and tube vinyl acetate synthesis reactor; (2) utilize stream-liquid phase balance to guarantee that the easy control of temperature of reactor can reduce the reactor temperature difference radially, improve the selective and yield of the thick vinyl acetate of product; (3) byproduct steam is so that synthesising reacting heat obtains rational Application; (4) move in the thermal siphon mode, thereby cut operating costs, cut down equipment investment and the operating costs such as heat-conducting medium circulating pump.
Description of drawings
The schematically overall longitudinal sectional view that Fig. 1 obtains along hatching A-A intercepting shown in Figure 3 for the calandria type fixed bed reactor that adopts according to the novel shell side structure of the first embodiment of the present utility model;
Fig. 2 is schematically vertical cutaway view Amplified image that the lower circle distributor in the calandria type fixed bed reactor shown in Figure 1 obtains along hatching A-A intercepting shown in Figure 3;
Fig. 3 for from directly over the schematic cross sectional views that obtains along hatching B-B intercepting shown in Figure 1 of lower circle distributor the calandria type fixed bed reactor shown in Figure 1 observed;
Fig. 4 is schematically vertical cutaway view Amplified image that the upper circle distributor in the calandria type fixed bed reactor shown in Figure 1 obtains along hatching A ' shown in Figure 5-A ' intercepting;
Fig. 5 for from directly over upper circle distributor the calandria type fixed bed reactor shown in Figure 1 observed along the schematic cross sectional views of hatching C-C shown in Figure 1;
Fig. 6 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the first embodiment of the present utility model;
Fig. 7 is according to the zone of the edge stringing in the novel shell side structure of the first embodiment of the present utility model and the center top view of the layout in stringing zone not;
Fig. 8 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the second embodiment of the present utility model; With
Fig. 9 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the 3rd embodiment of the present utility model.
The specific embodiment
For shell and tube vinyl acetate synthesis reactor, remove the thermal efficiency to reduce the reactor temperature difference radially be the target that the those skilled in the art constantly pursues all the time thereby reactor structure is constantly improved to improve reactor.This wherein, the setting of circle distributor, stringing mode and deflection plate set-up mode are to realize the key remove thermal medium Uniform Flow in the calandria type fixed bed reactor shell side.In a plurality of preferred embodiments below the structure of these three aspects is reasonably designed even distribution with temperature in the realization response device.
Fig. 1 for adopt according to the novel shell side structure of the first embodiment of the present utility model take water-water vapour as the calandria type fixed bed reactor 18 of removing thermal medium along the schematically overall longitudinal sectional view of hatching A-A shown in Figure 3.As shown in fig. 1, remove thermal medium enter the reactor shell side must through lower circle distributor 7 be positioned at the bottom of calandria type fixed bed reactor 18, remove thermal medium leave the reactor shell side must through upper circle distributor 1 be positioned at the top of calandria type fixed bed reactor 18.The utility model utilizes water to remove reaction heat in the latent heat of vaporization of calandria type fixed bed reactor shell side.Relative conduction oil, the heat-conducting mediums such as fused salt, it is higher that water-water vapour is removed the thermal efficiency as heat-conducting medium, not only is conducive to improve the thermal effect of removing of reactor, reduces the reactor temperature difference radially; Can also the by-product water vapour, thus make the vinyl acetate synthesising reacting heat obtain more reasonably utilizing; Move in the thermal siphon mode, can cut operating costs, cut down equipment investment and the operating costs such as heat-conducting medium circulating pump.
Fig. 2 is that lower circle distributor 7 in the calandria type fixed bed reactor 18 shown in Figure 1 is along the schematically vertically cutaway view Amplified image of hatching A-A shown in Figure 3; Fig. 3 for from directly over lower circle distributor 7 calandria type fixed bed reactor shown in Figure 1 18 observed along the schematic cross sectional views of hatching B-B shown in Figure 1; Fig. 4 is that upper circle distributor 1 in the calandria type fixed bed reactor 18 shown in Figure 1 is along the schematically vertically cutaway view Amplified image of hatching A ' shown in Figure 5-A '; Fig. 5 for from directly over upper circle distributor 1 calandria type fixed bed reactor shown in Figure 1 18 observed along the schematic cross sectional views of hatching C-C shown in Figure 1.
As shown in Fig. 1-5, what come from the outside removes thermal medium such as water, four inlet ports 10 of the lower circle distributor 7 by removing the thermal medium entrance as the reactor shell side enter in the circular passage 11 of lower circle distributor 7, and described four inlet ports 10 are by circular passage 11 fluid communication with each other of lower circle distributor 7.Then, water is via entering bottom-up the flowing of reactor shell side inner chamber along the distribution hole that diameter is less for inlet port 10 12 on 11 inboards, circular passage that circumferentially are arranged on equably lower circle distributor 7.In this course, water occurs to vaporize under the effect of the heat that the vinyl acetate synthetic reaction generates to be converted at least in part water vapour.Remove thermal medium subsequently, water-water vapour is via the circular passage 14 that enters upper circle distributor 1 along the circumferential distribution hole that diameter is less for outlet 13 15 that is arranged on equably on the upper circle distributor 1, at last, four outlets 13 of the upper circle distributor 1 of the water-water vapour in the circular passage 14 of upper circle distributor 1 by removing the thermal medium outlet as the reactor shell side are discharged from the reactor shell side, take away reaction heat.These four outlets 13 along the circumferential direction are arranged on the upper circle distributor 1 and circular passage 14 fluid communication with each other by upper circle distributor 1 equably.
The those skilled in the art can recognize: in order to realize above-mentioned purpose of the present utility model, can along the circumferential direction evenly arrange respectively at the upper/lower terminal of this novel shell side structure and have at least two the upper circle distributor 1 of (such as two, eight, 12 etc.) outlet 13 and at least two inlet port 10(such as two, eight, 16 etc.) lower circle distributor 7.Preferably, upper circle distributor 1 has the outlet 13 more than four, and lower circle distributor 7 has the inlet port 10 more than four.More inlet ports 10 and outlet 13 can reduce even eliminate and remove the Variable Mass Flow of thermal medium in the circular passage of circle distributor, thereby realize that for adopting the single-size distribution hole removing thermal medium creates conditions in interbank uniform distribution, so not only can simplify manufacturing and the installation of distributor, can also reduce the pressure drop of water in circle distributor, guarantee carrying out smoothly of the thermal siphon method of operation.
According to the novel shell side structure of the first embodiment of the present utility model take water-water vapour in the calandria type fixed bed reactor 18 of removing thermal medium, in order to reach better effect, the number of inlet port 10 is preferably 4-16 and circular passage 11 fluid communication with each other by lower circle distributor 7, and the diameter of described inlet port 10 is preferably in the scope of DN150-DN350; The number of outlet 13 is preferably 4-12 and circular passage 14 fluid communication with each other by upper circle distributor 1, and the diameter of described outlet 13 is preferably in the scope of DN100-DN300.Certainly, the those skilled in the art can recognize equally: described inlet port 10 also can divide into groups (every group comprises at least two inlet ports) along circumferentially evenly being arranged on lower circle distributor 7 outsides and circular passage 11 fluid communication with each other of the inlet port 10 in every group by lower circle distributor 7; Described outlet 13 also can divide into groups (every group comprises at least two inlet ports) along circumferentially evenly being arranged on circle distributor 1 outside and circular passage 14 fluid communication with each other of the outlet 13 in every group by upper circle distributor 1.The inboard of circle distributor 1 along the circumferential direction preferably is provided with 50-100 and evenly distributes distribution hole 15 of the same size on described.Described distribution hole 15 rounded, bar shapeds or square, its hydraulic diameter scope is preferably 40mm-300mm.Certainly, the those skilled in the art also can have according to concrete application choice the distribution hole 15 of other suitable shape and size.Along the circumferential direction preferably be provided with 15-30 distribution hole 12 equally distributed, of the same size in the inboard of described lower circle distributor 7.Described distribution hole 12 is rounded, bar shaped or square, and its hydraulic diameter scope is preferably 30mm-100mm.Certainly, the those skilled in the art also can have according to concrete application choice the distribution hole 12 of other suitable shape and size.
In addition, adopt water-water vapour to remove thermal medium and can utilize evaporation of water latent heat to remove reaction heat, the boiling heat transfer of water can promote the temperature in the reactor evenly to distribute.Along with water flows in shell side from bottom to top, the vaporization ratio improves gradually.Therefore the diameter that enlarges the annular deflection plate can reduce fluid resistance and fall, and promotes fluid well-distributing to distribute, and guarantees carrying out smoothly of the thermal siphon method of operation.
Fig. 6 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the first embodiment of the present utility model.In the novel shell side structure according to the first embodiment of the present utility model, polylith deflection plate along continuous straight runs is arranged between described upper circle distributor 1 and the described lower circle distributor 7.As shown in Figure 6, described deflection plate comprise nose-circle ring baffle plate 2, bottom annular deflection plate 6 and be arranged on described nose-circle ring baffle plate 2 and described bottom annular deflection plate 6 between disc deflection plate 3, thereby form the buffering flow region of removing thermal medium between circle distributor 1 and the described lower circle distributor 7 on described.
As shown in Figure 6, in the novel shell side structure according to the first embodiment of the present utility model, axially make progress along described reactor, the center resection rate of described annular deflection plate increases gradually.The center resection rate of described nose-circle ring baffle plate 2 is preferably 1.5-3 times of described bottom annular deflection plate 6.
Fig. 7 is according to the zone of the edge stringing in the novel shell side structure of the first embodiment of the present utility model and the center top view of the layout in stringing zone not.As shown in Figure 7, the utility model by the center not cloth area under control 17 and edge not the setting in cloth area under control 16 greatly reduced the Pressure Drop at position, easy generation dead band, promoted the uniform of radial temperature.
For example, in the novel shell side structure according to the first embodiment of the present utility model, the concrete structure parameter can be as described below, and the diameter of reactor is 5000 mm, is evenly arranged 4 DN80 inlet ports on the lower circle distributor 7, and the diameter of distribution hole 12 is DN15.The outlet of upper circle distributor 1 arranges 8 outlets 13.The center not the scope in stringing zone 17 be roughly the zone (centered by the r not stringing zone 17 inscribe radius of a circles) of r＜100 mm and edge not the scope in cloth area under control 16 be roughly R the zone (R is not cloth area under control 16 inscribe radius of a circles of edge) of 2400 mm.The diameter that circular ring type deflection plate central cut out section is divided is increased to the 2000mm on top by 1200 mm of reactor lower part.
Again for example, in the novel shell side structure according to the first embodiment of the present utility model, the concrete structure parameter can be as described below, and the diameter of reactor is 4000 mm, is evenly arranged 6 DN50 inlet ports on the lower circle distributor 7, and the diameter of distribution hole 12 is DN18.The outlet of upper circle distributor 1 arranges 12 outlets 13.The center not the scope in stringing zone 17 be roughly the zone (centered by the r not stringing zone 17 inscribe radius of a circles) of r＜80 mm and edge not the scope in cloth area under control 16 be roughly R the zone (R is not cloth area under control 16 inscribe radius of a circles of edge) of 1900 mm.The diameter that circular ring type deflection plate central cut out section is divided is increased to the 2000mm on top by 1200 mm of reactor lower part.
Fig. 8 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the second embodiment of the present utility model.
As shown in Figure 8, in the novel shell side structure according to the second embodiment of the present utility model, at uppermost nose-circle ring baffle plate 2 and between nethermost bottom annular deflection plate 6, be horizontally disposed with successively polylith disc deflection plate 4,3,5.Axially make progress along described reactor, the center resection rate of described annular deflection plate increases gradually.
Fig. 9 is the combining structure schematic diagram according to employed deflection plate in the novel shell side structure of the 3rd embodiment of the present utility model.
As shown in Figure 9, at uppermost nose-circle ring baffle plate 2 and between nethermost bottom annular deflection plate 6, alternately be horizontally disposed with polylith disc deflection plate 4,3,5 and annular deflection plate 8,9.In the novel shell side structure according to the 3rd embodiment of the present utility model, axially make progress along described reactor, the center resection rate of described annular deflection plate increases gradually.
In the utility model employed deflection plate can and reaction tube between have the gap (not shown) of 0.1mm-0.8mm size.Because water occurs to vaporize under the effect of the heat that the vinyl acetate synthetic reaction generates to be converted at least in part the stronger water vapour of the ability of flowing through in the vinyl acetate synthetic reaction process, therefore with respect to using conduction oil or fused salt as for the shell and tube vinyl acetate synthesis reactor of removing thermal medium, the gap between deflection plate of the present utility model and the reaction tube can be significantly less than the gap between conduction oil distribution grid and the reaction tube.Thus, shell side structure of the present utility model can be more compact, is conducive to the miniaturization of reactor.
Thereby the novel designs of the shell side structure for the vinyl acetate synthetic reaction of the present utility model is removed thermal medium flowing in shell side by guiding consciously and has been eliminated the ever-present thermal medium dead band of flowing of removing of prior art shell side, reduced to the full extent and removed the thermal medium flow, thereby improved removing thermal effect and reducing the reactor temperature difference radially of reactor.
Above embodiment has carried out describing in detail particularly to the novel shell side structure that is used for calandria type fixed bed reactor and the shell and tube vinyl acetate synthesis reactor that comprises this novel shell side structure.Certainly, the those skilled in the art can recognize: the utility model is not only applicable to shell and tube vinyl acetate synthesis reactor, can also be applicable to can to emit in the course of reaction shell and tube synthesis reactor (removing thermal medium with the water vapour conduct) of other chemicals that needs to absorb more heat transfer in the shell and tube synthesis reactor (water is as removing thermal medium) of other chemicals of more reaction heat and the course of reaction.In addition, the those skilled in the art can be by using for reference the content of this paper, and appropriate change structural parameters etc. are realized the utility model.Person skilled obviously can be changed or suitably change and combination product structure as herein described within not breaking away from the utility model content, spirit and scope, realizes the utility model technology.Special needs to be pointed out is that the replacement that all are similar and change are apparent to the those skilled in the art, they all are regarded as being included in the utility model spirit, scope and the content.
Reference numerals list
Circle distributor on 1
2 nose-circle ring baffle plates
3,4,5 disc deflection plates
6 bottom annular deflection plates
7 times circle distributors
8,9 annular deflection plates
The inlet port of 10 times circle distributors
The circular passage of 11 times circle distributors
The distribution hole of 12 times circle distributors
The outlet of circle distributor on 13
The circular passage of circle distributor on 14
The distribution hole of circle distributor on 15
16 edges are the cloth area under control not
17 centers are the cloth area under control not
18 calandria type fixed bed reactors
Claims (15)
1. the shell side structure of a shell and tube vinyl acetate synthesis reactor, it is characterized in that, at the upper/lower terminal of described shell side structure the upper circle distributor with at least two outlets and the lower circle distributor with at least two inlet ports are set evenly along the circumferential direction respectively, at least two outlets in described at least two outlets by the circular passage fluid communication with each other in the described upper circle distributor and described at least two at least two inlet ports that enter the mouth by the circular passage fluid communication with each other in the described lower circle distributor.
2. shell side structure as claimed in claim 1 is characterized in that, described reactor makes water-water vapour as removing thermal medium and moving in the thermal siphon mode.
3. shell side structure as claimed in claim 1 is characterized in that, the number of described inlet port is 4-16.
4. shell side structure as claimed in claim 1 is characterized in that, the diameter of described outlet is in the scope of DN100-DN300.
5. such as each described shell side structure among the claim 1-4, it is characterized in that the inboard of circle distributor along the circumferential direction is provided with 50-100 and evenly distributes distribution hole of the same size on described.
6. shell side structure as claimed in claim 5 is characterized in that, described distribution hole is rounded, bar shaped or square.
7. such as each described shell side structure among the claim 1-4, it is characterized in that, along the circumferential direction be provided with 15-30 distribution hole equally distributed, of the same size in the inboard of described lower circle distributor.
8. shell side structure as claimed in claim 7 is characterized in that, described distribution hole is rounded, bar shaped or square.
9. such as each described shell side structure among the claim 1-4, it is characterized in that, along continuous straight runs arranges deflection plate between circle distributor and the described lower circle distributor on described, described deflection plate comprise at least nose-circle ring baffle plate, bottom annular deflection plate and/or be arranged on described nose-circle ring baffle plate and described bottom annular deflection plate between annular deflection plate and disc deflection plate, thereby form the buffering flow region of removing thermal medium between circle distributor and the described lower circle distributor on described.
10. shell side structure as claimed in claim 9 is characterized in that, axially makes progress along described reactor, and the center resection rate of described annular deflection plate increases gradually.
11. shell side structure as claimed in claim 9 is characterized in that, the center resection rate of described nose-circle ring baffle plate is 1.5-3 times of described bottom annular deflection plate.
12. shell side structure as claimed in claim 9 is characterized in that, has the gap of 0.1mm-0.8mm size between described annular deflection plate and described disc deflection plate and the reaction tube.
13., it is characterized in that reaction tube is not arranged in the central area in described shell and tube vinyl acetate synthesis reactor shell side such as each described shell side structure among the claim 1-4.
14., it is characterized in that the fringe region in described shell and tube vinyl acetate synthesis reactor shell side is not arranged reaction tube such as each described shell side structure among the claim 1-4.
15. one kind comprises the shell and tube vinyl acetate synthesis reactor such as each described shell side structure among the claim 1-14.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220336835 CN202893319U (en) | 2012-07-12 | 2012-07-12 | Shell side structure and tubular vinyl acetate synthesis reactor comprising same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220336835 CN202893319U (en) | 2012-07-12 | 2012-07-12 | Shell side structure and tubular vinyl acetate synthesis reactor comprising same |
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| Publication Number | Publication Date |
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| CN202893319U true CN202893319U (en) | 2013-04-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220336835 Withdrawn - After Issue CN202893319U (en) | 2012-07-12 | 2012-07-12 | Shell side structure and tubular vinyl acetate synthesis reactor comprising same |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102784596A (en) * | 2012-07-12 | 2012-11-21 | 天津大学 | Shell side structure and shell and tube vinyl acetate synthesis reactor with same |
| CN104437269A (en) * | 2013-09-24 | 2015-03-25 | 中国石油化工股份有限公司 | Tubular reactor for producing vinyl acetate and vinyl acetate production method |
-
2012
- 2012-07-12 CN CN 201220336835 patent/CN202893319U/en not_active Withdrawn - After Issue
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102784596A (en) * | 2012-07-12 | 2012-11-21 | 天津大学 | Shell side structure and shell and tube vinyl acetate synthesis reactor with same |
| CN102784596B (en) * | 2012-07-12 | 2014-12-17 | 天津大学 | Shell side structure and shell and tube vinyl acetate synthesis reactor with same |
| CN104437269A (en) * | 2013-09-24 | 2015-03-25 | 中国石油化工股份有限公司 | Tubular reactor for producing vinyl acetate and vinyl acetate production method |
| CN104437269B (en) * | 2013-09-24 | 2016-08-24 | 中国石油化工股份有限公司 | The production method of shell and tube reactor and vinyl acetate for producing vinyl acetate |
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