CN102784603A - Gas distributor and vinyl acetate synthesis reactor comprising the same - Google Patents
Gas distributor and vinyl acetate synthesis reactor comprising the same Download PDFInfo
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- CN102784603A CN102784603A CN2012102406152A CN201210240615A CN102784603A CN 102784603 A CN102784603 A CN 102784603A CN 2012102406152 A CN2012102406152 A CN 2012102406152A CN 201210240615 A CN201210240615 A CN 201210240615A CN 102784603 A CN102784603 A CN 102784603A
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Abstract
The invention relates to a gas distributor and a vinyl acetate synthesis reactor comprising the same. The gas distributor comprises an expanding current stabilization part and a spherical head, wherein the first end of the expanding current stabilization part is connected with the head of a multitubular vinyl acetate synthesis reactor, the second end corresponding to the first end of the expanding current stabilization part is connected with the spherical head of the gas distributor or the second end and the spherical head are formed integrally, the diameter of the first end of the expanding current stabilization part is larger than that of a reactor inlet, and distributing pores are uniformly arranged in the area coverage of the spherical head. According to the invention, studies by computational fluid dynamics show that by using the gas distributor with the above structure, the uniform distribution of gas can be well realized; by using the catalyst support mode of the above structure, the structure of the reactor can be greatly simplified, the manufacturing, installation, disassembly and maintenance of devices are convenient, and the incidence that the catalyst falls off and other accidents can be reduced; by using the temperature measurement mode disclosed herein, the control precision of the reactor can be well raised.
Description
Technical field
Present invention relates in general to a kind of new gas distributor and a kind of vinyl acetate synthesis reactor.Particularly, the present invention relates to a kind of new gas distributor and the shell and tube vinyl acetate synthesis reactor that comprises this new gas distributor that can improve the reaction efficiency of ethene preparing vinyl acetate synthetic reaction.
Background technology
The ethene oxidizing process is the main a kind of process that is used for synthesizing vinyl acetate that adopts in industry.The raw material ethene of vinyl acetate synthetic reaction can particularly can be prepared by bio-ethanol by ethanol preparation.It is significant for biomass as resources as the process route of synthesizing vinyl acetate raw material to use bio-ethanol to produce ethene.This synthetic reaction process belongs to the gas-solid heterogeneous catalytic reaction, and calandria type fixed bed reactor is normally used synthesis device.Adopt the ethene oxidizing process to produce vinyl acetate and need use the precious metal palladium that is supported on the silica gel and gold, and need in technical process, add some potassium acetates as co-catalyst as catalyst.
In the vinyl acetate synthesis process, reaction cycle gas gets into synthesis reactor from the gas access that is positioned at shell and tube vinyl acetate synthesis reactor top.In general, the diameter of gas access pipeline is far smaller than the diameter of reactor, if reaction cycle gas is directly sprayed in the large diameter synthesis reactor by the gas access of minor diameter; In the near zone of gas access; Gas velocity is very big, and the energy that air-flow had is main with kinetic energy, and static energy is very little; Gas to getting in the synthesis reactor is very unfavorable along the distribution of synthesis reactor radial direction, often cause thus reacting gas in getting into synthesis reactor after skewness.In addition, especially when using co-catalyst, the liquor kalii acetici drop is being stained with the very difficult quadratic distribution in back on the inert ceramic balls, thereby makes each reaction tube in the reactor receive tolerance and co-catalyst to distribute difference bigger.Concerning synthesis reactor, this can cause the part catalyst utilization low, and the part catalyst is again because of the too high inactivation that shifts to an earlier date of loading; The phenomenon that the reaction heat in some reaction tube can not in time be taken away also can occur, cause hot-spot, even burn catalyst, make technological operation unstable.Concerning reaction mass,, overall vinyl acetate synthetic reaction conversion ratio and yield are reduced because the situation of participation reaction is inconsistent in each reaction tube.
For this reason, need distribution device in gas-fluid be set, reaction gas flow is carried out power conversion in shell and tube vinyl acetate synthesis reactor porch.Single-stage or multistage baffle plate, porous plate and deflector etc. be the normal form that adopts of distribution device in gas-fluid in the reactor (Xie Yile, the distribution device in gas-fluid of fixed bed catalytic reactor, the petrochemical equipment technology, 1990,11 (3), 2-9).
Below reactor inlet, a collar plate shape baffle plate is set can avoids of the impact of high speed incident air-flow beds, improve gas at reactor fluid ability radially.When reactor diameter is big, also can adopt the multistage baffle arrangement of disk-and-doughnut type.The deficiency that this baffle arrangement exists is to make the outside deflection of high velocity air easily, thereby flows downward along reactor wall, causes the skewness of another kind of form.And through behind this baffle arrangement, gas flow rate still can keep higher level, and above-mentioned reaction gas flow problem pockety still can occur.
The internals that adopts porous plate or similar structures be a kind of possibility of addressing the above problem (Xie Yile, the distribution device in gas-fluid of fixed bed catalytic reactor, the petrochemical equipment technology, 1990,11 (3), 2-9).This internals is installed on the entire cross section of synthesis reactor, can help the even distribution of realization response air-flow.But this internals can produce higher pressure drop, thereby can increase the operation operating cost.In addition, the whole cross section installation of internals brings very big trouble can for replacing, the regenerative operation of installation, maintenance and the decaying catalyst of synthesis reactor.
Use concentric conical deflector structure can incident gas be shunted, and be implemented in the progressively dispersion (referring to Chinese utility model patent CN201684583U) that reactor directly makes progress.Yet this distributor exists complex structure, the problem of design, manufacturing difficulty; If design, the improper appearance that still can cause the problems referred to above of manufacturing.
Therefore, need a kind of new gas distributor with characteristics such as simple in structure, that distribution of gas is even, pressure drop is little, manufacturing is easy for installation.
In addition, reaction tube is the core component of shell and tube vinyl acetate synthesis reactor, and the thermometric mode of the supporting way of good catalyst and bed is the important assurance of realization response device stable operation.For the support of catalyst, adopting pipe cap, support chip still is that the baffle plate mode that adds spring all exists some engineering problems.In addition, traditional thermometric mode is promptly arranged a point for measuring temperature in a reaction tube, can not satisfy the high-precision control requirement of synthesis reactor.
Therefore, also need a kind of the employing to make catalyst supporting structure easy for installation and can satisfy the vinyl acetate synthesis reactor that high-precision control requires to shell and tube vinyl acetate synthetic reaction.
Summary of the invention
The objective of the invention is to improve the reaction efficiency of ethene preparing vinyl acetate synthetic reaction.Above-mentioned purpose of the present invention realizes through following technological means, a kind of new gas distributor that can make the reacting gas that gets into the vinyl acetate synthesis reactor and co-catalyst be evenly distributed to beds promptly is provided, a kind of shell and tube vinyl acetate synthesis reactor that comprises said gas distributor is provided, a kind of shell and tube vinyl acetate synthesis reactor that comprises said gas distributor of making the thermocouple layout that has multi-point temperature measurement in catalyst supporting structure easy for installation and the reaction tube that adopts is provided.Shell and tube vinyl acetate synthesis reactor of the present invention comprises the reaction tube structure of said new gas distributor and the accurate measurement that can realize support that catalyst is reliable and stable and reaction bed temperature.
In the present invention, for example the diameter of the cylindrical housings through the enlargement gas distributor, in the end end regions that the said cylindrical housings of gas distributor links to each other with the dome head of gas distributor and the means of on said dome head, offering reduction SR such as distributed holes will change static pressure into via the dynamic pressure that the synthesis reactor gas access gets into the reaction cycle air-flow in the synthesis reactor.
The present invention provides a kind of gas distributor that is used for shell and tube vinyl acetate synthesis reactor; It is characterized in that; Said gas distributor comprises hole enlargement current stabilization portion's section and dome head; First end of said hole enlargement current stabilization portion section links to each other through flange with the end socket of this shell and tube vinyl acetate synthesis reactor; Thereby filling and the overhaul of the equipments of being convenient to catalyst in reactor for convenience detach; Second end of relative with said first end said hole enlargement current stabilization portion section links to each other with the dome head of said gas distributor or is integrally formed, and the diameter of said hole enlargement current stabilization portion section first end is provided with distributed holes greater than the diameter of reactor inlet equably in said dome head regional extent.
According to an aspect of the present invention, the proportion of the diameter of the diameter of said hole enlargement current stabilization portion section first end and said reactor inlet is 1.1-2.5.
According to an aspect of the present invention, the proportion of the diameter of the diameter of said hole enlargement current stabilization portion section first end and said reactor inlet is 1.4-2.0.
According to a further aspect of the invention, that the percent opening in the said dome head zone is 12%-40%.
According to another aspect of the present invention, around said hole enlargement current stabilization portion section distributed holes is set equably along the circumferential direction at the said hole enlargement current stabilization portion section second end place.
According to a further aspect of the invention, be 12%-40% at the percent opening at the said hole enlargement current stabilization portion section second end place.
According to a further aspect of the invention, the pore size of said distributed holes is 10-25 mm, and the pitch of holes size of said distributed holes is 15-35 mm.
According to a further aspect of the invention, the height of said hole enlargement current stabilization portion section is 0.2-0.6 with the ratio of the end socket height of said shell and tube vinyl acetate synthesis reactor.
According to a further aspect of the invention, the height of said hole enlargement current stabilization portion section is 0.2-0.3 with the ratio of the end socket height of said shell and tube vinyl acetate synthesis reactor.
According to a further aspect of the invention, the diameter of said hole enlargement current stabilization portion section second end can be identical with the diameter of said dome head.
According to a further aspect of the invention, the diameter of said dome head can be connected with said hole enlargement current stabilization portion section second end via the tapering transition section greater than the diameter of said hole enlargement current stabilization portion section second end and said dome head.
Show through the research of Fluid Mechanics Computation method: have the new gas distributor of said structure and can be effectively the kinetic energy of the recyclegas that gets into reactor be converted into static energy, thus realization response gas and the even distribution of co-catalyst on reactor cross section well).Specifically, it is better than the distribution of gas effect that does not have the cylindrical housings section that said gas distributor increases the cylindrical housings section, specifically be convenient to regulate circular head apart from the beds distance to best; Better in the terminal perforate of cylindrical housings section than the distribution of gas effect of not perforate, especially in zone near the reactor shell wall.
The present invention also provides a kind of shell and tube vinyl acetate synthesis reactor that comprises like the described gas distributor of the present invention of preamble.
According to an aspect of the present invention, said shell and tube vinyl acetate synthesis reactor also comprises reaction tube, and beds receives the support of the composite spring that is positioned at said reaction tube lower end in said reaction tube.
According to another aspect of the present invention; Said composite spring is cylinder and circular cone composite spring, and the spring wire of said cylinder and circular cone composite spring is from the cylinder form that is positioned at the lower end coniform shape that with beds contact of transition above being gradually.
According to a further aspect of the invention, the diameter of the spring wire of said composite spring is that the cylindrical section number of active coils of 2 mm-4 mm and said composite spring is greater than 6.
According to a further aspect of the invention; The conical section of said composite spring is by compression the time, the spacing between every coil spring silk less than the conical section bottom maximum gauge of the half the and said composite spring of catalyst granules diameter be said composite spring cylindrical section diameter 80%.
According to a further aspect of the invention, a plurality of points for measuring temperature are set vertically in the thermocouple sheath of each root reaction tube, in order to realize axial multiple spot thermometric simultaneously.
According to a further aspect of the invention, the number scope of said point for measuring temperature can be 2-20.
Catalyst supporting structure of the present invention is for realizing the firm support to catalyst through cylinder-circular cone composite spring interference chucking in reaction tube.Catalyst supporting way with said structure of the present invention can be simplified the structure of shell and tube vinyl acetate synthesis reactor greatly; Be convenient to the manufacturing of equipment; Installation and removal safeguard, and accident occurrence probability such as can reduce that catalyst comes off, and improve its reliability.Adopt the above-mentioned thermometric mode of the present invention can realize multi-point temperature measurement on the single reaction inner axial tube, can improve the reaction control accuracy of shell and tube vinyl acetate synthesis reactor better.
Description of drawings
Below, in conjunction with accompanying drawing exemplary embodiments of the present invention is described in detail, wherein:
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of first embodiment of the invention of Fig. 1 for obtaining along hatching B-B shown in Figure 5 intercepting;
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of second embodiment of the invention of Fig. 2 for obtaining along hatching B-B shown in Figure 5 intercepting;
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of third embodiment of the invention of Fig. 3 for obtaining along hatching B-B shown in Figure 5 intercepting;
The schematic cross sectional views according to the gas distributor of first embodiment of the invention of Fig. 4 for obtaining along line A-A shown in Figure 1 intercepting;
Fig. 5 is the observed vertical view inner according to the gas distributor of first embodiment of the invention in the C-C plane that in Fig. 4, marks downwards;
Fig. 6 schematically shows employed cylinder and the installation diagram of circular cone composite spring in reaction tube in vinyl acetate synthesis reactor of the present invention; With
Fig. 7 is the structural representation of cylinder shown in Figure 6 and circular cone composite spring.
The specific embodiment
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of first embodiment of the invention of Fig. 1 for obtaining along hatching B-B shown in Figure 5 intercepting.The schematic cross sectional views according to the gas distributor of first embodiment of the invention of Fig. 4 for obtaining along line A-A shown in Figure 1 intercepting.Fig. 5 is the observed vertical view inner according to the gas distributor of first embodiment of the invention in the C-C plane that in Fig. 4, marks downwards.
As shown in fig. 1, the top of shell and tube vinyl acetate synthesis reactor 1 of the present invention has elliposoidal end socket 2.Certainly, for the those skilled in the art, the shape of this shell and tube vinyl acetate synthesis reactor 1 top end socket 2 also can be other shape that is fit to, for example sphere etc.Recyclegas inlet (reactor inlet) 3 is set at the central authorities of elliposoidal end socket 2, and gas distributor 4 is set directly at above the elliposoidal end socket 2 and enters the mouth 3 concentric with recyclegas.Gas distributor 4 comprises and the hole enlargement current stabilization portion section 5 and the dome head 6 of the cylindrical hull shape of recyclegas inlet 3 concentric settings that first end (upper end) of hole enlargement current stabilization portion section 5 links to each other with the elliposoidal end socket 2 of this shell and tube vinyl acetate synthesis reactor 1; Second end (lower end) of the hole enlargement current stabilization portion section 5 relative with said first end links to each other with the dome head 6 of gas distributor 4 or is integrally formed.In this embodiment, the diameter of hole enlargement current stabilization portion section 5 so just makes hole enlargement current stabilization portion section 5 can play the effect of buffer gas flow effectively greater than the diameter of recyclegas inlet 3, makes that the distribution of gas that gets into reactor is more even, and flow velocity is more stable.The proportion of the diameter of said hole enlargement current stabilization portion section first end and the diameter of said reactor inlet is 1.1-2.5, and preferred proportion is 1.4-2.0.The too small hole enlargement steady flow result that does not then reach expection of this ratio; This ratio is crossed conference and is fallen the pressure of circulating current low excessively, and reaction speed can slow down.In addition, the height of said hole enlargement current stabilization portion section 5 is preferably 0.2-0.6 with the ratio of end socket 2 height of said shell and tube vinyl acetate synthesis reactor 1.
The dome head 6 of gas distributor 4 is provided with opening area.Percent opening in the said dome head zone be 12%-40%.In the present invention, the term percent opening be defined as the perforate gross area with by the percentage of the opening area gross area.In addition, alternatively, also can perforate 16 circumferentially be set on second end edge of hole enlargement current stabilization portion section 5.The 12%-40% that can be at the percent opening at the said hole enlargement current stabilization portion section second end place.The pore size of these distributed holes is 10-25 mm, and the pitch of holes size of said distributed holes is 15-35 mm, like Fig. 4 and shown in Figure 5.High velocity air from feed pipe at first pours this gas distributor 4 via recyclegas inlet 3, because the hole enlargement effect of hole enlargement current stabilization portion section 5 and dome head 6, most of kinetic energy of said high velocity air transforms for static energy.Gas through being arranged on the perforate 7 and the perforate 16 that is arranged on buffering wide diameter portion section 5 second ends on the dome head 6, in all directions relax even inflow reactor, thereby is realized the even distribution of gas under the driving of this static energy.
In order to guarantee to enter into the tolerance uniformity of the every reaction tube 8 (figure only schematically shows a reaction tube) that is arranged in the below in this shell and tube vinyl acetate synthesis reactor 1; Reactor upper perforated plate 18 is arranged on apart from gas distributor 4 position of certain distance bottom, and at the inert ceramic balls layer of arranging on the reactor upper perforated plate 18 more than one deck 15.Reactor upper perforated plate 18 plays the effect to the reaction tube support fixation together with the reactor lower perforated plate 17 shown in Fig. 6, simultaneously to realizing region separation in the reactor.In prior art shell and tube vinyl acetate synthesis reactor 1, need on the reactor upper perforated plate, laying depth be the inert ceramic balls layer of 500mm-1000mm generally, just can make the tolerance that gets in the reaction tube of below even substantially.By contrast; Owing in shell and tube vinyl acetate synthesis reactor 1 of the present invention, be provided with novel gas distributor 4; Therefore laying depth is the inert ceramic balls layer of 200mm-300mm on reactor upper perforated plate 18 of the present invention; Just can make the tolerance that gets in the below reaction tube 8 even substantially, make the desired thickness of inert ceramic balls layer 15 obviously to reduce thus.So just make the those skilled in the art might design more compact and take the shell and tube vinyl acetate synthesis reactor in littler space.In addition, thinner inert ceramic balls layer 15 used in the present invention make gas through the time resistance reduce, pressure reduction reduces, and can reduce the compressor load of cycle reaction gas thus.
Some design and installation examples of parameters of vinyl acetate synthesis reactor 1 according to first embodiment of the invention as shown in Figure 1 have been listed below.
Design and installation examples of parameters 1:
Carry out the manufacturing and the installation of gas distributor in the reactor of the present invention according to structure as shown in Figure 1.The concrete structure parameter is described below, and the diameter of reactor is 5000 mm, and the gas feed diameter is 600 mm, and gas distributor cylindrical housings diameter is 900 mm, and the diameter of gas distributor dome head is identical with it, and the length of cylindrical housings is 300 mm.The lower end of cylindrical housings and dome head are opened equally distributed aperture, and opening diameter is 22 mm, and the circular hole center distance is 30 mm.
Design and installation examples of parameters 2:
Carry out the manufacturing and the installation of gas distributor in the reactor of the present invention according to structure as shown in Figure 1.The concrete structure parameter is described below, and the diameter of reactor is 4000 mm, and the gas feed diameter is 500 mm, and gas distributor cylindrical housings diameter is 800 mm, and the diameter of dome head is identical with it, and the length of cylindrical housings is 250 mm.Dome head is opened equally distributed aperture, and opening diameter is 18 mm, and the circular hole center distance is 27 mm.
Design and installation examples of parameters 3:
Carry out the manufacturing and the installation of gas distributor in the reactor of the present invention according to structure as shown in Figure 1.The concrete structure parameter is described below; The diameter of reactor is 5000 mm, and the gas feed diameter is 600 mm, and gas distributor cylindrical housings diameter is 900 mm; The diameter of dome head is 1200 mm, and the height of the connection cone transitional section between the two is 120 mm.The lower end of cylindrical housings and dome head are opened equally distributed aperture, and opening diameter is 22 mm, and the circular hole center distance is 30 mm.
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of second embodiment of the invention of Fig. 2 for obtaining along hatching B-B shown in Figure 5 intercepting.
The top of second embodiment of vinyl acetate synthesis reactor of the present invention is structurally similar with the top of above-mentioned first embodiment.Difference is that in second embodiment of vinyl acetate synthesis reactor of the present invention, hole enlargement current stabilization portion section 5 is the truncated cone shape hull shape.First end of hole enlargement current stabilization portion section 5 directly links to each other with the elliposoidal end socket 2 of this shell and tube vinyl acetate synthesis reactor 1; Second end of the hole enlargement current stabilization portion section 5 relative with said first end directly links to each other with the dome head 6 of gas distributor 4 or is integrally formed.In this embodiment, the diameter of hole enlargement current stabilization portion section 5 first ends is greater than the diameter of the diameter of recyclegas inlet 3 and the hole enlargement current stabilization portion section 5 second ends diameter greater than hole enlargement current stabilization portion section 5 first ends.
The schematic longitudinal sectional view according to the top of the vinyl acetate synthesis reactor of third embodiment of the invention of Fig. 3 for obtaining along hatching B-B shown in Figure 5 intercepting.
The top of the 3rd embodiment of vinyl acetate synthesis reactor of the present invention is structurally similar with the top of above-mentioned first, second embodiment.Difference is that in the 3rd embodiment of vinyl acetate synthesis reactor of the present invention, hole enlargement current stabilization portion section 5 is up-narrow and down-wide one combined shaped.First end of hole enlargement current stabilization portion section 5 links to each other with the elliposoidal end socket 2 of this shell and tube vinyl acetate synthesis reactor 1; Second end of the hole enlargement current stabilization portion section 5 relative with said first end links to each other with the dome head 6 of gas distributor 4 or is integrally formed.In this embodiment, the diameter of hole enlargement current stabilization portion section 5 first ends is greater than the diameter of the diameter of recyclegas inlet 3 and the hole enlargement current stabilization portion section 5 second ends diameter greater than hole enlargement current stabilization portion section 5 first ends.
Fig. 6 schematically shows cylinder shown in Figure 7 and the installation diagram of circular cone composite spring 9 in reaction tube 8.Fig. 7 is the structural representation of employed cylinder and circular cone composite spring 9 in the reaction tube 8 of vinyl acetate synthesis reactor 1 according to the present invention.Cylinder and circular cone composite spring 9 comprise and interconnecting or integrally formed conical section 10 and cylindrical section 11.Conical section 10 is the big pyramidal structure in point bottom, top.As visible among Fig. 6, shell and tube vinyl acetate synthesis reactor 1 of the present invention also comprises reaction tube 8, and beds 14 receives the support of the composite spring that is positioned at said reaction tube lower end in said reaction tube.Said composite spring is cylinder and circular cone composite spring, and the spring wire of said cylinder and circular cone composite spring is from the cylinder form that is positioned at the lower end coniform shape that with beds contact of transition above being gradually.The diameter of the spring wire of said composite spring is that the cylindrical section number of active coils of 2 mm-4 mm and said composite spring is greater than 6.The conical section of said composite spring is not by compression the time; Spacing between every coil spring silk less than the conical section bottom maximum gauge of the half the and said composite spring of catalyst granules diameter be said composite spring cylindrical section diameter 80%; After noticing that thus the filling of assurance catalyst is accomplished, conical section can not pass through because of pressurized makes a coil spring silk arrange tension obstruction gas.In Fig. 6, schematically show four points for measuring temperature 13 that are provided with along the longitudinal axis of reaction tube 8, in order to realize axial multiple spot thermometric simultaneously.But the those skilled in the art should be readily appreciated that, in the thermocouple sheath of each root reaction tube, 2-20 point for measuring temperature can be set vertically, in order to realize axial multiple spot thermometric simultaneously.
Carry out the manufacturing and the installation of reaction tube inner catalyst support member of the present invention according to structure as shown in Figure 6.The concrete structure parameter is described below, and the internal diameter of reaction tube is 32mm, and under the composite spring nature, the diameter of cylindrical section is 34.5 mm, interference 2.5 mm.Adopt specific purpose tool that spring is torqued-up to along the hand of spiral during mounting spring and be slightly less than tube inner diameter, by the reaction tube lower end it is sent in the reaction tube then, be higher than reaction tube low side 20 mm to spring end.In catalyst supporting structure of the present invention, reaction tube and spring external diameter interference fit, the external diameter under the spring nature and the difference of tube inner diameter should satisfy ΔΦ=2.5-4 mm.During installation, send into appropriate location, reaction tube lower end after the employing specific purpose tool is screwed spring, (general spring end is apart from reacting the mouth of pipe apart from 20-30 mm or by technological requirement.) unclamp the power of screwing then, rely on the radical elasticity generation of spring and the gravity of the tension force bearing catalyst of reaction tube and the pressure of reacting gas import and export reaction tube to fall.Support spring should guarantee that catalyst does not leak and gas is passed through smoothly.After spring is installed in reaction tube, must be with the experiment of 10 times of single tube catalyst gravity, whether not coming off from reaction tube with spring, to be that standard is tested qualified.Catalyst adds from the upper end of reaction tube, and more during catalyst changeout, catalyst is from reaction tube upper end sucking-off.
Show through the research of Fluid Mechanics Computation method, adopt new gas distributor of the present invention, even distribution that can fine realization gas.Adopt the above-mentioned catalyst supporting way of the present invention can simplify the structure of reactor greatly, be convenient to the manufacturing of equipment, installation and removal safeguard, and accident occurrence probability such as can reduce that catalyst comes off; Adopt the above-mentioned thermometric mode of the present invention can improve the control accuracy that improves reactor better.
The present invention is open and proposed a kind of novel vinyl acetate gas reactor distributor and reaction tube structure, and those skilled in the art can be through using for reference the content of this paper, realizations such as appropriate change structural parameters.Method of the present invention and technology are described through preferred embodiment; Person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to method as herein described with technology is changed or suitably change and combination, realize the present invention's technology.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they all are regarded as and are included in spirit of the present invention, scope and the content.
Reference numerals list
1 vinyl acetate synthesis reactor
The elliposoidal end socket on 2 vinyl acetate synthesis reactor tops
3 recyclegas inlet
4 gas distributors
5 hole enlargement current stabilization portion sections
The dome head of 6 gas distributors
7 distributed holes
8 reaction tubes
9 cylinders and circular cone composite spring
The conical section of 10 composite springs
The cylindrical section of 11 composite springs
12 thermocouple sheaths
13 points for measuring temperature
14 beds
15 inert ceramic balls layers
16 are arranged on the perforate of buffering wide diameter portion section second end
17 reactor lower perforated plates
18 reactor upper perforated plates
Claims (16)
1. gas distributor that is used for shell and tube vinyl acetate synthesis reactor; It is characterized in that; Said gas distributor comprises hole enlargement current stabilization portion's section and dome head; First end of said hole enlargement current stabilization portion section links to each other with the end socket of this shell and tube vinyl acetate synthesis reactor; Second end of relative with said first end said hole enlargement current stabilization portion section links to each other with the dome head of said gas distributor or is integrally formed, and the diameter of said hole enlargement current stabilization portion section first end is provided with distributed holes greater than the diameter of reactor inlet equably in said dome head regional extent.
2. gas distributor as claimed in claim 1 is characterized in that, the proportion of the diameter of said hole enlargement current stabilization portion section first end and the diameter of said reactor inlet is 1.1-2.5.
3. gas distributor as claimed in claim 2 is characterized in that, the proportion of the diameter of said hole enlargement current stabilization portion section first end and the diameter of said reactor inlet is 1.4-2.0.
4. gas distributor as claimed in claim 1 is characterized in that, the percent opening in the said dome head zone be 12%-40%.
5. gas distributor as claimed in claim 1 is characterized in that, around said hole enlargement current stabilization portion section distributed holes is set equably along the circumferential direction at the said hole enlargement current stabilization portion section second end place.
6. gas distributor as claimed in claim 5 is characterized in that, the percent opening at the said hole enlargement current stabilization portion section second end place is 12%-40%.
7. like each described gas distributor among the aforementioned claim 1-6, it is characterized in that the pore size of said distributed holes is 10-25 mm, the pitch of holes size of said distributed holes is 15-35 mm.
8. gas distributor as claimed in claim 1 is characterized in that, the height of said hole enlargement current stabilization portion section is 0.2-0.6 with the ratio of the end socket height of said shell and tube vinyl acetate synthesis reactor.
9. gas distributor as claimed in claim 8 is characterized in that, the height of said hole enlargement current stabilization portion section is 0.2-0.3 with the ratio of the end socket height of said shell and tube vinyl acetate synthesis reactor.
10. one kind comprises the shell and tube vinyl acetate synthesis reactor like each described gas distributor among the aforementioned claim 1-9.
11. shell and tube vinyl acetate synthesis reactor according to claim 10; It is characterized in that; Said shell and tube vinyl acetate synthesis reactor also comprises reaction tube, and beds receives the support of the composite spring that is positioned at said reaction tube lower end in said reaction tube.
12. shell and tube vinyl acetate synthesis reactor according to claim 11; It is characterized in that; Said composite spring is cylinder and circular cone composite spring, and the spring wire of said cylinder and circular cone composite spring is from the cylinder form that is positioned at the lower end coniform shape that with beds contact of transition above being gradually.
13. shell and tube vinyl acetate synthesis reactor according to claim 12 is characterized in that, the diameter of the spring wire of said composite spring is that the cylindrical section number of active coils of 2 mm-4 mm and said composite spring is greater than 6.
14. shell and tube vinyl acetate synthesis reactor according to claim 13; It is characterized in that; The conical section of said composite spring is by compression the time, the spacing between every coil spring silk less than the conical section bottom maximum gauge of the half the and said composite spring of catalyst granules diameter be said composite spring cylindrical section diameter 80%.
15., it is characterized in that, a plurality of points for measuring temperature are set vertically, in the thermocouple sheath of each root reaction tube in order to realize axial multiple spot thermometric simultaneously according to each described shell and tube vinyl acetate synthesis reactor among the aforementioned claim 11-14.
16. shell and tube vinyl acetate synthesis reactor as claimed in claim 15 is characterized in that, the number scope of said point for measuring temperature is 2-20.
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| CN2012102406152A CN102784603A (en) | 2012-07-12 | 2012-07-12 | Gas distributor and vinyl acetate synthesis reactor comprising the same |
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| CN2012102406152A CN102784603A (en) | 2012-07-12 | 2012-07-12 | Gas distributor and vinyl acetate synthesis reactor comprising the same |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104436987A (en) * | 2014-11-29 | 2015-03-25 | 无锡纳润特科技有限公司 | Slow air inflow dispersing device of adsorber |
| CN105312013A (en) * | 2015-11-09 | 2016-02-10 | 东华工程科技股份有限公司 | Supporting method for catalyst inside heat exchange tubes of shell and tube reactor |
| CN111111567A (en) * | 2016-02-25 | 2020-05-08 | 亚申科技(浙江)有限公司 | Tube array type fixed bed reactor |
| US11559799B2 (en) * | 2020-12-22 | 2023-01-24 | Scientific Design Company, Inc. | Removable impingement basket for ethylene oxide (EO) reactors |
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| CN105312013B (en) * | 2015-11-09 | 2020-07-10 | 东华工程科技股份有限公司 | Method for supporting catalyst in heat exchange tube of tubular reactor |
| CN111111567A (en) * | 2016-02-25 | 2020-05-08 | 亚申科技(浙江)有限公司 | Tube array type fixed bed reactor |
| CN111111567B (en) * | 2016-02-25 | 2022-03-01 | 亚申科技(浙江)有限公司 | Tube array type fixed bed reactor |
| US11559799B2 (en) * | 2020-12-22 | 2023-01-24 | Scientific Design Company, Inc. | Removable impingement basket for ethylene oxide (EO) reactors |
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