CN203494494U - Tubular fixed bed reactor applicable to synthesis of vinyl acetate - Google Patents
Tubular fixed bed reactor applicable to synthesis of vinyl acetate Download PDFInfo
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- CN203494494U CN203494494U CN201320587303.9U CN201320587303U CN203494494U CN 203494494 U CN203494494 U CN 203494494U CN 201320587303 U CN201320587303 U CN 201320587303U CN 203494494 U CN203494494 U CN 203494494U
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Abstract
The utility model relates to a tubular fixed bed reactor applicable to synthesis of vinyl acetate, which mainly aims at solving the problems of reduction of selectivity and yield of a target product, namely vinyl acetate due to uneven increase of heat exchange medium flowing in a reactor and large radial temperature difference caused by continuous increase of the diameter of a large reactor along with the enlargement of the production scale of the vinyl acetate. The tubular fixed bed reactor comprises a reactor cylinder (1), reaction tubes (2a, 2b and 2c), a heat-carrying fluid inlet guide cylinder (3), a heat-carrying fluid outlet guide cylinder (4), at least two annular baffle plates (7) and at least one disc-shaped baffle disc (8), wherein bypass holes (24 and 25) are formed between perforation holes (20a, 20b, 21a and 21b) of each reaction tube on the annular baffle plates (7) and the disc-shaped baffle discs (8). Through the tubular fixed bed reactor, the problem can be solved well; the tubular fixed bed reactor is applicable to industrial production of vinyl acetate through an ethylene gas phase method.
Description
Technical field
The utility model relates to for the synthetic calandria type fixed bed reactor of vinyl acetate.Specifically, relate to a kind of calandria type fixed bed reactor of producing vinyl acetate for ethene vapor phase method.
Background technology
Vinyl acetate (having another name called vinylacetate or vinyl acetate) is a kind of Organic Chemicals that extensive use is worth that has, by self-polymerization or with other monomer copolymerization, can generate the products such as polyvinyl alcohol (PVA), vinyl acetate/ethylene copolymer (VAE) and vinyl chloride/acetate ethylene copolymer (PVCA).The purposes of these products is very extensive, generally can be used for bonding agent, the cementing agent of paper or fabric, paint, ink, leather processing, emulsifying agent, water-solubility membrane, soil conditioner etc.Vinyl acetate is as intermediate, and the expansion along with the non-fiber art application of polyvinyl alcohol, improves constantly the needs of vinyl acetate.The demand of future China vinyl acetate is by the speed increment with 8%.
At present, vinyl acetate main production route is ethylene process and acetylene method.It is that to take the gas phase mixture of ethene, acetic acid and oxygen be raw material that ethylene process is produced vinyl acetate, and under uniform temperature and pressure condition, by the fixed bed of catalyst is housed, generation vinyl acetate reacts.Acetylene method can be divided into again two kinds of carbide acetylene method and gas acetylene methods by raw material sources.There is serious environmental issue in carbide acetylene method, gas acetylene method exists long flow path, plant investment is large, technical difficulty is large shortcoming.And in acetylene method vinyl acetate, aldehydes content, higher than ethylene process, although this class aldehydes absolute content is not high, has larger impact to polymerisation.Therefore acetylene method only just has certain competitiveness at calcium carbide and natural gas resource than more rich area.Ethene gas phase rule is because manufacturability, good economy performance are occupied an leading position, and production capacity surpasses 85% of vinyl acetate total productive capacity.Therefore ethene vapor phase method is produced the attention that vinyl acetate technique is more and more subject to everybody.
Patent CN102381966 discloses a kind of method for producing vinyl acetate.Proposition adds the method for inert gas to improve the explosion limit of oxygen in recyclegas, expand the temperature province of reaction system, improve reaction system oxygen concentration, thereby reduction reaction temperature, extending catalyst service life, improve the selective of vinyl acetate, reduce production costs, improve vinyl acetate output.
Patent CN1224000 discloses a kind of method of producing vinyl acetate.Also be to have proposed reduction ethylene loss amount from technological angle, raising vinyl acetate is selective, the method for yield.
Patent CN202113842 discloses a kind of novel fixed bed reactors of synthesizing vinyl acetate.This reactor has improved heat exchanger effectiveness to a certain extent, can effectively avoid the generation of " temperature runaway " phenomenon, has also reduced the consumption of thermophore, has reduced the running cost of device.But in the method, there is the shortcomings such as processing difficulties, cost of equipment height.
It is exothermic reaction that ethene vapor phase method is produced vinyl acetate, and reaction liberated heat need be removed in time, and a good reaction condition just can be provided, thereby reaches higher selective and yield.And that calandria type fixed bed reactor has is easy to operate, reaction tube inner catalyst mechanical wear is little, moves the advantages such as thermal velocity is fast, is particularly useful for ethene vapor phase method and produces vinyl acetate reaction system.In recent years, along with the continuous expansion of vinyl acetate production scale, reactor diameter constantly increases, and even, rapid moving heat problem just becomes one of key issue of engineering development.This is summed up as again the problem that is uniformly distributed of reactor inner fluid.If fluid can not be uniformly distributed, heat can not be removed in time, form temperature runaway, cause local temperature too high, not only affect the utilization ratio of catalyst and reactor, affect selective, the yield of object product, and may cause the damage of reactor, finally affect the safe operation of device.
Summary of the invention
Technical problem to be solved in the utility model is in conventional art, to exist heat transferring medium between major diameter calandria type fixed bed reactor shell side pipe to flow inhomogeneous, there is larger flow dead in shell side, cause reactor to exist heat exchange efficiency not high, the shortcoming that radial temperature is bigger than normal, thereby the problem that causes the selective of vinyl acetate and yield reduction, provides a kind of reactor of producing vinyl acetate for ethene vapor phase method.This reactor has even fluid distribution, and flow dead is little, and heat exchanger effectiveness is high, and catalyst utilization is high, and conversion ratio is high, and object product vinyl acetate is selectively good, and device is manufactured the advantages such as simple.
For addressing the above problem, the technical solution adopted in the utility model is as follows: for the synthetic calandria type fixed bed reactor of vinyl acetate, comprise reactor shell (1), reaction tube (2a, 2b, 2c), heat transport fluid import guide shell (3), heat transport fluid outlet guide shell (4), at least two ring-type deflection plates (7) and at least one plate-like baffling dish (8), described deflection plate (7) and baffling dish (8) are along reaction tube (2a, 2b, 2c) axial alternative arrangement, on deflection plate (7) and baffling dish (8), have for reaction tube (2a, 2b, perforation (20a 2c) passing, 20b, 21a, 21b), each reaction tube perforation (20a wherein, 20b, 21a, 21b), open bypass opening (24, 25), described reaction tube (2a, 2b, 2c) is fixed between upper perforated plate (6) and lower perforated plate (5), described reactor shell (1) top is provided with material inlet (11), bottom is provided with product discharging opening (13), middle part is provided with heat transport fluid import guide shell (3), heat transport fluid outlet guide shell (4), wherein heat transport fluid import guide shell (3) is positioned at reaction tube (2a, 2b, 2c) on lower end cylindrical shell (1) wall, the outer side surface (19) of heat transport fluid import guide shell (3) is provided with thermophore entrance (9), heat transport fluid entrance (9) is by the import aperture (16) and reaction tube (2a that arrange on heat transport fluid import guide shell (3) and inner side cylindrical shell (1) wall, 2b, gap 2c) communicates, heat transport fluid outlet guide shell (4) is positioned at reaction tube (2a, 2b, 2c) on upper end cylindrical shell (1) wall, the outer side surface (23) of heat transport fluid outlet guide shell (4) is provided with heat transport fluid outlet (10), on cylindrical shell (1) wall of inner side, have outlet aperture (17), thermophore outlet (10) exports by heat transport fluid the outlet aperture (17) arranging on guide shell (4) and inner side cylindrical shell (1) wall and communicates with the gap between reaction tube, described upper perforated plate (6) top charging aperture (11) below is provided with feed distributor (12), lower perforated plate (5) is positioned at discharging opening (13) top, and catalyst is contained in reaction tube (2a, 2b, 2c), catalyst bottom and top are filled to respectively few one deck inert ceramic balls (15a, 15b, 15c, 22a, 22b, 22c), reaction tube lower surface is provided with catalyst bracing or strutting arrangement (18).
In technique scheme, many one than the number of plate-like baffling dish (8) of the number of preferred described ring-type deflection plate (7).
In technique scheme, preferably ring-type deflection plate (7) is loop configuration, and described plate-like baffling dish (8) is circular configuration.
In technique scheme, preferred described baffle ring (7) and the perforation of the reaction tube on baffling dish (8) (20a, 20b, 21a, 21b) equilateral triangle are evenly distributed.
Upper each reaction tube perforation of preferred described baffle ring (7) and baffling dish (8) (20a in technique scheme, 20b, 21a, 21b) between open the bypass opening (24 for heat transport fluid process, 25), each reaction tube perforation (20a, 20b, 21a, 21b) be uniformly distributed 6 bypass openings (24 around, 25), bypass opening (24,25) is any one in circular, square, ellipse.
In technique scheme, preferred described bypass opening (24,25) is arranged between two parties between reaction tube perforation (20a, 20b, 21a, 21b), and diameter phi 1 is 1 ~ 3mm, and the percent opening of reaction tube distributed areas bypass opening is 0.1 ~ 1%.Upper bypass opening (24) the region annular radii R1 for heat transport fluid process of baffle ring (7) is greater than baffle ring radius R 2, and R1/ R2 is 1.2 ~ 1.5.
In technique scheme, upper bypass opening (25) the zone radius R3 for heat transport fluid process of preferred described baffling dish (8) is less than baffling dish radius R 4, and R3/ R4 is 0.4 ~ 0.8.
The calandria type fixed bed reactor of producing vinyl acetate for ethene vapor phase method of the present utility model, deflection plate,, baffling dish, heat transport fluid import guide shell, heat transport fluid outlet guide shell etc. are all the technical measures that adopt in order to strengthen the heat-transfer effect of calandria type fixed bed reactor shell-side fluid, wherein traditional deflection plate and baffling dish can increase the less turbulence of shell-side fluid, improve the coefficient of heat transfer, but also can cause regional area fluid flow impedes, turbulence strength decreased, form flow dead, cause larger radial temperature difference.The calandria type fixed bed reactor of producing vinyl acetate for ethene vapor phase method of the present utility model, by flowing, between the perforation of dead zone area reaction tube, the bypass opening axially passing for heat transport fluid is set on deflection plate and baffling dish, can reduce the flow dead of shell-side fluid, improve regional area turbulence intensity, improve the coefficient of heat transfer, dwindle radial temperature difference, when especially high pressure saturation water is as heat transport fluid, in reactor shell after heat exchange, part is evaporated to water vapour and forms biphase gas and liquid flow, water vapour is easily assembled at deflection plate place and is formed flow dead, affect heat transfer effect, on deflection plate and baffling dish bypass opening the part gas-vapor mix that is arranged so that on the one hand along deflection plate, do Radial Flow, along the bypass opening on deflection plate, do axial flow on the one hand, thereby reduced the existence of flow dead.Thereby reactor has even fluid distribution, the advantage such as flow dead is little, and heat exchange area utilization rate is high, and heat transfer efficiency is high, and radial temperature difference is little.The uniformity maximum deviation that fluid distributes on same radial section is 4.5%, has obtained good technique effect.
Accompanying drawing explanation
Fig. 1 is the utility model calandria type fixed bed reactor schematic diagram;
Fig. 2 is the A-A direction top view of the utility model heat transport fluid import guide shell (3);
Fig. 3 is the C-C directional profile figure of the utility model heat transport fluid import guide shell (3);
Fig. 4 is the B-B direction top view of the utility model heat transport fluid outlet guide shell (4);
Fig. 5 is the D-D directional profile figure of the utility model heat transport fluid outlet guide shell (4);
Fig. 6 is the front view of baffle ring of the present utility model (7);
Fig. 7 is the top view of baffle ring of the present utility model (7);
Fig. 8 is the front view of baffling dish of the present utility model (8);
Fig. 9 is the top view of baffling dish of the present utility model (8);
In Fig. 1,1 is reactor shell; 2 is reaction tube; 3 is heat transport fluid import guide shell; 4 is heat transport fluid outlet guide shell; 5 is lower perforated plate; 6 is upper perforated plate; 7 is deflection plate; 8 is baffling dish; 9 is thermophore entrance; 10 is thermophore outlet; 11 is charging aperture; 12 is feed distributor; 13 is discharging opening; 14 unload outlet for catalyst; 15 is reaction tube bottom inert ceramic balls; 16 is import aperture; 17 is outlet aperture; 20 is deflection plate perforation; 21 is baffling disk perforation; 22 is reaction tube top inert ceramic balls.Reaction tube does not all illustrate, and only take three reaction tube 2a, 2b, 2c is representative.
In Fig. 2,19 is the outer side surface of heat transport fluid import guide shell (3), and arrow represents fluid flow direction.
In Fig. 3,18 is catalyst support spring or grid.
In Fig. 4,23 outer side surfaces for heat transport fluid outlet guide shell (4), arrow represents fluid flow direction.
In Fig. 7,24 is the bypass opening on deflection plate (7), and R1 is ring radius in bypass opening region, and R2 is ring radius in deflection plate.
In Fig. 9,25 is the bypass opening on baffling dish (8), and R3 is bypass opening zone radius, and R4 is baffling dish radius.
Below by embodiment, the utility model is further elaborated, but is not limited only to the present embodiment.
The specific embodiment
[embodiment 1]
Press Fig. 1, calandria type fixed bed reactor internal diameter is 3800mm.Heat transport fluid is high pressure saturation water, 2 of deflection plates, and 1, baffling dish, reaction tube arranges ring-type deflection plate bottom, deflection plate and the axial cross arrangement of baffling rim reaction tube, bypass opening φ 1 is 2mm, R1 is 1400mm, R2 is 1000mm, and R3 is 680mm, and R4 is 1580mm; The high 800mm of heat transport fluid import guide shell, width is 150mm, 20 of inboard cylinder body wall face upper inlet apertures, diameter 70mm; The high 1000mm of heat transport fluid outlet guide shell, width is 150mm, 20 of inboard cylinder body wall face upper outlet apertures, diameter 80mm; Reaction tube inner catalyst top and bottom respectively fill one deck diameter 3mm porcelain ball, high 150mm, and catalyst bracing or strutting arrangement is spring supporting.Under above structural parameters, the calandria type fixed bed reactor of ethene vapor phase method being produced to vinyl acetate by the utility model designs, and can obtain comparatively ideal shell-side fluid flow effect.The calandria type fixed bed reactor of pressing the design of the utility model method, on its radial section, the mobile uniformity maximum deviation of fluid is 4.5%.
[embodiment 2]
Press Fig. 1, calandria type fixed bed reactor internal diameter is 4500mm.Heat transport fluid is high pressure saturation water, 3 of deflection plates, and 2, baffling dish, reaction tube arranges ring-type deflection plate bottom, deflection plate and the axial cross arrangement of baffling rim reaction tube, bypass opening φ 1 is 3mm, R1 is 1500mm, R2 is 1250mm, and R3 is 1000mm, and R4 is 1800mm; The high 900mm of heat transport fluid import guide shell, width is 150mm, 22 of inboard cylinder body wall face upper inlet apertures, diameter 140mm; The high 1100mm of heat transport fluid outlet guide shell, width is 150mm, 22 of inboard cylinder body wall face upper outlet apertures, diameter 150mm; Reaction tube inner catalyst top and bottom respectively fill one deck diameter 3mm porcelain ball, high 100mm, and catalyst bracing or strutting arrangement is spring supporting.Under above structural parameters, the calandria type fixed bed reactor of ethene vapor phase method being produced to vinyl acetate by the utility model designs, and can obtain comparatively ideal shell-side fluid flow effect.The calandria type fixed bed reactor of pressing the design of the utility model method, on its radial section, the mobile uniformity maximum deviation of fluid is 5.3%.
[embodiment 3]
Press Fig. 1, calandria type fixed bed reactor internal diameter is 5500mm.Heat transport fluid is high pressure saturation water, 2 of deflection plates, and 1, baffling dish, reaction tube arranges ring-type deflection plate bottom, deflection plate and the axial cross arrangement of baffling rim reaction tube, bypass opening φ 1 is 1mm, R1 is 2250mm, R2 is 1500mm, and R3 is 1800mm, and R4 is 2300mm; The high 1100mm of heat transport fluid import guide shell, width is 200mm, 28 of inboard cylinder body wall face upper inlet apertures, diameter 110mm; The high 1200mm of heat transport fluid outlet guide shell, width is 200mm, 28 of inboard cylinder body wall face upper outlet apertures, diameter 130mm; Reaction tube inner catalyst top and bottom respectively fill one deck diameter 3mm porcelain ball, high 200mm, and catalyst bracing or strutting arrangement is spring supporting.Under above structural parameters, the calandria type fixed bed reactor of ethene vapor phase method being produced to vinyl acetate by the utility model designs, and can obtain comparatively ideal shell-side fluid flow effect.The calandria type fixed bed reactor of pressing the design of the utility model method, on its radial section, the mobile uniformity maximum deviation of fluid is 5.9%.
[comparative example 1]
Calandria type fixed bed reactor internal diameter is 3800mm.From embodiment 1 unique different be on deflection plate, not open bypass opening, high pressure saturation water directly enters reactor by inlet tube, and by the direct outflow reactor of outlet, other structural parameters are constant.At all conditions, all under the condition identical with embodiment 1, on its radial section, the mobile uniformity maximum deviation of fluid is 6.5%.
[comparative example 2]
Calandria type fixed bed reactor internal diameter is 4500mm.From embodiment 2 unique different be on deflection plate, not open bypass opening, high pressure saturation water directly enters reactor by inlet tube, and by the direct outflow reactor of outlet, other structural parameters are constant.At all conditions, all under the condition identical with embodiment 2, on its radial section, the mobile uniformity maximum deviation of fluid is 6.9%.
[comparative example 3]
Calandria type fixed bed reactor internal diameter is 5500mm.From embodiment 3 unique different be on deflection plate, not open bypass opening, high pressure saturation water directly enters reactor by inlet tube, and by the direct outflow reactor of outlet, other structural parameters are constant.At all conditions, all under the condition identical with embodiment 3, on its radial section, the mobile uniformity maximum deviation of fluid is 7.5%.
Claims (8)
1. for the synthetic calandria type fixed bed reactor of vinyl acetate, comprise reactor shell (1), reaction tube (2a, 2b, 2c), heat transport fluid import guide shell (3), heat transport fluid outlet guide shell (4), at least two ring-type deflection plates (7) and at least one plate-like baffling dish (8), described deflection plate (7) and baffling dish (8) are along reaction tube (2a, 2b, 2c) axial alternative arrangement, on deflection plate (7) and baffling dish (8), have for reaction tube (2a, 2b, perforation (20a 2c) passing, 20b, 21a, 21b), each reaction tube perforation (20a wherein, 20b, 21a, 21b), open bypass opening (24, 25), described reaction tube (2a, 2b, 2c) is fixed between upper perforated plate (6) and lower perforated plate (5), described reactor shell (1) top is provided with material inlet (11), bottom is provided with product discharging opening (13), middle part is provided with heat transport fluid import guide shell (3), heat transport fluid outlet guide shell (4), wherein heat transport fluid import guide shell (3) is positioned at reaction tube (2a, 2b, 2c) on lower end cylindrical shell (1) wall, the outer side surface (19) of heat transport fluid import guide shell (3) is provided with thermophore entrance (9), heat transport fluid entrance (9) is by the import aperture (16) and reaction tube (2a that arrange on heat transport fluid import guide shell (3) and inner side cylindrical shell (1) wall, 2b, gap 2c) communicates, heat transport fluid outlet guide shell (4) is positioned at reaction tube (2a, 2b, 2c) on upper end cylindrical shell (1) wall, the outer side surface (23) of heat transport fluid outlet guide shell (4) is provided with heat transport fluid outlet (10), on cylindrical shell (1) wall of inner side, have outlet aperture (17), thermophore outlet (10) exports by heat transport fluid the outlet aperture (17) arranging on guide shell (4) and inner side cylindrical shell (1) wall and communicates with the gap between reaction tube, described upper perforated plate (6) top charging aperture (11) below is provided with feed distributor (12), lower perforated plate (5) is positioned at discharging opening (13) top, and catalyst is contained in reaction tube (2a, 2b, 2c), catalyst bottom and top are filled to respectively few one deck inert ceramic balls (15a, 15b, 15c, 22a, 22b, 22c), reaction tube lower surface is provided with catalyst bracing or strutting arrangement (18).
2. calandria type fixed bed reactor according to claim 1, many one than the number of plate-like baffling dish (8) of the number that it is characterized in that described ring-type deflection plate (7).
3. a kind of calandria type fixed bed reactor for vinyl acetate according to claim 2, is characterized in that described ring-type deflection plate (7) is for loop configuration, and described plate-like baffling dish (8) is circular configuration.
4. calandria type fixed bed reactor according to claim 2, is characterized in that described baffle ring (7) and the perforation of the reaction tube on baffling dish (8) (20a, 20b, 21a, 21b) equilateral triangle are evenly distributed.
5. calandria type fixed bed reactor according to claim 2, is characterized in that upper each reaction tube perforation of described baffle ring (7) and baffling dish (8) (20a, 20b, 21a, 21b), open the bypass opening (24,25) for heat transport fluid process, each reaction tube perforation (20a, 20b, 21a, 21b) be uniformly distributed 6 bypass openings (24,25) around, bypass opening (24,25) is any one in circular, square, ellipse.
6. calandria type fixed bed reactor according to claim 5, is characterized in that described bypass opening (24,25) is at reaction tube perforation (20a, 20b, 21a, 21b) between arrange between two parties, diameter phi 1 is 1 ~ 3mm, and the percent opening of reaction tube distributed areas bypass opening is 0.1 ~ 1%.
7. calandria type fixed bed reactor according to claim 5, is characterized in that upper bypass opening (24) the region annular radii R1 for heat transport fluid process of described baffle ring (7) is greater than baffle ring radius R 2, and R1/ R2 is 1.2 ~ 1.5.
8. calandria type fixed bed reactor according to claim 5, is characterized in that upper bypass opening (25) the zone radius R3 for heat transport fluid process of described baffling dish (8) is less than baffling dish radius R 4, and R3/ R4 is 0.4 ~ 0.8.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201320587303.9U CN203494494U (en) | 2013-09-24 | 2013-09-24 | Tubular fixed bed reactor applicable to synthesis of vinyl acetate |
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| CN201320587303.9U CN203494494U (en) | 2013-09-24 | 2013-09-24 | Tubular fixed bed reactor applicable to synthesis of vinyl acetate |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104190328A (en) * | 2014-08-12 | 2014-12-10 | 中国天辰工程有限公司 | Reactor used for preparing gas-phase hydrogen cyanide |
| CN106237966A (en) * | 2016-08-23 | 2016-12-21 | 南京大学 | The reactor of aromatic aldehyde is produced for the oxidation of toluene class material |
-
2013
- 2013-09-24 CN CN201320587303.9U patent/CN203494494U/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104190328A (en) * | 2014-08-12 | 2014-12-10 | 中国天辰工程有限公司 | Reactor used for preparing gas-phase hydrogen cyanide |
| CN106237966A (en) * | 2016-08-23 | 2016-12-21 | 南京大学 | The reactor of aromatic aldehyde is produced for the oxidation of toluene class material |
| CN106237966B (en) * | 2016-08-23 | 2018-11-09 | 南京大学 | The reactor of production aromatic aldehyde is aoxidized for toluene substance |
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