CN102258962B - Gas solid phase catalytic reactor - Google Patents
Gas solid phase catalytic reactor Download PDFInfo
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Abstract
The invention discloses a gas solid phase catalytic reactor. The gas solid phase catalytic reactor comprises a shell of which the upper part is provided with an inlet and the lower part is provided with an outlet, catalytic bed assemblies and flower plates provided with passage ports; each catalytic bed assembly comprises an inlet distribution member with small holes, an outlet distribution member with small holes and a seal plate; the seal plate is arranged on the top of the inlet distribution member and the outlet distribution member; the gap between the inlet distribution member and the outlet distribution member is provided with a catalytic bed filled with the catalyst; the other side of the inlet distribution member is a fluid inlet passage which is communicated with an inlet; and the other side of the outlet distribution member is a fluid outlet passage which is communicated with a passage port on each flower plate; and the flower plates are fixed on the lower part in the shell, and the lower end of each inlet distribution member, the lower end of each outlet distribution member and the flower plate are hermetically sealed. The formed bed is extremely low in pressure drop, can effectively save energy and reduce consumption, and can be widely applied to petrochemical industry, inorganic chemistry industry, or organic chemical industry.
Description
Technical field
The present invention relates to be used in the chemical field fixed bed catalytic reactor of gas-solid catalysis.
Background technology
In chemical industry and petrochemical industry, fixed bed catalytic reactor is a kind of widely used nucleus equipment, in synthetic ammonia, sulfuric acid, methyl alcohol, catalytic reforming, ethylbenzene dehydrogenation, ethene and acetic acid reaction system ethyl acetate, isomerization, hydrofinishing or the like chemical process, the reactor pattern all has and adopts fixed bed.
Fixed bed catalytic reactor can be divided into axial flow reactor and radial reactor two big classes by the mode of fluid by bed.Fluid is called axial flow reactor with the direction of the reactor center axle indication reactor by beds.Fluid by the reactor of catalytic bed, is called radial reactor along radial direction or diametric(al).
Axial flow reactor is simple in structure, easy to use, but the fluid passage is subjected to the restriction of equipment cross section, causes bed pressure drop bigger, and is higher to the requirement of strength of catalyst simultaneously, generally uses under the condition of normal pressure, mesolow.Axially the bed pressure drop is as (1) formula:
Wherein: each symbol definition is as follows:
Δ P-bed pressure drop, Pa
The L-bed length, m
ε-bed porosity
ρ-fluid density, kg/m3
φ-particle shape factor
The equal-volume equivalent diameter of de-particle
The viscosity of μ-fluid, cP
The mass flow of w-fluid, kg/h
Radial reactor is compared with axial flow reactor, under the same time of staying, because bigger flow area and short flow process are arranged, therefore bed pressure drop is little, can use advantages such as catalyst particle, but must adopt compulsive means that gas is evenly distributed, internal structure is complicated, in the large-scale production process of negative pressure or mesohigh, it is a kind of novel fixed bed catalyst equipment.The radial bed pressure drop is as (2) formula:
Wherein each symbol definition is as follows:
Ri-radial bed internal diameter, m
Ro-radial bed external diameter, m
Other are the same.
Therefore radial reactor exists fluid even distribution problem vertically because the fluid flow area is big, and beds is thinner.If reacting gas is skewness in catalyst bed, will influence Temperature Distribution, CONCENTRATION DISTRIBUTION, heat endurance of reactor etc., also can cause the catalytic bed hot-spot, influence the production capacity of product quality and reactor.Radial reactor generally is made up of inside and outside porous distribution tube and housing, stows catalyst between the inside and outside distribution tube, and the top of the tube that distributes is left one section not perforate and partly constituted catalyst sealing.In order to prevent the backflow of reacting gas, behind the deflection of having considered catalyst, catalyst sealing must leave enough height, in order to avoid the short circuit of catalyst decline causing gas causes the decline of output and conversion ratio; The catalyst sealing height is too much, and the overstand of reacting gas can cause the increase of side reaction again, and this moment, the activity in catalyst sealing district often can not effectively be utilized.Many patents have been described the mode of various fluids control, for example CN85103262, CN91110640.5, CN02820795.5 or as US2634194, US3533754, US4181701, US4478793.
Axial-radial flow reactor is a kind of radial reactor that adopts the novelty of catalyst self-sealing structure at the bed top, it equals proposition first in 1981 by Zardi, as US4372920, US4405562, be that discharge is than the low certain height of gas-distributing pipe, so that the top of radial bed causes the diameter of axle to flow to two dimension.This catalyst sealing had both been simplified the hermetically-sealed construction on radial bed top, had made full use of reactor inner space again, can improve conversion ratio, also helped simultaneously to reduce the caused side reaction in catalyst sealing dead band, had further reduced the resistance of bed simultaneously.
Generally speaking, why people reduce bed resistance as far as possible to satisfying under the reaction condition, The key factor still can be saved energy and reduce the cost, because a large amount of courses of reaction all is the circular response process, after separating product, a large amount of unreacted reactants must be compressed again the Returning reactor inlet, bed pressure drop is directly related with the circulation power consumption, reduces the economy that pressure drop means the process that improved.For example in the ammonia synthesis process, ammonia net value is 12-18% only generally, and a large amount of hydrogen and nitrogen gas needs circulation; The naphtha catalytic reforming, hydrogen/oil mol ratio 10-30 times, a large amount of hydrogen needs circulation, and pressure drop means the economy of high process for a short time.
But the industrial bed resistance that how further to reduce for example drops to the order of magnitude of 1KPa, and obvious above-mentioned type of reactor is to be difficult to reach with the mode of economical rationality.Obvious above-mentioned industrial requirement is true the existence, the catalytic burning of normal pressure tail gas for example, the catalytic burning of the atmosphere volatile matter of industrial solvent etc.Active demand proposes a kind of simple and easy to do gas-solid catalyst reactor of ultra low dropout.
Summary of the invention
The objective of the invention is to propose a kind of gas solid catalytic reactor, to overcome the above-mentioned defective that prior art exists.
Gas solid catalytic reactor of the present invention comprises that top is provided with the card that inlet, bottom are provided with cylindrical shell, the catalytic bed assembly of outlet and are provided with the passway;
Described catalytic bed assembly is by in the housing 1 of mechanical method fixation between entrance and exit, and coaxial with housing;
Described catalytic bed assembly comprises: be provided with aperture the import distributed component, be provided with the outlet distributed component and the sealing plate of aperture, import distributed component and outlet distributed component are coaxial, sealing plate is arranged on the top of import distributed component and outlet distributed component, gap between import distributed component and the outlet distributed component is the catalytic bed of catalyst filling, the opposite side of import distributed component is the fluid inlet channel that is connected with inlet, the fluid issuing passage of the opposite side of outlet distributed component for being connected with passway on the card;
Described card is fixed on the bottom in the housing, and the lower end and the described card of the lower end of import distributed component, outlet distributed component are tightly connected.
Gas-solid catalyst reactor of the present invention, catalytic bed is divided into sheet or central column, because its thickness is less, length and width are bigger, so flow path of formed bigger flow area, lacking, the bed that is constituted has extremely low pressure drop, can effectively save energy and reduce the cost, and can be widely used among petrochemical industry, inorganic chemistry industry or the organic chemical industry.
Description of drawings
Fig. 1 is the gas solid catalytic reactor structural representation.
Fig. 2 is card and catalytic bed modular construction schematic diagram.
Fig. 3 is laminated structure reactor cross section figure.
Fig. 4 is a central column structural response device profile.
The specific embodiment
Referring to Fig. 1 and Fig. 2, gas solid catalytic reactor of the present invention comprises that top is provided with inlet 101, the bottom is provided with cylindrical shell 1, catalytic bed assembly 2 that exports 102 and the card 3 that is provided with passway 301;
Described catalytic bed assembly 2 by mechanical method fixation at inlet 101 with export in the housing 1 between 102, and coaxial with housing 1;
Described mechanical means is conventional, as: adopt anchor ear that catalytic bed assembly 2 is fixed on the inwall of cylindrical shell 1, perhaps adopt carriage catalytic bed assembly 2 to be fixed on the inwall etc. of cylindrical shell 1;
Described catalytic bed assembly 2 comprises: be provided with the import distributed component 5 of aperture, the outlet distributed component 6 that is provided with aperture and sealing plate 7, import distributed component 5 and outlet distributed component 6 are coaxial, sealing plate 7 is arranged on the top of import distributed component 5 and outlet distributed component 6, gap between import distributed component 5 and the outlet distributed component 6 is the catalytic bed 8 of catalyst filling, the opposite side of import distributed component 5 is the fluid inlet channel 602 that is connected with inlet, the fluid issuing passage 601 of the opposite side of outlet distributed component 6 for being connected with passway 301 on the card;
Described card 3 is fixed on the bottom in the housing 1, and the lower end and the described card 3 of the lower end of import distributed component 5, outlet distributed component 6 are tightly connected;
Preferably, referring to Fig. 1 and Fig. 2, catalytic bed assembly 2 is a laminated structure, described import distributed component 5 is two flat boards that are provided with aperture, outlet distributed component 6 is two flat boards that are provided with aperture, 6 coaxial being arranged between the import distributed component 5 of outlet distributed component, between import distributed component 5 and the outlet distributed component 6 is the catalytic bed 8 of catalyst filling, as the gap between two flat boards of outlet distributed component 6 is fluid issuing passage 601, and sealing plate 7 is arranged on the top and the bottom of import distributed component 5 and outlet distributed component 6;
Described card 3 is fixed on the bottom in the housing 1, and the lower end and the described card 3 of the lower end of import distributed component 5, outlet distributed component 6 are tightly connected, and fluid issuing passage 601 is connected with passway 301;
Unstripped gas enters reactor by the inlet 101 on reactor top, enters catalytic bed 8 by import distributed component 5 then, enters fluid issuing passage 601 by outlet distributed component 6 again, discharges reactor by the outlet 102 of reactor lower part then;
Perhaps, referring to Fig. 1～Fig. 4, catalytic bed assembly 2 is the central column structure, described import distributed component 5 and outlet distributed component 6 are pipe, import distributed component 5 is enclosed within outside the outlet distributed component 6, sealing plate 7 is arranged on the top of import distributed component 5 and outlet distributed component 6, is the catalytic bed 8 of catalyst filling between two pipes, is fluid issuing passage 601 as the pipe that exports distributed component 6;
Described card 3 is fixed on the bottom in the housing 1, and the lower end and the described card 3 of the lower end of import distributed component 5, outlet distributed component 6 are tightly connected, and fluid issuing passage 601 is connected with passway 301;
Unstripped gas enters reactor by the inlet 101 on reactor top, enters catalytic bed 8 by import distributed component 5 then, enters fluid issuing passage 601 by outlet distributed component 6 again, discharges reactor by the outlet 102 of reactor lower part then;
Further, the thickness of catalytic bed 8 is 30～300mm, preferably 100～300mm;
Further, described import distributed component 5 and outlet distributed component 6 are porous structure materials such as orifice plate, Johnson's net or silk screen, and the percent opening of porous material is 0.1～40%, preferably 10～25%, and the aperture is 0.5～10mm, preferably 1～5mm;
Described percent opening is defined as follows:
Percent opening=the porous material of porous material is in the total X 100% of the perforated area/porous material on the flow direction vertical plane on flow direction hangs down the plane.
Embodiment 1
The cis-butenedioic anhydride vent gas treatment
In benzene method air oxidation system maleic anhydride process, its composition and flow are as shown in table 1.
Certain company's cis-butenedioic anhydride tail gas of table 1
| Form | Content (%wt) |
| Benzene | 0.05 |
| Oxygen | 14 |
| Nitrogen | 74 |
| Water | 6.5 |
| Carbon monoxide | 1.6 |
| Carbon dioxide | 4.0 |
| Flow | 20000kg/h |
| Temperature | 45℃ |
| Pressure | 10KPa |
The structure of reactor parameter:
Diameter: 1000mm adopts Fig. 1 and central column catalytic bed assembly 2 shown in Figure 3, and quantity is 15, and import distributed component 5 is a pipe, and diameter is 150mm, and outlet distributed component 6 is a pipe, and diameter is 50mm, and the percent opening of porous material is 25%, and the aperture is 1.8mm;
Catalyst is catalyst based with the Cu of Mn remodeling, and granularity Φ 2, length 6-12mm, and reaction temperature 320-600 ℃, the reactor assembly pressure drop has reduced by 400% less than 1KPa than existing reactors.
Described catalyst can adopt commercially produced product, as the VOC of Shell Co. Ltd catalyst.
Embodiment 2
Adopt the laminated structure catalytic bed assembly of Fig. 1 and Fig. 3.
The percent opening of porous material is 10%, and the aperture is 5mm; The thickness of catalytic bed 8 is 300mm;
Other are identical with embodiment 1, and the reactor assembly pressure drop has reduced by 400% less than 1KPa than existing reactors.
Claims (5)
1. gas solid catalytic reactor is characterized in that, described gas solid catalytic reactor comprises that top is provided with the card (3) that inlet (101), bottom are provided with cylindrical shell (1), the catalytic bed assembly (2) of outlet (102) and are provided with passway (301);
Described catalytic bed assembly (2) by mechanical method fixation at inlet (101) with export in the housing (1) between (102), and coaxial with housing (1);
Described catalytic bed assembly (2) comprising: the import distributed component (5) that is provided with aperture, be provided with the outlet distributed component (6) and the sealing plate (7) of aperture, import distributed component (5) and outlet distributed component (6) are coaxial, sealing plate (7) is arranged on the top of import distributed component (5) and outlet distributed component (6), gap between import distributed component (5) and the outlet distributed component (6) is the catalytic bed (8) of catalyst filling, the opposite side of import distributed component (5) is the fluid inlet channel (602) that is connected with inlet, the fluid issuing passage (601) of the opposite side of outlet distributed component (6) for being connected with passway (301) on the card;
Described card (3) is fixed on the bottom in the housing (1), the lower end and the described card (3) of the lower end of import distributed component (5) and outlet distributed component (6) are tightly connected, described catalytic bed assembly (2) is a laminated structure, described import distributed component (5) is two flat boards that are provided with aperture, outlet distributed component (6) is two flat boards that are provided with aperture, coaxial being arranged between the import distributed component (5) of outlet distributed component (6), between import distributed component (5) and the outlet distributed component (6) is the catalytic bed (8) of catalyst filling, as the gap between two flat boards of outlet distributed component (6) is fluid issuing passage (601), and sealing plate (7) is arranged on the top and the bottom of import distributed component (5) and outlet distributed component (6);
Described card (3) is fixed on the bottom in the housing (1), and the lower end and the described card (3) of the lower end of import distributed component (5), outlet distributed component (6) are tightly connected, and fluid issuing passage (601) is connected with passway (301).
2. gas solid catalytic reactor according to claim 1 is characterized in that, the thickness of catalytic bed (8) is 30～300mm.
3. gas solid catalytic reactor according to claim 2 is characterized in that, the thickness of catalytic bed (8) is 100～300mm.
4. according to each described gas solid catalytic reactor of claim 1～3, it is characterized in that, described import distributed component (5) and outlet distributed component (6) are orifice plate, Johnson's net or silk screen, and the percent opening of porous material is 0.1～40%, and the aperture is 0.5～10mm.
5. gas solid catalytic reactor according to claim 4 is characterized in that, the percent opening of porous material is 10～25%, and the aperture is 1～5mm.
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| CN 201110135700 CN102258962B (en) | 2011-05-24 | 2011-05-24 | Gas solid phase catalytic reactor |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1341585A (en) * | 2001-10-08 | 2002-03-27 | 华东理工大学 | Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment |
| CN1454970A (en) * | 2003-05-16 | 2003-11-12 | 华东理工大学 | Continuous catalytic reforming reactor |
| CN200955019Y (en) * | 2006-04-21 | 2007-10-03 | 中国石油天然气股份有限公司 | Synthesized multi-sectional radial cold-exciting type reactor |
| US7901640B2 (en) * | 2008-05-13 | 2011-03-08 | Uop Llc | Optimized counter-current flow baffle |
-
2011
- 2011-05-24 CN CN 201110135700 patent/CN102258962B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1341585A (en) * | 2001-10-08 | 2002-03-27 | 华东理工大学 | Reaction method of dimethyl benzene isomerization and methylbenzene disproportionation and its equipment |
| CN1454970A (en) * | 2003-05-16 | 2003-11-12 | 华东理工大学 | Continuous catalytic reforming reactor |
| CN200955019Y (en) * | 2006-04-21 | 2007-10-03 | 中国石油天然气股份有限公司 | Synthesized multi-sectional radial cold-exciting type reactor |
| US7901640B2 (en) * | 2008-05-13 | 2011-03-08 | Uop Llc | Optimized counter-current flow baffle |
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| CN102258962A (en) | 2011-11-30 |
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Address after: 201102 602, room 41, Lane 1458, long Ming Road, Minhang District, Shanghai. Co-patentee after: CHANGZHOU RUIHUA CHEMICAL ENG & TECH Co.,Ltd. Patentee after: Xu Zhigang Address before: 201102 602, room 41, Lane 1458, long Ming Road, Minhang District, Shanghai. Co-patentee before: CHANGZHOU RUIHUA CHEMICAL ENG&TECH CO.,LTD. Patentee before: Xu Zhigang |
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Effective date of registration: 20180418 Address after: 213000 room 398-1, No. 1718 middle Tongjiang Road, Xinbei District, Jiangsu, Changzhou Patentee after: CHANGZHOU RUIHUA CHEMICAL ENG & TECH Co.,Ltd. Address before: 201102 602, room 41, Lane 1458, long Ming Road, Minhang District, Shanghai. Co-patentee before: CHANGZHOU RUIHUA CHEMICAL ENG & TECH Co.,Ltd. Patentee before: Xu Zhigang |