CN102580626B - Double-shaft radial flow reactor - Google Patents
Double-shaft radial flow reactor Download PDFInfo
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- CN102580626B CN102580626B CN 201210073372 CN201210073372A CN102580626B CN 102580626 B CN102580626 B CN 102580626B CN 201210073372 CN201210073372 CN 201210073372 CN 201210073372 A CN201210073372 A CN 201210073372A CN 102580626 B CN102580626 B CN 102580626B
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Abstract
A double-shaft radial flow reactor comprises a shell (2) and a reactor internal part (3), wherein the reactor internal part (3) is located in the shell (2). A reactor inlet (1) and a reactor outlet (8) are disposed on the shell (2). The reactor internal part (3) comprises a distribution cylinder (4) and a gas collection cylinder (6), a catalyst bed (5) is arranged between the gas collection cylinder (6) and the distribution cylinder (4), and a reactor outlet (8) is communicated with the outlet end of the gas collection cylinder (6). The double-shaft radial flow reactor is characterized in that the upper end and the lower end of the reactor internal part (3) respectively form an upper axial reaction section (14) and a lower axial reaction section (16), and a radial reaction section (15) is formed between the upper axial reaction section (14) and the lower axial reaction section (16). A multi-hole upper cover and screen mesh (12) are installed at the upper end of the catalyst bed (5), and a multi-hole basket bottom and screen mesh (7) is installed at the lower end of the catalyst bed (5). The double-shaft radial flow reactor is simple in structure, good in reaction effect, capable of not only increasing reaction efficiency by more than 10% but also prolonging service life of the catalyst by more than 20% and remarkable in economic efficiency.
Description
Technical field
The present invention relates to a kind of gas reactor, especially a kind of reaction is more abundant, the reactor based on radial flow at no bias current and reaction dead angle, specifically a kind of double-shaft radial flow reactor.
Background technology
Many institutes hit and know, the exploitation of Radial Flow reactor and the history of using existing decades, what occur the earliest is that overall diameter is to flow reactor (seeing Fig. 1-1), be that air-flow (also can from the center to the periphery) from the periphery to the center all reacts by beds with radial direction, its great advantage is fluid resistance low (only being axial flow reactor 10%～50%), and can use the high activity catalyst particle, thereby promote the ability of reactor significantly.
Along with the development descendant of technology thinks that overall diameter reduces its utilization rate to the catalyst in reactor a district because factors such as sinking cause short circuit, so develop shaft radial flow reactors (seeing Fig. 1-2) again, namely cancel top cover and make this part catalyst be the section axial stream mode, so form the so-called diameter of axle to flow reactor.But the expansion along with reactor diameter increasing and range of application, and the accumulation of practical experience, find that this class reactor bottom b district also has problems: the one, there be " dead angle " in the part catalyst in the bottom butterfly end socket of large-scale reactor, causes the bias current of air-flow; Because factors such as the deflation of the pressurized of bottom catalyst and efflorescence more strengthen the degree of its bias current, this very easily causes b district catalyst overheating inactivation for some strong exothermal reactions, even sintering simultaneously; The 2nd, radial reactor needs setting to move hot cell when inner, during as cold pipe (plate) (seeing Fig. 1-3), need to arrange big or small header and tube connector in a district and b district, cold pipe (plate) is then arranged in middle primary area, therefore the Radial Flow in a district, b district and middle primary area has very big difference, and it is even more serious that there are problems such as bias current, dead angle in the b district like this.
Summary of the invention
The objective of the invention is to have bias current, dead angle and influence the problem of reaction efficiency at existing radial flow reactors, design a kind of double-shaft radial flow reactor that does not have bias current and reaction dead angle.
Technical scheme of the present invention is:
A kind of double-shaft radial flow reactor, it comprises shell 2 and reactor internals 3, reactor internals 3 are arranged in shell 2, described shell 2 is provided with reactor inlet 1 and reactor outlet 8, reactor internals 3 comprise distribute tube 4 and gas collecting jar with ground-on cover plate 6, between gas collecting jar with ground-on cover plate 6 and distribution tube 4, beds 5 is installed, reactor outlet 8 is connected with the port of export of gas collecting jar with ground-on cover plate 6, the top and bottom that it is characterized in that described reactor internals 3 respectively are formed with a upward axial conversion zone 14 and following axial conversion zone 16, are formed with radially conversion zone 15 between last axial conversion zone 14 and following axial conversion zone 16; Porous loam cake and silk screen 12 are installed in the upper end of described beds 5, and the lower end is equipped with at the bottom of the porous basket and silk screen 7; Reaction gas after reactor inlet 1 enters respectively from last axial conversion zone 14, down axial conversion zone 16 and radially conversion zone 15 enter that the reaction back flows into gas collecting jar with ground-on cover plate 6, the reactor outlet 8 outflow reactor shells 2 from being connected with gas collecting jar with ground-on cover plate 6 again the catalyst.
In the described beds 5 heat-transfering device 23 is installed also.
Described heat-transfering device 23 is formed by moving heat tubesheet 21, big header 18, little header 19, connecting tube 20, cooling fluid inlet pipe 17 and cooling fluid outlet 22, the import and export end that respectively moves heat tubesheet 21 connecting tube 20 by separately respectively is connected with corresponding little header 19, each little header 19 is connected with corresponding big header 18, and big header 18 is connected with corresponding cooling fluid inlet pipe 17 or cooling fluid outlet 22.
Describedly porous loam cake and the silk screen 12 that axial conversion zone 14 installed by not perforate section 11 and described beds 5 upper ends on the distribution tube of not perforate section 13, tube 4 epimeres that distribute on the gas collecting jar with ground-on cover plate on gas collecting jar with ground-on cover plate 6 tops and surrounded, and the upper bottom surface of gas collecting jar with ground-on cover plate 6 be can not air inlet closed structure.
The length L of not perforate section 13 on the described gas collecting jar with ground-on cover plate
2Be not less than the length L of not perforate section 11 on the tube that distributes
1, and 1≤L
2/ L
1≤ 10.
At the bottom of the porous basket that described down axial conversion zone 16 is installed by not perforate section 10 and described beds 5 lower ends under the distribution tube of not perforate section 9, tube 4 hypomeres that distribute under the gas collecting jar with ground-on cover plate of gas collecting jar with ground-on cover plate 6 bottoms and silk screen 7 surround, and the gas outlet, lower end of gas collecting jar with ground-on cover plate 6 is connected with reactor outlet 8 on the housing 2.
The length L of not perforate section 9 under the described gas collecting jar with ground-on cover plate
2' do not go up in the tube not perforate section 10L down that distributes
1' length, and 1≤L
2'/L
1'≤10.
At the bottom of described porous loam cake and silk screen 12 and the porous basket and the ventilation opening rate on the silk screen 7 be 1%～100%.For porous loam cake and silk screen 12, when percent opening reaches 100%, then equal to cancel loam cake and silk screen, this structure is often used at the reactor of simplifying.
Beneficial effect of the present invention:
The present invention has thoroughly eliminated the reaction dead angle, bottom that existing reactors exists, can not produce the air-flow bias current, more can not cause the part of catalyst to cross the heat inactivation sintering phenomenon, especially can eliminate the bias current dead angle problem that causes because of the tube sheet layout for the reactor that moves hot cell is installed.
The present invention is simple in structure, and reaction effect is good, not only can improve reaction efficiency more than 10%, and service life that can prolong catalyst more than 20%, and business efficiency is remarkable.
Description of drawings
Fig. 1 is the structural representation of existing radially reaction stream.
Wherein:
The existing overall diameter of Fig. 1-1 is to the structural representation of flow reactor.
Fig. 1-2 is that existing single shaft is to the structural representation that adds radial flow reactors.
Fig. 1-the 3rd, have move hot cell single shaft to the structural representation that adds radial flow reactors.
The structural representation of Fig. 2 double-shaft radial flow reactor of the present invention.
Wherein:
The structural representation of the double-shaft radial flow reactor that Fig. 2-1 ecto-entad of the present invention flows.
The structural representation of Fig. 2-2 double-shaft radial flow reactor that flows from inside to outside of the present invention.
Fig. 2-3 structural representation that has the double-shaft radial flow reactor of heat-transfering device of the present invention.
Fig. 3 is the common type structural representation of double-shaft radial flow reactor of the present invention.
Wherein:
Fig. 3-the 1st, the equivalent schematic diagram of Fig. 2-1.
Fig. 3-the 2nd, the equivalent schematic diagram of Fig. 2-2.
Fig. 3-the 3rd, the structural representation when being positioned at the same end of housing with the air inlet of Fig. 3-1 equivalence and gas outlet.
Fig. 3-the 4th, the structural representation when being positioned at the same end of housing with the air inlet of Fig. 3-2 equivalence and gas outlet.
The specific embodiment
The present invention is further illustrated below in conjunction with drawings and Examples.
Embodiment one.
Shown in Fig. 2-1,3-3.
A kind of double-shaft radial flow reactor, it comprises shell 2 and reactor internals 3, reactor internals 3 are arranged in shell 2, described shell 2 is provided with reactor inlet 1 and reactor outlet 8, reactor internals 3 comprise distribute tube 4 and gas collecting jar with ground-on cover plate 6, between gas collecting jar with ground-on cover plate 6 and distribution tube 4, beds 5 is installed, reactor outlet 8 is connected with the port of export of gas collecting jar with ground-on cover plate 6, the top and bottom of described reactor internals 3 respectively are formed with one and go up axial conversion zone 14 and following axial conversion zone 16, are formed with radially conversion zone 15 between last axial conversion zone 14 and following axial conversion zone 16; Porous loam cake and silk screen 12 are installed in the upper end of described beds 5, and the lower end is equipped with at the bottom of the porous basket and silk screen 7; Reaction gas after reactor inlet 1 enters respectively from last axial conversion zone 14, down axial conversion zone 16 and radially conversion zone 15 enter that the reaction back flows into gas collecting jar with ground-on cover plate 6, the reactor outlet 8 outflow reactor shells 2 from being connected with gas collecting jar with ground-on cover plate 6 again the catalyst.Gas collecting jar with ground-on cover plate 6 is positioned at the centre of the tube 4 that distributes, shown in Fig. 2-1, describedly porous loam cake and the silk screen 12 that axial conversion zone 14 installed by not perforate section 11 and described beds 5 upper ends on the distribution tube of not perforate section 13, tube 4 epimeres that distribute on the gas collecting jar with ground-on cover plate on gas collecting jar with ground-on cover plate 6 tops and surrounded, and the upper bottom surface of gas collecting jar with ground-on cover plate 6 be can not air inlet closed structure.The length L of not perforate section 13 on the described gas collecting jar with ground-on cover plate
2Be not less than the length L of not perforate section 11 on the tube that distributes
1, and 1≤L
2/ L
1≤ 10.At the bottom of the porous basket that described down axial conversion zone 16 is installed by not perforate section 10 and described beds 5 lower ends under the distribution tube of not perforate section 9, tube 4 hypomeres that distribute under the gas collecting jar with ground-on cover plate of gas collecting jar with ground-on cover plate 6 bottoms and silk screen 7 surround, and the gas outlet, lower end of gas collecting jar with ground-on cover plate 6 is connected with reactor outlet 8 on the housing 2.The length L of not perforate section 9 under the described gas collecting jar with ground-on cover plate
2' do not go up in the tube not perforate section 10L down that distributes
1' length, and 1≤L
2'/L
1'≤10.At the bottom of described porous loam cake and silk screen 12 and the porous basket and the ventilation opening rate on the silk screen 7 be 1%～100%.For porous loam cake and silk screen 12, when percent opening reaches 100%, then equal to cancel loam cake and silk screen, this structure is often used at the reactor of simplifying.
Shown in Fig. 2-1, reacting gas is entered by reactor inlet 1, a part gas in the axial flow mode through porous loam cake and silk screen 12, entering axle radial section 14 reacts in the back inflow gas collecting jar with ground-on cover plate 6 with catalytic bed, part gas with overall diameter to the type of flow through the tube 4 that distributes, enter in the gas collecting jar with ground-on cover plate 6 by the full radial section 15 in middle part, the passage that other some gas flows through between shell 2 and the distribution tube 4 flows down to down axial conversion zone 16, react in the back inflow gas collecting jar with ground-on cover plate 6 with the catalyst bed of axial flow mode through at the bottom of the porous frame of bottom and silk screen 7 and bottom, three strands of gases are all converged by gas collecting jar with ground-on cover plate 6, go out reactor through exporting 8.Upper end 11 at the tube 4 that distributes is equipped with not perforate section L1 and a L with lower end 10
1, in the top and bottom of gas collecting jar with ground-on cover plate 13, be equipped with not perforate section L2 and a L
2, constituted last axial direction part 14 and the following axial direction part 16 of top and bottom respectively by them, remaining then is middle full radial-flow section 15.
As Fig. 3-the 3rd of present embodiment equivalent structure, the entrance and exit of reactor is arranged on the same end of reactor shell, all the other are all identical or equivalent identical with Fig. 2-1.
Realize the even utilization of the whole catalyst of upper, middle and lower layer, must realize that full response device air-flow reasonably evenly distributes, for this reason, must carry out comprehensive hydrodynamics to whole reactor and calculate, thereby determine every structural parameters of reactor:
(1) each not perforate length L 1 .L2, L 1, L 2 distribute the height ratio of epimere and hypomere axle radial layer and the key parameter of corresponding tolerance distribution up and down for distribution tube and gas collecting jar with ground-on cover plate, must at first determine and distribute with the height ratio of the full radial layer 15 in centre and tolerance to adapt, realize the airflow uniform distribution of whole reactor.
(2) the perforate aperture d of basket and perforate quantity n also must be determined by calculating cooperate with each not perforate length L 1 .L2, L 1, L 2 at the bottom of distribution tube, gas collecting jar with ground-on cover plate, porous loam cake and the porous, to satisfy uniform requirement.
(3) the not perforate length L 2 of common gas collecting jar with ground-on cover plate, not perforate length L 1, the L 1 that L 2 is greater than atmolysis cylinder, the size of each numerical value and reactor diameter D, and height H, and ratio of height to diameter (H/D) is all directly related.L2/L1 and L 2/L 1 are between 1～10 times.
For perforate aperture d and the perforate quantity n at the bottom of atmolysis cylinder, gas collecting jar with ground-on cover plate, porous loam cake and the porous frame, then decided by calculating, the ventilation opening rate is 1%～100%, for porous loam cake and silk screen 12, when percent opening reaches 100%, then equal to cancel loam cake and silk screen, this structure is often used at the reactor of simplifying.Concrete number of aperture is general many between 1～100 every square decimeter.
Embodiment two.
As Fig. 2-2,3-4.
The difference of present embodiment and embodiment one is that the distribution tube 4 of present embodiment is arranged in gas collecting jar with ground-on cover plate, and the gas collecting jar with ground-on cover plate 6 of embodiment one is arranged in the tube 4 that distributes, reacting gas is entered by reactor inlet 1, a part gas in the axial flow mode through porous loam cake and silk screen 12, entering axle radial section 14 reacts in the gas collecting jar with ground-on cover plate 6 of inflow outer ring, back with catalytic bed, middle overall diameter is that direct distribution tube 6 from reactor center enters the gas collecting jar with ground-on cover plate by the full radial section 15 in middle part from inside to outside to the reaction gas of conversion zone, the full radial sections that other some gas flows through in the middle of the tube 4 that distributes directly enter into down axial conversion zone 16, react in the back inflow gas collecting jar with ground-on cover plate 6 with the catalyst bed of axial flow mode through at the bottom of the porous frame of bottom and silk screen 7 and bottom, three strands of gases are all converged by gas collecting jar with ground-on cover plate 6, go out reactor through exporting 8.
Embodiment three.
Shown in Fig. 2-3.
Present embodiment is also to be equipped with heat-transfering device 23 with the difference of implementing one, two in catalytic bed 5, heat-transfering device 23 is formed by moving heat tubesheet 21, big header 18, little header 19, connecting tube 20, cooling fluid inlet pipe 17 and cooling fluid outlet 22, the import and export end that respectively moves heat tubesheet 21 connecting tube 20 by separately respectively is connected with corresponding little header 19, each little header 19 is connected with corresponding big header 18, big header 18 is connected with corresponding cooling fluid inlet pipe 17 or cooling fluid outlet 22, shown in Fig. 2-3.The heat-transfering device of present embodiment both can be used for the reactor (embodiment one) of ecto-entad fluidal texture, also was applicable to the reactor of fluidal texture (embodiment two) from inside to outside.
Have the double-shaft radial reactor (seeing Fig. 2-3) that moves hot cold pipe (plate) in the catalyst bed for present embodiment, for realizing the even utilization of the whole catalyst of upper, middle and lower layer, must realize that full response device air-flow reasonably evenly distributes, for this reason, must carry out comprehensive hydrodynamics to whole reactor calculates, thereby determine every structural parameters of reactor, also need to count this moment moves heat pipe (plate) 21, size header 18,19, connecting tube 20, the diameter of axle of cooling fluid, 17,22 pairs of upper, middle and lower each section catalyst of turnover pipe is to flow resistance △ P
On With △ P
Down With intermediate radial flow resistance △ P
In Influence, in uniform fluid distribution calculates, must be included.
During concrete enforcement, on the basis of the basic block diagram of the double-shaft radial reactor of each figure shown in Fig. 2-1, Fig. 2-2 and Fig. 2-3, can also there be multiple variation in the flow direction and the walking upwards of radial flow that import and export at primary air, as shown in Figure 3.
(1) Fig. 3-1,3-2, for primary air is entered by the reactor upper end, (or opposite) flowed out in the lower end, and this belongs to И type stream, and the radial flow direction then can flow from outside to inside, or flow from inside to outside.
(2) Fig. 3-3,3-4 then are that primary air is passed in and out by the same end of reactor, can also can be П type stream all in the lower end all in the upper end, and the radial air flow direction then can be to flow from outside to inside or from inside to outside too.
(3) on the basis of above-mentioned И type and П type stream, what can there be various structures the inside of reactor moves hot cell (cooling tube, plate etc.) and the various and configuration header structure, all can realize purpose of the present invention.
(4) the double-shaft radial reactor of some simplification can be cancelled the porous loam cake, as long as design suitably can realize even distribution equally.
In addition, when specifically implementing, also can carry out equivalence to embodiment one to three and replace, with at the bottom of porous loam cake and silk screen 12 and the porous basket and the ventilation opening rate on the silk screen 7 be made as 100%, be equivalent to cancel loam cake and silk screen, become through hole.
The part that the present invention does not relate to all prior art that maybe can adopt same as the prior art is realized.
Claims (6)
1. double-shaft radial flow reactor, it comprises shell (2) and reactor internals (3), reactor internals (3) are arranged in shell (2), described shell (2) is provided with reactor inlet (1) and reactor outlet (8), reactor internals (3) comprise distribute tube (4) and gas collecting jar with ground-on cover plate (6), between gas collecting jar with ground-on cover plate (6) and distribution tube (4), beds (5) is installed, reactor outlet (8) is connected with the port of export of gas collecting jar with ground-on cover plate (6), the top and bottom that it is characterized in that described reactor internals (3) respectively are formed with upward axial conversion zone (14) and a following axial conversion zone (16), are formed with radially conversion zone (15) between last axial conversion zone (14) and following axial conversion zone (16); Porous loam cake and silk screen (12) are installed in the upper end of described beds (5), and the lower end is equipped with at the bottom of the porous basket and silk screen (7); Reaction gas after reactor inlet (1) enters respectively from last axial conversion zone (14), down axial conversion zone (16) and radially conversion zone (15) enter reaction back inflow gas collecting jar with ground-on cover plate (6), reactor outlet (8) the outflow reactor shell (2) from being connected with gas collecting jar with ground-on cover plate (6) again the catalyst; Describedly porous loam cake and the silk screen (12) that axial conversion zone (14) installed by not perforate section (11) and described beds (5) upper end on the distribution tube of not perforate section (13), tube (4) epimere that distributes on the gas collecting jar with ground-on cover plate on gas collecting jar with ground-on cover plate (6) top and surrounded, and the upper bottom surface of gas collecting jar with ground-on cover plate (6) be can not air inlet closed structure; At the bottom of the porous basket that described down axial conversion zone (16) is installed by not perforate section (10) and described beds (5) lower end under the distribution tube of not perforate section (9), tube (4) hypomere that distributes under the gas collecting jar with ground-on cover plate of gas collecting jar with ground-on cover plate (6) bottom and silk screen (7) surround, and the gas outlet, lower end of gas collecting jar with ground-on cover plate (6) is connected with reactor outlet (8) on the housing (2).
2. double-shaft radial flow reactor according to claim 1 is characterized in that also being equipped with in the described beds (5) heat-transfering device (23).
3. double-shaft radial flow reactor according to claim 2, it is characterized in that described heat-transfering device (23) is by moving heat pipe (21), big header (18), little header (19), connecting tube (20), cooling fluid inlet pipe (17) and cooling fluid outlet (22) are formed, respectively move advancing of heat pipe (21), the port of export connecting tube (20) by separately respectively is connected with corresponding little header (19), each little header (19) is connected with corresponding big header (18), and big header (18) is connected with corresponding cooling fluid inlet pipe (17) or cooling fluid outlet (22).
4. double-shaft radial flow reactor according to claim 1 is characterized in that the length L of not perforate section (13) on the described gas collecting jar with ground-on cover plate
2Be not less than the length L of not perforate section (11) on the tube that distributes
1, and 1≤L
2/ L
1≤ 10.
5. double-shaft radial flow reactor according to claim 1 is characterized in that the length L of not perforate section (9) under the described gas collecting jar with ground-on cover plate
2' do not go up in tube not perforate section (10) L down that distributes
1' length, and 1≤L
2'/L
1'≤10.
6. double-shaft radial flow reactor according to claim 1 is characterized in that at the bottom of described porous loam cake and silk screen (12) and the porous basket and the ventilation opening rate on the silk screen (7) is 1%～100%.
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| CN105582855A (en) * | 2014-10-23 | 2016-05-18 | 新煤化工设计院（上海）有限公司 | Radial-flow uniform-temperature methanation furnace with byproduct steam |
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| CN109603689B (en) * | 2018-12-26 | 2021-08-31 | 湖南安淳高新技术有限公司 | Axial radial reactor |
| CN109701456A (en) * | 2019-03-12 | 2019-05-03 | 江苏永大化工机械有限公司 | A kind of novel radial reactor |
| CN112403400A (en) * | 2020-10-27 | 2021-02-26 | 中国科学院过程工程研究所 | Radial flow tower equipment and application thereof |
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| CN102029129B (en) * | 2009-09-25 | 2013-01-23 | 华东理工大学 | Axial-radial flow gas-solid phase fixed bed catalytic reactor |
| JP5538023B2 (en) * | 2010-03-29 | 2014-07-02 | 東洋エンジニアリング株式会社 | Reactor |
| CN102166449B (en) * | 2011-03-17 | 2012-12-05 | 北京科净源科技股份有限公司 | Water treatment device with constant resistance regulation and control function and water treatment method thereof |
| CN202516537U (en) * | 2012-03-20 | 2012-11-07 | 南京国昌化工科技有限公司 | Double-axial and radial flow reactor |
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| CP02 | Change in the address of a patent holder | ||
| CP02 | Change in the address of a patent holder |
Address after: 211500 No. 186, Shidai Avenue, Liuhe Economic Development Zone, Nanjing City, Jiangsu Province Patentee after: Nanjing Goodchina Chemical Technologies Co., Ltd. Address before: 210044, No. 355, Ning six road, Liuhe Industrial Development Zone, Nanjing District, Jiangsu, Nanjing Patentee before: Nanjing Goodchina Chemical Technologies Co., Ltd. |