CN202516537U - Double-axial and radial flow reactor - Google Patents
Double-axial and radial flow reactor Download PDFInfo
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- CN202516537U CN202516537U CN2012201044588U CN201220104458U CN202516537U CN 202516537 U CN202516537 U CN 202516537U CN 2012201044588 U CN2012201044588 U CN 2012201044588U CN 201220104458 U CN201220104458 U CN 201220104458U CN 202516537 U CN202516537 U CN 202516537U
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Abstract
A double-axial and radial flow reactor comprises a shell (2) and a reactor internal part (3), wherein the reactor internal part (3) is positioned in the shell (2), a reactor inlet (1) and a reactor outlet (8) are formed on the shell (2), the reactor internal part (3) comprises a distribution barrel (4) and a gas collection barrel (6), a catalyst bed (5) is installed between the gas collection barrel (6) and the distribution barrel (4), and the reactor outlet (8) is communicated with the outlet end of the gas collection barrel (6). The double-shaft radial reactor is characterized in that an upper axial reaction section (14) and a lower axial reaction section (16) are respectively arranged at the upper end and the lower end of the reactor internal part (3), and a radial reaction section (15) is formed between the upper axial reaction section (14) and the lower axial reaction section (16); and the upper end of the catalyst bed (5) is provided with a porous top cover and a wire mesh (12), and the lower end of the catalyst bed (5) is provided with a porous basket bottom and a wire mesh (7). The double-axial and radial flow reactor has a simple structure and a good reaction effect, not only can the reaction efficiency be improved by above 10%, but also the service life of the catalyst can be prolonged by above 20%, so the economic efficiency is remarkable.
Description
Technical field
The utility model relates to a kind of gas reactor, and especially a kind of reaction is more abundant, no bias current and reaction dead angle be main reactor with the radial flow, specifically a kind of double-shaft radial flow reactor.
Background technology
Many knowledges of hitting; The exploitation of Radial Flow reactor and the history of using existing decades; Occur the earliest be overall diameter to flow reactor (seeing Fig. 1-1), promptly air-flow (also can from the center to the periphery) from the periphery to the center all reacts through beds with radial direction, its great advantage is fluid resistance low (being merely 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 of factors such as sinking cause short circuit; So develop shaft radial flow reactors (seeing Fig. 1-2) again; Promptly 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 expansion along with reactor diameter increasing and range of application; And the accumulation of practical experience; Find that this type 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 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 moves hot cell when inside needs to be provided with; During like 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, so 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 purpose of the utility model is to have bias current, dead angle and influence the problem of reaction efficiency to existing radial flow reactors, design a kind of do not have bias current and the double-shaft radial flow reactor that reacts the dead angle.
The technical scheme of the utility model 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, and described shell 2 is provided with reactor inlet 1 and reactor outlet 8, and 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, it is characterized in that the top and bottom of described reactor internals 3 respectively are formed with a upward axial conversion zone 14 and following axial conversion zone 16, between last axial conversion zone 14 and following axial conversion zone 16, is formed with radially conversion zone 15; 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 gets into respectively from last axial conversion zone 14, down axial conversion zone 16 and radially conversion zone 15 get into 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 through 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 12 on the silk screen 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 surround, 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 vent 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.
The beneficial effect of the utility model:
The utility model has thoroughly been 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 utility model 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 the double-shaft radial flow reactor of Fig. 2 the utility model.
Wherein:
The structural representation of the double-shaft radial flow reactor that the ecto-entad of Fig. 2-1 the utility model flows.
The structural representation of the double-shaft radial flow reactor that flows from inside to outside of Fig. 2-2 the utility model.
The structural representation of the double-shaft radial flow reactor that has heat-transfering device of Fig. 2-3 the utility model.
Fig. 3 is the common type structural representation of the double-shaft radial flow reactor of the utility model.
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
Below in conjunction with accompanying drawing and embodiment the utility model is further described.
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, and described shell 2 is provided with reactor inlet 1 and reactor outlet 8, and 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, and 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, between last axial conversion zone 14 and following axial conversion zone 16, are formed with radially conversion zone 15; 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 gets into respectively from last axial conversion zone 14, down axial conversion zone 16 and radially conversion zone 15 get into 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 12 on the silk screen 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 surround, 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 vent 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 got into by reactor inlet 1, and through porous loam cake and silk screen 12, axle radial section 14 reacts in the back inflow gas collecting jar with ground-on cover plate 6 with catalytic bed a part of gas in the entering with the axial flow mode; Part gas with overall diameter to the type of flow through the tube 4 that distributes; Get in the gass collecting jar with ground-on cover plate 6 through the full radial section in middle part 15, some gas flows through shell 2 and flows down to down axial conversion zone 16 with the passage that distributes between the tube 4 in addition, with the axial flow mode through at the bottom of the porous frame of bottom and the catalyst bed of silk screen 7 and bottom react after in the inflow gas collecting jar with ground-on cover plate 6; Three strands of gases are all converged by gas collecting jar with ground-on cover plate 6, go out reactor through outlet 8.Upper end 11 at the tube 4 that distributes is equipped with a not perforate section L1 and a L with lower end 10
1,, be equipped with a not perforate section L2 and a L in the top and bottom of gas collecting jar with ground-on cover plate 13
2, constituted the last axial direction part 14 and 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 with Fig. 2-1 or equivalent identical.
The even utilization of the whole catalyst of lower floor in realizing must reasonably evenly distribute by realization full response device air-flow, and for this reason, must carry out comprehensive hydrodynamics to whole reactor and calculate, thus each item structural parameters of definite 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 confirm and distribute to adapt, realize the airflow uniform distribution of whole reactor with the height ratio of the full radial layer 15 in centre and tolerance.
(2) the perforate aperture d of basket and perforate quantity n also must confirm through 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, are uniformly distributed with requirement to satisfy.
(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 decide by calculating; The vent 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.
Like 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 got into by reactor inlet 1; Through porous loam cake and silk screen 12, react in the gas collecting jar with ground-on cover plate 6 of inflow outer ring, back in the entering by a radial section 14 and catalytic bed with the axial flow mode for a part of gas, and middle overall diameter is that direct distribution tube 6 from reactor center passes through the full radial section 15 entering gass collecting jar with ground-on cover plate 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 the back with the catalyst bed of axial flow mode through at the bottom of the porous frame of bottom and silk screen 7 and bottom and flow in the gas collecting jar with ground-on cover plate 6, 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 in catalytic bed 5, also to be equipped with heat-transfering device 23 with the difference of implementing one, two; 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 through 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; Be the even utilization of the whole catalyst of lower floor in realizing, must realize that full response device air-flow reasonably evenly distributes, for this reason; Must carry out comprehensive hydrodynamics to whole reactor calculates; Thereby confirm each item structural parameters of reactor, also need count this moment moves heat pipe (plate) 21, big or small 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 practical implementation, 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, and be as shown in Figure 3.
(1) Fig. 3-1,3-2, for primary air is got into 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 various and the configuration header structure, all can realize the purpose of the utility model.
(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, during practical implementation, also can carry out equivalence replacement to embodiment one to three, with at the bottom of porous loam cake and silk screen 12 and the porous basket and the vent rate on the silk screen 7 be made as 100%, be equivalent to cancel loam cake and silk screen, become through hole.
The utility model does not relate to all identical with the prior art prior art that maybe can adopt of part to be realized.
Claims (8)
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) are installed, and 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 an axial conversion zone (14) and a following axial conversion zone (16), between last axial conversion zone (14) and following axial conversion zone (16), are formed with radially conversion zone (15); 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) gets into respectively from last axial conversion zone (14), axial conversion zone (16) gets into 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 with conversion zone (15) radially down.
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 1; It is characterized in that described heat-transfering device (23) forms by moving heat pipe (plate) (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 pipe (plate) (21) connecting tube (20) through 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 and 2; It is characterized in that 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 surrounding, and the upper bottom surface of gas collecting jar with ground-on cover plate (6) be can not air inlet closed structure.
5. double-shaft radial flow reactor according to claim 4 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.
6. double-shaft radial flow reactor according to claim 1 and 2; It is characterized in that at the bottom of the porous basket that described down axial conversion zone (16) 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) surrounds, 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).
7. double-shaft radial flow reactor according to claim 6 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.
8. 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 vent rate on the silk screen (7) is 1%～100%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201044588U CN202516537U (en) | 2012-03-20 | 2012-03-20 | Double-axial and radial flow reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201044588U CN202516537U (en) | 2012-03-20 | 2012-03-20 | Double-axial and radial flow reactor |
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| Publication Number | Publication Date |
|---|---|
| CN202516537U true CN202516537U (en) | 2012-11-07 |
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ID=47099507
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| CN2012201044588U Expired - Fee Related CN202516537U (en) | 2012-03-20 | 2012-03-20 | Double-axial and radial flow reactor |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580626A (en) * | 2012-03-20 | 2012-07-18 | 南京国昌化工科技有限公司 | Double-shaft radial flow reactor |
| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN106475015A (en) * | 2015-08-27 | 2017-03-08 | 中国石化工程建设有限公司 | Particulate matter bed supporting construction and Axial and radial catalytic reactor |
| CN111701540A (en) * | 2020-06-29 | 2020-09-25 | 南京国昌化工科技有限公司 | Combined radial flow distributor of bubbling plate slot plate |
-
2012
- 2012-03-20 CN CN2012201044588U patent/CN202516537U/en not_active Expired - Fee Related
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102580626A (en) * | 2012-03-20 | 2012-07-18 | 南京国昌化工科技有限公司 | Double-shaft radial flow reactor |
| CN104096514A (en) * | 2013-04-09 | 2014-10-15 | 上海国际化建工程咨询公司 | Isothermal fixed bed reactor loading catalyst among heat exchange tubes |
| CN104096514B (en) * | 2013-04-09 | 2018-01-30 | 上海国际化建工程咨询公司 | A kind of isothermal fixed bed reactors that catalyst is loaded between heat exchanger tube |
| CN106475015A (en) * | 2015-08-27 | 2017-03-08 | 中国石化工程建设有限公司 | Particulate matter bed supporting construction and Axial and radial catalytic reactor |
| CN106475015B (en) * | 2015-08-27 | 2019-05-10 | 中国石化工程建设有限公司 | Particulate matter bed support construction and axis radial catalystic reactor |
| CN111701540A (en) * | 2020-06-29 | 2020-09-25 | 南京国昌化工科技有限公司 | Combined radial flow distributor of bubbling plate slot plate |
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Granted publication date: 20121107 Termination date: 20140320 |