CN211754820U - Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor - Google Patents
Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor Download PDFInfo
- Publication number
- CN211754820U CN211754820U CN201921726353.4U CN201921726353U CN211754820U CN 211754820 U CN211754820 U CN 211754820U CN 201921726353 U CN201921726353 U CN 201921726353U CN 211754820 U CN211754820 U CN 211754820U
- Authority
- CN
- China
- Prior art keywords
- gas
- reactor
- liquid distribution
- distribution structure
- liquid
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
An upstroke gas-liquid distribution structure and a hydrocarbon oil hydrogenation reactor, the upstroke gas-liquid distribution structure comprising: the ceramic membrane (3) that central pipe (2) and top cover, central pipe bottom opening be import (1), the open-top is export (4). The hydrocarbon oil hydrogenation reactor comprises: the reactor comprises a reactor shell, a plurality of sections of catalyst bed layers in the reactor shell and a flow baffle plate arranged at the bottom of the reactor, wherein the flow baffle plate is provided with an opening, the upflow gas-liquid distribution structure is arranged corresponding to the opening, the bottom of the reactor shell is provided with an inlet, and the top of the reactor shell is provided with an outlet. The utility model provides an upstroke gas-liquid distribution structure is applicable to liquid phase diesel oil hydrogenation technology reactor or light fraction diesel oil hydrogenation process, can strengthen the double-phase mass transfer rate of gas-liquid, improves the speed that hydrogen dissolved in liquid phase oil.
Description
Technical Field
The present invention relates to a reactor internals and a reactor, and more particularly to a gas-liquid distribution internals and a hydrocarbon oil hydrogenation reactor.
Background
In the liquid phase circulation hydrogenation process, a proper hydrogen dissolving method is the key of the liquid phase circulation hydrogenation process. Hydrogen, raw oil and circulating oil need to be mixed and fully dissolved before entering a reactor so as to supply necessary hydrogen for hydrogenation reaction; or hydrogen can be quickly dissolved in liquid phase oil in the reactor, so that the hydrogen consumed in the liquid phase can be quickly supplemented.
Meanwhile, the problems that hot spots are easy to appear on a bed layer, local temperature rise is overlarge and the like are often found in the operation of the upflow reactor. The fluid mechanics characteristic in the upflow reactor is unstable, and the influence factors are uncertain, which directly influence the amplification, optimization, application and the like of the upflow reactor. Meanwhile, the hydrogenation reaction is an exothermic reaction, local hot spots are probably caused by local blockage, too low local flow rate, prolonged residence time, additional heat release and the like, the hydrodynamic characteristics are greatly related to the initial gas-liquid distribution of the reactor, and the initial gas-liquid distribution is influenced by components in the reactor. The two aspects are integrated: two problems that need to be solved by the internals of the up-flow reactors at present are as follows: a: how quickly hydrogen dissolves in diesel, i.e. the kinetics of hydrogen dissolution; b: how the hydrogen is evenly distributed in the diesel oil: stable gas-liquid distribution is crucial to improving the flow characteristics and catalyst utilization in the reactor; the main purpose of this patent is how to solve the problem of rapid dissolution of hydrogen in liquid phase diesel.
CN 101632911B discloses an upflow reactor and its application, in which the initial distributor and the intermediate distributor are arranged to achieve the breaking and uniform distribution of bubbles. After the mixture of hydrogen and heavy oil enters the reactor from the bottom of the reactor, dispersed phase bubbles collide with the conical baffle plate and then are crushed and move around, and after passing through the sieve plate with the uneven open pore structure, the bubbles are crushed again, so that the local uniform distribution of gas is realized. The structure has the defect that hydrogen consumed in the oil phase cannot be timely supplemented, so that the performance of the device is influenced.
CN 201776132U discloses an up-flow hydrogenation reactor with an anti-clogging grid, which creates conditions for uniform distribution of fluid by arranging a space between two catalyst bed layers, wherein the space grid is divided into an upper part and a lower part, the upper part is a small flow passage component which is a sieve plate, a pore plate, a grid or a net structure with the flow passage size smaller than the particle size of catalyst particles, and the lower part is a interception component which is a flow passage component with an inclined or zigzag flow passage. The raw material and hydrogen flow upwards in parallel flow to pass through the catalyst bed layer, so that the catalyst bed layer has lower pressure drop and larger pressure drop increase resistance, different catalyst bed layers can be filled, different catalysts cannot be back-mixed, the anti-blocking bed layer spacer grid can effectively prevent catalyst particles carried by fluid from blocking a distributor or a runner of the spacer grid, and favorable conditions are created for uniform distribution of the fluid.
CN 202621143U discloses an up-moving gas-liquid distributor, the distributor adopted comprises a distribution pipe and a distribution plate, the upper end of the distribution pipe is in fluid communication with the distribution plate, and the lower end of the distribution pipe is provided with an oblique angle opening; the gas-liquid distributor also comprises a baffle plate, the bevel angle opening is connected with the baffle plate, and the baffle plate covers the bevel angle opening; the wall of the distribution pipe is provided with a gas channel. Compared with the prior art, the utility model has the advantages of the gas-liquid distribution degree of consistency is high, the operation elasticity is big, simple structure, manufacturing are convenient, save investment. But the disadvantage is that the structure also has no function of radial diffusion of the gas.
CN 102039105B discloses a gas-liquid countercurrent reactor and a gas-liquid countercurrent hydrogenation process, a novel inner member has been adopted in the reactor, contain a gas-liquid contact member and gas-liquid collection component, the gas-liquid contact member sets up in gas collection component top, gas collection component includes the division board, the pipeline of falling liquid and exhaust duct, the division board has the through-hole, the through-hole is connected with the pipeline of falling liquid and the exhaust duct that set up, the pipeline of falling liquid sets up below the division board for the nozzle stub structure, exhaust duct sets up on the division board, exhaust duct passes last layer catalyst bed and communicates with each other with the reactor outside.
US 6,554,994 discloses a fluid distribution device and a cold hydrogen system for simultaneously distributing gas and liquid in a multi-bed fixed bed hydrogenation reactor. The fluid distribution means may take a variety of forms, for example, screens, grids, perforated plates, and the like. The fluid dispensing device has two main functions: (1) fluid passing through the reactor evenly distributed over the level of the catalyst layer; (2) has the functions of breaking large bubbles and mixing fluid. The holes of the central riser, enable an optimal distribution of the fluid: each riser has at least one opening in its side wall. Vapor enters the riser holes through the openings and liquid surrounding the deflector and passes through the openings in the riser bottom, up through the perforations in the fluid distribution plate into the spaces and up through the catalyst support grid into the next adjacent partition.
SUMMERY OF THE UTILITY MODEL
The to-be-solved technical problem of the utility model is to solve the problem that the hydrogen can not be quick dissolved in liquid phase oil in the up-going hydrocarbon oil hydrogenation reactor in the prior art. The mass transfer rate between gas phase and liquid phase in the diesel oil and light oil hydrogenation reactor is improved, so that the hydrogen is quickly dissolved in the liquid phase oil.
The utility model provides an upstroke gas-liquid distribution structure, include: the ceramic membrane device comprises a central circular tube 2 and a ceramic membrane 3 covered at the top, wherein the bottom opening of the central circular tube is an inlet 1, and the top opening is an outlet 4.
The utility model provides a hydrocarbon oil hydrogenation ware, include: the reactor comprises a reactor shell, a plurality of sections of catalyst bed layers in the reactor shell and a flow baffle plate arranged at the bottom of the reactor, wherein the flow baffle plate is provided with an opening, the upflow gas-liquid distribution structure is arranged corresponding to the opening, the bottom of the reactor shell is provided with an inlet, and the top of the reactor shell is provided with an outlet.
The utility model provides an upstroke gas-liquid distribution structure is applicable to in the hydrocarbon oil hydrogenation ware, installs on the board is kept off to the bottom as reactor internals, and hydrogenous gas and liquid phase hydrocarbon fraction get into upstroke hydrogenation ware from the bottom entry, after keeping off the board and carrying out preliminary dispersion, the double-phase mixture of gas-liquid follow the import of upstroke gas-liquid distribution structure get into after further mixing in the upstroke gas-liquid distribution structure, the gas-liquid mixture gets into the ceramic membrane under the pressure effect, because the microporous structure of ceramic membrane, the passageway size of gas-liquid mixture reduces suddenly, its velocity of motion increase, the mass transfer rate increase of gas-liquid. Meanwhile, the bent pore channels of the ceramic membrane enable the gas-liquid mixture to further collide, and therefore the mass transfer effect is greatly promoted.
The utility model provides an upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation ware's beneficial effect does:
the utility model provides an upstroke gas-liquid distribution structure is suitable for and installs in hydrocarbon oil hydrogenation ware, including diesel oil hydrogenation ware and light oil hydrogenation ware, compare with the gas-liquid distributor among the prior art, the utility model provides an improvement that upstroke gas-liquid distribution structure is showing that the gaseous phase is dissolved in the mass transfer rate of liquid phase oil, the dissolution effect has obtained obvious improvement. The utility model provides a hydrocarbon oil hydrogenation ware's simple structure, hydrogen dissolve effectually in hydrocarbon oil, are showing and have improved reaction efficiency, have improved hydrocarbon oil hydrogenation's conversion.
Drawings
Fig. 1 is a schematic structural view of an embodiment of the ascending gas-liquid distribution structure.
Fig. 2 is a schematic structural view of another embodiment of the ascending gas-liquid distribution structure.
FIG. 3 is a schematic view of the lower part of a hydrocarbon oil hydrogenation reactor.
Fig. 4 is a schematic view of the structure of the gas-liquid distributor employed in the comparative example.
Wherein, 1-inlet, 2-central circular tube, 3-ceramic membrane, 4-outlet, 5-through hole, 6-reactor shell, 7-reactor inlet, 8-baffle plate, and 9-catalyst bed layer.
Detailed Description
In the following description of the embodiments of the present invention, the "upper part" of the container mentioned in the present specification means a position from the bottom to the top of 0 to 50% of the container, the "lower part" of the container means a position from the bottom to the top of 50 to 100% of the container, the "middle part" of the container means a position from the bottom to the top of 30 to 70% of the container, and the "bottom" of the container means a position from the bottom to the top of 95 to 100% of the container.
The utility model provides an upstroke gas-liquid distribution structure, include: the ceramic membrane device comprises a central circular tube 2 and a ceramic membrane 3 covered at the top, wherein the bottom opening of the central circular tube is an inlet 1, and the top opening is an outlet 4.
Preferably, the height-diameter ratio of the central circular tube is 2-5: 1, the height is 160-320mm, the inner diameter is 60-80mm, and the wall thickness is 3-6 mm.
Preferably, the side wall of the central circular tube is provided with a plurality of through holes, the diameter of each through hole is 3-6mm, the number of the through holes is 2-12, and the number of the through holes is preferably 4-8.
Preferably, the ceramic membrane is a flat plate structure, the aperture is less than 0.5 μm, and the porosity is 30% -50%.
The utility model provides a hydrocarbon oil hydrogenation ware, include: the reactor comprises a reactor shell, a plurality of sections of catalyst bed layers in the reactor shell and a flow baffle plate arranged at the bottom of the reactor, wherein the flow baffle plate is provided with an opening, the upflow gas-liquid distribution structure is arranged corresponding to the opening, the bottom of the reactor shell is provided with an inlet, and the top of the reactor shell is provided with an outlet.
Preferably, a flow baffle and the upflow gas-liquid distribution structure are also arranged between the catalyst beds.
Preferably, the distance between the flow baffle and the bottom of the reactor is 100mm and 300 mm.
Preferably, the ratio of the ascending gas-liquid distribution structure to the reactor is 1 (25-35).
Preferably, the aperture ratio of the flow baffle is 0.2-0.4, the flow baffle is provided with 20-30 round holes, and each hole is correspondingly provided with the ascending gas-liquid distribution structure.
The utility model provides a hydrocarbon oil hydrogenation ware is upstroke hydrogenation ware, the fender of reactor bottom flow plate on be equipped with a plurality of upstroke gas-liquid distribution structures, its main function is to introduce the distribution to the catalyst bed with the entrance of gas-liquid mixture from the bottom to improve gas-liquid mixture's distribution performance.
In the up-going gas-liquid distribution structure, the ceramic membrane has the main functions of reducing the circulation space of a gas-liquid mixture by utilizing the special membrane pore channel, improving the gas-liquid speed, and enabling gas and liquid to collide and turn back in the bent pore channel, thereby achieving the effect of strengthening the gas-liquid distribution performance. The ceramic membrane is preferably made of alumina, is preferably of a flat plate structure, has a pore diameter of less than 0.5 mu m according to actual requirements, and has a porosity of 30-50%.
Preferably, the side wall of the central circular tube is provided with round holes with the diameter of 3-6mm, preferably 4-8 round holes which are respectively distributed at the positions 30mm, 60mm and 90mm above the inlet, and the main purpose is to enable the gas-liquid mixture to enter the tube more ways and reduce the pressure drop in the process.
The utility model provides an upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation ware's theory of operation is, gaseous phase and liquid phase raw materials get into hydrocarbon oil hydrogenation ware from the raw materials import of bottom, carry out preliminary dispersion through keeping off the flow board earlier, then, gas-liquid double-phase mixture gets into in the center pipe from the entry of upstroke gas-liquid distribution structure and the round hole on the center pipe and carries out further mixture, later, the gas-liquid mixture gets into in the ceramic membrane that the top covered under the external pressure effect; as the micropore structure of the ceramic membrane has small size of 10nm-00.5 mu m, the size of a channel through which a gas-liquid mixture flows is suddenly reduced, the movement speed is increased, and the mass transfer rate of gas and liquid is increased. Meanwhile, the bent pore channels of the ceramic membrane enable the gas-liquid mixture to further collide, so that the mass transfer effect is promoted. Compare with the central straight tube-type gas-liquid distribution structure who adopts among the prior art, the utility model provides an upstroke gas-liquid distribution structure is showing and has improved the mass transfer rate that gas dissolved in liquid phase oil, has obviously improved the dissolution effect.
Adopted the utility model discloses an upstroke gas-liquid distribution structure's hydrocarbon oil hydrogenation ware can promote the solubility of hydrogen at reaction raw materials hydrocarbon oil, can improve reaction efficiency, submits the conversion rate of target product.
The following further describes the ascending gas-liquid distribution structure and the hydrocarbon oil hydrogenation reactor provided by the present invention with reference to the attached drawings. Fig. 1 and 2 are schematic structural views of an upward gas-liquid distribution structure. As shown in fig. 1, the ascending gas-liquid distribution structure includes: the device comprises a central circular tube 2 and a ceramic membrane 3, wherein the central circular tube 2 is a hollow straight tube, an outlet 4 at the top of the central circular tube is covered with the ceramic membrane 3, and an inlet 1 at the bottom of the central circular tube is an inlet of a gas-liquid mixture. The wall of the central circular tube is provided with a through hole 5, and the side wall of the central circular tube 2 in the attached figure 1 is provided with at least two circular holes 5 which are distributed centrosymmetrically. As shown in fig. 2, the central tube has no openings.
Fig. 3 is a schematic perspective view of the lower part of a hydrocarbon oil hydrogenation reactor, which, as shown in fig. 3, comprises: the reactor comprises a reactor shell 6, a plurality of sections of catalyst bed layers 9 in the reactor shell and a flow baffle plate 8 arranged at the bottom of the reactor, wherein the flow baffle plate 8 is provided with an opening, the upflow gas-liquid distribution structure is arranged corresponding to the opening, the bottom of the reactor shell is provided with an inlet 7, and the top of the reactor shell is provided with an outlet.
The following examples further illustrate the structure and effectiveness of the upflow gas-liquid distributor of the present invention. The present invention is not limited thereto.
Example 1
An upward gas-liquid distribution structure is adopted as shown in the attached figure 1, wherein: the outer diameter of the central circular tube is 60mm, the wall thickness is 4mm, and the length is 180 mm; the ceramic membrane is made of alumina and has a flat plate structure, and the aperture is maintained at<0.5 μm, with a porosity of 40%; the side wall of the central circular tube is provided with 6 circular holes with the diameter of 4mm, and the circular holes are respectively distributed at the positions which are 30mm, 60mm and 90mm away from the inlet at the bottom of the central circular tube. The upward distribution system is installed on the flow-blocking plate at the bottom of cold tower of hydrocarbon oil hydrogenation reactorThe diameter of the desert tower is 300mm, the height is 1000mm, and the tower body is made of organic glass, so that the flow condition of fluid in the reactor and at the inlet and outlet of the gas-liquid distributor can be observed. The air flow adopted by the cold model test is 2-8 m3The water flow is 0.2-1.0 m3/h。
Comparative example 1
The central tube type up-flow gas-liquid distribution structure shown in figure 4 is adopted, the outer diameter of the central tube is 60mm, the wall thickness is 4mm, and the length is 180 mm. The side wall of the central tube is distributed with 6 round holes with the diameter of 4mm, which are respectively distributed at the positions 30mm, 60mm and 90mm above the inlet at the bottom of the central tube. The remaining conditions were the same as in example 1.
In the gas phase flow of 2-8 m3Within the range of/h, the distribution uniformity of the gas-liquid two-phase fluid in the cold desert tower of the embodiment 1 is better.
At a gas phase flow rate of 3m3The bubble diameter unevenness in the liquid phase in the desert column of example 1 was about 0.15 under the condition of/h, while the bubble diameter unevenness of the comparative example structure was about 0.2.
The gas phase flow rate is 2-3 m3The diameter of the bubbles generated by the gas-liquid distribution structure in the desert tower of example 1 is about 4mm, and the diameter of the bubbles generated by the gas-liquid distribution structure in the desert tower of comparative example 1 is about 6-7 mm under the low flow rate condition of/h.
The gas phase flow is 5-8 m3Under the high flow rate condition of/h, the diameters of the bubbles generated by the gas-liquid distribution structures in the cold desert towers of the example 1 and the comparative example 1 are not greatly different, and are both about 4.5 mm.
In conclusion, the utility model provides an upstroke gas-liquid distribution structure has better gas-liquid mixture performance under low gaseous phase flow condition, has better fluid distribution homogeneity, and is less with prior art's distribution performance difference under the high tolerance condition.
Claims (10)
1. An upstroke gas-liquid distribution structure comprising: the ceramic membrane (3) that central pipe (2) and top cover, central pipe bottom opening be import (1), the open-top is export (4).
2. The upflow gas-liquid distribution structure as recited in claim 1, wherein the central circular tube has a height-diameter ratio of 2 to 5: 1, the height is 160-320mm, the inner diameter is 60-80mm, and the wall thickness is 3-6 mm.
3. An upstroke gas-liquid distribution structure according to claim 1 or 2, wherein said central circular tube has a plurality of through holes (5) formed in its side wall, said through holes having a diameter of 3 to 6 mm.
4. An upstroke gas-liquid distribution structure as claimed in claim 3, wherein said central circular tube has 4-8 through holes (5) on its side wall.
5. An upflow gas-liquid distribution structure as in claim 1 or 2, in which the ceramic membrane (3) is a flat plate structure with a pore size of <0.5 μm and a porosity of 30% to 50%.
6. A hydrocarbon oil hydrogenation reactor comprising: the reactor comprises a reactor shell, a plurality of sections of catalyst beds in the reactor shell, and a flow baffle plate arranged at the bottom of the reactor, wherein the flow baffle plate is provided with an opening, the upflow gas-liquid distribution structure as claimed in any one of claims 1 to 4 is arranged corresponding to the opening, the bottom of the reactor shell is provided with an inlet, and the top of the reactor shell is provided with an outlet.
7. A hydrocarbon oil hydrogenation reactor as defined in claim 6, wherein flow baffles and said upflow gas-liquid distribution structure are also provided between said catalyst beds.
8. The hydrocarbon oil hydrogenation reactor according to claim 6, wherein the distance between the bottom baffle plate and the bottom of the reactor is 100mm-300 mm.
9. The hydrocarbon oil hydrogenation reactor according to claim 6 or 7, wherein the ratio of the ascending gas-liquid distribution structure to the reactor is 1 (25-35).
10. The hydrocarbon oil hydrogenation reactor according to claim 6 or 7, wherein the flow baffle is provided with 20 to 30 openings, and each opening is correspondingly provided with the ascending gas-liquid distribution structure.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921726353.4U CN211754820U (en) | 2019-10-15 | 2019-10-15 | Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201921726353.4U CN211754820U (en) | 2019-10-15 | 2019-10-15 | Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN211754820U true CN211754820U (en) | 2020-10-27 |
Family
ID=72935045
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201921726353.4U Active CN211754820U (en) | 2019-10-15 | 2019-10-15 | Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN211754820U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115074151A (en) * | 2021-03-15 | 2022-09-20 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reaction system and raw oil reinforced hydrogen mixing device thereof |
-
2019
- 2019-10-15 CN CN201921726353.4U patent/CN211754820U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN115074151A (en) * | 2021-03-15 | 2022-09-20 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reaction system and raw oil reinforced hydrogen mixing device thereof |
| CN115074151B (en) * | 2021-03-15 | 2024-03-01 | 中国石油天然气股份有限公司 | Liquid phase hydrogenation reaction system and raw oil reinforced hydrogen mixing device thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA2595478C (en) | Distribution device for two-phase concurrent downflow vessels | |
| CN101274245B (en) | Annular space air-lift gas-solid loop flow reactor | |
| RU2542248C2 (en) | Device of fluid medium flow distribution for catalytic reactors with descending flow | |
| CN101279228B (en) | Gas-liquid distributor of trickle bed reactor | |
| CN101279229A (en) | Trickle bed reactor | |
| EA034637B1 (en) | Mixing device with tangential inlets for two-phase concurrent vessels | |
| CN104028176A (en) | Reaction device for preparing bio-aviation kerosene through hydrocracking | |
| CN101708452A (en) | Filler assembly capable of eliminating amplification effect | |
| CN211754820U (en) | Upstroke gas-liquid distribution structure and hydrocarbon oil hydrogenation reactor | |
| CN204051631U (en) | A kind of fluid distributor and fluid predistribution dish | |
| CN106732200B (en) | Turbine type cold hydrogen box | |
| CN201348462Y (en) | Film distributor for vertical tube falling film absorber | |
| CN101940848B (en) | Catalytic rectification column member | |
| CN103871503A (en) | Nuclear reactor lower chamber plate-like flow distribution apparatus | |
| CN1259124C (en) | Annular space gas lifting type loop reactor | |
| CN115090220B (en) | Down-flow type mixed bubble flow hydrogenation reactor | |
| CN211754819U (en) | Upward gas-liquid distributor and hydrocarbon oil hydrogenation reactor | |
| CN217248777U (en) | Gas phase distributor and reactor | |
| CN116694360A (en) | Hydrogenation reaction system | |
| CN216419330U (en) | Novel falling film reactor | |
| CN205435685U (en) | Hybrid system | |
| CN111013178B (en) | Stepped liquid circulation bubble tower and method for dispersing gas | |
| CN210700043U (en) | Micropore plate gas distributor | |
| WO2006093437A2 (en) | Catalytic process reactor | |
| CN203737216U (en) | Uplink gas-liquid distributor applicable to gas-liquid-solid three-phase reactor |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant |