CN209866000U - Axial-radial HPPO fixed bed reactor - Google Patents
Axial-radial HPPO fixed bed reactor Download PDFInfo
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- CN209866000U CN209866000U CN201920462331.5U CN201920462331U CN209866000U CN 209866000 U CN209866000 U CN 209866000U CN 201920462331 U CN201920462331 U CN 201920462331U CN 209866000 U CN209866000 U CN 209866000U
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Abstract
The utility model discloses an axial-radial HPPO fixed bed reactor, which comprises a shell (1), wherein the upper end socket of the shell is provided with a material inlet pipe (2), the lower end socket of the shell is provided with a material outlet pipe (3), the shell comprises n radial flow catalyst bed layers (4), wherein n is an integer more than 2; every radial flow catalyst bed is equipped with outer barrel (5) and interior barrel (6), interior barrel center is equipped with central heat transfer section of thick bamboo (9), and its export sets up mixing arrangement (12), install center tube (7) in the center heat transfer section of thick bamboo, the upper portion of center tube is higher than radial flow catalyst bed, and the part of higher than sets up premixing device (10), every radial flow catalyst bed all is connected with drainage tube (11), the drainage tube with center tube upper portion premixing device links to each other. The utility model discloses reactor temperature distribution is even, and heat exchange efficiency is high, and the operation is swift, takes up an area of for a short time, enlargies easily.
Description
Technical Field
The utility model belongs to the technical field of petrochemical, concretely relates to axial direction HPPO fixed bed reactor.
Background
Propylene oxide is the second largest class of propylene derivatives second only to polypropylene, and the current domestic process for producing propylene oxide comprises the following steps: chlorohydrin processes, co-oxidation processes, and direct oxidation of hydrogen peroxide processes (HPPO processes). The production of propylene oxide by chlorohydrin method and co-oxidation method has the disadvantages of long flow, high equipment cost, large environmental pollution and the like. The HPPO method is to synthesize propylene oxide by catalyzing propylene oxide with hydrogen peroxide under the action of a titanium-silicon molecular sieve catalyst. Simple process, mild condition, basically no pollution and single product, and is the most environment-friendly production technology recognized at present.
The propylene epoxidation reaction is a strong exothermic reaction, the unit reaction exotherm is about 220KJ/mol, and the adiabatic temperature rise is more than 100 ℃. The requirement on the reactor is extremely high, and the reaction fluid needs to be uniformly distributed and quickly exchanges heat so as to control the reaction temperature and ensure the selectivity of the propylene oxide and the service life of the catalyst. The traditional control scheme is to use a tubular fixed bed reactor and use a large amount of cooling water to remove the heat of reaction. And the pipe diameter of the tube array is small, so that the wall effect is easily caused, the catalyst is not uniformly filled, and the material distribution is not uniform.
Chinese patent CN103638876A discloses an energy-saving optimization method for HPPO device reactor. Introducing a cooling medium into a jacket of the tubular fixed bed reactor to exchange heat with the reactor, and controlling the temperature rise in the reactor; when the reaction temperature is 30-40 ℃, removing the heat of the reaction by adopting chilled water; when the reaction temperature is 40-50 ℃, circulating water is adopted to remove heat generated by the reaction; when the reaction temperature is 50-60 ℃, circulating water with higher temperature is adopted to remove heat generated by the reaction. The method adopts a large amount of chilled water and circulating water, and has high operation cost and low economic benefit.
Chinese patent CN103724299A discloses a method for preparing propylene oxide. The propylene raw material is mixed with a methanol solvent and then mixed with hydrogen peroxide, the mixture sequentially enters n series reactors and contacts with the titanium-silicon molecular sieve catalyst in each reactor, and the product stream of each reactor can selectively enter a subsequent separation section and/or enter at least one of the other reactors. The method adopts a multistage series process to carry out reaction, cooling and control in stages, and has the defect that each reactor is not provided with a control means when overtemperature or hot spot temperature occurs.
Therefore, it is desirable to provide an axial-radial HPPO fixed bed reactor to solve the above problems.
SUMMERY OF THE UTILITY MODEL
The utility model aims to solve the problems that in the prior art, the catalyst is not uniformly loaded, a large amount of cooling water is needed to be used for removing reaction heat, the reaction temperature is not uniform, and the temperature control means is not flexible.
The utility model provides an axial HPPO fixed bed reactor, it includes the casing, and the casing includes upper cover, low head. The shell also comprises n radial flow catalyst bed layers, wherein n is an integer more than 2, each radial flow catalyst bed layer is provided with an outer cylinder and an inner cylinder, the center of the inner cylinder is a central heat exchange cylinder, and an outlet of the central heat exchange cylinder is provided with a mixing device; a central pipe is arranged in the central heat exchange cylinder, the upper part of the central pipe is higher than the radial flow catalyst bed layer, and a premixing device is arranged at the higher part of the central pipe; each radial flow catalyst bed layer is connected with a draft tube, and the draft tube is connected with a premixing device at the upper part of the central tube.
Preferably, the outer cylinder body is a porous cylinder with an uneven surface, the diameter of the pores is smaller than the granularity of the catalyst, and a wire mesh is laid between the outer cylinder body and the catalyst, and the mesh number of the wire mesh is smaller than the granularity of the catalyst.
Preferably, the inner cylinder body is a porous cylinder with an uneven surface, the diameter of the hole is smaller than the granularity of the catalyst, and a wire mesh is laid between the inner cylinder body and the catalyst, and the mesh number of the wire mesh is smaller than the granularity of the catalyst.
The inner cylinder body and the outer cylinder body are porous cylinders with uneven surfaces, so that radial flow is uniformly distributed, the reaction is sufficient, and the effect is good; the laying of the silk screen can eliminate dead angles and make the radial flow more uniform.
Preferably, the surface of the central tube is provided with nozzles which are regularly arranged, and the nozzles are in at least one of fan shape, conical shape and straight flow shape or a combination of a plurality of nozzles.
The surface of the central pipe is provided with the nozzles which are regularly distributed, so that cold fluid in the drainage pipe and hot fluid which flows out of the radial flow catalyst bed layer are fully mixed in the central heat exchange cylinder for heat exchange, and the heat efficiency is improved; the cold fluid or the mixed fluid impacts the rugged inner cylinder body, so that the mixing effect and the heat transfer between the cold fluid and the hot fluid can be enhanced.
Preferably, the outlet of the central heat exchange cylinder is provided with a mixing device, and at least one or a combination of a plurality of ceramic balls, pall rings, saddle blocks, stepped rings and spherical fillers is filled in the mixing device.
The outlet of the central heat exchange cylinder is provided with a mixing device, so that the contact time of the cold and hot fluid mixed fluid can be prolonged, and the cold and hot fluid mixed fluid is fully mixed.
Preferably, the upper part of the central pipe is provided with a premixing device, and the premixing device is filled with at least one or a combination of a pall ring, a square saddle, a stepped ring and spherical packing;
the central pipe is provided with a premixing device, so that the cold fluid in the drainage pipe is premixed, and the uniform mixing between the cold fluid and the hot fluid is enhanced.
Preferably, the cold fluid in the draft tube is propylene, hydrogen peroxide solution, methanol solution.
Cold propylene, hydrogen peroxide solution and methanol solution are introduced into the central heat exchange cylinder through the drainage tube, heat exchange can be carried out on the propylene, the hydrogen peroxide solution and the methanol solution and hot fluid at the outlet of the radial flow catalyst bed layer, the cold fluid and the hot fluid enter the next radial flow catalyst bed layer for reaction after heat exchange and mixing, heat transfer and preheating between adjacent radial flow catalyst bed layers are realized, and heat is efficiently utilized. The temperature of the radial flow catalyst bed layer is simply and conveniently adjusted, and the temperature control of the whole reactor is greatly facilitated.
Preferably, a catalyst is filled between the outer cylinder and the inner cylinder, ceramic balls are paved at the lower end of the catalyst, the ceramic balls fill the discharge opening gap of each section of radial flow catalyst bed layer, the ceramic balls are also paved at the upper end of the catalyst, and the particle size of the ceramic balls is slightly larger than that of the catalyst.
The catalyst is filled between the outer cylinder and the inner cylinder, the lower end of the radial flow catalyst bed layer is fully paved with ceramic balls, and the ceramic balls fill the discharge opening gap of each section of radial flow catalyst bed layer to play a filling role. And ceramic balls are also paved at the upper end of the radial flow catalyst bed layer, and the upper end of the radial flow catalyst bed layer is fixed by a silk screen, a pressure ring and a pressing strip after the ceramic balls are paved.
Preferably, the upper end socket is provided with a material inlet pipe and a safety valve, the lower end socket is provided with a material outlet pipe, a manhole is arranged between adjacent radial flow catalyst bed layers, and the bottom of each radial flow catalyst bed layer is provided with a discharge opening.
The upper end enclosure is provided with a safety valve to ensure that the reactor is released when the temperature and the pressure are over-high.
And a manhole is arranged between two pairs of adjacent radial flow catalyst beds for filling and overhauling the catalyst.
The bottom of each radial flow catalyst bed layer is provided with a discharge opening for disassembling the catalyst and the ceramic ball.
Compared with the prior art, the utility model has the advantages of it is following:
1. the radial flow is uniformly distributed, the effect is good, the dead angle area of the catalyst bed layer is eliminated, and the synthesis efficiency is high.
2. Cold and hot fluid between adjacent catalyst bed layers is remixed and redistributed, so that heat is effectively utilized, and the temperature distribution of the reactor bed layers is uniform. In addition, the reactor can be cooled in time, so that the possibility of local temperature runaway is prevented.
3. The temperature of the catalyst bed is controlled by adjusting the flow of cold fluid through the drainage tube, and the operation is simple and quick.
4. The catalyst is tightly and uniformly filled, bridging is not easy to form, and the space utilization rate is high.
5. The axial and radial fixed bed reactor has smaller occupation area than a common fixed bed, uniform distribution, easy amplification and strong adaptability.
The utility model discloses an axial radial fixed bed reactor carries out temperature control and heat transfer through center tube spun cold fluid, and it is even to have temperature distribution, and heat exchange efficiency is high, and the operation is swift, takes up an area of for a short time, advantages such as enlarge easily.
Drawings
FIG. 1 is a schematic structural view of an axial-radial HPPO fixed bed reactor of the present invention;
FIG. 2 is a schematic view of the outer cylinder and the inner cylinder of the present invention;
figure 3 is a schematic view of the center tube of the present invention.
The device comprises a shell 1, a material inlet pipe 2, a material outlet pipe 3, a radial flow catalyst bed layer 4, an outer cylinder 5, an inner cylinder 6, a central pipe 7, a nozzle 8, a central heat exchange cylinder 9, a premixing device 10, a drainage pipe 11, a mixing device 12, a manhole 13, a safety valve 14 and a discharge opening 15.
Detailed Description
The invention is further described with reference to the following figures and specific embodiments.
The axial and radial HPPO fixed bed reactor as shown in figures 1 to 3 comprises an upper head, a lower head, a shell 1 and the like. The upper end enclosure is provided with a material inlet pipe 2 communicated with the interior of the upper end enclosure, and the lower end enclosure of the shell 1 is provided with a material outlet pipe 3 communicated with the interior of the lower end enclosure. The shell 1 is internally provided with a plurality of radial flow catalyst bed layers 4, and each radial flow catalyst bed layer 4 is provided with an outer cylinder 5 and an inner cylinder 6. The center of the inner cylinder 6 is provided with a central tube 7, the surface of the inner cylinder is provided with conical nozzles 8 which are regularly arranged, hot fluid at the outlet of the inner cylinder 6 exchanges heat with cold fluid sprayed from the central tube 7 in a central heat exchange cylinder 9, so that heat released by the reaction of the material through the radial flow catalyst bed layer 4 is taken away, and the material entering the next bed layer is preheated. The part of the upper part of the central tube 7, which is higher than the radial flow catalyst bed layer 4, is provided with a premixing device 10, propylene, hydrogen peroxide solution and methanol solution enter the premixing device 10 through a drainage tube 11 for premixing and enter the central tube 7 after being mixed for ejection heat exchange, and the drainage tube 11 (a pair of) penetrates through the shell 1 to be connected with a corresponding cold source outside. The outlet of the central heat exchange cylinder 9 is provided with a mixing device 12, and the mixing device 12 can prolong the contact time of the mixed cold and hot fluid and improve the mass transfer and heat transfer efficiency. The cold and hot fluids are mixed and then enter the next radial flow catalyst bed layer 4 for continuous reaction. A manhole 13 is arranged between every two adjacent radial flow catalyst bed layers 4 for filling and maintaining the catalyst, a safety valve 14 is arranged on an upper end enclosure to prevent the reactor from being over-heated and over-pressurized, ceramic balls are paved at the upper end and the lower end of each radial flow catalyst bed layer 4, the lower end ceramic balls fill the gap of a discharge opening 15 of each section of radial flow catalyst bed layer 4, and the upper end ceramic balls are fixed by a silk screen, a pressing strip and a pressing plate. The outer cylinder body 5 and the inner cylinder body 6 are porous cylinders with uneven surfaces, a catalyst is filled between the outer cylinder body 5 and the inner cylinder body 6, the diameter of each pore is smaller than the granularity of the catalyst, a wire mesh is laid between the outer cylinder body 5 and the catalyst, a wire mesh is laid between the inner cylinder body 6 and the catalyst, and the mesh number of the wire mesh is smaller than the granularity of the catalyst.
Propylene epoxidation was carried out in an axial-radial fixed bed reactor having a diameter of 500mm and a height of 4300 mm. The reactor is filled with 120KgTS-1 type titanium silicalite molecular sieve catalyst, and the catalyst is filled in four layers by equal weight. The total feed flow of the hydrogen peroxide solution with the mass content of 50 percent is 45.4Kg/h, and the hydrogen peroxide solution is divided into four strands, enters the first layer of radial flow catalyst bed layer 4 through the material inlet pipe 2, and respectively enters the second, third and fourth layers of radial flow catalyst bed layers 4 through the drainage pipe 11. The total feed flow of the methanol solution with the mass content of 99.5 percent is 320.2Kg/h, and the methanol solution is divided into four strands, enters the first layer of radial flow catalyst bed layer 4 through the material inlet pipe 2, and respectively enters the second, third and fourth layers of radial flow catalyst bed layers 4 through the drainage pipe 11. The total feed flow of the liquid propylene is 115.2Kg/h, and the liquid propylene is divided into four strands, enters a first layer of radial flow catalyst 4 through a material inlet pipe 2, and respectively enters a second layer, a third layer and a fourth layer of radial flow catalyst bed layers 4 through a drainage pipe 11. The pressure of the reactor is adjusted to be 3.2MPa, the temperature of hydrogen peroxide solution, methanol solution and propylene entering the material inlet pipe 2 is adjusted to be 25-40 ℃ by a heater, and then the temperature of the hydrogen peroxide solution (0-25 ℃), the methanol solution (0-25 ℃) and the propylene (0-25 ℃) in the drainage pipe 11 are jointly controlled, so that the inlet temperature and the outlet temperature of each layer of radial flow catalyst bed layer 4 are uniform and controllable. Specifically, when the temperature of the hydrogen peroxide solution, the methanol solution and the propylene solution in the material inlet pipe 2 is 35 ℃, the inlet and outlet temperatures of each radial flow catalyst bed layer 4 are specifically shown in the following table through the common regulation of cold fluid in the drainage pipe 11. Through analysis and detection, the conversion rate of the hydrogen peroxide after the reaction is 98.5 percent, and the selectivity of the propylene oxide is 97 percent. The reacted materials are led out from a material outlet pipe 3 and go to subsequent propylene, propylene oxide and other refining and recycling systems.
| Radial flow catalyst bed | Inlet temperature/. degree.C | Exit temperature/. degree.C |
| A layer of | 35 | 55 |
| Two layers | 35 | 51 |
| Three layers | 36 | 52 |
| Four layers | 38 | 50 |
The present invention is not limited to the embodiments described herein.
The structure and the implementation of the present invention are explained by applying specific embodiments, and the description of the above embodiments is only used to help understand the core idea of the present invention. It should be noted that, for those skilled in the art, without departing from the principle of the present invention, the present invention can be further modified and modified, and such modifications and modifications also fall within the protection scope of the appended claims.
Claims (9)
1. An axial-radial HPPO fixed bed reactor is characterized by comprising a shell (1), wherein the upper end of the shell (1) is provided with a material inlet pipe (2), the lower end of the shell (1) is provided with a material outlet pipe (3), the shell (1) comprises n radial flow catalyst beds (4), and n is an integer more than 2; every radial flow catalyst bed (4) are equipped with outer barrel (5) and interior barrel (6), interior barrel (6) center is equipped with central heat transfer section of thick bamboo (9), the export of central heat transfer section of thick bamboo (9) sets up mixing arrangement (12), install center tube (7) in central heat transfer section of thick bamboo (9), the upper portion of center tube (7) is higher than radial flow catalyst bed (4) the higher part of center tube (7) sets up premixing device (10), every radial flow catalyst bed (4) all are connected with drainage tube (11), drainage tube (11) with center tube (7) upper portion premixing device (10) link to each other.
2. An axial-radial HPPO fixed bed reactor according to claim 1, characterized in that the outer cylinder (5) and the inner cylinder (6) are perforated cylinders with uneven surfaces, that between the outer cylinder (5) and the inner cylinder (6) a catalyst is packed, that the diameter of the perforations is smaller than the particle size of the catalyst, that between the outer cylinder (5) and the catalyst, and between the inner cylinder (6) and the catalyst, wire meshes are laid, the mesh number of which is smaller than the particle size of the catalyst.
3. An axial-radial HPPO fixed bed reactor as claimed in claim 1, characterized in that the lower end of the catalyst is padded with ceramic balls which fill the discharge gap of each section of the radial flow catalyst bed (4), the upper end of the catalyst is also padded with ceramic balls, and the upper end of the radial flow catalyst bed (4) is fixed by a wire mesh, a press ring and a batten after the ceramic balls are padded, wherein the particle size of the ceramic balls is larger than that of the catalyst.
4. An axial HPPO fixed bed reactor according to claim 1, characterized in that the surface of the central tube (7) is provided with regularly arranged nozzles (8), which nozzles (8) are at least one or a combination of fan, cone, or straight flow.
5. An axial-radial HPPO fixed bed reactor according to claim 1, characterized in that the mixing device (12) is packed with at least one of ceramic balls, pall rings, intalox saddles, stepped rings, spherical packing or a combination of several.
6. An axial-radial HPPO fixed bed reactor according to claim 1, characterized in that the premixing device (10) is packed with at least one or a combination of pall rings, intalox saddles, step rings, spherical packing.
7. An axial HPPO fixed bed reactor according to claim 1, characterized in that the upper head is provided with a safety valve (14).
8. An axial HPPO fixed bed reactor according to claim 1, characterized in that a manhole (13) is arranged between adjacent radial flow catalyst beds (4).
9. An axial-radial HPPO fixed bed reactor according to claim 1, characterized in that the bottom of each of said radial flow catalyst beds (4) is provided with discharge openings (15).
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| CN201920462331.5U CN209866000U (en) | 2019-04-08 | 2019-04-08 | Axial-radial HPPO fixed bed reactor |
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| CN201920462331.5U CN209866000U (en) | 2019-04-08 | 2019-04-08 | Axial-radial HPPO fixed bed reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109833832A (en) * | 2019-04-08 | 2019-06-04 | 江苏扬农化工集团有限公司 | A kind of axis radial direction HPPO fixed bed reactors |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109833832A (en) * | 2019-04-08 | 2019-06-04 | 江苏扬农化工集团有限公司 | A kind of axis radial direction HPPO fixed bed reactors |
| CN109833832B (en) * | 2019-04-08 | 2024-01-26 | 江苏扬农化工集团有限公司 | Axial and radial HPPO fixed bed reactor |
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