CN210079474U - Multistage cold shock formula fixed bed reactor material distributor group - Google Patents
Multistage cold shock formula fixed bed reactor material distributor group Download PDFInfo
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- CN210079474U CN210079474U CN201920664424.6U CN201920664424U CN210079474U CN 210079474 U CN210079474 U CN 210079474U CN 201920664424 U CN201920664424 U CN 201920664424U CN 210079474 U CN210079474 U CN 210079474U
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- 239000000463 material Substances 0.000 title claims abstract description 83
- 230000035939 shock Effects 0.000 title claims abstract description 17
- 239000007791 liquid phase Substances 0.000 claims abstract description 98
- 239000012071 phase Substances 0.000 claims abstract description 66
- 239000007789 gas Substances 0.000 claims abstract description 40
- 239000007792 gaseous phase Substances 0.000 claims abstract description 20
- 238000004804 winding Methods 0.000 claims abstract description 14
- 238000010791 quenching Methods 0.000 claims description 5
- 238000004891 communication Methods 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 2
- 230000000149 penetrating effect Effects 0.000 claims 1
- 239000003054 catalyst Substances 0.000 abstract description 12
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 45
- 238000006243 chemical reaction Methods 0.000 description 10
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 description 8
- 238000000034 method Methods 0.000 description 5
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 4
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 4
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 3
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 description 3
- 238000000889 atomisation Methods 0.000 description 3
- 239000003245 coal Substances 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
- 239000002131 composite material Substances 0.000 description 2
- 230000008602 contraction Effects 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- SQNZJJAZBFDUTD-UHFFFAOYSA-N durene Chemical compound CC1=CC(C)=C(C)C=C1C SQNZJJAZBFDUTD-UHFFFAOYSA-N 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000010117 shenhua Substances 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 230000008646 thermal stress Effects 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 description 1
- 229910021536 Zeolite Inorganic materials 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 238000004939 coking Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000004941 influx Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000035882 stress Effects 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 239000008096 xylene Substances 0.000 description 1
- 239000010457 zeolite Substances 0.000 description 1
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Abstract
The utility model provides a multistage cold shock formula fixed bed reactor material distributor group, including liquid phase pipe, gaseous phase pipe and a plurality of combination nozzles, combination nozzle is equipped with the liquid phase feedstock channel who communicates with liquid phase pipe respectively and the gaseous phase feedstock channel who communicates with gaseous phase pipe for make up the blowout with the liquid phase material in the liquid phase pipe and the gaseous phase material in the gaseous phase pipe, and the interval distribution has a plurality of spiral winding pipes on the liquid phase pipe, and the spiral winding pipe is coiled by straight tube spiral and is formed; the gas phase pipe is provided with a plurality of nozzle holes along the length direction, and the combined nozzle is arranged at the position corresponding to the nozzle holes in the gas phase pipe respectively so as to discharge materials sprayed out by the combined nozzle through the nozzle holes. The utility model provides a multistage cold shock formula fixed bed reactor material distributor group can realize the abundant evenly distributed that atomizes of material high-efficiently, accurate control catalyst bed temperature, assurance target product yield and the long period steady operation of catalyst.
Description
Technical Field
The utility model belongs to the fixed bed field, in particular to multistage cold shock formula fixed bed reactor material distributor group.
Background
China has abundant coal resources and huge methanol yield obtained by coal conversion, so that the development of the technology for preparing propylene, aromatic hydrocarbon and gasoline from methanol or dimethyl ether has important strategic significance.
The reaction of preparing propylene, aromatic hydrocarbon or gasoline (MTN for short) from methanol or dimethyl ether is a strong exothermic process, and the methanol conversion reaction is seriously influenced by temperature. In the reaction process, especially in a fixed bed reaction system, heat cannot be removed in time, so that the temperature runaway of the reactor can be caused, the yield of reaction products is reduced, and the catalyst is quickly deactivated. The methanol conversion reaction is mostly carried out under the catalysis of acid sites on the surface of the molecular sieve catalyst, the catalyst can also carry out coking reaction besides the generated products, so that carbon deposition in a catalytic activity center is inactivated, and when the carbon deposition amount reaches a certain degree, the reaction needs to be stopped, and the molecular sieve catalyst is subjected to scorching regeneration treatment. Temperature control is an important index for guaranteeing the overall activity and service life of the catalyst.
Shanxi Zeolite science and technology Limited and Sading engineering Limited (CN201410704722.5) disclose a method for preparing aromatic hydrocarbon mixture rich in benzene, toluene and xylene by methanol conversion in a fixed bed reactor, wherein methanol steam is divided into a plurality of strands, one of the strands is mixed with circulating LPG and water vapor and then enters the fixed bed reactor from a material inlet arranged at the top of the fixed bed reactor, and the rest of the methanol steam enters the fixed bed reactor from a material inlet positioned on the side wall of the reactor to obtain the aromatic hydrocarbon mixture rich in BTX.
The high-environment-friendly energy research institute company and the Dalian Longtai science and technology development company (CN201511026372.2) disclose a device for preparing gasoline from methanol and a method for preparing gasoline by using the device and taking methanol as a raw material through catalytic reaction, wherein a reaction system comprises a raw material supply end, a vaporizer, a heating furnace and a fixed bed reactor; at least two bed layers are arranged in the fixed bed reactor in the vertical direction, and a gas distributor is arranged between the bed layers; the utility model has the advantages of simple process, short flow, low operation energy consumption, low investment, few byproducts and durene content (mass fraction) in the gasoline lower than 2 percent.
Shenhua group Limited liability company and Shenhua Ningxia coal industry group Limited liability company (CN 201510954855.2) disclose a method for preparing propylene from methanol, dimethyl ether generated by methanol dehydration is separated from raw material methanol, fresh methanol and unreacted methanol are merged into a first reactor, dimethyl ether and water enter a second reactor and respectively enter different beds of the reactors from the top and the side of the reactor, the temperature is accurately controlled, and the high propylene selectivity and the catalyst single-cycle life are ensured.
In MTN reaction process, adopt each bed temperature of intersegment quench means control, guarantee that temperature regulation is accurate in every bed catalyst interval, just require the quench material fully to atomize under given load condition, distribute evenly, above-mentioned utility model all adopts intersegment quench control bed temperature, material distribution etc. but does not have concrete description material distributor and technology.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a be used for multistage cold shock formula fixed bed reactor material distributor group for realize the abundant evenly distributed that atomizes of material high-efficiently, accurate control catalyst bed temperature, guarantee target product yield and catalyst long period steady operation.
In order to achieve the above object, the utility model adopts the following technical scheme:
the multi-stage cold shock type fixed bed reactor material distributor group comprises a liquid phase pipe for conveying liquid phase materials, a gas phase pipe for conveying gas phase materials and a plurality of combined nozzles, wherein the combined nozzles are provided with a liquid phase feeding channel communicated with the liquid phase pipe and a gas phase feeding channel communicated with the gas phase pipe respectively and used for carrying out combined ejection on the liquid phase materials in the liquid phase pipe and the gas phase materials in the gas phase pipe, a plurality of spiral winding pipes are distributed on the liquid phase pipe at intervals, and the spiral winding pipes are formed by spirally winding straight pipes; the gas phase pipe is provided with a plurality of nozzle holes along the length direction, and the combined nozzle is arranged at the position in the gas phase pipe corresponding to the nozzle holes respectively so as to discharge the materials sprayed out by the combined nozzle through the nozzle holes.
The utility model discloses an in the structure, through set up a plurality of spirals on the liquid phase pipe and lead to pipeline deformation, tearing problem around the thermal stress shrink that the difference in temperature between cold material and the inside high temperature environment of reactor arouses in the liquid phase pipe, the continuous, feeding steadily of liquid phase material in the guarantee liquid phase pipe.
Preferably, the front end of the liquid phase pipe communicating with each combined nozzle is the spirally wound pipe.
The utility model discloses in the structure, the front end of the intercommunication department of liquid phase pipe and combination nozzle indicates by the flow direction along the intraductal liquid phase material of liquid phase, and the liquid phase pipe section that the liquid phase material belonged to before the combination nozzle of influx can be said to be located the front end of the intercommunication department of liquid phase pipe and combination nozzle.
Preferably, the liquid phase pipe and the gas phase pipe are arranged in parallel, so that the arrangement and installation of pipelines are convenient, and cold and hot materials can be randomly adjusted according to the reaction temperature of a bed layer.
Preferably, the liquid phase pipe and the gas phase pipe are both annular pipes, a liquid phase feed port for feeding liquid phase materials of the reactor is arranged on the liquid phase pipe, and a gas phase feed port for feeding gas phase materials of the reactor is arranged on the gas phase pipe.
Preferably, the liquid phase pipe is an equal-diameter pipe, namely the inner diameters of the spiral wound pipe of the liquid phase pipe and other pipe sections of the liquid phase pipe are equal everywhere.
Preferably, the combination nozzle comprises an inner nozzle and an outer nozzle, the inner nozzle being arranged through the outer nozzle so as to form a liquid-phase feed channel within the inner nozzle and a gas-phase feed channel between the outer nozzle and the inner nozzle; the side wall of the inner nozzle is provided with a plurality of airflow holes for introducing part of gas-phase materials in the gas-phase feeding channel into the liquid-phase feeding channel; and a swirler is arranged in the liquid-phase feeding channel and is used for fully mixing the gas-phase material entering the liquid-phase feeding channel with the liquid-phase material in the liquid-phase feeding channel and performing swirl spraying.
Preferably, the outer wall of the inner nozzle is further provided with an annular protruding portion extending into the gas-phase feeding channel, and the protruding portion is further distributed with a plurality of swirl grooves for enabling the gas-phase material in the gas-phase feeding channel to form swirl after flowing through the swirl grooves.
Preferably, the air flow holes are arranged along a tangential direction of the inner wall of the inner nozzle.
Preferably, the outlet end of the outer nozzle is provided with an end plate for plugging the gas-phase feeding channel, and the end plate is provided with one or more swirl holes, so that the gas-phase material of the gas-phase feeding channel is swirled and sprayed out through the swirl holes.
The utility model discloses following beneficial technological effect has:
the utility model provides a multistage cold shock formula fixed bed reactor material distributor group sets up a plurality ofly by the coiled spiral of straight tube spiral around the pipe through interval on the liquid phase pipe, has solved the thermal stress shrink that cold liquid phase material and the inside high temperature environment of reactor between the difference in temperature arouse in the liquid phase pipe to the pipeline that leads to warp, tearing problem, also further guarantee in the liquid phase pipe continuous, the feeding steadily of liquid phase material.
The utility model discloses in be provided with a plurality of nozzle holes at the length direction of gas phase pipe, the position that the nozzle hole corresponds is established to the combination nozzle, can accurately will be discharged by the nozzle hole through gas phase material, the liquid phase material after the combination nozzle mixes.
Drawings
FIG. 1 is a schematic structural diagram of a material distributor group of a multistage cold quenching type fixed bed reactor of the present invention;
FIG. 2 is a preferred embodiment of the composite spout of the present invention;
FIG. 3 is a cross-sectional view taken along line A-A of the inner nozzle of FIG. 2;
the gas-liquid separator comprises a liquid phase pipe 1, a liquid phase pipe 2, a gas phase pipe 3, a protruding part 4, a combined nozzle 5, an inner nozzle 6, an outer nozzle 7, a cyclone 8, a spiral winding pipe 9, a gas phase feeding channel 10, a liquid phase feeding channel 11, a cyclone groove 12, an airflow hole 13 and a cyclone hole.
Detailed Description
The present invention will be described in detail with reference to examples. In which like parts are designated by like reference numerals. It should be noted that the terms "front," "back," "left," "right," "upper" and "lower" used in the following description refer to directions in the drawings of the specification, and the terms "inner" and "outer" refer to directions toward and away from, respectively, the geometric center of a particular component.
As shown in fig. 1, the utility model provides a multistage cold shock formula fixed bed reactor material distributor group, including the liquid phase pipe 1 that is used for carrying the liquid phase material, a gaseous phase pipe 2 and a plurality of combination nozzle 4 for carrying the gaseous phase material, combination nozzle 4 is equipped with respectively with liquid phase feed channel 10 of liquid phase pipe 1 intercommunication and with gaseous phase feed channel 9 of gaseous phase pipe 2 intercommunication for make up the blowout with the gaseous phase material in the liquid phase pipe 1 and the gaseous phase pipe 2, interval distribution has a plurality of spirals around pipe 8 on the liquid phase pipe 1.
In the structure of the utility model, the liquid phase pipe 1 and the gas phase pipe 2 are both annular pipes, the liquid phase pipe 1 is provided with a liquid phase feed inlet for feeding liquid phase materials of the reactor, and the gas phase pipe 2 is provided with a gas phase feed inlet for feeding gas phase materials of the reactor; a plurality of the combined nozzles 4 are distributed at intervals along the material flow direction of the liquid phase pipe 1 and the gas phase pipe 2; meanwhile, the gas phase pipe 2 is provided with a plurality of nozzle holes along the length direction, and the combined nozzles 4 are arranged in the gas phase pipe 2 and in one-to-one correspondence with the nozzle holes, so that the materials mixed by gas and liquid in the combined nozzles 4 are discharged from the nozzle holes.
The utility model provides a fixed bed reactor material distributor group can be according to catalyst bed plane scope and atomizing nozzle area of coverage accounting combination nozzle 4's quantity, and the adjustment is nimble, adapts to different reactor sizes. In some embodiments, the liquid phase pipe 1 and the gas phase pipe 2 are arranged in parallel, which facilitates the arrangement and installation of pipelines.
The liquid phase material in the liquid phase pipe 1 passes through the spiral winding pipe 8 when entering the front end of the communication part of the combined nozzle 4, thereby ensuring that the liquid phase material can fully carry out heat exchange with the temperature in the reactor in the liquid phase pipe 1 before entering the combined nozzle 4.
The spiral winding pipe 8 is formed by spirally winding a straight pipe, and the inner diameters of the spiral winding pipe 8 on the liquid phase pipe 1 and other pipe sections of the liquid phase pipe 1 are equal, so that the inner diameter of the liquid phase pipe 1 in the whole direction is not changed, the flowing of liquid phase materials in a pipeline is stable and rapid, the impact force on the pipe wall is small, the elastic stress caused by expansion with heat and contraction with cold can be better resisted, and the acting force generated by expansion and contraction of the pipeline is reduced.
In the present invention, as shown in fig. 2, the composite spout 4 includes an inner spout 5 and an outer spout 6, the inner spout 5 is inserted into the outer spout 6, so that a liquid phase feeding passage 10 is formed inside the inner spout 5, and a gas phase feeding passage 9 is formed between the outer spout 6 and the inner spout 5.
A plurality of airflow holes 12 are formed in the side wall of the inner nozzle 5 and used for introducing a part of gas-phase materials in the gas-phase feeding channel 9 into the liquid-phase feeding channel 10; in some embodiments, as shown in fig. 3, the airflow holes 12 are arranged along a tangential direction of the inner wall of the inner nozzle 5.
In some embodiments, the outer wall of the inner nozzle 5 is further provided with an annular protrusion 3 extending into the gas-phase feed channel 9, and the protrusion 3 is further distributed with a plurality of swirl grooves 11 for forming a swirl after the gas-phase material in the gas-phase feed channel 9 flows through the swirl grooves 11.
The utility model discloses an in the structure, be equipped with swirler 7 in liquid phase feedstock channel 10, the gaseous phase material that comes from in liquid phase feedstock channel 10 and the liquid phase material that gets into in liquid phase feedstock channel 10 can intensive mixing and whirl blowout in swirler 7.
The utility model discloses an in the structure, the outlet end of outer nozzle 6 is equipped with the end plate of shutoff gaseous feed channel 9, has seted up one or more whirl hole 13 on the end plate to make gaseous phase feed channel 9's gaseous phase material spout via 13 whirl holes whirl.
After the gas-phase material enters the combined nozzle 4 through the gas-phase feeding channel 9, a part of the gas-phase material is mixed with the liquid-phase material in the liquid-phase feeding channel 10 through the airflow holes 12 on the inner nozzle 5 to form spray, and the spray is rotationally sprayed out through the swirler 7; another part of the gas phase material passes through the protruding part 3 on the inner nozzle 5, so that the gas phase material flow passes through a plurality of swirl grooves 11 distributed on the protruding part 3 and is rotationally sprayed out through swirl holes 13 on the outer nozzle 6, further atomization is realized, and the atomization range is enlarged.
To the design of the utility model, the liquid phase feed channel 10 no longer only relies on pressure atomization, but promotes the liquid phase forward through sneaking into of air current, has improved the atomizing homogeneity.
In the present invention, the specific connection/communication manner of the combination nozzle 4 and the liquid phase pipe 1 and the gas phase pipe 2 is well known in the art, for example, the connection/communication is performed by the connection end seat of the combination nozzle 4, which is not described herein again.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (9)
1. Multistage cold shock formula fixed bed reactor material distributor group, including liquid phase pipe (1) that is used for carrying the liquid phase material, gaseous phase pipe (2) and a plurality of combination nozzle (4) that are used for carrying gaseous phase material, combination nozzle (4) be equipped with respectively with liquid phase feed channel (10) of liquid phase pipe (1) intercommunication and with gaseous phase feed channel (9) of gaseous phase pipe (2) intercommunication for with liquid phase material in liquid phase pipe (1) and gaseous phase material in gaseous phase pipe (2) make up the blowout, its characterized in that: a plurality of spiral winding pipes (8) are distributed on the liquid phase pipe (1) at intervals, and the spiral winding pipes (8) are formed by spirally winding a straight pipe; the gas phase pipe (2) is provided with a plurality of nozzle holes along the length direction, and the combined nozzle (4) is arranged at the position in the gas phase pipe (2) corresponding to the nozzle holes respectively so as to discharge the materials sprayed out by the combined nozzle (4) through the nozzle holes.
2. The multi-stage cold shock fixed bed reactor material distributor group of claim 1, wherein: the front end of the communication part of the liquid phase pipe (1) and each combined nozzle (4) is the spiral winding pipe (8).
3. The multi-stage cold shock fixed bed reactor material distributor group of claim 2, wherein: the liquid phase pipe (1) and the gas phase pipe (2) are arranged in parallel.
4. The multi-stage cold shock fixed bed reactor material distributor group of claim 3, wherein: the reactor is characterized in that the liquid phase pipe (1) and the gas phase pipe (2) are both annular pipes, a liquid phase feed inlet for feeding liquid phase materials of the reactor is formed in the liquid phase pipe (1), and a gas phase feed inlet for feeding gas phase materials of the reactor is formed in the gas phase pipe (2).
5. The bank of multistage cold shock fixed bed reactor materials distributor of claim 4, wherein: the liquid phase pipe (1) is an equal-diameter pipe.
6. The multi-stage quench fixed bed reactor material distributor group of any one of claims 1-5, wherein:
the combined nozzle (4) comprises an inner nozzle (5) and an outer nozzle (6), the inner nozzle (5) is arranged in the outer nozzle (6) in a penetrating way, so that a liquid-phase feeding channel (10) is formed in the inner nozzle (5), and a gas-phase feeding channel (9) is formed between the outer nozzle (6) and the inner nozzle (5);
the side wall of the inner nozzle (5) is provided with a plurality of airflow holes (12) for introducing part of gas-phase materials in the gas-phase feed channel (9) into the liquid-phase feed channel (10); and a swirler (7) is arranged in the liquid-phase feeding channel (10) and is used for fully mixing the gas-phase material entering the liquid-phase feeding channel (10) with the liquid-phase material in the liquid-phase feeding channel (10) and performing swirl spraying.
7. The multi-stage cold shock fixed bed reactor material distributor group of claim 6, wherein: the outer wall of the inner nozzle (5) is further provided with an annular protruding portion (3) extending into the gas-phase feeding channel (9), and a plurality of swirl grooves (11) are further distributed on the protruding portion (3) and used for enabling gas-phase materials in the gas-phase feeding channel (9) to flow through the swirl grooves (11) to form swirl.
8. The bank of multistage cold shock fixed bed reactor materials distributor of claim 7, wherein: the airflow holes (12) are arranged along the tangential direction of the inner wall of the inner nozzle (5).
9. The bank of multistage cold shock fixed bed reactor materials distributor of claim 8, wherein: the outlet end part of the outer nozzle (6) is provided with an end plate for plugging the gas-phase feeding channel (9), and one or more swirl holes (13) are formed in the end plate so that gas-phase materials of the gas-phase feeding channel (9) can be swirled and sprayed out through the swirl holes (13).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920664424.6U CN210079474U (en) | 2019-05-10 | 2019-05-10 | Multistage cold shock formula fixed bed reactor material distributor group |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920664424.6U CN210079474U (en) | 2019-05-10 | 2019-05-10 | Multistage cold shock formula fixed bed reactor material distributor group |
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| CN210079474U true CN210079474U (en) | 2020-02-18 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112316885A (en) * | 2020-09-29 | 2021-02-05 | 中国船舶重工集团公司第七一一研究所 | Gas-liquid distribution device and reaction tower |
| CN113694835A (en) * | 2021-09-30 | 2021-11-26 | 江苏航运职业技术学院 | Spiral propelling fixed bed reactor |
-
2019
- 2019-05-10 CN CN201920664424.6U patent/CN210079474U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112316885A (en) * | 2020-09-29 | 2021-02-05 | 中国船舶重工集团公司第七一一研究所 | Gas-liquid distribution device and reaction tower |
| CN113694835A (en) * | 2021-09-30 | 2021-11-26 | 江苏航运职业技术学院 | Spiral propelling fixed bed reactor |
| CN113694835B (en) * | 2021-09-30 | 2023-06-27 | 江苏航运职业技术学院 | Spiral propulsion fixed bed reactor |
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