CN203648503U - Spray circuit reaction device for gas-liquid-solid three-phase catalytic reaction - Google Patents
Spray circuit reaction device for gas-liquid-solid three-phase catalytic reaction Download PDFInfo
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- CN203648503U CN203648503U CN201320808166.7U CN201320808166U CN203648503U CN 203648503 U CN203648503 U CN 203648503U CN 201320808166 U CN201320808166 U CN 201320808166U CN 203648503 U CN203648503 U CN 203648503U
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Abstract
The utility model relates to the technical field of fine chemical engineering, and in particular relates to a reaction device. The spray circuit reaction device for a gas-liquid-solid three-phase catalytic reaction comprises a fixed bed reactor and a stock solution storage tank, wherein a Venturi sprayer is arranged on the top of the fixed bed reactor; a feed port is formed in the Venturi sprayer, and is respectively connected with the discharge port of a first heat exchanger and the discharge port of a second heat exchanger; and the fixed bed reactor is respectively connected with the feed port of the first heat exchanger and the feed port of the second exchanger through a circulating pump. The reaction device does not have the problems of no reaction temperature runaway, reaction heat withdrawal and the like, and can be used for effectively reclaiming reaction heat in a strong exothermic reaction; the reaction device can be used for flexibly controlling the transformation rate of a reaction, the products need no filtration, and continuous operation can be realized; the reaction device has the remarkable advantages of high reaction efficiency, good reaction effect, safety and reliability and the like.
Description
Technical field
The utility model relates to fine chemical technology field, is specifically related to a kind of reaction unit.
Background technology
Nearly all gas-liquid-solid catalytic reaction is all exothermic reaction, and thermal discharge is very large, this just requires heat exchanger itself to have enough exchange capability of heat, be not only as early as possible heating material to be arrived to initial reaction temperature before reaction starts, the more important thing is and in course of reaction, can shift out in time reaction institute liberated heat.
Traditional gas-liquid-solid reactor, as fixed bed catalytic reactor, can only carry out heat exchange by chuck and coiled pipe, and its heat exchange area is subject to the restriction of the size of reactor own, and therefore the size of common response device often can not be done too much.Because reaction heat is removed problem, be also easy to cause reaction temperature runaway, side reaction is serious.And for example in tank reactor, grained catalyst filters difficulty, and cannot realize the problem of continuous operation.
In addition, traditional gas-liquid-solid reactor is owing to being subject to the impact of exchange capability of heat, and often have to be forced to consider with delaying programming rate, and adopt and carry out limited reactions speed compared with the way of low reaction temperatures, minimizing reaction heat, otherwise temperature is by uncontrollable.
The injection reactor of China publication CN201906610U, has realized homogeneous catalytic reaction and gas liquid reaction, but can not realize gas-liquid-solid catalytic reaction, and is difficult to accomplish and effective heat exchange of production technology material the recycling of realization response heat.
China's open source literature " for the loop reactor of gas-solid-liquid heterogeneous reaction " (" chemical equipment technology " 1994 the 15 volume third phases) is introduced effective combination that a kind of loop reactor is injector and reactor, can solve reacting replacing heat problem, but after finishing, reaction also there is the filtration problem of catalyst, particularly to some hydrogenation catalysts, because catalyst itself is very thin, so the filtration problem of post catalyst reaction is difficult to process, and can cause the loss of catalyst itself and product.
Utility model content
The purpose of this utility model is, a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction is provided, and solves above technical problem.
The technical problem that the utility model solves can realize by the following technical solutions:
A kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction, comprise fixed bed reactors, described fixed bed reactors connect a material liquid storage tank, it is characterized in that, the top of described fixed bed reactors is provided with a venturi-type eductors, and the main jet of described venturi-type eductors is towards below, described fixed bed reactors inside;
Described venturi-type eductors is provided with a charging aperture, and described charging aperture connects respectively the discharging opening of First Heat Exchanger, the discharging opening of the second heat exchanger;
Described fixed bed reactors connect respectively the charging aperture of described First Heat Exchanger, the charging aperture of described the second heat exchanger by a circulating pump.
The preferred adopting process material of heat transferring medium of described First Heat Exchanger, the heat transferring medium of described the second heat exchanger preferably adopts cooling water.
When the utility model work, circulating pump starts, and the reaction liquid of initial reaction will be recycled pump and siphon away, the process stream heat exchange in delivering to First Heat Exchanger and producing, and be design temperature by the second heat exchanger maintenance system temperature.Then reactant liquor large flow circulation in loop, in injector place high velocity jet, reaction is proceeded, in the time that the content of product reaches setting till.
Traditional fixed bed catalytic reactor exists reaction heat to withdraw from problem, is easy to cause reaction temperature runaway, and side reaction is serious.And reaction unit of the present utility model can effectively reclaim the reaction heat of strong exothermal reaction by external double heat exchanger, the heat exchange of realization response heat and process stream, and by the automatic control of cooling water heat exchange realization response temperature.
Traditional tank reactor exists grained catalyst to filter difficulty and cannot realize the problem of continuous operation.And reaction unit of the present utility model can be controlled the conversion ratio of reaction flexibly, product, without filtration, can be realized continued operation.
Compared with traditional tubular reactor, overcome in tubular reactor, due to the problem that Gas-liquid interfacial area is little, conversion ratio is not high.Venturi-type eductors in reaction unit of the present utility model is a kind of high efficiency to gas instrument, and it can be uniform in liquid phase by microbubble subtly, produces strong shear-mixed in nozzle, then highly effective reaction in fixed bed bed.
Comparison with existing spray circuits reactor, existing spray circuits reactor can not realization response product without the gas-liquid-solid catalytic reaction of filtering, the design realizes the serial operation of injector and fixed bed reactors, can realize gas-liquid-solid catalytic reaction, and reaction finishes afterproduct without filtering catalyst.This reaction unit design double heat exchanger, is easy to effective heat exchange of realization and production technology material, the recycling of realization response heat.
The discharging opening of described circulating pump also connects a product recycling can.In the time that the content of product reaches setting, just can, by circulating pump discharging to product recycling can, now quantitatively supplement as required fresh reactant liquor.
Described venturi-type eductors is provided with an air inlet, and described air inlet connects a gas buffer tank (safety can).In the utility model gas phase inlet line, gas buffer tank is set, avoids (as delivery side of pump valve is closed by mistake) reactant liquor suck-back under maloperation condition to enter raw gas line and cause production accident.In addition, if there is no the cushioning effect of surge tank, the bad control of feeding rate of gas.
Gas phase porch between described gas buffer tank and described venturi-type eductors is provided with a vapor liquid equilibrium pipe, and described vapor liquid equilibrium pipe is positioned at the top of described fixed bed reactors, and fixed bed reactors inside described in UNICOM.The complete gas of unreacted is got back to fixed bed top, is jointly again sucked and continues on for reacting by venturi-type eductors with live gas by vapor liquid equilibrium pipe, improves the utilization rate of gas and the conversion ratio of reaction, also can avoid system overpressure simultaneously.
The heat transferring medium porch of described the second heat exchanger is provided with a flowmeter, and the charging aperture place of described circulating pump is provided with a temperature controller, described flowmeter and described temperature controller interlocking.The reaction temperature of the inflow control reactant liquor by cooling water, maintenance system temperature is design temperature.
Described material liquid storage tank connects described fixed bed reactors by a material liquid delivery pump.
Described material liquid delivery pump and described fixed bed reactors are provided with a control valve;
Described fixed bed reactors are also provided with a liquid level gauge for detection of reactant liquor liquid level in described fixed bed reactors outward; Described liquid level gauge and described control valve interlocking.In the time that the content of product reaches setting, just can, by circulating pump discharging to product recycling can, now quantitatively supplement fresh reactant liquor according to the registration of the liquid level gauge of fixed bed reactors by control valve.
Described venturi-type eductors comprises main jet, be coated on induction chamber outside described main jet, be positioned at the mixing chamber of described induction chamber below and induction chamber UNICOM, is positioned at the diffuser casing of described mixing chamber below and mixing chamber UNICOM;
Downward, the top of described main jet is provided with nozzle material-feeding mouth to the jet of described main jet, and described nozzle material-feeding mouth is the discharging opening of First Heat Exchanger, the discharging opening of the second heat exchanger described in UNICOM respectively;
One side of described induction chamber is provided with air inlet, and described air inlet is gas buffer tank, described vapor liquid equilibrium pipe described in UNICOM respectively.Nozzle of the present utility model is self-priming high speed nozzle, reaction liquid is large flow circulation in loop, in venturi-type eductors place high velocity jet, form negative pressure at main jet place, unstrpped gas in gas buffer tank is sucked, fully contact at mixing chamber, after going out, in fixed bed reactors, fully react with catalyst granules, preliminary buffering, cooling, gas and fluid separation applications, the complete gas of unreacted is got back to fixed bed top, is jointly again sucked and continues on for reacting by venturi-type eductors with live gas by vapor liquid equilibrium pipe.
The position of the air inlet of described induction chamber side is higher than the jet position of described nozzle.To realize fully contact at mixing chamber.
The inwall of described diffuser casing is up-narrow and down-wide frusto-conical configuration.
Beneficial effect: owing to adopting technique scheme, the reactionless temperature runaway of the utility model, reaction heat such as remove at the problem, can effectively reclaim the reaction heat of strong exothermal reaction.Reaction unit can be controlled the conversion ratio of reaction flexibly, and product, without filtration, can be realized continued operation.There is the remarkable advantages such as reaction efficiency is high, reaction effect good, safe and reliable.
Accompanying drawing explanation
Fig. 1 is a kind of structural representation of the present utility model;
Fig. 2 is a kind of structural representation of the utility model venturi-type eductors.
The specific embodiment
For technological means, creation characteristic that the utility model is realized, reach object and effect is easy to understand, below in conjunction with further elaboration the utility model of concrete diagram.
With reference to Fig. 1, a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction, comprises the fixed bed reactors 4, circulating pump 6, the double heat exchanger that connect successively, and wherein double heat exchanger is First Heat Exchanger 9, the second heat exchanger 8 in parallel.Material liquid storage tank 2 is connected and fixed bed bioreactor 4 by material liquid delivery pump 3, control valve 13 successively.The outer liquid level gauge 12 that is also provided with of fixed bed reactors 4, liquid level gauge 12 is interlocked with control valve 13.The top of fixed bed reactors 4 is provided with venturi-type eductors 5, and the main jet of venturi-type eductors 5 is towards the inner below of fixed bed reactors 4.Venturi-type eductors 5 is provided with charging aperture, air inlet, and charging aperture connects respectively the discharging opening of First Heat Exchanger 9, the discharging opening of the second heat exchanger 8.Air inlet connects respectively gas buffer tank 1, vapor liquid equilibrium pipe 14, and vapor liquid equilibrium pipe 14 is positioned at the top of fixed bed reactors 4, and UNICOM's fixed bed reactors 4 inside.
The preferred adopting process material of heat transferring medium of First Heat Exchanger 9, the heat transferring medium of the second heat exchanger 8 preferably adopts cooling water.
The charging aperture place of circulating pump 6 is provided with temperature controller 11, and the discharging opening of circulating pump 6 also connects product recycling can 7.The heat transferring medium porch of the second heat exchanger 8 is provided with flowmeter 10, and flowmeter 10 is interlocked with temperature controller 11.
With reference to Fig. 2, venturi-type eductors 5 and fixed bed reactors 4 serial operations, venturi-type eductors 5 comprises main jet 15, be coated on induction chamber 16 outside main jet 15, be positioned at the mixing chamber 17 of induction chamber 16 belows and induction chamber 16 UNICOMs, is positioned at the diffuser casing 18 of mixing chamber 17 belows and mixing chamber 17 UNICOMs.The inwall of diffuser casing 18 is up-narrow and down-wide frusto-conical configuration.
Downward, the top of main jet 15 is provided with nozzle material-feeding mouth to the jet of main jet 15, the discharging opening of nozzle material-feeding mouth difference UNICOM First Heat Exchanger 9, the discharging opening of the second heat exchanger 8.One side of induction chamber 16 is provided with air inlet, and air inlet is UNICOM's gas buffer tank 1, vapor liquid equilibrium pipe 14 respectively.The position of the air inlet of induction chamber 16 sides is higher than the jet position of nozzle.
When the utility model work, circulating pump 6 starts, reaction liquid is large flow circulation in loop, in venturi-type eductors 5 place's high velocity jet, at main jet, 15 places form negative pressure, unstrpped gas in gas buffer tank 1 is sucked, fully contact at mixing chamber 17, after going out, in fixed bed reactors 4, fully react with catalyst granules, preliminary buffering, cooling, gas and fluid separation applications, the complete gas of unreacted is got back to fixed bed top, is jointly again sucked and continues on for reacting by venturi-type eductors 5 with live gas by vapor liquid equilibrium pipe 14; The reaction liquid of initial reaction will be recycled pump 6 and siphon away, process stream heat exchange in delivering to First Heat Exchanger 9 and producing, and by the second heat exchanger 8 by public work flow with react outlet temperature chain come maintenance system temperature be design temperature, reaction is proceeded; In the time that the content of product reaches setting, just can, by circulating pump 6 dischargings to product recycling can 7, now show according to the liquid level gauge 12 at the bottom of fixed bed, coordinate control valve 13 quantitatively to supplement fresh reactant liquor.Fixed bed reactors 4 can intermittently operated and continued operation; Fixed bed reactors 4 are semi-automatic operation.
More than show and described basic principle of the present utility model and principal character and advantage of the present utility model.The technical staff of the industry should understand; the utility model is not restricted to the described embodiments; that in above-described embodiment and description, describes just illustrates principle of the present utility model; do not departing under the prerequisite of the utility model spirit and scope; the utility model also has various changes and modifications, and these changes and improvements all fall within the scope of claimed the utility model.The claimed scope of the utility model is defined by appending claims and equivalent thereof.
Claims (10)
1. the spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction, comprise fixed bed reactors, described fixed bed reactors connect a material liquid storage tank, it is characterized in that, the top of described fixed bed reactors is provided with a venturi-type eductors, and the main jet of described venturi-type eductors is towards below, described fixed bed reactors inside;
Described venturi-type eductors is provided with a charging aperture, and described charging aperture connects respectively the discharging opening of First Heat Exchanger, the discharging opening of the second heat exchanger;
Described fixed bed reactors connect respectively the charging aperture of described First Heat Exchanger, the charging aperture of described the second heat exchanger by a circulating pump.
2. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 1, is characterized in that, the heat transferring medium adopting process material of described First Heat Exchanger, and the heat transferring medium of described the second heat exchanger adopts cooling water.
3. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 1, is characterized in that, the discharging opening of described circulating pump also connects a product recycling can.
4. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 1, is characterized in that, described venturi-type eductors is provided with an air inlet, and described air inlet connects a gas buffer tank.
5. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 4, it is characterized in that, gas phase porch between described gas buffer tank and described venturi-type eductors is provided with a vapor liquid equilibrium pipe, described vapor liquid equilibrium pipe is positioned at the top of described fixed bed reactors, and fixed bed reactors inside described in UNICOM.
6. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 5, it is characterized in that, the heat transferring medium porch of described the second heat exchanger is provided with a flowmeter, the charging aperture place of described circulating pump is provided with a temperature controller, described flowmeter and described temperature controller interlocking.
7. according to a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction described in any one in claim 1 to 6, it is characterized in that, described material liquid storage tank connects described fixed bed reactors by a material liquid delivery pump;
Described material liquid delivery pump and described fixed bed reactors are provided with a control valve;
Described fixed bed reactors are also provided with a liquid level gauge for detection of reactant liquor liquid level in described fixed bed reactors outward; Described liquid level gauge and described control valve interlocking.
8. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 5, it is characterized in that, described venturi-type eductors comprises main jet, be coated on induction chamber outside described main jet, be positioned at the mixing chamber of described induction chamber below and induction chamber UNICOM, is positioned at the diffuser casing of described mixing chamber below and mixing chamber UNICOM;
Downward, the top of described main jet is provided with nozzle material-feeding mouth to the jet of described main jet, and described nozzle material-feeding mouth is the discharging opening of First Heat Exchanger, the discharging opening of the second heat exchanger described in UNICOM respectively;
One side of described induction chamber is provided with air inlet, and described air inlet is gas buffer tank, described vapor liquid equilibrium pipe described in UNICOM respectively.
9. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 8, is characterized in that, the position of the air inlet of described induction chamber side is higher than the jet position of described nozzle.
10. a kind of spray circuits reaction unit for gas-liquid-solid three phase catalytic reaction according to claim 8, is characterized in that, the inwall of described diffuser casing is up-narrow and down-wide frusto-conical configuration.
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| CN201320808166.7U CN203648503U (en) | 2013-12-10 | 2013-12-10 | Spray circuit reaction device for gas-liquid-solid three-phase catalytic reaction |
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| CN201320808166.7U CN203648503U (en) | 2013-12-10 | 2013-12-10 | Spray circuit reaction device for gas-liquid-solid three-phase catalytic reaction |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN105413590A (en) * | 2015-12-02 | 2016-03-23 | 青岛迈特达新材料有限公司 | Butane catalytic oxidation reaction device |
| CN107233851A (en) * | 2017-06-23 | 2017-10-10 | 江苏九九久科技有限公司 | A kind of gas liquid reaction method and special purpose device |
| CN111054279A (en) * | 2019-12-31 | 2020-04-24 | 广东雪迪龙环境科技有限公司 | Catalytic oxidation process device and method for magnesium sulfite |
| CN112500418A (en) * | 2020-12-31 | 2021-03-16 | 山东中科新材料研究院有限公司 | Method for synthesizing 1, 8-diazabicycloundecen-7-ene by adopting loop reactor |
| CN112979437A (en) * | 2021-03-05 | 2021-06-18 | 江苏诺盟化工有限公司 | Preparation method of benzaldehyde and special reactor |
| CN113372194A (en) * | 2021-06-10 | 2021-09-10 | 江苏诺盟氢能技术有限公司 | Continuous production method of sodium methoxide |
| CN113372192A (en) * | 2021-06-10 | 2021-09-10 | 江苏诺盟氢能技术有限公司 | Synthetic method of low-carbon sodium alkoxide |
| CN114225884A (en) * | 2021-12-29 | 2022-03-25 | 江苏吉华化工有限公司 | Continuous nitration reaction device |
| CN114486584A (en) * | 2020-11-12 | 2022-05-13 | 国家能源投资集团有限责任公司 | Measuring device, nozzle and nozzle assembly of catalyst intensity |
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2013
- 2013-12-10 CN CN201320808166.7U patent/CN203648503U/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105413590A (en) * | 2015-12-02 | 2016-03-23 | 青岛迈特达新材料有限公司 | Butane catalytic oxidation reaction device |
| CN105413590B (en) * | 2015-12-02 | 2018-03-06 | 青岛迈特达新材料有限公司 | A kind of catalyzed butane oxidation reaction unit |
| CN107233851A (en) * | 2017-06-23 | 2017-10-10 | 江苏九九久科技有限公司 | A kind of gas liquid reaction method and special purpose device |
| CN107233851B (en) * | 2017-06-23 | 2020-06-23 | 江苏九九久科技有限公司 | Gas-liquid reaction method and special device |
| CN111054279A (en) * | 2019-12-31 | 2020-04-24 | 广东雪迪龙环境科技有限公司 | Catalytic oxidation process device and method for magnesium sulfite |
| CN114486584A (en) * | 2020-11-12 | 2022-05-13 | 国家能源投资集团有限责任公司 | Measuring device, nozzle and nozzle assembly of catalyst intensity |
| CN112500418A (en) * | 2020-12-31 | 2021-03-16 | 山东中科新材料研究院有限公司 | Method for synthesizing 1, 8-diazabicycloundecen-7-ene by adopting loop reactor |
| CN112979437A (en) * | 2021-03-05 | 2021-06-18 | 江苏诺盟化工有限公司 | Preparation method of benzaldehyde and special reactor |
| CN113372194A (en) * | 2021-06-10 | 2021-09-10 | 江苏诺盟氢能技术有限公司 | Continuous production method of sodium methoxide |
| CN113372192A (en) * | 2021-06-10 | 2021-09-10 | 江苏诺盟氢能技术有限公司 | Synthetic method of low-carbon sodium alkoxide |
| CN113372194B (en) * | 2021-06-10 | 2023-09-01 | 江苏诺盟氢能技术有限公司 | Continuous production method of sodium methoxide |
| CN114225884A (en) * | 2021-12-29 | 2022-03-25 | 江苏吉华化工有限公司 | Continuous nitration reaction device |
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