CN2581061Y - Gas-liquid parallel flow reactor - Google Patents
Gas-liquid parallel flow reactor Download PDFInfo
- Publication number
- CN2581061Y CN2581061Y CN 02286630 CN02286630U CN2581061Y CN 2581061 Y CN2581061 Y CN 2581061Y CN 02286630 CN02286630 CN 02286630 CN 02286630 U CN02286630 U CN 02286630U CN 2581061 Y CN2581061 Y CN 2581061Y
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- CN
- China
- Prior art keywords
- tower body
- gas
- liquid
- distributor
- heat exchange
- 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.)
- Expired - Lifetime
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Abstract
The utility model discloses a gas-liquid parallel flow reactor in the field of chemical industries or correlation techniques. The utility model is mainly characterized in that a heat exchanging distributing apparatus with a novel structure and a vortex type gas-liquid separator are arranged in a tower body. The integration of reaction and separation is realized. Other associated equipment is reduced so that oxidized yield is increased from the existing about 90% to more than 98%. The utility model has the advantages of low equipment investment, low maintenance cost and high yield of benefit.
Description
Technical field
The utility model relates to a kind of device of chemical technology field, relates in particular to a kind of gas and liquid flowing reactor.
Background technology
Existing gas and liquid flowing reactor, be made of a joint or two joint reaction towers, tower bottom has end-of-the-pipe, has gas inlet tube, liquid inlet and heat exchanger in the tower body, owing to himself structural reason, there are two big deficiencies, the one, its heat exchanger has taken dischargeable capacity, hinders material stream passed, cause bias current, oxidation is incomplete, thereby oxidization-hydrogenation ratio is low, and 88-92% is generally only arranged; The 2nd, can not make gas-liquid separation, thereby also need outside device, gas-liquid separator, oxidation liquid storage tank and oxidation liquid pump to be set, the site location that a large amount of hold facilities is more, and increased pipe arrangement cost and workload.
Summary of the invention
The purpose of this utility model provides gas and liquid flowing reactor a kind of integrated reaction and separation, that improve oxidization-hydrogenation ratio at the deficiency that existing gas and liquid flowing reactor exists.
The purpose of this utility model is achieved through the following technical solutions: a kind of gas and liquid flowing reactor, comprise tower body, the end-of-the-pipe of tower body bottom, feed gas inlet tube and the liquid inlet on the tower body wall and several manholes on the tower body wall in the tower body, it is characterized in that fixedly installing the heat exchange type distributor on the tower body inwall bearing of the gas inlet tube top in the tower body, the medium of heat exchange type distributor is imported and exported pipe and is passed the tower body wall, on the tower body inwall bearing of heat exchange type distributor top the spiral-flow type gas-liquid separator is set, the tower body inner top of spiral-flow type gas-liquid separator top is provided with demister, demister communicates with gas vent on the tower body top wall, is provided with by leading to the outer liquid outlet tube of tower body in the tower body on the other tower body wall of spiral-flow type gas-liquid separator; The spiral-flow type gas-liquid separator is made of the vertex of a cone of central tube, the solid welding of central tube lower port and the cyclone of upper port solid welding, and the big bead solid welding of the vertex of a cone is on the bearing of tower body inwall; Cyclone is made of some vortex boards along central nozzle one all solid weldings between two blocks of plectanes that spacing arranged and the plectane, on the above tower body wall of spiral-flow type gas-liquid separator bearing interface of the level gauge is set, and on the tower body wall on the nearly bearing discharging hole is set; The heat exchange type distributor is imported and exported by casing, the medium that communicates with cabinets cavity vertically disposedly in pipe, the casing somely has the deflection plate of spacing and the vertical some distributor pipes that pass casing to constitute; Deflection plate one end and cabinet wall solid welding, the other end and cabinet wall have spacing, and an adjacent deflection plate oppositely fixedly installs; Distributor pipe upper orifice end is provided with pipe cap, and some through holes are arranged on the pipe cap; It is total that pipe cap can be many distributor pipes.
The utility model is by being provided with heat exchange type distributor and spiral-flow type gas-liquid separator in tower body, the one, substituted existing U-shaped heat exchange of heat pipe, make the repeatedly heat exchange distribution in device of gas liquid reaction material, guarantee gas-liquid material even contact, the yield of oxidation reaction is brought up to more than 98% by existing about 90%, can be cooled off reaction mass again; The 2nd, gas-liquid mixture directly separates in device, gas-liquid mixture enters the spiral-flow type gas-liquid separator from central tube, separating back gas discharges from cat head through demister, liquid is discharged through the fluid-tight trailing flank, has realized integrated reaction and separation, reduces the apparatus arrangement engaged position, reduce pipe arrangement cost and workload, and gas-liquid separation is more complete, utilizes the pressure reduction of operating pressure and separation liquid level, uses the atmospheric extraction tower that the tower working solution is directly sent into subsequent processing.Adopt the utility model, a large amount of equipment investments and a large amount of maintenance costs had both been reduced, the output that high yield is arranged again, experiment shows, the utility model device that to produce 50000 tons of concentration per year be 27.5% hydrogen peroxide, oxidization-hydrogenation ratio improves 6%, is consuming under the constant fully situation, every year can the fecund 3000 tons of products, nearly 3,000,000 yuan of direct economic benefit.The utility model has very remarkable economic efficiency and social benefit.
Description of drawings
Accompanying drawing 1 is the utility model sectional structure schematic diagram
Accompanying drawing 2 is a heat exchange type structure of distributor schematic diagram in the utility model
Accompanying drawing 3 is the plan structure schematic diagram of heat exchange type distributor after removing top panel in the utility model
In the accompanying drawing, the 1st, gas inlet tube, the 2nd, heat exchange type distributor, the 3rd, media outlet pipe, the 4th, temperature-measuring port, the 5th, liquid level gauge lower interface, the 6th, central tube, the 7th, interface on the liquid level gauge, the 8th, gas vent, the 9th, demister, the 10th, cyclone, the 11st, manhole, the 12nd, liquid outlet, the 13rd, the vertex of a cone, the 14th, discharging hole, the 15th, tower body, the 16th, pipe cap, the 17th, heat exchange distributor pipe, the 18th, medium inlet, the 19th, liquid inlet, the 20th, sewage draining exit, the 21st, deflection plate.
The specific embodiment
The bottom of the utility model tower body 15 is a sewage draining exit 20, gas inlet tube 1 and the solid liquid inlet of stretching in the tower body 19 on the tower body wall of dress arranged at tower body 15 bottoms, tower body 15 is provided with several manholes 11 from bottom to top, temperature-measuring port 4 is set, liquid level gauge lower interface 5, interface 7 on the liquid level gauge, gas vent 8 is arranged at tower body 15 tops, fixedly install heat exchange type distributor 2 on the bearing of gas inlet tube 1 top tower body inwall in the tower body 15, the media outlet pipe 3 of heat exchange type distributor 2, medium inlet 18 passes tower body 15 walls respectively, some deflection plates 21 that spacing is arranged mutually vertically are set in the casing chamber of heat exchange type distributor 2, one end of deflection plate 21 and inboard wall of tube body solid welding, the other end and cabinet wall have spacing, 21 of adjacent deflection plates oppositely fixedly install, thereby form the medium runner of a plurality of S shapes, the some heat exchange distributor pipes 17 that vertically pass casing are set, distributor pipe 17 upper orifice ends are provided with pipe cap 16, some through holes are arranged on the pipe cap 16, and it is total that pipe cap 16 also can be many distributor pipes 17; Solid welding spiral-flow type gas-liquid separator on the bearing of heat exchange type distributor 2 top tower body inwalls, the spiral-flow type gas-liquid separator is by the vertex of a cone 13, central tube 6 and cyclone 10 constitute, the big bead of the vertex of a cone 13 and bearing solid welding, one end solid welding of its osculum and central tube 6, the other end of central tube and cyclone 10 solid weldings, cyclone 10 is made of some vortex boards along central nozzle one all solid weldings between two blocks of plectanes that spacing arranged and the plectane, the liquid outlet 12 that solid welding is stretched out from inside to outside on the tower body wall of spiral-flow type gas-liquid separator one side, the vertex of a cone 13 bearings tops is solid welding discharging hole 4 on the tower body wall at place a bit, and the tower body top gas exports in the tower body of 8 belows and is provided with demister 9.
Claims (7)
1, a kind of gas and liquid flowing reactor, comprise tower body, the end-of-the-pipe of tower body bottom, feed gas inlet tube and liquid inlet on the tower body wall and the some manholes on the tower body wall in the tower body, it is characterized in that fixedly installing the heat exchange type distributor on the tower body inwall bearing of the gas inlet tube top in the tower body, the medium of heat exchange type distributor is imported and exported pipe and is passed the tower body wall, on the tower body inwall bearing of heat exchange type distributor top the spiral-flow type gas-liquid separator is set, the tower body inner top of spiral-flow type gas-liquid separator top is provided with demister, demister communicates with gas vent on the tower body top wall, is provided with by leading to the outer liquid outlet tube of tower body in the tower body on the other tower body wall of spiral-flow type gas-liquid separator.
2, gas and liquid flowing reactor according to claim 1 is characterized in that the spiral-flow type gas-liquid separator is made of the vertex of a cone of central tube, the solid welding of central tube lower port and the cyclone of upper port solid welding, and the big bead solid welding of the vertex of a cone is on the bearing of tower body inwall.
3, gas and liquid flowing reactor according to claim 1 and 2 is characterized in that the cyclone in the spiral-flow type gas-liquid separator is made of some vortex boards along central nozzle one all solid weldings between two blocks of plectanes that spacing arranged and the plectane.
4, gas and liquid flowing reactor according to claim 1 and 2 is characterized in that on the above tower body wall of spiral-flow type gas-liquid separator bearing interface of the level gauge being set, and on the tower body wall on the nearly bearing discharging hole is set.
5, gas and liquid flowing reactor according to claim 1 is characterized in that the heat exchange type distributor imported and exported by casing, the medium that communicates with cabinets cavity and vertically disposedly in pipe, the casing somely have the deflection plate of spacing and the vertical some distributor pipes that pass casing to constitute.
6, gas and liquid flowing reactor according to claim 1 or 5 is characterized in that deflection plate one end and cabinet wall solid welding in the heat exchange type distributor, and the other end and cabinet wall have spacing, and an adjacent deflection plate oppositely fixedly installs.
7, gas and liquid flowing reactor according to claim 1 or 5 is characterized in that the distributor pipe upper orifice end in the heat exchange type distributor is provided with pipe cap, and some through holes are arranged on the pipe cap, and it is total that pipe cap also can be many distributor pipes.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02286630 CN2581061Y (en) | 2002-12-09 | 2002-12-09 | Gas-liquid parallel flow reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 02286630 CN2581061Y (en) | 2002-12-09 | 2002-12-09 | Gas-liquid parallel flow reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN2581061Y true CN2581061Y (en) | 2003-10-22 |
Family
ID=33747286
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 02286630 Expired - Lifetime CN2581061Y (en) | 2002-12-09 | 2002-12-09 | Gas-liquid parallel flow reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN2581061Y (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102269491A (en) * | 2010-06-07 | 2011-12-07 | 四川空分设备(集团)有限责任公司 | Noncondensable gas separation and refrigerant recycling device and method for refrigerating system |
| CN102641716A (en) * | 2012-04-24 | 2012-08-22 | 江苏长荣化工设备有限公司 | Combined heat-transferring dispersing reaction device |
| CN102674428A (en) * | 2012-05-17 | 2012-09-19 | 贵州红星发展股份有限公司 | High-whiteness spherical nano barium sulfate and preparation method thereof |
-
2002
- 2002-12-09 CN CN 02286630 patent/CN2581061Y/en not_active Expired - Lifetime
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102269491A (en) * | 2010-06-07 | 2011-12-07 | 四川空分设备(集团)有限责任公司 | Noncondensable gas separation and refrigerant recycling device and method for refrigerating system |
| CN102641716A (en) * | 2012-04-24 | 2012-08-22 | 江苏长荣化工设备有限公司 | Combined heat-transferring dispersing reaction device |
| CN102674428A (en) * | 2012-05-17 | 2012-09-19 | 贵州红星发展股份有限公司 | High-whiteness spherical nano barium sulfate and preparation method thereof |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| C17 | Cessation of patent right | ||
| CX01 | Expiry of patent term |
Expiration termination date: 20121209 Granted publication date: 20031022 |