CN210885304U - High-efficient hydrogen peroxide solution production oxidation reactor - Google Patents
High-efficient hydrogen peroxide solution production oxidation reactor Download PDFInfo
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- CN210885304U CN210885304U CN201921906013.XU CN201921906013U CN210885304U CN 210885304 U CN210885304 U CN 210885304U CN 201921906013 U CN201921906013 U CN 201921906013U CN 210885304 U CN210885304 U CN 210885304U
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Abstract
An oxidation reactor for producing high-efficiency hydrogen peroxide relates to a hydrogen peroxide production process, and comprises a tower body, wherein an air inlet, a tail gas outlet, a working liquid inlet, a working liquid outlet and a residual liquid outlet are arranged on the tower body; the tower body is internally connected with an air distributor, a plurality of groups of baffle assemblies, a filler and a wire mesh demister from bottom to top in sequence; the air distributor is communicated with the air inlet; each group of deflection assemblies has the same structure and comprises a sieve plate and a baffle plate which are fixedly connected with the inner side of the tower body, a first channel is arranged between the sieve plate and the tower body, the baffle plate is arranged below the first channel and extends to the lower part of the sieve plate, a second channel is arranged between the baffle plate and the tower body, the first channel and the second channel are communicated to form a lower liquid channel, and the lower liquid channels of the deflection assemblies are arranged in a left-right alternating manner; the filler is arranged below the working solution inlet, and the wire mesh demister is arranged above the working solution inlet. The utility model discloses with low costs, efficient.
Description
Technical Field
The utility model relates to a hydrogen peroxide production process, in particular to a structure of an oxidation tower.
Background
In the production process of hydrogen peroxide, hydrogenated liquid generated after the hydrogenation of working liquid is subjected to oxidation reaction with air sent from the outside in the reactor, and the hydrogenated liquid is generally referred to as an oxidation tower for short. The hydrogenated liquid oxidation equipment is a key equipment in hydrogen peroxide production, and the structure of the equipment determines the oxidation speed, the oxidation efficiency, the oxidation yield and the generation amount of degradation products and has a great relationship.
The internal structure of the oxidation tower in the prior traditional process is as follows: the oxidation tower in the traditional process consists of two sections or three sections (described according to the two sections), fresh air is introduced from the bottoms of the upper section and the lower section, the fresh air is dispersed upwards through a gas distributor, and the amount of the air introduced into the tower is controlled according to the oxidation efficiency and the residual oxygen content in tail gas. The hydrogenated liquid from the hydrogenation process is pressurized by a hydrogenated liquid pump and firstly enters the bottom of an upper section of an oxidation tower, the hydrogenated liquid entering the bottom of the upper section of the oxidation tower is upwards dispersed under the action of a liquid distributor and is dispersed into small bubbles together with fresh air sent from the outside under the action of a gas distributor to flow upwards for oxidation reaction, the large bubbles are gradually produced by the small bubbles in the process of the upwards reaction, the oxidation reaction is not facilitated, and the oxidation tower is provided with a plurality of layers of sieve plates to redistribute the air and the working liquid. Working liquid and air flow upwards in parallel to reach the top of an upper tower of an oxidation tower for gas-liquid separation, gas flows to a tail gas system through a wire mesh demister, the separated working liquid flows to a working liquid inlet at the bottom of a lower tower through an external communicating pipe by gravity, flows upwards in parallel with fresh air sent from the outside and continues to be oxidized, a gas-liquid mixture from the upper part of the lower tower enters an oxidation liquid-gas separator, the oxidized working liquid (called as oxidation liquid) in the oxidation liquid separator is cooled by an oxidation liquid cooler after a certain liquid level in the separator is controlled by a self-control instrument, and then enters an oxidation liquid storage tank, and then is sent to the bottom of an extraction tower by an oxidation liquid pump. The gas separated from the top of the lower tower and the gas separated from the upper tower are converged by the oxidized tail gas expansion unit and the tail gas adsorbent unit to recover the solvent carried in the tail gas, and then the solvent is discharged at high altitude.
The oxidation tower in the traditional process has the defects of two or three sections of towers:
① when the traditional oxidation tower is divided into two or three parallel flow towers, the equipment volume is large, for example, taking 10 ten thousand tons of 27.5% hydrogen peroxide produced per year as an example, the diameter of the oxidation tower is about phi 4.2m, the total height is about 43m, and the volume is 440m3(ii) a The working fluid occupies a large amount.
② besides, an oxidation gas-liquid separator must be arranged in addition to the main body of the oxidation tower (two oxidation gas-liquid separators are arranged in three stages), and additional equipment investment is needed.
③ the oxidation tower of the structure is not good for the oxidation reaction of air and hydrogenated liquid, the initial fresh air and the fresh hydrogenated liquid are easy to contact and react, once the exhaust gas flows upwards in parallel and reacts with part of the hydrogenated liquid which is difficult to react more difficultly (the reaction speed of the hydroanthraquinone is high, the reaction speed of the tetrahydrohydroanthraquinone is slow), the oxidation yield is low, and the oxidation yield of the oxidation tower of the structure is generally about 90-93%.
④ the oxidation tower with the structure has large air consumption, and 1400Nm air quantity needs to be consumed by one ton of hydrogen peroxide (27.5 percent)3About 90-93% of oxidation yield can be achieved only when the oxygen content of the oxidation tail gas is controlled to be 6-9%.
⑤ the oxidation tower with the structure can ensure normal oxidation yield only when the oxygen content of the oxidation tail gas is controlled to be 6-9%, and the tail gas with higher oxygen content has the risk of tail gas aromatic hydrocarbon flash explosion in normal production.
⑥ the oxidation tower has longer oxidation reaction time and higher reaction temperature, and the reaction is easier to generate epoxy degradation products.
⑦ the oxidation tower has long oxidation reaction time, high temperature of cocurrent flow, serious decomposition of hydrogen peroxide solution, and large amount of residual liquid.
In addition, in the prior art patent, patent No. ZL201820373458.5, which is named as a gas-liquid countercurrent oxidation tower, the sieve plate structure of the tower is a bubble cap tower structure, and the implementation difficulty is large because it is difficult to overcome the resistance between the upward movement of gas from the inside of the bubble cap and the downward movement of the hydrogenated liquid through the sieve plate holes.
Disclosure of Invention
The utility model aims to overcome the defects of the prior art and provide a high-efficiency hydrogen peroxide production oxidation reactor with low cost and high efficiency.
The purpose of the utility model is realized like this: an oxidation reactor for producing high-efficiency hydrogen peroxide comprises a tower body, wherein an air inlet, a tail gas outlet, a working liquid inlet, a working liquid outlet and a residual liquid outlet are arranged on the tower body, the air inlet and the working liquid outlet are positioned at the lower part of the tower body, the residual liquid outlet is positioned at the bottom of the tower body, the working liquid inlet is positioned at the upper part of the tower body, and the tail gas outlet is positioned at the top of the tower body; the tower body is internally connected with an air distributor, a plurality of groups of baffle assemblies, a filler and a wire mesh demister from bottom to top in sequence; the air distributor is communicated with the air inlet; each group of deflection assemblies has the same structure and comprises a sieve plate and a baffle plate which are fixedly connected with the inner side of the tower body, a first channel is arranged between the sieve plate and the tower body, the baffle plate is arranged below the first channel and extends to the lower part of the sieve plate, a second channel is arranged between the baffle plate and the tower body, the first channel and the second channel are communicated to form a lower liquid channel, and the lower liquid channels of the deflection assemblies are arranged in a left-right alternating manner; the filler is arranged below the working solution inlet, and the wire mesh demister is arranged above the working solution inlet.
The utility model has the advantages that:
① the oxidation tower structure of gas-liquid countercurrent (gas entering from the lower part and working liquid entering from the upper part) has larger driving force than gas-liquid cocurrent flow mass transfer, faster oxidation speed, shorter required retention time and higher production efficiency of equipment with the same volume.
② Equipment management systemThe volume is less, the original loading of the working solution is less, and the initial investment is less. For example, taking 10 ten thousand tons of 27.5% hydrogen peroxide produced every year as an example, the diameter of the oxidation tower is about phi 3.4m, and the total height is about 32 m. The volume is 290m3(ii) a The occupied amount of the working fluid is about 60 square compared with the traditional oxidation tower.
③ the oxidation tower with the countercurrent structure has the advantages of short oxidation reaction time, uniform external cooling, less hydrogen peroxide decomposition amount, and higher oxidation yield, and the oxidation yield of the oxidation tower with the countercurrent reaction is generally 95-98%.
④ in the oxidation tower with the countercurrent structure, the hydrogenated liquid turns back from the upper part to the lower part to pass through the liquid descending channels of the sieve plates at each layer in a advection way, the required resistance is small, the pressure difference between the upper part and the lower part of the oxidation tower is small on the whole, which is beneficial to the addition of air and the descending of the hydrogenated liquid, and the feasibility of the normal operation of the equipment can be realized.
⑤ when the amount of air consumed by each ton of hydrogen peroxide (27.5%) in the oxidation tower with the countercurrent structure is small, 1300Nm of the amount of air consumed by each ton of hydrogen peroxide (27.5%) is required3About, when the oxygen content of the oxidation tail gas is 3%, the oxidation yield can also reach 95%, and the air quantity needing to be conveyed from the outside is less.
⑥ when the oxygen content of the oxidation tail gas of the oxidation tower with the structure is low (the oxygen content is 3-5%), the oxidation yield is not changed greatly, and the tail gas of the oxidation tower with the structure is safer compared with the tail gas of the traditional process when the oxygen content is low.
The utility model discloses an air distributor includes that the air is responsible for and many air branch pipe, and many air branch pipe fixed connection are respectively in the both sides that the air was responsible for, and many air branch pipe all are linked together with the air is responsible for, all set up the gas pocket on air is responsible for and many air branch pipe.
The sieve plate of the utility model is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the sieve plate is fixedly connected with the tower body, and the first channel is formed between the plane of the sieve plate and the tower body; the baffle is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the baffle is fixedly connected with the tower body, and the second channel is formed between the plane of the baffle and the tower body. The flow direction of the working liquid is that the working liquid inlet → the sieve plate of the first layer → the first channel → the baffle plate of the first layer → the second channel → the sieve plate of the second layer turns back from top to bottom in a advective way.
The utility model discloses the integrative downward hem that sets up in plane of sieve sets up the hem that makes progress in the integrative setting in plane of baffle. The downward folding edge of the sieve plate can prevent air below the sieve plate from directly blocking the downward movement of the working liquid through the liquid discharge channel; the upward folding edge of the baffle plate aims to baffle air bubbles floating from the lower part of the air partition plate to the lower part of the sieve plate so as to prevent the air bubbles from flowing down the liquid channel.
The utility model discloses a sieve includes the polylith splice plate, and the polylith splice plate passes through bolted connection, sets up a plurality of through-hole, easy to assemble and production on every splice plate.
In order to further ensure the oxidation effect, five to ten sets of baffle assemblies are provided.
The utility model discloses the outer coil pipe cooler of outside fixed connection of tower body, the outer coil pipe cooler of tower do not occupy the equipment inner space, do not have the influence to inside air upwards dispersion and hydrogenation liquid flow distribution, and heat exchange efficiency is higher, does not need a large amount of circulating water.
Drawings
Fig. 1 is a schematic structural diagram of the present invention.
Fig. 2 is a view from a-a in fig. 1.
Fig. 3 is a top view of the baffle.
Fig. 4 is a view from B-B in fig. 1.
Detailed Description
As shown in fig. 1-4, the high-efficiency hydrogen peroxide production oxidation reactor comprises a tower body 11, and an outer coil cooler 4 is fixedly connected to the outer side of the tower body 11. Set up air intlet 8, tail gas export 1, working solution import 3, working solution export 6 and raffinate export 7 on tower body 11, air intlet 8 and working solution export 6 are located the lower part of tower body 11, and raffinate export 7 is located the bottom of tower body, and working solution import 3 is located the upper portion of tower body 11, and tail gas export 1 is located the top of tower body 11.
The tower body 11 is internally connected with an air distributor 5, five groups of baffle assemblies 9, a filler 10 and a wire mesh demister 2 from bottom to top in sequence. The filler 10 is arranged below the working liquid inlet 3, and the wire mesh demister 2 is arranged above the working liquid inlet 3. The air distributor 5 comprises an air main pipe 5-1 and a plurality of air branch pipes 5-2, the air main pipe 5-1 is communicated with an air inlet 8, the plurality of air branch pipes 5-2 are respectively and fixedly connected to two sides of the air main pipe 5-1, the plurality of air branch pipes 5-2 are communicated with the air main pipe 5-1, and the air main pipe 5-1 and the plurality of air branch pipes 5-2 are respectively provided with a plurality of small holes.
The baffling assemblies 9 can be five to ten groups, each group of baffling assemblies 9 is identical in structure and comprises a sieve plate 9-1 and a baffle plate 9-2, the sieve plate 9-1 is fixedly connected with the inner side of the tower body 11, the sieve plate 9-1 is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the sieve plate 9-1 is fixedly connected with the tower body 11, a first channel 12 is formed between the plane of the sieve plate 9-1 and the tower body 11, and the plane of the sieve plate 9-1 is bent downwards to form a lower folded edge 14. The sieve plate 9-1 comprises four splicing plates 9-1-1, the four splicing plates 9-1-1 are connected through bolts, and a plurality of through holes 9-1-2 are formed in each splicing plate 9-1-1. The baffle 9-2 is arranged below the first channel 12 and extends to the lower part of the sieve plate 9-1, the baffle 9-2 is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the baffle 9-2 is fixedly connected with the tower body 11, a second channel 13 is formed between the plane of the baffle 9-2 and the tower body, and the plane of the baffle 9-2 is bent upwards to form an upper folding edge 15. The first channel 12 is communicated with the second channel 13 to form a lower liquid channel, and the lower liquid channels of the five groups of baffle assemblies 9 are arranged in a left-right alternating manner.
The utility model has the characteristics of it is following:
① external structure, the diameter of the single tower is determined according to the capacity of the device, the diameter of the oxidation tower is about 3.4 meters for producing 10 ten thousand tons of 27.5% hydrogen peroxide per year, the cooling mode of the oxidation tower adopts external coil type cooling, the external coil type is better for the small device, namely a half welded pipe is added outside the oxidation tower body and cooled by circulating water.
② the internal structure is that the space above the oxidation tower is a gas-liquid separation section, the top of the gas-liquid separation section is a wire mesh demister, the wire mesh demister is arranged to intercept oxidation tail gas and entrain part of working liquid mist in the upward process, the space below the oxidation tower is provided with multiple layers of sieve plates, generally 5-10 layers are normally arranged, 7-8 layers are normally arranged to be optimal, the sieve plates are arranged to reduce the contact reaction area of air and working liquid in the contact reaction process of air bubbles dispersed upwards from an air distributor at the bottom of the oxidation tower and hydrogen liquid returning back downwards in a reverse flow mode, the small air bubbles collide with each other to gradually generate large air bubbles, the normal oxidation reaction is not facilitated, the sieve plates are arranged to re-disperse the large air bubbles flowing upwards into small air bubbles through the sieve plates, the gas-liquid separation filler is generally arranged on the first sieve plate at the top, the stainless steel deflection demister, the coil cooler is arranged outside the oxidation reaction to achieve exothermic reaction, the heat of the reaction is timely conducted through the sieve plates, the baffle plate which prevents water from the normal reaction when the temperature is too high, the normal reaction, the air bubbles pass through the baffle plate, the lower air deflector plate, the air bubble deflector plate is arranged to be directly connected with the lower air baffle plate, the air baffle plate is arranged below the air baffle plate, the air baffle plate is arranged to be directly connected with the air baffle plate, the air baffle plate is arranged below the air baffle plate, the air baffle.
③ the detailed oxidation process comprises feeding working liquid into the upper part of the oxidation tower to contact with fresh air from the bottom of the tower, arranging a wire mesh demister at the top of the oxidation tower, arranging a space at the upper part of the oxidation tower to ensure that gas and liquid are separated in the separation section at the upper part of the oxidation tower, allowing the liquid to flow downwards by means of potential difference, returning downwards by means of multiple layers of sieve plates to fully disperse the air from the bottom of the oxidation tower by means of multiple layers of sieve plates, and then performing countercurrent contact reaction, gradually feeding the reacted working liquid (called oxidation liquid) into the oxidation bottom, controlling the liquid level of the gas and liquid separation section at the upper part of the oxidation tower by a liquid level control valve outside the oxidation tower, feeding the oxidation liquid into an oxidation liquid head tank (the oxidation liquid head tank is arranged at the fifth floor of the frame) by means of the bottom pressure of the oxidation tower.
Claims (7)
1. An oxidation reactor for producing high-efficiency hydrogen peroxide comprises a tower body, and is characterized in that: the tower body is provided with an air inlet, a tail gas outlet, a working liquid inlet, a working liquid outlet and a residual liquid outlet, the air inlet and the working liquid outlet are positioned at the lower part of the tower body, the residual liquid outlet is positioned at the bottom of the tower body, the working liquid inlet is positioned at the upper part of the tower body, and the tail gas outlet is positioned at the top of the tower body; the tower body is internally connected with an air distributor, a plurality of groups of baffle assemblies, a filler and a wire mesh demister from bottom to top in sequence; the air distributor is communicated with the air inlet; each group of deflection assemblies has the same structure and comprises a sieve plate and a baffle plate which are fixedly connected with the inner side of the tower body, a first channel is arranged between the sieve plate and the tower body, the baffle plate is arranged below the first channel and extends to the lower part of the sieve plate, a second channel is arranged between the baffle plate and the tower body, the first channel and the second channel are communicated to form a lower liquid channel, and the lower liquid channels of the deflection assemblies are arranged in a left-right alternating manner; the filler is arranged below the working solution inlet, and the wire mesh demister is arranged above the working solution inlet.
2. The high-efficiency oxidation reactor for hydrogen peroxide production according to claim 1, which is characterized in that: the air distributor comprises an air main pipe and a plurality of air branch pipes, wherein the air branch pipes are fixedly connected to two sides of the air main pipe respectively, the air branch pipes are communicated with the air main pipe, and air holes are formed in the air main pipe and the air branch pipes.
3. The high-efficiency oxidation reactor for hydrogen peroxide production according to claim 1, which is characterized in that: the sieve plate is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the sieve plate is fixedly connected with the tower body, and the first channel is formed between the plane of the sieve plate and the tower body; the baffle is D-shaped and comprises an arc-shaped surface and a plane, the arc-shaped surface of the baffle is fixedly connected with the tower body, and the second channel is formed between the plane of the baffle and the tower body.
4. The high-efficiency hydrogen peroxide production oxidation reactor as set forth in claim 3, which is characterized in that: the plane of the sieve plate is integrally provided with a downward folded edge, and the plane of the baffle plate is integrally provided with an upward folded edge.
5. The high-efficiency hydrogen peroxide production oxidation reactor as set forth in claim 3, which is characterized in that: the sieve plate comprises a plurality of splicing plates which are connected through bolts, and a plurality of through holes are formed in each splicing plate.
6. The high-efficiency oxidation reactor for hydrogen peroxide production according to claim 1, which is characterized in that: the multiple sets of baffle assemblies have five to ten sets.
7. The high-efficiency oxidation reactor for hydrogen peroxide production according to claim 1, which is characterized in that: and the outer side of the tower body is fixedly connected with an outer coil cooler.
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| CN201921906013.XU CN210885304U (en) | 2019-11-07 | 2019-11-07 | High-efficient hydrogen peroxide solution production oxidation reactor |
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| CN201921906013.XU CN210885304U (en) | 2019-11-07 | 2019-11-07 | High-efficient hydrogen peroxide solution production oxidation reactor |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116077969A (en) * | 2023-02-09 | 2023-05-09 | 邢台市茂新化工产品有限公司 | Multipolar chemical industry distillation column |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN116077969A (en) * | 2023-02-09 | 2023-05-09 | 邢台市茂新化工产品有限公司 | Multipolar chemical industry distillation column |
| CN116077969B (en) * | 2023-02-09 | 2023-11-17 | 吉林市新跃新材料有限公司 | Multipolar chemical industry distillation column |
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Address after: Room 101, Building 11, Jinrong Science and Technology Park, No. 158 Ji'an South Road, High tech Development Zone, Yangzhou City, Jiangsu Province, 225128 Patentee after: Jiangsu Zhongxu Technology Co.,Ltd. Address before: No. 4, Huagang Road, Hanjiang Industrial Park, Yangzhou, Jiangsu 225128 Patentee before: Yangzhou Rongxiang Technology Development Co.,Ltd. |