CN201309829Y - Oxidation device for producing hydrogen peroxide by anthraquinone process - Google Patents
Oxidation device for producing hydrogen peroxide by anthraquinone process Download PDFInfo
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- CN201309829Y CN201309829Y CNU2008201485141U CN200820148514U CN201309829Y CN 201309829 Y CN201309829 Y CN 201309829Y CN U2008201485141 U CNU2008201485141 U CN U2008201485141U CN 200820148514 U CN200820148514 U CN 200820148514U CN 201309829 Y CN201309829 Y CN 201309829Y
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Abstract
The utility model discloses an oxidation device for producing hydrogen peroxide by the anthraquinone process, which has high efficiency, low consumption and simple structure and aims to overcome technical defects existing on oxidation devices for producing hydrogen peroxide at present. The oxidation device comprises a filter, a hydrogenated liquid cooler, an oxidized liquid pump, an oxidation upper-section column, an oxidation middle-section column, an oxidation lower-section column, an oxidation off-gas cooler, an oxidized liquid gas-liquid separator, an off-gas exchanger and an intermediate storage tank for aromatic hydrocarbon, wherein all the components are connected via pipes. The oxidation device is characterized in that the oxidation upper-section column, the oxidation middle-section column and the oxidation lower-section column form multiple oxidations in the technical scheme, and all the columns are connected by pipes, and a plurality of perforated-plate re-distributors are mounted in the three columns. The utility model has the advantages that by utilizing the re-distributors to distribute air time and time again, current bias and back mixing of two materials in the columns are reduced, thereby increasing oxidation yield (>=96%) and improving efficiency of the columns.
Description
Technical field:
The utility model belongs to the hydrogen peroxide production technical field, relates in particular to a kind of oxidation unit of hydrogen dioxide solution production by anthraquinone process.
Technical background:
What the oxidation unit of the hydrogen peroxide of China's production at present generally adopted is two tower void tower oxidation technologies, and the technological deficiency that its exists is:
(1) be the void tower oxidation owing to what adopt, the air draught skewness, it is insufficient to cause air to contact with hydride.
(2) hydride easily causes bias current and back-mixing in oxidizing tower, has reduced the efficient of tower.
(3) owing to adopt the double tower oxidation to cause oxidation incomplete, air utilization ratio is low.
(4) the hydride oxidation is incomplete, has increased the burden of back operation, causes back operation operation not steady.
Summary of the invention:
For overcoming the technological deficiency that exists on the present production hydrogen peroxide oxidation device, the utility model discloses a kind of efficient low-consume, hydrogen dioxide solution production by anthraquinone process oxidation unit simple in structure.
The technical scheme that the utility model is dealt with problems is:
A kind of hydrogen dioxide solution production by anthraquinone process oxidation unit, by strainer, the hydride water cooler, the oxidation liquid pump saves tower in the oxidation, save tower in the oxidation, joint tower under the oxidation, the oxidized tail gas water cooler, oxidation liquid gas-liquid separator, exhaust gas heat exchanger, formations such as aromatic hydrocarbons process tank, be connected by pipeline between them, it is characterized in that: this programme saves tower by saving tower in the oxidation in the oxidation, and joint tower three towers formation is carried out repeatedly oxidation under the oxidation, be connected by pipeline between tower and the tower, save tower in the oxidation, save tower in the oxidation, a plurality of porous plate redistributors are installed in joint tower three towers under the oxidation.
The porous plate redistributor is drilled with a plurality of apertures by a stainless steel plate, and the aperture is between 5-10mm, and pitch of holes is between 15-30mm, and hole shape can be circle, also can be other shapes, and the size of porous plate is determined by the diameter of tower, generally between 2-5m.
In the joint tower 2 porous plate redistributors are housed in the oxidation, the joint tower is equipped with 4 porous plate redistributors in the oxidation, the joint tower is equipped with 3 porous plate redistributors under the oxidation, wherein 2 the porous plate redistributors of joint in the tower are contained in the front and back of first cooling water tank respectively in the oxidation, 4 porous plate redistributors in the oxidation in the joint tower are contained in the front and back of each cooling water tank respectively, and 3 porous plate redistributors under the oxidation in the joint tower are contained in the front and back of two water towers respectively.
The advantage of technical solutions of the utility model is:
(1) oxidizing tower utilizes redistribution technology to improve biphase rate of mass transfer in air and the hydride reaction process in this device, avoids bubble coalescence to become than air pocket, has increased the two-phase medium contact area.
(2) utilize redistributor that air is repeatedly distributed again, reduce the bias current and the back-mixing of two materials in the tower, improved oxidization-hydrogenation ratio (〉=96%), improve column efficiency.
(3) adopt three tower oxidations be exactly with in, the waste gas of tower utilizes once more down, to reduce air consumption, save power, reduce exhaust emissions amount (oxygen level in the oxidized tail gas is 4～5%) and supplies consumption, thereby reduced the discharging and the product cost of atmospheric polluting material.
(4) reduce hydrofenating anthraquinone content in the oxidation liquid, alleviated the load of extraction and postprocessing working procedures, increased hydrogen peroxide output.
Description of drawings:
Accompanying drawing 1 is a structural representation of the present utility model
Accompanying drawing 2 is structural representations of porous plate redistributor of the present utility model
In accompanying drawing 1, the 1st, air filter, the 2nd, hydride water cooler, the 3rd, the hydrogenation liquid pump, the 4th, save tower in the oxidation, the 5th, save tower in the oxidation, the 6th, joint tower under the oxidation, the 7th, oxidized tail gas water cooler, the 8th, oxidation liquid gas-liquid separator A, the 9th, oxidation liquid gas-liquid separator B, the 10th, oxidized tail gas heat exchanger, the 11st, aromatic hydrocarbons process tank, the 12nd, oxidation liquid storage tank, the 13rd, oxidation liquid pump, the 14th, ammonia cooler, the 15th, porous plate redistributor, the 16th, the distribution hole of porous plate redistributor.
(4a), (4b) be 2 the porous plate redistributors of joint in the tower in the oxidation, (5a), (5b), (5c), (5d) be 4 porous plate redistributors in the joint tower in the oxidation, (6a), (6b), (6c) be joint tower porous plate redistributor under the oxidation,
Embodiment:
Below in conjunction with accompanying drawing the utility model is further described:
A kind of hydrogen dioxide solution production by anthraquinone process oxidation unit, by strainer (1), hydride water cooler (2), oxidation liquid pump (3), save tower (4) in the oxidation, save tower (5) in the oxidation, joint tower (6) under the oxidation, oxidized tail gas water cooler (7), oxidation liquid gas-liquid separator (8) exhaust gas heat exchanger (9), aromatic hydrocarbons process tank formations such as (11), be connected by pipeline between them, save tower (4) in the oxidation, save tower (5) in the oxidation, joint tower (6) three towers constitute and to carry out repeatedly oxidation under the oxidation, are connected by pipeline between tower and the tower.
Porous plate redistributor (15) is drilled with a plurality of apertures (16) by a stainless steel plate, and the aperture is between 5-10mm, and pitch of holes is between 15-30mm, hole shape can be circle, also can be other shapes, porous plate divides the size of device (15) to be determined by the diameter of tower again, generally between 2-6m.
Save in the oxidation 2 porous plate redistributors (4a), (4b) are housed in the tower (4), save tower (5) in the oxidation 4 porous plate redistributors (5a), (5b), (5c), (5d) are housed, joint tower (6) is equipped with 3 porous plate redistributors (6a), (6b), (6c) under the oxidation, 2 porous plate redistributors in the oxidation in the joint tower are contained in the front and back of first cooling water tank respectively, 4 porous plate redistributors in the oxidation in the joint tower are contained in the front and back of each cooling water tank respectively, and 3 porous plate redistributors under the oxidation in the joint tower are contained in the front and back of two water towers respectively.
The utility model principle of work is: joint tower (5) and following joint tower (6) in entering after pressurized air filters through filter (1), carry out oxidizing reaction with hydride from last joint tower (4) and middle joint tower (5) respectively; Reacted tail gas after separator A (8) and separator B (9) carry out gas-liquid separation one enter joint tower (4), the hydride of carrying with hydrogenation liquid pump (3) after water cooler (2) is adjusted temperature carries out oxidizing reaction, in this reaction process, air distributes repeatedly once more through the perforated-plate distributor of upper, middle and lower Jie Tanei, has improved oxidation efficiency.Discharge after after last joint tower (4) reacted tail gas is successively passed through oxidized tail gas water cooler (7), oxidized tail gas heat exchanger (10), ammonia cooler (14) condensation, reclaiming the organic solvent of wherein carrying secretly, the organic solvent that condensation is reclaimed is stored in the aromatic hydrocarbons process tank (11), regularly be discharged in the oxidation liquid storage tank (12), the oxidation liquid that reaction generates is delivered to next operation with oxidation liquid pump (13).
Claims (3)
1, a kind of hydrogen dioxide solution production by anthraquinone process oxidation unit, by strainer (1), hydride water cooler (2), oxidation liquid pump (3), save tower (4) in the oxidation, save tower (5) in the oxidation, joint tower (6) under the oxidation, oxidized tail gas water cooler (7), oxidation liquid gas-liquid separator (8) exhaust gas heat exchanger (9), aromatic hydrocarbons process tank (9), porous plate redistributor formations such as (15), be connected by pipeline between them, it is characterized in that: save tower (4) in the oxidation, save tower (5) in the oxidation, joint tower (6) three towers constitute repeatedly oxidation under the oxidation, be connected by pipeline between tower and the tower, save tower in the oxidation, save tower in the oxidation, be provided with a plurality of porous plate redistributors (15) under the oxidation in joint tower three towers.
2, according to claim 1, a kind of hydrogen dioxide solution production by anthraquinone process oxidation unit, it is characterized in that: porous plate redistributor (15) is drilled with a plurality of apertures (16) by a stainless steel plate, the aperture is between 5-10mm, pitch of holes is between 15-30mm, and hole shape can be circle, also can be other shapes, the size of porous plate is determined by the diameter of tower, generally between 2-6m.
3, according to claim 1, a kind of hydrogen dioxide solution production by anthraquinone process oxidation unit, it is characterized in that: save in the oxidation 2 porous plate redistributors (4a) are housed in the tower (4), (4b), save tower (5) in the oxidation 4 porous plate redistributors (5a) are housed, (5b), (5c), (5d), joint tower (6) is equipped with 3 porous plate redistributors (6a) under the oxidation, (6b), (6c), 2 porous plate redistributors in the oxidation in the joint tower are contained in the front and back of first cooling water tank respectively, 4 porous plate redistributors in the oxidation in the joint tower are contained in the front and back of each cooling water tank respectively, and 3 porous plate redistributors under the oxidation in the joint tower are contained in the front and back of two water towers respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201485141U CN201309829Y (en) | 2008-08-14 | 2008-08-14 | Oxidation device for producing hydrogen peroxide by anthraquinone process |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2008201485141U CN201309829Y (en) | 2008-08-14 | 2008-08-14 | Oxidation device for producing hydrogen peroxide by anthraquinone process |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201309829Y true CN201309829Y (en) | 2009-09-16 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNU2008201485141U Expired - Fee Related CN201309829Y (en) | 2008-08-14 | 2008-08-14 | Oxidation device for producing hydrogen peroxide by anthraquinone process |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101837956A (en) * | 2010-04-29 | 2010-09-22 | 扬州惠通化工技术有限公司 | Oxidation system for producing hydrogen peroxide |
| CN102583257A (en) * | 2012-01-12 | 2012-07-18 | 天津大学 | Extraction equipment and method for preparing oxyful via anthraquinone process |
| 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 |
| CN102757020A (en) * | 2012-07-10 | 2012-10-31 | 潜江益和化学品有限公司 | Working solution pre-heating device |
| CN103663385A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Method and device of producing hydrogen peroxide |
| CN105399056A (en) * | 2015-12-25 | 2016-03-16 | 江阴中南重工有限公司 | Oxidation tower with heating device |
-
2008
- 2008-08-14 CN CNU2008201485141U patent/CN201309829Y/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101837956A (en) * | 2010-04-29 | 2010-09-22 | 扬州惠通化工技术有限公司 | Oxidation system for producing hydrogen peroxide |
| CN101837956B (en) * | 2010-04-29 | 2011-09-28 | 扬州惠通化工技术有限公司 | Oxidation system for producing hydrogen peroxide |
| WO2011134344A1 (en) * | 2010-04-29 | 2011-11-03 | 扬州惠通化工技术有限公司 | Oxidation system of hydrogen peroxide production |
| CN102583257A (en) * | 2012-01-12 | 2012-07-18 | 天津大学 | Extraction equipment and method for preparing oxyful via anthraquinone process |
| CN102583257B (en) * | 2012-01-12 | 2014-02-12 | 天津大学 | Extraction equipment and method for preparing oxyful via anthraquinone process |
| 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 |
| CN102757020A (en) * | 2012-07-10 | 2012-10-31 | 潜江益和化学品有限公司 | Working solution pre-heating device |
| CN103663385A (en) * | 2012-09-21 | 2014-03-26 | 中国石油化工股份有限公司 | Method and device of producing hydrogen peroxide |
| CN105399056A (en) * | 2015-12-25 | 2016-03-16 | 江阴中南重工有限公司 | Oxidation tower with heating device |
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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 | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20090916 Termination date: 20110814 |