CN103588176A - Production method of hydrogen peroxide - Google Patents
Production method of hydrogen peroxide Download PDFInfo
- Publication number
- CN103588176A CN103588176A CN201310535309.6A CN201310535309A CN103588176A CN 103588176 A CN103588176 A CN 103588176A CN 201310535309 A CN201310535309 A CN 201310535309A CN 103588176 A CN103588176 A CN 103588176A
- Authority
- CN
- China
- Prior art keywords
- hydrogenation
- fluidisation
- hydrogen peroxide
- reaction
- working solution
- 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.)
- Pending
Links
Images
Abstract
Relating to the technical field of large-scale high concentration hydrogen peroxide production technologies, particularly to hydrogen peroxide production technologies by an anthraquinone process, the invention provides a production method of hydrogen peroxide. The method includes: taking heavy aromatics, tetrabutylurea and trioctyl phosphate as solvents, adopting 2-ethylanthraquinone as a reaction material, adding a well prepared working solution into a circulating working solution storage tank, making use of a circulating working solution pump to send the working solution into a working solution thermoregulator, using circulating cooling water to lower the temperature of the working solution to about 35DEG C, then bringing the working solution to the bottom of a fluidization hydrogenation reactor, adding a hydrogenation catalyst into the fluidization hydrogenation reactor in advance through a catalyst adding groove, at the same time, passing compressed hydrogen through a hydrogen buffer filter to filter out impurities, then letting the compressed hydrogen enter the bottom of the fluidization hydrogenation reactor, using the compressed hydrogen to blow and stir the catalyst and the working solution so as to undergo hydrogenation reaction at a temperature of about 50DEG C, under a pressure of about 0.26mPa, and at hydrogenation efficiency of about 13g/L.
Description
Technical field
The present invention relates to the hydrogen peroxide technical field of producing of extensive high density, particularly anthraquinone hydrogen peroxide production technology.
Background technology
Existing domestic anthraquinone hydrogen peroxide hydrogenator is fixed bed form, catalyzer is fixed, liquid drip in catalyst layer flows downward, hydrogen and liquid flow downward simultaneously and carry out hydrogenation reaction, have the defects such as bias current, channel, catalyst agglomeration, hydrogenation are inhomogeneous, reaction resistance is large, side reaction is many, raw materials consumption is high, catalyst levels is large, product cost is high; Oxidation reactor is working liquid and pressurized air and flows to upper flowing, and has that oxidizing tower efficiency is low, oxidization-hydrogenation ratio is low, air consumption is high, a defect such as oxygen level height in tail gas; Extraction column plate is single plate structure, has that working liquid polymerization is bad, product concentration is low, a defect such as residual dioxygen water yield height in working liquid; Utilize high alkali liquid to remove hydrogen peroxide residual in working liquid and moisture content, the defect such as alkali consumes, and production waste high, that produce is difficult to process, and system production security is poor.
Summary of the invention
In order to overcome the deficiencies in the prior art; the invention provides a kind of novel hydrogen peroxide production method; to reach, be beneficial to saving investment, the reduction raw materials consumption of large-scale production; can production high density hydrogen peroxide product; device is produced more safe and reliable, makes the further object improving of production capacity of production equipment.
The present invention includes stream fluidisation hydrogenation, oxidizing reaction, extraction and purification step.
When fluidisation hydrogenation, under palladium catalyst existence condition, the pungent fat of heavy aromatics, tetrabutyl urea and tricresyl phosphate of take is solvent, by 2-ethyl-anthraquinone and excessive hydrogen temperature in fluidisation hydrogenator, is to react under 50 ± 2 ℃ of conditions, obtains reaction solution.
In fluidisation hydrogenator, pass into palladium catalyst and by heavy aromatics, tetrabutyl urea, the pungent fat of tricresyl phosphate, 2-ethyl-anthraquinone and 2-ethyl-anthraquinone, be mixed to form, temperature is the cycle working fluid of 35 ± 2 ℃, then the bottom by fluidisation hydrogenator upwards passes into compression hydrogen, catalyzer and working fluid is blown afloat to stir and carry out fluidisation hydrogenation reaction.
The reacting liquid filtering that fluidisation hydrogenation is obtained, purifies after removal palladium catalyst.
When purifying: the reaction solution that fluidisation hydrogenation is obtained filters with activated alumina, obtains filtered solution.
During oxidizing reaction, in being provided with the oxidizing tower of water cooler, the filtered solution that purification is obtained does not react higher than the condition of 52 ℃ in temperature of reaction with oxygen, obtains oxidation solution.
Pressurized air is entered after air filter impurity screening to oxidizing tower bottom and upwards flow, the airborne oxygen filtered solution downward with autoxidation tower top reacts, and at the bottom of autoxidation tower, obtains oxidation solution.
While being to extract, extraction agent is the phosphate aqueous solution that 45 ± 2 ℃ of temperature, pH value are 3～3.6, extraction agent is downward by extracting tower top, carry out counter-current extraction with the oxidation solution making progress at the bottom of extraction tower, while reaching 42 ± 2% to the thick hydrogen peroxide solution concentration of extraction tower bottom, by potential difference, obtain hydrogen peroxide extraction liquid;
During purification, with heavy aromatic solvent, purify.
The principle of the invention: will be with heavy aromatics, the pungent fat of tetrabutyl urea and tricresyl phosphate is solvent, take 2-ethyl-anthraquinone as reactive material, the working fluid preparing is added in cycle working fluid storage tank, utilize cycle operation liquid pump that working fluid is sent into working fluid thermosistor, utilize recirculated cooling water that working fluid temperature is dropped to 35 ℃ of left and right, then enter the bottom of fluidisation hydrogenator, in advance hydrogenation catalyst is added in fluidisation hydrogenator by catalyzer adding trough, compression hydrogen also enters fluidisation hydrogenator bottom after hydrogen buffering strainer impurity screening simultaneously, utilize compression hydrogen by catalyzer and working fluid blow afloat stir add hydrogenation should, 50 ℃ of left and right of temperature of reaction, reaction pressure 0.26mPa left and right, hydrogenation reaction hydrogenation efficiency is 13g/l left and right.
Excessive hydrogen is discharged after the pressurization of hydrogen recycle machine and is again entered in fluidisation hydrogenator and react from the top of reactor.
Working fluid after hydrogenation reaction flows out from the middle and upper part of reactor, enters catalyst filter the catalyzer of carrying secretly in liquid is filtered, and the clean liquid flowing out from catalyst filter enters in hydride storage tank.Catalyst filter quantity is provided with many, when the filter cake thickness of a catalyst filter is during to certain thickness, utilize recoil liquid pump to extract liquid clean in hydride storage tank catalyst filter is carried out to back flushing, the catalyzer that catalyst filter cartridge surface is adhered to springs back in fluidisation hydrogenator and again utilizes.
When carrying out hydrogenation reaction, there is micro-side reaction deposits yields, in order to be kept for the clean level of the working fluid of oxidizing reaction, from hydride pump discharge, draw a small amount of liquid and enter and in working fluid regenerator column, utilize the activated alumina purification of regenerating, the liquid after regeneration purifies turns back in hydride storage tank.
Liquid in hydride storage tank utilizes hydrogenation liquid pump flow through cartridge filter, water cooler, fall within the range of 46 ℃ of left and right and send into oxidizing tower top, because oxidation is thermopositive reaction, in order to keep oxidizing reaction temperature not higher than 52 ℃, at oxidizing tower, be provided with water cooler, pressurized air enters oxidizing tower bottom and upwards flows after air filter impurity screening, and airborne oxygen carries out oxidizing reaction with the hydrogenation material in the liquid flowing downward, generate hydrogen peroxide, hydrogenation material is reduced into the starting substance.
The tail gas that does not participate in reaction is discharged from oxidizing tower top, and desolventizing recovery process reclaims the solvent of carrying secretly in tail gas.
Working liquid after oxidizing reaction enters oxidation solution medial launder, utilizes oxidation solution pump delivery to extraction tower bottom.
Extraction tower is multi-layer porous sieve-tray tower.Pure water is through pure water storage tank, utilize pure water pump to deliver to di water heater, utilizing steam that pure water is preheating to 45 ℃ of left and right sneaks into after a small amount of phosphoric acid solution is adjusted into 3-3.6 by its pH value and enters extraction tower top, in tower, flow downward, with the working liquid counter-current extraction that makes progress floating, the hydrogen peroxide extraction that working liquid is contained out, during to extraction tower bottom, thick hydrogen peroxide solution concentration reaches 42% left and right by potential difference inflow scavenging tower top, heavy aromatic solvent is added from scavenging tower bottom, heavy aromatic solvent enters after scavenging tower by upwards floating with the density difference of hydrogen peroxide, carry out counter current contact with the thick hydrogen peroxide solution flowing downward, the most of organic carbon containing in clean thick hydrogen peroxide solution extracts, finished product hydrogen peroxide solution after purification removes hold tank.
Working liquid in extraction tower floats to extraction tower top and flows out, and enters coalescer and water eliminator and removes micro-hydrogen peroxide and the moisture content of wherein carrying secretly, and the working liquid that removes hydrogen peroxide and moisture content flows in cycle working fluid and recycles.
Heavy aromatic solvent after purification flows out from scavenging tower top.
The invention has the beneficial effects as follows:
1, catalyst levels, less than original 5%, calculates with 40,000 tons of a set of production capacities (folding concentration 100% is calculated) oxydol production apparatus, and catalyzer cost of investment can reduce approximately 2,700 ten thousand yuans.
2, hydrogenation efficiency can be brought up to 11-14g/l, hydrogen peroxide product that can direct production concentration 45% left and right.
3, hydrogen peroxide product per ton (folding concentration 100% is calculated) can reduce production costs 240 yuan of left and right.
4, can realize large-scale production, single cover system production peak can reach 250,000 tons (folding concentration 100% is calculated).
5, utilize coalescer and water trap to remove hydrogen peroxide residual in working liquid and moisture content, no longer need to use high alkali liquid to remove hydrogen peroxide residual in working liquid and moisture content, production waste is easily processed, and whole production system is processed under acid state and is moved, more safe and reliable.
6, equipment volume is little, and working liquid consumption is few, and investment is saved more.
Accompanying drawing explanation
Fig. 1 is equipment of the present invention and schema.
Embodiment
As shown in Figure 1, present device has: fluidisation hydrogenator, oxidizing tower, extraction tower, scavenging tower, hydrogen buffering strainer, air filter, catalyst filter, hydrogen recycle machine, catalyzer adding trough, pure water storage tank, di water heater, pure water pump, working fluid thermosistor, cycle operation liquid pump, cycle working fluid storage tank, working fluid regenerator column, working fluid well heater, hydride storage tank, hydrogenation liquid pump, recoil liquid pump, cartridge filter, hydride water cooler, oxidation solution medial launder, oxidation liquid pump, coalescer, water trap.
Specific operation process:
By heavy aromatics, tetrabutyl urea, the pungent fat of tricresyl phosphate, four kinds of industrial chemicals of 2-ethyl-anthraquinone are mixed with working fluid (heavy aromatics wherein according to a certain percentage, the pungent fat of tetrabutyl urea and tricresyl phosphate is solvent, 2-ethyl-anthraquinone is solute), the working fluid preparing is added in cycle working fluid storage tank, utilize cycle operation liquid pump that working fluid is sent into working fluid thermosistor, utilize recirculated cooling water that working fluid temperature is dropped to 35 ℃ of left and right, then enter the bottom of fluidisation hydrogenator, in advance the palladium catalyst of hydrogenation is added in fluidisation hydrogenator by adding trough, compression hydrogen also enters fluidisation hydrogenator bottom after hydrogen buffering strainer impurity screening simultaneously, utilize compression hydrogen by palladium catalyst and working fluid blow afloat stir add hydrogenation should, 50 ℃ of left and right of temperature of reaction, reaction pressure 0.26mPa left and right, hydrogenation reaction hydrogenation efficiency is 13g/l left and right.
Excessive hydrogen is discharged after the pressurization of hydrogen recycle machine and is again entered in fluidisation hydrogenator and react from the top of reactor.
Working fluid after hydrogenation reaction flows out from the middle and upper part of reactor, enters catalyst filter the palladium catalyst of carrying secretly in liquid is filtered, and the clean liquid flowing out from catalyst filter enters in hydride storage tank.Catalyst filter quantity is provided with many, when the filter cake thickness of a catalyst filter is during to certain thickness, utilize recoil liquid pump to extract liquid clean in hydride storage tank catalyst filter is carried out to back flushing, the palladium catalyst that catalyst filter cartridge surface is adhered to springs back in fluidisation hydrogenator and again utilizes.
When carrying out hydrogenation reaction, there is micro-side reaction deposits yields, in order to be kept for the clean level of the working fluid of oxidizing reaction, from hydride pump discharge, draw a small amount of liquid and enter and in working fluid regenerator column, utilize the activated alumina purification of regenerating, the liquid after regeneration purifies turns back in hydride storage tank.
Liquid in hydride storage tank utilizes hydrogenation liquid pump flow through cartridge filter, water cooler, fall within the range of 46 ℃ of left and right and send into oxidizing tower top, because oxidation is thermopositive reaction, in order to keep oxidizing reaction temperature not higher than 52 ℃, at oxidizing tower, be provided with water cooler, pressurized air enters oxidizing tower bottom and upwards flows after air filter impurity screening, and airborne oxygen carries out oxidizing reaction with the hydrogenation material in the liquid flowing downward, generate hydrogen peroxide, hydrogenation material is reduced into the starting substance.
The tail gas that does not participate in reaction is discharged from oxidizing tower top, and desolventizing recovery process reclaims the solvent of carrying secretly in tail gas.
Working liquid after oxidizing reaction enters oxidation solution medial launder, utilizes oxidation solution pump delivery to extraction tower bottom.
Extraction tower is multi-layer porous sieve-tray tower.Pure water is through pure water storage tank, utilize pure water pump to deliver to di water heater, utilizing steam that pure water is preheating to 45 ℃ of left and right sneaks into after a small amount of phosphoric acid solution is adjusted into 3-3.6 by its pH value and enters extraction tower top, in tower, flow downward, with the working liquid counter-current extraction that makes progress floating, the hydrogen peroxide extraction that working liquid is contained out, during to extraction tower bottom, thick hydrogen peroxide solution concentration reaches 42% left and right by potential difference inflow scavenging tower top, heavy aromatic solvent is added from scavenging tower bottom, heavy aromatic solvent enters after scavenging tower by upwards floating with the density difference of hydrogen peroxide, carry out counter current contact with the thick hydrogen peroxide solution flowing downward, the most of organic carbon containing in clean thick hydrogen peroxide solution extracts, finished product hydrogen peroxide solution after purification removes hold tank.
Working liquid in extraction tower floats to extraction tower top and flows out, and enters coalescer and water eliminator and removes micro-hydrogen peroxide and the moisture content of wherein carrying secretly, and the working liquid that removes hydrogen peroxide and moisture content flows in cycle working fluid and recycles.
Heavy aromatic solvent after purification flows out from scavenging tower top.
Claims (9)
1. a hydrogen peroxide producing and manufacturing technique, is characterized in that comprising fluidisation hydrogenation, oxidizing reaction, extraction and purification step.
2. method according to claim 1, it is characterized in that when fluidisation hydrogenation, under palladium catalyst existence condition, the pungent fat of heavy aromatics, tetrabutyl urea and tricresyl phosphate of take is solvent, by 2-ethyl-anthraquinone and excessive hydrogen temperature in fluidisation hydrogenator, be to react under 50 ± 2 ℃ of conditions, obtain reaction solution.
3. method according to claim 2, it is characterized in that passing in fluidisation hydrogenator palladium catalyst and by heavy aromatics, tetrabutyl urea, the pungent fat of tricresyl phosphate, 2-ethyl-anthraquinone and 2-ethyl-anthraquinone, be mixed to form, temperature is the cycle working fluid of 35 ± 2 ℃, then the bottom by fluidisation hydrogenator upwards passes into compression hydrogen, palladium catalyst and working fluid is blown afloat to stir and carry out fluidisation hydrogenation reaction.
4. method according to claim 1, is characterized in that reacting liquid filtering that fluidisation hydrogenation is obtained, purifies after removing palladium catalyst.
5. according to method described in claim 1 or 2, it is characterized in that when purifying: the reaction solution that fluidisation hydrogenation is obtained filters with activated alumina, obtains filtered solution.
6. method according to claim 1, while it is characterized in that oxidizing reaction, in being provided with the oxidizing tower of water cooler, the filtered solution that purification is obtained does not react higher than the condition of 52 ℃ in temperature of reaction with oxygen, obtains oxidation solution.
7. method according to claim 6, is characterized in that pressurized air to enter after air filter impurity screening oxidizing tower bottom and upwards flows, and the airborne oxygen filtered solution downward with autoxidation tower top reacts, and at the bottom of autoxidation tower, obtains oxidation solution.
8. method according to claim 1, while it is characterized in that extracting, extraction agent is the phosphate aqueous solution that 45 ± 2 ℃ of temperature, pH value are 3～3.6, extraction agent is downward by extracting tower top, carry out counter-current extraction with the oxidation solution making progress at the bottom of extraction tower, while reaching 42 ± 2% to the thick hydrogen peroxide solution concentration of extraction tower bottom, by potential difference, obtain hydrogen peroxide extraction liquid.
9. method according to claim 1, while it is characterized in that purifying, purifies with heavy aromatic solvent.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310535309.6A CN103588176A (en) | 2013-11-04 | 2013-11-04 | Production method of hydrogen peroxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201310535309.6A CN103588176A (en) | 2013-11-04 | 2013-11-04 | Production method of hydrogen peroxide |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN103588176A true CN103588176A (en) | 2014-02-19 |
Family
ID=50078544
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201310535309.6A Pending CN103588176A (en) | 2013-11-04 | 2013-11-04 | Production method of hydrogen peroxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN103588176A (en) |
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104401944A (en) * | 2014-10-29 | 2015-03-11 | 广西田东达盛化工科技有限公司 | Preparation process of high-purity hydrogen peroxide |
| CN104555932A (en) * | 2014-12-29 | 2015-04-29 | 安徽淮化股份有限公司 | Decoloration method of hydrogen peroxide concentrated residual liquid |
| CN106672911A (en) * | 2015-11-11 | 2017-05-17 | 中国石油化工股份有限公司 | Oxidation-extraction technology for production of hydrogen peroxide by anthraquinone process |
| CN108862205A (en) * | 2018-08-29 | 2018-11-23 | 江苏德邦工程有限公司 | A kind of dioxygen water preparation apparatus |
| CN109336059A (en) * | 2018-11-09 | 2019-02-15 | 乳源东阳光电化厂 | A kind of hydrogen peroxide vacuum dewatering system and its dewatering |
| CN110040690A (en) * | 2019-01-31 | 2019-07-23 | 滨化集团股份有限公司 | Hydrogenation fluid catalyst separation extraction technique and its device in a kind of hydrogen peroxide manufacture |
| CN110294460A (en) * | 2019-06-28 | 2019-10-01 | 平湖石化有限责任公司 | A kind of dicyandiamide solution of the complete acid hydrogen-peroxide working solution of anthraquinone production |
| CN110436418A (en) * | 2019-09-23 | 2019-11-12 | 扬州荣祥科技发展有限公司 | A kind of technique of hydrogen dioxide solution production by anthraquinone process |
| CN111732083A (en) * | 2020-05-26 | 2020-10-02 | 湖北三里枫香科技有限公司 | Fluidized bed hydrogen peroxide process |
| CN112499592A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | System and process for preparing hydrogen peroxide based on anthraquinone method |
| CN112499593A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | Automatic strengthening system and process for preparing hydrogen peroxide based on anthraquinone method |
| CN114162789A (en) * | 2021-12-30 | 2022-03-11 | 连云港市工投集团利海化工有限公司 | Process and device for preparing hydrogen peroxide |
| CN114506820A (en) * | 2022-03-18 | 2022-05-17 | 西安吉利电子新材料股份有限公司 | Method for directly producing electronic grade hydrogen peroxide from hydrogen and oxygen |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB718307A (en) * | 1952-04-28 | 1954-11-10 | Laporte Chemical | Improvements in or relating to hydrogenation |
| CN101746736A (en) * | 2008-12-10 | 2010-06-23 | 中国科学院大连化学物理研究所 | Method for preparing hydrogen peroxide by utilizing microchannel technology |
| CN102001631A (en) * | 2010-12-28 | 2011-04-06 | 上海福磊国际贸易有限公司 | Method for preparing hydrogen peroxide |
-
2013
- 2013-11-04 CN CN201310535309.6A patent/CN103588176A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB718307A (en) * | 1952-04-28 | 1954-11-10 | Laporte Chemical | Improvements in or relating to hydrogenation |
| CN101746736A (en) * | 2008-12-10 | 2010-06-23 | 中国科学院大连化学物理研究所 | Method for preparing hydrogen peroxide by utilizing microchannel technology |
| CN102001631A (en) * | 2010-12-28 | 2011-04-06 | 上海福磊国际贸易有限公司 | Method for preparing hydrogen peroxide |
Cited By (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104401944A (en) * | 2014-10-29 | 2015-03-11 | 广西田东达盛化工科技有限公司 | Preparation process of high-purity hydrogen peroxide |
| CN104555932A (en) * | 2014-12-29 | 2015-04-29 | 安徽淮化股份有限公司 | Decoloration method of hydrogen peroxide concentrated residual liquid |
| CN106672911A (en) * | 2015-11-11 | 2017-05-17 | 中国石油化工股份有限公司 | Oxidation-extraction technology for production of hydrogen peroxide by anthraquinone process |
| CN106672911B (en) * | 2015-11-11 | 2018-08-14 | 中国石油化工股份有限公司 | A kind of oxidation-extraction technique of hydrogen dioxide solution production by anthraquinone process |
| CN108862205A (en) * | 2018-08-29 | 2018-11-23 | 江苏德邦工程有限公司 | A kind of dioxygen water preparation apparatus |
| CN108862205B (en) * | 2018-08-29 | 2023-09-12 | 江苏德邦工程有限公司 | Hydrogen peroxide preparation device |
| CN109336059A (en) * | 2018-11-09 | 2019-02-15 | 乳源东阳光电化厂 | A kind of hydrogen peroxide vacuum dewatering system and its dewatering |
| CN110040690A (en) * | 2019-01-31 | 2019-07-23 | 滨化集团股份有限公司 | Hydrogenation fluid catalyst separation extraction technique and its device in a kind of hydrogen peroxide manufacture |
| CN110294460A (en) * | 2019-06-28 | 2019-10-01 | 平湖石化有限责任公司 | A kind of dicyandiamide solution of the complete acid hydrogen-peroxide working solution of anthraquinone production |
| WO2021047044A1 (en) * | 2019-09-14 | 2021-03-18 | 南京延长反应技术研究院有限公司 | System and process for preparing hydrogen peroxide based on anthraquinone process |
| CN112499592A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | System and process for preparing hydrogen peroxide based on anthraquinone method |
| CN112499593A (en) * | 2019-09-14 | 2021-03-16 | 南京延长反应技术研究院有限公司 | Automatic strengthening system and process for preparing hydrogen peroxide based on anthraquinone method |
| CN110436418A (en) * | 2019-09-23 | 2019-11-12 | 扬州荣祥科技发展有限公司 | A kind of technique of hydrogen dioxide solution production by anthraquinone process |
| CN111732083A (en) * | 2020-05-26 | 2020-10-02 | 湖北三里枫香科技有限公司 | Fluidized bed hydrogen peroxide process |
| CN114162789A (en) * | 2021-12-30 | 2022-03-11 | 连云港市工投集团利海化工有限公司 | Process and device for preparing hydrogen peroxide |
| CN114506820A (en) * | 2022-03-18 | 2022-05-17 | 西安吉利电子新材料股份有限公司 | Method for directly producing electronic grade hydrogen peroxide from hydrogen and oxygen |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103588176A (en) | Production method of hydrogen peroxide | |
| CN109911859B (en) | Working solution for preparing hydrogen peroxide by anthraquinone process and application thereof | |
| CN110436418A (en) | A kind of technique of hydrogen dioxide solution production by anthraquinone process | |
| CN101254985B (en) | PTA refined mother liquor reclaiming method and system | |
| CN101016175B (en) | Method of eliminating magnesium sulfate from magnesium sulfate containing waste water solution | |
| CN106422667B (en) | The method of one-step removal acidic components and water from gas | |
| RU2010153978A (en) | METHOD FOR METHANE EXTRACTION AND METHOD FOR CLEANING THE BIOGAS | |
| CN102816063B (en) | Method for producing high purity 2-hydroxy-3-naphthoic acid | |
| CN107720872B (en) | Purifying device and purifying method for washing water of methanol-to-olefin device | |
| CN205099601U (en) | System for hydrogenation device and production hydrogen peroxide | |
| CN206970213U (en) | A kind of argon gas EGR in monocrystalline silicon production | |
| CN106861401B (en) | Liquefied petroleum gas desulfurization purification system and purification method | |
| CN201842708U (en) | Purifying device for online separation of metal salt and free acid in pickling solution | |
| CN104561592A (en) | Nickel-containing electroplating wastewater treatment and nickel recovery method | |
| CN106745886A (en) | Free acid and metallic salt separator in industrial waste acid | |
| CN108671747A (en) | A kind of method and system discharging recycling purification helium in exhaust gas from preform sintering furnace | |
| CN106542589A (en) | MTO chilled water (chw)s and washing water purification process technique | |
| CN112844006A (en) | Yellow phosphorus tail gas purification method | |
| CN106178591A (en) | A kind of method purifying organic amine | |
| CN110482764A (en) | The regenerative system of raffinate in hydrogen dioxide solution production by anthraquinone process technique | |
| CN110482493A (en) | The regeneration technology of working solution in hydrogen dioxide solution production by anthraquinone process technique | |
| CN114452679A (en) | Alkali tower and method for post-treatment of hydrogen peroxide working solution by anthraquinone process | |
| CN206368077U (en) | Free acid and metallic salt separator in industrial waste acid | |
| JP2000159510A (en) | Method and apparatus for treating gas mixture of hydrogen sulfide and sulfur dioxide including by- products-removing process | |
| CN104498983A (en) | Method for preparation of high purity oxygen by water electrolysis |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20140219 |