WO2007129769A1 - 作動溶液の再生工程を含む過酸化水素の製造方法 - Google Patents
作動溶液の再生工程を含む過酸化水素の製造方法 Download PDFInfo
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- WO2007129769A1 WO2007129769A1 PCT/JP2007/059813 JP2007059813W WO2007129769A1 WO 2007129769 A1 WO2007129769 A1 WO 2007129769A1 JP 2007059813 W JP2007059813 W JP 2007059813W WO 2007129769 A1 WO2007129769 A1 WO 2007129769A1
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- working solution
- distillation
- hydrogen peroxide
- anthraquinones
- anthraquinone
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B15/00—Peroxides; Peroxyhydrates; Peroxyacids or salts thereof; Superoxides; Ozonides
- C01B15/01—Hydrogen peroxide
- C01B15/022—Preparation from organic compounds
- C01B15/023—Preparation from organic compounds by the alkyl-anthraquinone process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
- B01J21/04—Alumina
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
- B01J21/12—Silica and alumina
Definitions
- the present invention relates to a method for producing hydrogen peroxide including a regeneration step of a working solution.
- anthraquinone having an alkyl substituent hereinafter sometimes simply referred to as “anthraquinone”
- a 5, 6, 7, 8-tetrahydroanthraquinone having an alkyl substituent hereinafter simply “ The present invention relates to a method for producing hydrogen peroxide by repeatedly reducing and oxidizing a working solution containing “tetrahydroanthraquinone”. More specifically, the present invention relates to a method for producing hydrogen peroxide, which can efficiently remove from the working solution inert substances produced as a by-product in the production of hydrogen peroxide.
- anthraquinone or tetrahydroanthraquinone (hereinafter sometimes referred to as “anthraquinones”) is used after being dissolved in a suitable organic solvent.
- An organic solvent is used alone or as a mixture, but usually a mixture of two organic solvents is used.
- a solution prepared by dissolving anthraquinones in an organic solvent is called a working solution.
- An anthraquinone method is known as an industrial method for producing hydrogen peroxide.
- anthraquinones are dissolved in an organic solvent to obtain a working solution, and in the hydrogenation step, the anthraquinones are reduced with hydrogen in the presence of a hydrogenation catalyst, and an anthrahydroquinone having an alkyl substituent or an alkyl substituent.
- anthrahydroquinones 5,6,7,8-Tetrahydroanthrahydroquinone (hereinafter sometimes referred to as “anthrahydroquinones”).
- anthrahydroquinones are converted back to anthraquinones, and at the same time, hydrogen peroxide is generated.
- Hydrogen peroxide in the working solution is separated from the working solution by methods such as water extraction.
- the working solution from which hydrogen peroxide has been extracted is returned to the hydrogenation step again to form a circulation process.
- the concentration of the solute component which is the sum of the “active substance” and the “inert substance”
- increases increasing the liquid viscosity and the liquid specific gravity. Bring.
- An increase in liquid viscosity increases the flow resistance of the filter, making it difficult to secure the liquid flow rate.
- the increase in liquid specific gravity hinders the formation of the liquid-liquid interface when hydrogen peroxide is extracted from the working solution because the specific gravity difference between the oil layer and the water layer is reduced.
- the concentration of the active substance is low and the hydrogenation rate is relatively increased, which is an adverse effect of the high hydrogenation rate. It causes some deterioration of hydrogenation selectivity. That is, there is a need for a working solution that suppresses the concentration of the inert substance and maintains the concentration of the active substance at a sufficiently high level.
- the first type is a method in which the by-product itself is not generated as much as possible
- the second type is a method in which the by-product is regenerated into anthraquinones
- the third type is a method in which the by-product is removed.
- the first type includes: 1) 1) a method in which the circulation system is mild, 1) 2) a method using a highly selective hydrogenation catalyst, 1) 1) 3. a chemically stable reaction medium 1-4. Methods using chemically stable solvents.
- the second type of method includes a method of regenerating with 2-1. Y-alumina, activated alumina, etc. (Japanese Patent Publication No.
- a method of regenerating with alkali There are three types of methods: 3-1. Removal by distillation, 3-2. Removal by crystallization or extraction, 3-3. Removal by adsorption with activated alumina, etc.
- the first type of method cannot prevent the increase of by-products in the working solution over time. In general, the regeneration reaction of by-products is very slow, so irreversible by-products are produced. For this reason, it is difficult even with the second type of method, and it is difficult to prevent the increase of by-products in the working solution over time even if both are combined.
- the light degradation product is useful as a solubility aid for hydroquinones, so it is not removed and the purpose is to remove only harmful heavy degradation products.
- 6 8 g of anthraquinones (active substance) is contained in 14 5 g of the distillate described in Example 1 of JP-B-5 5-2 3 7 6 2
- it contains more than half (53% by weight) of light degradation products (inert substances). That is, this method has a problem that the anthraquinones which are active substances cannot be recovered with high purity.
- a method of selectively extracting active substances JPB 4 1 2 1 6 0 2
- a method of selectively extracting inactive substances JPB 5— 1 2 2 8 1
- the working solution is mixed with an acyclic hydrocarbon and separated into a first layer containing an active substance (acyclic hydrocarbon layer) and a second layer containing a lot of inert substances.
- a purification operation is performed.
- it is necessary to distill off and remove the non-cyclic hydrocarbons after the separation, which causes an energy problem because of the large amount.
- JP 5 _ 1 2 2 8 1 the working solution and liquefied carbon dioxide are brought into contact with each other, and the inert material is extracted and removed from the carbon dioxide layer.
- the ratio of anthraquinones in the recovered liquid is 85% by weight, and it can be purified to a sufficiently high concentration of the active substance.
- epoxy derivatives that are inactive substances are also anthraquinones, exactly 85% of them are not active substances. This is presumed to be a computational process performed because an epoxy compound is a substance that can be converted into an active substance by a regeneration reaction.
- the problem with this method is that it requires a high-pressure reactor in order to use liquid carbon dioxide, and there is a problem with the treatment of liquid carbon dioxide after separation.
- the present inventors recovered the organic solvent by distillation under atmospheric pressure or lower pressure, and then obtained anthraquinones by distillation at a lower pressure of 20 ° C. or more and a residence time of 1 hour or more. It was discovered that the by-product in the working solution before distillation can be regenerated or converted into a material that can be easily regenerated by recovering and reusing the entire distillate obtained as a working solution. Furthermore, it has been found that by treating the working solution obtained from the entire distillate with a regenerated catalyst, a working solution containing a high concentration of effective anthraquinones that is regenerated into anthraquinones, which are active ingredients, can be obtained.
- a solution regeneration step i) a first distillation step in which the organic solvent is recovered by distillation at atmospheric pressure or lower, and ii) a residence time of 200 ° C. or higher at a lower pressure.
- the method further comprises a step of bringing the working solution prepared using the organic solvent, anthraquinone and tetrahydroanthraquinone recovered in the first and second distillation steps into contact with the regenerated catalyst.
- the main component of the regenerated catalyst is alumina or silica alumina.
- the pressure in the first distillation step is in the range of 1 kPa to lOOkPa.
- the pressure in the second distillation step is 1 kPa or less.
- the temperature in the second distillation step is in the range of 200 ° C. to 300 ° C.
- the residence time in the second distillation step is in the range of 1 hour to 10 hours.
- the alkyl substituent is an amyl group.
- an anthraquinone that is an active substance can be efficiently recovered from a working solution in which an inert substance is accumulated, and a working solution in which a regeneration reaction easily proceeds can be obtained.
- a working solution having a high concentration of the active substance can be obtained, and the capability of each step of hydrogen peroxide production can be maintained at a high level.
- a working solution containing an organic solvent, an anthraquinone having an alkyl substituent, and a tetrahydroanthraquinone having an alkyl substituent is acidified after reduction to produce hydrogen peroxide.
- an inert substance produced as a by-product in the production of hydrogen peroxide is removed from the working solution, and the working solution from which the inert substance has been removed is recycled to the hydrogen peroxide production process.
- a solution prepared by dissolving anthraquinones in an organic solvent is called a working solution.
- Examples of the anthraquinone having an alkyl substituent used in the present invention include ethylanthraquinone, t-ptylanthraquinone, and amylanthraquinone. These may be used alone or in combination of two or more.
- examples of the tetrahydroanthraquinone having an alkyl substituent include ethyltetrahydroanthraquinone, t-butyltetrahydroanthraquinone, and aminolettetrahydroanthraquinone. These may be used alone or in combination of two or more.
- the organic solvent used for preparing the working solution in the present invention is not particularly limited, but preferred organic solvents include a combination of an aromatic hydrocarbon and a higher alcohol, an aromatic hydrocarbon and a sucrose. Examples include combinations of oral hexanols or alkyl carboxylic esters of oral hexanols, and combinations of aromatic hydrocarbons with tetrasubstituted ureas or cyclic ureas.
- the working solution regeneration step includes: i) a first distillation step in which the organic solvent is recovered by distillation under a pressure of atmospheric pressure or lower; and ii) a lower pressure then And a second distillation step for recovering the anthraquinone and tetrahydroanthraquinone by distillation at a temperature of 200 ° C. or more and a residence time of 1 hour or more. Furthermore, it is preferable to have a step of bringing the working solution prepared using the organic solvent, anthraquinone and tetrahydroanthraquinone recovered in the first and second distillation steps into contact with the regenerated catalyst.
- the first distillation step in the working solution regeneration step of the present invention consists of distilling the organic solvent in the working solution at atmospheric pressure or lower.
- a commonly used distillation facility can be used and there is no particular limitation.
- batch distillation equipment, ream A secondary distillation apparatus, a thin-film distillation apparatus, and the like can be mentioned.
- a batch distillation apparatus that can be used in common with the apparatus used in the second distillation step is preferable.
- the temperature and pressure in the first distillation step are appropriately selected depending on the organic solvent used in the working solution, and thus cannot be specified unconditionally, but the following conditions are preferably selected.
- the pressure is preferably 1 k Pa to l 0 0 k Pa (atmospheric pressure), more preferably 5 to 30 k Pa.
- the distillation temperature is determined as the conditions for distillation until the residual solvent amount is 5 wt% or less. Usually, when the temperature rises from about 50 to about L 0 0 ° C from the temperature at which the solvent starts distilling, the end of the first distillation is considered. For example, when the solvent starts to distill at 13 ° C. under a reduced pressure of 13 kPa, it is preferable to end the first distillation when reaching 200 ° C.
- anthraquinones are distilled at a lower pressure than in the first distillation step.
- the apparatus a batch distillation apparatus is preferable because a residence time of 1 hour or more is required.
- the “residence time” means the time from the start to the stop of the distillation or take-out when the kettle temperature reaches 200 ° C., and the production of hydrogen peroxide according to the present invention.
- the method includes both batch and continuous distillation.
- the pressure is preferably 1 k Pa or less, more preferably 50 to 50 0 Pa, in order to increase the recovery rate of anthraquinones.
- the distillation temperature is 200 ° C. or higher, preferably in the range of 200 ° C. to 300 ° C., and more preferably in the range of 230 ° C. to 2800 ° C.
- the reaction of converting the by-products into anthraquinones or converting them into easily recyclable substances does not proceed sufficiently.
- the hydrogenation catalyst is contaminated. This is preferable because it causes a reduction in the performance of the circulation process.
- the residence time in distillation needs to be distilled over 1 hour after reaching 200 ° C, but from the viewpoint of operation, such as the entire process in batch distillation being completed within 24 hours. Usually, a range of 1 to 10 hours is preferable, and a range of 6 to 10 hours is more preferable.
- the high boiling residue remaining in the distillation kettle increases in viscosity as the temperature decreases and becomes a solid state at room temperature. Therefore, it is preferable to collect it in a low viscosity state at a high temperature after distillation.
- the product also undergoes various reactions and is recovered at a composition ratio slightly different from the amount in the raw material. Furthermore, during the distillation operation, a partial force of the compound that seems to be an adduct of anthraquinone and solvent proceeds, and the reaction that decomposes into anthraquinones, solvent, and water proceeds, and most of the reaction is completed in 1 hour at 20 ° C. It is. As a result, the recovery rate of anthraquinones gradually increases by distillation, and the recovery rate of the anthraquinones after the regeneration reaction exceeds the material balance. In addition, it can be confirmed that the solvent adduct is decomposed because the solvent and water gradually accumulate in the cold trap of the vacuum pipe, and that it is generated by distillation operation at 200 ° C or higher.
- a working solution is prepared from the recovered solvent and anthraquinones and treated with a regenerated catalyst to obtain a working solution having a high “active substance”
- a working solution is prepared by mixing the solvent recovered in the first distillation and the anthraquinones obtained in the second distillation.
- a working solution is prepared by passing the prepared working solution through a fixed bed or a fluidized bed containing a regenerated catalyst, a part of the light boiling decomposition product is regenerated into active anthraquinones. It is preferable to circulate through the reaction because a single flow may not be sufficient.
- the regenerated catalyst used here is preferably activated alumina or silica alumina, more preferably activated alumina.
- the surface area and particle size of the regenerated catalyst are appropriately selected depending on the reaction conditions and equipment, but are not particularly limited.
- the reaction temperature is preferably in the range of 0 ° C to 200 ° C, more preferably from 50 ° C to 150 ° C.
- hydroquinones accumulate and the progress of some regeneration reactions slows down, so it is desirable to contact hydroquinones with oxygen or air in the course of circulation. .
- the peroxidation can be achieved by introducing the working solution obtained by distillation into the hydrogen peroxide production apparatus. It is also possible to carry out a regeneration reaction while producing hydrogen.
- the first distillation step in the present invention was performed on a small scale.
- the working solution used for the production of hydrogen peroxide was extracted from the hydrogen peroxide production apparatus and used for the experiment.
- preload the working solution with about 200 g in a 50 O ml flask equipped in the distillation kettle, and control the degree of vacuum to 13 kPa to control the temperature from room temperature. It was raised.
- the moving solution was successively added, and the addition was stopped at a total charge of 100 g.
- the addition of the working solution was stopped, the distillation was continued until the temperature of the distillation kettle reached 200 ° C., and the solvent was collected over about 2 hours.
- the second distillation step in the present invention was performed on a small scale. Distillation of anthraquinones was performed at a lower pressure than in the first distillation step. A solid containing 300 g of anthraquinones remained in the flask provided in the distillation kettle following Example 1, and distillation was performed using this. Heating was performed by reducing the pressure to 100 Pa using a vacuum pump. At this time, the remaining solvent component is distilled off, which affects the degree of vacuum. The temperature was raised gradually and finally distillation was performed up to 2550 ° C ⁇ 100 Pa for 3 hours. The resulting distillate was 2 3 8 g. Also, the amount of the solvent water trapped in the trap was 2 g, which contradicts the result of Example 1 and indicates that it was produced during distillation. Conversely, when the anthraquinones in the residue left in the distillation kettle were examined by LC, it was 3% or less, indicating that the target compound was almost distilled off.
- the regenerated catalyst contact step in the present invention was performed on a small scale.
- a working solution was prepared using the anthraquinones distilled in Example 2 and the solvent recovered in Example 1. The concentration of this working solution was adjusted to the concentration of the original working solution and regenerated using an alumina fixed bed.
- As activated alumina 2800 g of KH D-12 produced by Sumitomo Chemical Co., Ltd. was used, and the solution was passed through at 80 ° C.
- Each composition analyzed by LC is shown below.
- Example 3 Composition of each working solution (in parentheses is% by weight in solid)
- Example 2 the same operation as in Example 1 was performed to obtain a solid containing 300 g of anthraquinones.
- anthraquinones were distilled according to Example 2.
- a thin-film distillation apparatus was used to confirm the difference in short residence time.
- Anthraquinones were preliminarily heated to 70 ° C to form a molten state, and distilled at a temperature of 25 ° C and 10 O Pa. The drip rate was adjusted so that the residence time was approximately 10 minutes or less.
- hot water at 80 ° C was used for the condenser to prevent the distillate from consolidating with the condenser.
- the obtained distillate was 204 g.
- Example 3 this distillate was circulated and regenerated by adjusting the recovered solvent so that it had the same concentration as the initial working solution.
- the working solution obtained by reconstitution The amount of catalyst was reduced to 2 40 g for comparison, and the flow rate was set to 2 5 7 m 1 Zh. The ratio of the regeneration amount is also compared with the catalyst contact time.
- Table 2 Comparative Example 1 Composition of each working solution (in parentheses is% by weight in solid)
- Example 2 the same operation as in Example 1 was performed to obtain a solid containing 300 g of anthraquinones.
- anthraquinones were distilled according to Example 2.
- the distillation was finally performed at a temperature of 190 ° C for 3 hours. Since the distillation temperature was low, there were few decomposition products into water / solvent, and a small amount was trapped in the trap. In addition, the degree of vacuum finally became 5 O Pa or less.
- the obtained distillate was 2 10 g, and a working solution was prepared according to Example 3 to perform circulation regeneration. However, since the working solution obtained by re-preparation was a small amount of 700 g, the catalyst amount was 2 4 7 for comparison.
- the flow rate was set to 2 65 m 1. Combine the catalyst contact time and compare the regeneration ratio. Table 3, Comparative Example 2 Composition of each working solution (in parentheses is% by weight in solid)
- the amount of recovered anthraquinones by distillation is less than that of Example 3 because of the effect of temperature.
- the regeneration reaction progressed and the effective force was almost the same.
- Example 3 In order to confirm the effect of the presence or absence of distillation, circulating liquid was passed through the alumina catalyst without distillation, following Example 3.
- the working solution amount was 793 g according to Example 3.
- Table 4 Comparative Example 3 Composition of each working solution (in parentheses is% by weight in solid)
- the solvent component was recovered from 20 L of the working solution in an experimental apparatus having the same equipment configuration as in Example 1 except that the flask scale was scaled up to 10 L.
- the difference from Example 1 is that a mantle heater is used in place of the oil bath, and the pipe diameter is increased according to the scale-up.
- 3 L of working solution was charged in the flask in advance, and the temperature was raised from room temperature by controlling the vacuum to 1 3 kPa, and the amount of liquid in the flask decreased when distillation started. Therefore, the working solution was added in succession, and the addition was stopped when the total charged amount was 20 L (18.6 kg).
- Example 5 Composition of each working solution (in parentheses is% by weight in solid)
- Example 4 For the initial working solution (without distillation) used in Example 4, continuous circulation operation was similarly performed using the apparatus of Example 5. The changes in the composition of the working solution after 30 days of continuous operation are shown below. Table 6, Comparative Example 4 Composition of each working solution (in parentheses is% by weight in solid)
- the effective component tended to decrease due to continuous operation. xiii) When only the alumina regeneration process was performed as in the state after continuous operation, the effective content in the working solution showed a decreasing trend, and the hydrogen peroxide production capacity further decreased in proportion.
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Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2008514532A JP5233668B2 (ja) | 2006-05-09 | 2007-05-07 | 作動溶液の再生工程を含む過酸化水素の製造方法 |
KR1020087028986A KR101362495B1 (ko) | 2006-05-09 | 2007-05-07 | 작동용액의 재생공정을 포함하는 과산화수소의 제조방법 |
EP07743248.2A EP2022757B1 (en) | 2006-05-09 | 2007-05-07 | Process for hydrogen peroxide production including step for regeneration of working solution |
US12/226,280 US20090169469A1 (en) | 2006-05-09 | 2007-05-07 | Process for Hydrogen Peroxide Production Including Step for Regeneration of Working Solution |
CN2007800130959A CN101421184B (zh) | 2006-05-09 | 2007-05-07 | 含工作溶液再生工序的过氧化氢制造方法 |
Applications Claiming Priority (2)
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JP2006-129860 | 2006-05-09 | ||
JP2006129860 | 2006-05-09 |
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WO2007129769A1 true WO2007129769A1 (ja) | 2007-11-15 |
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PCT/JP2007/059813 WO2007129769A1 (ja) | 2006-05-09 | 2007-05-07 | 作動溶液の再生工程を含む過酸化水素の製造方法 |
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US (1) | US20090169469A1 (ja) |
EP (1) | EP2022757B1 (ja) |
JP (1) | JP5233668B2 (ja) |
KR (1) | KR101362495B1 (ja) |
CN (1) | CN101421184B (ja) |
TW (1) | TWI383951B (ja) |
WO (1) | WO2007129769A1 (ja) |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015025735A1 (ja) * | 2013-08-23 | 2015-02-26 | 三菱瓦斯化学株式会社 | 過酸化水素製造に使用される作動溶液の再生方法、並びに再生した作動溶液を用いた過酸化水素の製造方法 |
KR20190028289A (ko) | 2017-09-08 | 2019-03-18 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소의 제조 방법 |
KR20190028290A (ko) * | 2017-09-08 | 2019-03-18 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소 제조용 작동 용액의 조제 방법 |
JP2020007201A (ja) * | 2018-07-11 | 2020-01-16 | 三菱瓦斯化学株式会社 | 過酸化水素水溶液の製造方法 |
WO2020105500A1 (ja) * | 2018-11-20 | 2020-05-28 | 三菱瓦斯化学株式会社 | 作動溶液の処理方法 |
JP2022535021A (ja) * | 2019-06-21 | 2022-08-04 | ヒソン カタリスツ コーポレイション | 過酸化水素合成及び再生触媒、並びにその製造方法 |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
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CN103803502B (zh) * | 2012-11-07 | 2015-12-16 | 中国石油化工股份有限公司 | 一种蒽醌法生产过氧化氢的工作液再生方法 |
CN104418307B (zh) * | 2013-08-22 | 2016-06-22 | 中国石油化工股份有限公司 | 一种蒽醌法生产双氧水多段氢化工艺 |
CN108101002B (zh) * | 2018-01-25 | 2021-09-14 | 江苏理文化工有限公司 | 一种提高过氧化氢成品品质的方法 |
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2007
- 2007-03-30 TW TW096111191A patent/TWI383951B/zh active
- 2007-05-07 KR KR1020087028986A patent/KR101362495B1/ko active IP Right Grant
- 2007-05-07 EP EP07743248.2A patent/EP2022757B1/en not_active Not-in-force
- 2007-05-07 JP JP2008514532A patent/JP5233668B2/ja active Active
- 2007-05-07 WO PCT/JP2007/059813 patent/WO2007129769A1/ja active Application Filing
- 2007-05-07 CN CN2007800130959A patent/CN101421184B/zh active Active
- 2007-05-07 US US12/226,280 patent/US20090169469A1/en not_active Abandoned
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Cited By (16)
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KR20160048077A (ko) | 2013-08-23 | 2016-05-03 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소 제조에 사용되는 작동 용액의 재생 방법, 및 재생한 작동 용액을 사용한 과산화수소의 제조 방법 |
JPWO2015025735A1 (ja) * | 2013-08-23 | 2017-03-02 | 三菱瓦斯化学株式会社 | 過酸化水素製造に使用される作動溶液の再生方法、並びに再生した作動溶液を用いた過酸化水素の製造方法 |
US10138123B2 (en) | 2013-08-23 | 2018-11-27 | Mitsubishi Gas Chemical Company, Inc. | Method for regenerating working solution used for production of hydrogen peroxide and method for producing hydrogen peroxide using regenerated working solution |
WO2015025735A1 (ja) * | 2013-08-23 | 2015-02-26 | 三菱瓦斯化学株式会社 | 過酸化水素製造に使用される作動溶液の再生方法、並びに再生した作動溶液を用いた過酸化水素の製造方法 |
KR102610949B1 (ko) | 2017-09-08 | 2023-12-06 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소 제조용 작동 용액의 조제 방법 |
KR20190028289A (ko) | 2017-09-08 | 2019-03-18 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소의 제조 방법 |
KR20190028290A (ko) * | 2017-09-08 | 2019-03-18 | 미츠비시 가스 가가쿠 가부시키가이샤 | 과산화수소 제조용 작동 용액의 조제 방법 |
JP2019048739A (ja) * | 2017-09-08 | 2019-03-28 | 三菱瓦斯化学株式会社 | 過酸化水素製造用作動溶液の調製方法 |
JP2019048740A (ja) * | 2017-09-08 | 2019-03-28 | 三菱瓦斯化学株式会社 | 過酸化水素の製造方法 |
JP2020007201A (ja) * | 2018-07-11 | 2020-01-16 | 三菱瓦斯化学株式会社 | 過酸化水素水溶液の製造方法 |
JP7322363B2 (ja) | 2018-07-11 | 2023-08-08 | 三菱瓦斯化学株式会社 | 過酸化水素水溶液の製造方法 |
JPWO2020105500A1 (ja) * | 2018-11-20 | 2021-09-30 | 三菱瓦斯化学株式会社 | 作動溶液の処理方法 |
JP7327414B2 (ja) | 2018-11-20 | 2023-08-16 | 三菱瓦斯化学株式会社 | 作動溶液の処理方法 |
WO2020105500A1 (ja) * | 2018-11-20 | 2020-05-28 | 三菱瓦斯化学株式会社 | 作動溶液の処理方法 |
JP2022535021A (ja) * | 2019-06-21 | 2022-08-04 | ヒソン カタリスツ コーポレイション | 過酸化水素合成及び再生触媒、並びにその製造方法 |
JP7336539B2 (ja) | 2019-06-21 | 2023-08-31 | ヒソン カタリスツ コーポレイション | 過酸化水素合成及び再生触媒、並びにその製造方法 |
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JP5233668B2 (ja) | 2013-07-10 |
EP2022757B1 (en) | 2015-07-29 |
CN101421184A (zh) | 2009-04-29 |
KR101362495B1 (ko) | 2014-02-13 |
JPWO2007129769A1 (ja) | 2009-09-17 |
EP2022757A1 (en) | 2009-02-11 |
US20090169469A1 (en) | 2009-07-02 |
TW200744947A (en) | 2007-12-16 |
CN101421184B (zh) | 2011-04-13 |
KR20090016561A (ko) | 2009-02-16 |
TWI383951B (zh) | 2013-02-01 |
EP2022757A4 (en) | 2011-03-30 |
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