WO1999062818A1 - Procede de production de polysulfure par oxydation catalytique - Google Patents
Procede de production de polysulfure par oxydation catalytique Download PDFInfo
- Publication number
- WO1999062818A1 WO1999062818A1 PCT/JP1999/002786 JP9902786W WO9962818A1 WO 1999062818 A1 WO1999062818 A1 WO 1999062818A1 JP 9902786 W JP9902786 W JP 9902786W WO 9962818 A1 WO9962818 A1 WO 9962818A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- anode
- polysulfide
- producing
- nickel
- chamber
- Prior art date
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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
- C01B17/00—Sulfur; Compounds thereof
- C01B17/22—Alkali metal sulfides or polysulfides
- C01B17/34—Polysulfides of sodium or potassium
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/0057—Oxidation of liquors, e.g. in order to reduce the losses of sulfur compounds, followed by evaporation or combustion if the liquor in question is a black liquor
-
- D—TEXTILES; PAPER
- D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
- D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
- D21C11/00—Regeneration of pulp liquors or effluent waste waters
- D21C11/04—Regeneration of pulp liquors or effluent waste waters of alkali lye
Definitions
- the present invention relates to a method for producing a polysulfide by electrolytic oxidation, and more particularly to a method for producing a polysulfide cooking liquor by electrolytically oxidizing white liquor or green liquor in a pulp production process.
- the cooking liquor in the polysulfide cooking process is manufactured by oxidizing an alkaline aqueous solution containing sodium sulfide, so-called white liquor, with molecular oxygen such as air in the presence of a catalyst such as activated carbon (eg, reaction formula 1).
- a catalyst such as activated carbon (eg, reaction formula 1).
- polysulfide is also referred to as polysulfide sulfur (PS—S).
- PS—S polysulfide sulfur
- sodium sulfide has a valence of 0 in Na 2 SX , That is, (x-1) atoms.
- PCT International Publication No. WO 95/00701 describes the electrolytic production of polysulfide cooking liquor.
- a method is described. In this method, an anode is used in which a carrier is coated with oxides of lutetium, iridium, platinum, and palladium. Specifically, a three-dimensional mesh electrode of a carrier in which a number of expanded metals are combined is disclosed.
- WO97 / 412125 describes a method for electrolytic production of a polysulfide cooking liquor by the present applicants. In this method, a porous anode made of at least carbon is used as the anode, and in particular, an aggregate of carbon fibers having a diameter of 1 to 300 ⁇ m is used.
- the present invention provides a method for obtaining high-concentration polysulfide from a sulfide ion in a solution by an electrolytic method, and in particular, converting a digestion liquor containing high-concentration polysulfide from white liquor in a pulp production process into thiosulfate ion
- the aim is to produce with high selectivity and low power by minimizing by-products.
- Another object of the present invention is to provide a method for producing a polysulfide cooking liquor under conditions of low pressure loss in the electrolysis operation. Disclosure of the invention
- the present invention has a physically continuous three-dimensional network structure made of nickel or a nickel alloy containing at least 50% by weight of nickel at least on the surface, and has a per unit volume of the anode chamber.
- An anode chamber with a porous anode with a surface area of 500 to 2000 m 2 / m 3 , a force sword chamber with a force sword, and a diaphragm that separates the anode and cathode chambers Provided is a method for producing a polysulfide, characterized in that a solution containing a sulfide ion is introduced into an anode chamber of an electrolytic cell having the same, and polysulfide ions are obtained by electrolytic oxidation.
- the anode chamber has a physically continuous three-dimensional network structure made of nickel or a nickel alloy containing at least 50% by weight of nickel, and the unit volume of the anode chamber A porous anode having a surface area of 500 to 2000 m 2 / m 3 per pound is provided. Since at least the surface portion of the anode is made of nickel or a nickel alloy, the anode has sufficient durability for production of polysulfide. Nickel is relatively inexpensive, and its elution potential and oxide generation Since the formation potential is higher than the formation potential of polydisulfide sulfate, it is a suitable electrode material for obtaining polysulfide ions by electrolytic oxidation.
- the anode surface in the present invention is preferably made of nickel, but a nickel alloy containing 50% by weight or more of nickel can also be used. In the nickel alloy, it is more preferable that the nickel content is 80% by weight or more.
- the anode since it is porous and has a three-dimensional network structure, it has a large surface area, and when used as an anode, the desired electrolytic reaction occurs on the entire surface of the electrode, suppressing the generation of by-products. it can. Furthermore, unlike the aggregate of fibers, the anode has a physically continuous network structure, exhibits sufficient electrical conductivity as the anode, and can reduce the IR drop at the anode, thereby increasing the cell voltage. Can be lowered. In addition, since the anode has good electric conductivity, the porosity of the anode can be increased, and the pressure loss can be reduced.
- the anode surface area per unit volume of the anode compartment it is necessary that 5 0 0 ⁇ 2 0 0 0 O m 2 / m 3.
- the volume of the anode chamber is the volume of a portion defined by the effective current-carrying surface of the diaphragm and the current collector plate of the anode. If the surface area of the anode is smaller than 50 O m 2 / m 3 , the current density on the anode surface will increase, and not only will by-products such as thiosulfate ions be easily generated, but also the nickel will cause anode dissolution.
- the surface area of the anode is set to be larger than 2000 Om 2 m 3 because a problem in electrolysis operation such as a large pressure loss of the liquid may occur. More preferably, the surface area of the anode per unit volume of the anode chamber is in the range of 1000 to 1000 m 2 / m 3.
- the surface area of the anode is preferably 2 to 10 Om2 / m2 per unit area of the diaphragm separating the anode chamber and the force sword chamber.
- the anode must have at least nickel or nickel alloy on the surface, and the entire anode may be nickel or nickel alloy.
- the anode has a physically continuous three-dimensional network structure, forming a porous structure.
- the network structure is physically continuous, and may be continuous by welding or the like. Specifically, for example, Porous nickel obtained by plating nickel on the skeleton of a foamed polymer material and then baking off the polymer material inside can be given.
- the average pore size of the anode network is preferably 0.1 to 5 mm. If the average pore size of the mesh is larger than 5 mm, the anode surface area cannot be increased, the current density on the surface of the node increases, and not only is it easier to generate by-products such as thiosulfate ions, but also Nickel is likely to cause anode dissolution, which is not desirable. If the average pore diameter of the mesh is smaller than 0.1 mm, there is a possibility that a problem in the electrolytic operation such as a large pressure loss of the liquid may occur, which is not preferable. More preferably, the average pore size of the anode network is 0.2 to 2 mm.
- the diameter of the wire constituting the mesh is preferably 0.01 to 2 mm: the diameter of the wire is reduced to 0.01 mm. Less than this is undesirable because it is extremely difficult to manufacture, costly, and difficult to handle. If the diameter of the wire is more than 2 mm, a large surface area of the anode cannot be obtained, the current density on the anode surface increases, and by-products such as thiosulfate ions are easily generated, which is not preferable. . It is particularly preferable that the diameter of the linear material constituting the mesh is 0.02 to 1 mm.
- the anode may be disposed in the anode chamber so as to be in contact with the diaphragm, or may be disposed so as to have some gap between the anode and the diaphragm. Since the liquid to be treated needs to flow through the anode, the anode preferably has a sufficient space. In any of these cases, the porosity of the anode is preferably 90 to 99%. If the porosity is less than 90%, the pressure loss at the anode increases, which is not preferable. If the porosity exceeds 99%, it is not preferable because it becomes difficult to increase the surface area of the anode. It is particularly preferable that the porosity is 90 to 98%.
- a current density at the diaphragm of 0.5 to 20 kAZm2. If the current density on the diaphragm surface is less than 0.S k A / m 2 , unnecessarily large electrolysis equipment will be required. If the amount exceeds the above, it is not preferable because not only the by-products such as thiosulfuric acid, sulfuric acid and oxygen are increased, but also nickel may cause anodic dissolution. Current density at diaphragm surface is 2 ⁇ The case of 15 kA / m 2 is more preferable. In the present invention, since the anode having a large surface area is used for the area of the diaphragm, the operation can be performed in a range where the current density on the anode surface is small.
- the current density on the anode surface can be made small. Assuming that the current density on the surface of each part of the anode is uniform, when the current density on the anode surface is calculated from the surface area of the anode, the value is preferably 5 to 300 Am2. Masure, A more preferred range is from 10 to 150 A / m 2. When the current density on the anode surface is less than 5 AZm 2 , unnecessarily large electrolytic equipment is required, which is not preferable.
- the anode is a physically continuous network structure, and has a good electrical conductivity. Can increase the porosity. Therefore, the pressure loss of the anode can be reduced.
- the anolyte in the anode chamber is not agitated, and in some cases, deposits tend to accumulate on the membrane facing the anode chamber, and the cell voltage tends to increase over time.
- the pressure loss of the anode can be kept small even when the flow rate of the anolyte is set to a large value, the advantage is that the anolyte near the surface of the diaphragm is agitated and deposits are less likely to accumulate.
- the average superficial velocity in the anode room is preferably 1 to 30 cm / sec.
- the flow rate of the force sword liquid is not limited, but is determined by the magnitude of the buoyancy of the generated gas.
- a more preferred range for the average superficial velocity in the anode compartment is 1 to 15 cm / sec, and a particularly preferred range is 2 to 10 cm / sec.
- a current is supplied to the anode through the anode current collector.
- a material of the current collector a material having excellent alkali resistance is preferable.
- nickel, titanium, carbon, gold, platinum, stainless steel, and the like can be used.
- the surface of the current collector may be planar: It may simply supply current through mechanical contact with the anode, but is preferably physically bonded by welding or the like:
- the cathode material is preferably an alkali resistant material, and nickel, Raney nickel, nickel sulfide, steel, stainless steel copper and the like can be used.
- the force sword one having a flat plate or mesh shape, or a plurality of the force swords are used in a multilayer structure.
- a three-dimensional electrode combining linear electrodes can also be used.
- As the electrolytic cell a two-chamber electrolytic cell consisting of one anode chamber and one power sword chamber is used. Electrolyzers combining three or more rooms are also used. Multiple cells can be arranged in a monopolar or bipolar configuration.
- a cation exchange membrane as the membrane separating the anode chamber and the power source chamber.
- the cation exchange membrane directs cations from the anode compartment to the force sword compartment, preventing the transfer of sulfide and polysulfide ions.
- a polymer membrane in which a cation exchange group such as a sulfonic acid group or a carboxylic acid group is introduced into a hydrocarbon-based or fluororesin-based polymer is preferable.
- the temperature of the c ⁇ Roh one de chamber may be used such as Anion exchange membrane is preferably in a range of 70 ⁇ 1 1 0 ° C. If the temperature of the anode chamber is lower than 70 ° C., it is not preferable because not only the cell voltage becomes high, but also nickel anodic dissolution and by-products may be easily generated. The upper temperature limit is practically limited by the material of the electrolytic cell or diaphragm.
- the anode potential, S 2 2 ⁇ as an oxidation product of sulfide ions, S 3 2 -, S 4 2 -, S 5 2 - polysulfide ions such as (S x 2 -) is generated, Chio sulfate ions 3 anode potential is preferably maintained so as but not-product, it is preferable to drive so as to be in the range one 0. 75 tens 0. 25 V: If the anode potential is lower than one 0.1 75 V is However, it is not preferable because the formation of polysulfide ions does not substantially occur.
- the electrode potential is HgZHg 2 C 1 in a 25 C saturated KC 1 solution.
- the anode used in the present invention is a three-dimensional electrode, the anode potential can be accurately determined. It is not easy to measure. Therefore, industrially, it is preferable to control the production conditions by regulating the cell voltage or the current density on the diaphragm, rather than controlling the production conditions by regulating the potential.
- the electrolysis method is preferably a constant current electrolysis, but it is also possible to change the current density.
- the solution containing sulfide ions introduced into the anode compartment is subjected to one-pass treatment or circulation treatment.
- the counter cation of sulfide ion is preferably an alkali metal ion.
- the alkali metal ion a sodium ion or a lithium ion is preferable.
- the method of the present invention is' particularly suitable for treating white liquor or green liquor in a pulp production process to obtain a polysulfide cooking liquor.
- a pulp production process to obtain a polysulfide cooking liquor.
- composition of white liquor which is currently used for kraft pulp digestion, usually contains 2 to 6 mo1 ZL as alkali metal ions, of which 90% or more is sodium ion. Yes, the rest is almost potassium ions.
- Anions are mainly composed of hydroxide ion, sulfide ion and carbonate ion, and also include sulfate ion, thiosulfate ion, chloride ion and sulfite ion. It also contains trace components such as calcium, silicon, aluminum, phosphorus, magnesium, copper, manganese, and iron.
- the main components of the white liquor are sodium sulfide and sodium hydroxide, whereas sodium sulfide and sodium carbonate are the main components.
- Other anions and trace components in green liquor are the same as in white liquor.
- the PS—S concentration in the solution obtained by electrolysis is preferably 5 to 15 g- / L. If the concentration of PS-S is less than 5 gZL, the effect of increasing the pulp yield during cooking may not be sufficiently obtained. When the concentration of PS—S is higher than 15 g / L, the valve yield does not increase because the Na 2 S state content decreases.
- the conversion rate (reaction rate) of sulfide ions to PS—S is preferably 15% or more and 75% or less, more preferably 72% or less.
- the reaction in the power sword chamber it is preferable to use a reaction in which hydrogen gas is generated from power water that can be selected in various ways.
- the resulting hydroxide ions and the alkali metal ions traveling from the anode compartment form alkali hydroxide:
- the solution introduced into the cathode compartment consists essentially of water and alkali metal hydroxide.
- a solution comprising water and sodium or sodium hydroxide is particularly preferred.
- the concentration of the metal hydroxide is not limited, but is, for example, 1 to 15 mO 1 / L, and preferably 2 to 5 mO 1 / L.
- the generated hydrogen gas can be used as fuel or as a raw material for hydrogen peroxide.
- the resulting alkali hydroxide can be used for pulp bleaching as well as pulp digestion, especially since it has few impurities.
- Example 1 Nickel plate for the anode current collector, nickel foam for the anode (Cermet, trade name, 10 OmmX 2 OmmX 4 mm, manufactured by Sumitomo Electric), mesh-like nickel electrode for power source, and fluorine resin cation exchange for diaphragm Assembling a two-chamber electrolytic cell using a membrane (made by Asahi Glass Co., Ltd., trade name: Flemion) 3.
- the anode chamber is 10 Omm high, 2 Omm wide and 4 mm thick, and the power sword chamber is high. It was 10 Omm wide, 2 Omm wide and 5 mm thick, and the effective area of the diaphragm was 20 cm2.
- the nickel foam used as the anode was bonded to the nickel plate of the anode current collector by electric welding.
- the electrolytic cell was assembled by pressing the diaphragm from the force source chamber side with a cathode and pressing it toward the anode side.
- the physical properties and electrolysis conditions of the anode are as follows.
- Anode thickness 4mm
- Anode thickness 4mm
- Electrolysis temperature 85 ° C
- Current density across diaphragm 6 kA / m 2
- model white liquor (N aa S: 1 6 g / L in Iou terms of atom, N a OH: 90 g / L, N a 2 CO 3: 34 g / L) was 1 L preparation, the anode chamber 3N: 2 L NaOH aqueous solution is used as a three- sword solution circulated at a flow rate of 144 mLZ (superficial velocity: 3 cmZ seconds) while extracting from the lower side and extracting to the upper side. It was circulated at a flow rate of 8 OmLZ while being introduced from the lower side of the chamber and withdrawn upward.
- a heat exchanger was provided on both the anode side and the power source side so that the anode liquid and the power source liquid were heated and introduced into the cell:
- a constant current electrolysis is performed at a current of 12 A (current density at the diaphragm: 6 kA / m 2 ) to synthesize a polysulfide digest, and at a predetermined time, the cell voltage is measured and the circulating fluid is sampled.
- the PS-S, Na2S state, and thiosulfate ions in the solution were analyzed and quantified. The analysis was performed based on the method described in JP-A-7-92148.
- the time courses of the quantitative values of the concentrations of various sulfur compounds and the measured values of the cell voltage were as follows.
- the composition of the polysulfide cooking liquor was 3.1 g / L for PS-S, 12.2 g / L for Na2S, and increased thiosulfate.
- the average value of X of the polysulfide ion (S x 2- ) was 2.9, during which the current efficiency was 94% and the selectivity was 97%.
- Example 2 Using the same model white liquor as in Example 1, changing the anode surface area, the average mesh pore size of the anode, the porosity of the anode chamber, the anolyte superficial velocity, the current density in the diaphragm, the reaction temperature, etc.
- the constant current electrolysis was performed in the same manner as described above.
- the following are examples of (1) change in anode surface area, (2) change in superficial velocity of anolyte, (3) change in current density, and (4) change in temperature (reaction temperature) in the electrolytic cell, based on each example. This is the result of considering from each viewpoint of change. It should be noted that the examples used in the consideration of (4) are not shown.
- Nickel was eluted when the average value of X of the polysulfide ion (S x 2- ) became 3.6 or when the electrolysis reaction changed from the PS-S formation reaction to the thiosulfate formation reaction. .
- Nickel was eluted after the electrolysis reaction was changed to thiosulfate ion generation reaction, or nickel was not eluted.
- the “initial cell voltage” shown in Table 1 indicates a constant and stable voltage value after the start of electrolysis. Taking Example 1 as an example, the cell voltage for about one hour from the start of electrolysis is constant and stable at 1.0 to 1.1 V, and then gradually rises. Points to a value.
- Example 4 Constant current electrolysis was performed in the same manner as in Example 1 except that the anode surface area per anode chamber was changed from 7000 m 2 / m 3 to 625 m 2 m 3 among the conditions of Example 1.
- Table 1 shows the conditions and results.
- the anode surface area was the same as that of Example 1, and the anode liquid superficial velocity was 5 cmZ seconds.
- Example 5 the anode liquid superficial velocity was 4 cm / sec.
- the porosity of each anode compartment was 95%.
- the unit of the anode pressure loss in Table 1 is “kgf / cm 2 ZmJ.
- Example 7 the larger the anode surface area, the lower the initial cell voltage and the longer the time required for nickel to elute.
- the pressure loss was relatively large because the average pore diameter of the mesh was small. It can be seen that even when the anolyte superficial velocity is 4 cmZs as in Example 5, the above tendency is not affected.
- nickel was eluted before PS—S became 8 g / L, but the anode pressure loss was as low as 0.05 kgf / cm 2 Zm and the initial cell voltage was 1.34 V.
- Example 2 and Example 12 and Example 11 and Example 13 are the cases where the current density was changed under the same other conditions.
- Example 2 current density 6 kAZm 2
- Example 1 2 current density 8 kAZm 2
- nickel was eluted somewhat earlier, but no nickel was eluted until the electrolysis reaction shifted from the PS-S generation reaction to the thiosulfate ion generation reaction. Yes (Evaluation 1) Table 3
- Example 14 Under the same conditions as in Example 2 except for the temperature in the electrolysis cell, the temperature (reaction temperature) in the electrolysis cell was set to 70 e. C (Example 14), 80 ° C. (Example 15), and 90 ° C. (Example 16), and constant current electrolysis was performed.
- the anode pressure loss was 0.26 kgfc m2 / m and the initial cell voltage was 1.3 V, 1.2 V and 1. IV, respectively, all showing good results.
- the nickel dissolution evaluation was ⁇ in Example 14 and ⁇ in Examples 15 and 16.
- Example 7 As described above, Examples 2 to 16 have been described. However, in all cases, except for Example 7, the current efficiency is as high as about 95% and the PS-S concentration is about 11 gZL, as in Example 1. High concentration polysulfide cooking liquor could be obtained. Moreover, the pressure loss was small, and the elution of nickel was suppressed. As for the polysulfide ion (S x 2- ), when the average value of X is about 3.5 to 4, the polysulfide ion decreases while maintaining the average value, and the formation reaction of thiosulfate proceeds. did.
- the anode chamber (thickness: 4 mm) of the electrolytic cell used in Example 1 was filled with 6 mm-thick carbon felt (thickness of the filled carbon felt: 4 mm).
- the physical properties of the anode in the filled state are as follows.
- Carbon fiber diameter 12 ⁇ m
- Example 2 Using the same model white liquor as in Example 1, except that the current was circulated at 12 A (6 kA / m2) and the anolyte flow rate was 96 mL / min (superficial velocity: 2 cm / sec) Constant current electrolysis was performed under the same conditions as in Example 1. As a result, a polysulfide cooking liquor with a PS / S concentration of about 11 g / L was obtained with a current efficiency of around 90%. After that, when the average value of X becomes about 3.5 to 4 for polysulfide ions (S x 2- ), the polysulfide ions decrease while maintaining the average value of X, and the thiosulfate ion formation reaction occurs. The initial cell voltage was about 1.3 V and further increased before the formation of thiosulfate ions. The pressure loss at the node was as large as 0.6 kgf / cm 2 / m . Industrial applicability
- the by-product of a thiosulfate ion is extremely small, and the cooking liquor containing a high density
- Pulp yield can be effectively increased by using cooking liquor for cooking.
- the anode is a physically continuous network structure, and the cell voltage can be lowered, so that the operating cost can be kept low.
- the anode used in the present invention has good electrical conductivity, it is possible to increase the porosity of the anode and reduce the pressure loss. Also, clogging of the electrode with the suspended solids can be suppressed.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Inorganic Chemistry (AREA)
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
- Electrodes For Compound Or Non-Metal Manufacture (AREA)
- Polymers With Sulfur, Phosphorus Or Metals In The Main Chain (AREA)
- Paper (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Addition Polymer Or Copolymer, Post-Treatments, Or Chemical Modifications (AREA)
- Electrolytic Production Of Metals (AREA)
Description
Claims
Priority Applications (7)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA002297106A CA2297106C (en) | 1998-05-29 | 1999-05-27 | Method for producing polysulfides by electrolytic oxidation |
NZ502198A NZ502198A (en) | 1998-05-29 | 1999-05-27 | Method for producing polysulfide by electrolytic oxidation |
US09/463,581 US6264819B1 (en) | 1998-05-29 | 1999-05-27 | Method for producing polysulfide by electrolytic oxidation |
AT99922510T ATE480497T1 (de) | 1998-05-29 | 1999-05-27 | Verfahren zur herstellung von polysulfiden durch elektrolytische oxidation |
DE69942736T DE69942736D1 (de) | 1998-05-29 | 1999-05-27 | Verfahren zur herstellung von polysulfiden durch elektrolytische oxidation |
EP99922510A EP1018486B1 (en) | 1998-05-29 | 1999-05-27 | Method for producing polysulfide by electrolytic oxidation |
NO20000455A NO330931B1 (no) | 1998-05-29 | 2000-01-28 | Fremgangsmate for fremstilling av polysulfid ved elektrolytisk oksydasjon |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP10/166374 | 1998-05-29 | ||
JP16637498A JP4187826B2 (ja) | 1998-05-29 | 1998-05-29 | 電解酸化による多硫化物の製造方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1999062818A1 true WO1999062818A1 (fr) | 1999-12-09 |
Family
ID=15830235
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP1999/002786 WO1999062818A1 (fr) | 1998-05-29 | 1999-05-27 | Procede de production de polysulfure par oxydation catalytique |
Country Status (12)
Country | Link |
---|---|
US (1) | US6264819B1 (ja) |
EP (1) | EP1018486B1 (ja) |
JP (1) | JP4187826B2 (ja) |
CN (1) | CN1196647C (ja) |
AT (1) | ATE480497T1 (ja) |
CA (1) | CA2297106C (ja) |
DE (1) | DE69942736D1 (ja) |
ID (1) | ID24214A (ja) |
NO (1) | NO330931B1 (ja) |
NZ (1) | NZ502198A (ja) |
RU (1) | RU2220096C2 (ja) |
WO (1) | WO1999062818A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2001018278A1 (fr) * | 1999-09-06 | 2001-03-15 | Kawasaki Kasei Chemicals Ltd. | Procede de production de polysulfure |
EP1178009A1 (en) * | 1999-02-26 | 2002-02-06 | Asahi Glass Company Ltd. | Method for producing polysulfide by use of electrolytic oxidation |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP4230612B2 (ja) | 1999-05-28 | 2009-02-25 | 日本製紙株式会社 | クラフト法パルプ製造プロセスにおける薬品回収方法 |
WO2000077295A1 (en) * | 1999-06-15 | 2000-12-21 | Kawasaki Kasei Chemicals Ltd. | Digestion method for pulp |
US7534413B2 (en) * | 2004-10-29 | 2009-05-19 | Heritage Environment Services, Llc | Calcium-sodium polysulfide chemical reagent and production methods |
KR100564062B1 (ko) * | 2005-05-31 | 2006-03-24 | 순천대학교 산학협력단 | 유기폐액의 복합매개산화 처리장치 |
US7378068B2 (en) * | 2005-06-01 | 2008-05-27 | Conocophillips Company | Electrochemical process for decomposition of hydrogen sulfide and production of sulfur |
JP4975402B2 (ja) * | 2006-09-06 | 2012-07-11 | クロリンエンジニアズ株式会社 | 電解方法 |
EP1767671B1 (en) | 2005-09-26 | 2012-05-02 | CHLORINE ENGINEERS CORP., Ltd. | Three-dimensional electrode for electrolysis, ion exchange membrane electrolytic cell and method of electrolysis using the three-dimensional electrode |
US8916117B2 (en) * | 2012-08-07 | 2014-12-23 | Exxonmobil Research And Engineering Company | Corrosion control in acid gas removal equipment by the situ generation of polysulfide ions |
EP2905360B1 (en) | 2012-10-01 | 2019-02-06 | Nippon Paper Industries Co., Ltd | Continuous electrolysis method by means of electrolytic bath for polysulfide manufacturing |
FI128221B (fi) * | 2015-04-27 | 2019-12-31 | Metsae Fibre Oy | Menetelmä polysulfidilipeän valmistamiseen käytetyn katalyytin regeneroimiseksi |
KR101978415B1 (ko) * | 2017-03-03 | 2019-05-14 | 울산과학기술원 | 메조기공성 삼차원 니켈 전극, 및 이를 포함하는 고성능의 유연성 슈퍼캐패시터 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08284089A (ja) * | 1995-04-06 | 1996-10-29 | Eka Nobel Ab | 電気化学方法 |
JPH08512099A (ja) * | 1993-06-28 | 1996-12-17 | エカ ノーベル アクチェボラーグ | 硫化物を含有する白液の電解による多硫化物の製造 |
WO1997041295A1 (en) * | 1996-04-26 | 1997-11-06 | Asahi Glass Company Ltd. | Method for producing polysulfides by electrolytic oxidation |
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1998
- 1998-05-29 JP JP16637498A patent/JP4187826B2/ja not_active Expired - Lifetime
-
1999
- 1999-05-27 AT AT99922510T patent/ATE480497T1/de not_active IP Right Cessation
- 1999-05-27 ID IDW20000111A patent/ID24214A/id unknown
- 1999-05-27 NZ NZ502198A patent/NZ502198A/en not_active IP Right Cessation
- 1999-05-27 CN CNB998008206A patent/CN1196647C/zh not_active Expired - Lifetime
- 1999-05-27 RU RU2000104851/15A patent/RU2220096C2/ru active
- 1999-05-27 EP EP99922510A patent/EP1018486B1/en not_active Expired - Lifetime
- 1999-05-27 DE DE69942736T patent/DE69942736D1/de not_active Expired - Lifetime
- 1999-05-27 CA CA002297106A patent/CA2297106C/en not_active Expired - Lifetime
- 1999-05-27 US US09/463,581 patent/US6264819B1/en not_active Expired - Lifetime
- 1999-05-27 WO PCT/JP1999/002786 patent/WO1999062818A1/ja active Application Filing
-
2000
- 2000-01-28 NO NO20000455A patent/NO330931B1/no not_active IP Right Cessation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH08512099A (ja) * | 1993-06-28 | 1996-12-17 | エカ ノーベル アクチェボラーグ | 硫化物を含有する白液の電解による多硫化物の製造 |
JPH08284089A (ja) * | 1995-04-06 | 1996-10-29 | Eka Nobel Ab | 電気化学方法 |
WO1997041295A1 (en) * | 1996-04-26 | 1997-11-06 | Asahi Glass Company Ltd. | Method for producing polysulfides by electrolytic oxidation |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP1178009A1 (en) * | 1999-02-26 | 2002-02-06 | Asahi Glass Company Ltd. | Method for producing polysulfide by use of electrolytic oxidation |
EP1178009A4 (en) * | 1999-02-26 | 2004-10-06 | Asahi Glass Co Ltd | PROCESS FOR PRODUCING POLYSULFIDE BY ELECTROLYTIC OXIDATION |
WO2001018278A1 (fr) * | 1999-09-06 | 2001-03-15 | Kawasaki Kasei Chemicals Ltd. | Procede de production de polysulfure |
Also Published As
Publication number | Publication date |
---|---|
EP1018486A4 (en) | 2004-11-10 |
ATE480497T1 (de) | 2010-09-15 |
NO20000455D0 (no) | 2000-01-28 |
ID24214A (id) | 2000-07-13 |
EP1018486A1 (en) | 2000-07-12 |
CA2297106A1 (en) | 1999-12-09 |
NO20000455L (no) | 2000-03-10 |
NO330931B1 (no) | 2011-08-22 |
CN1196647C (zh) | 2005-04-13 |
JP4187826B2 (ja) | 2008-11-26 |
US6264819B1 (en) | 2001-07-24 |
CA2297106C (en) | 2009-09-15 |
NZ502198A (en) | 2001-10-26 |
EP1018486B1 (en) | 2010-09-08 |
CN1272094A (zh) | 2000-11-01 |
RU2220096C2 (ru) | 2003-12-27 |
JPH11343106A (ja) | 1999-12-14 |
DE69942736D1 (de) | 2010-10-21 |
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