CN1220969A - The production method of sodium persulfate - Google Patents
The production method of sodium persulfate Download PDFInfo
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- CN1220969A CN1220969A CN98126033A CN98126033A CN1220969A CN 1220969 A CN1220969 A CN 1220969A CN 98126033 A CN98126033 A CN 98126033A CN 98126033 A CN98126033 A CN 98126033A CN 1220969 A CN1220969 A CN 1220969A
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- C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
- C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
- C25B1/00—Electrolytic production of inorganic compounds or non-metals
- C25B1/01—Products
- C25B1/28—Per-compounds
- C25B1/29—Persulfates
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Abstract
本发明公开了一种过硫酸钠的生产方法,该方法包括:步骤(1):在阳极电解含有硫酸铵的溶液、和步骤(2);由最终在阳极产生的液体和氢氧化钠形成过硫酸钠、除去硫酸钠的步骤(如果需要)、步骤(3):晶化在步骤(2)中产生的反应液体(如果需要)。按照以上方法,在电解中能以较高的电流效率和较高的生产率高效地生产纯度很高而氮组分又几乎没有的过硫酸钠。The invention discloses a production method of sodium persulfate. The method comprises: step (1): electrolyzing a solution containing ammonium sulfate at the anode; Sodium sulfate, step of removing sodium sulfate (if necessary), step (3): crystallization of the reaction liquid produced in step (2) (if necessary). According to the above method, sodium persulfate having high purity and almost no nitrogen component can be efficiently produced in electrolysis with high current efficiency and high productivity.
Description
The present invention relates to the production method of Sodium Persulfate, now, Sodium Persulfate is widely used in the industrial circle as the treatment agent of the polymerization starter of polyvinyl chloride and polyacrylonitrile and printed circuit board (PCB).
As the ordinary method of producing Sodium Persulfate, people know a kind of production method of reacting by ammonium persulfate and sodium hydroxide in the aqueous solution, in aforesaid method, the first step must form the ammonium persulfate starting raw material by electrolysis process, and formed ammonium persulfate is concentrated and separate by vacuumizing crystallization, centrifuging etc., obtain the ammonium persulfate crystal subsequently.Simultaneously, contain crystalline solution (being commonly referred to " mother liquor ") with the liquid mixing that produces at negative electrode and as the anodic starting raw material.
In next step, the ammonium persulfate that so obtains is dissolved again, and it is moved on in the step of reacting with sodium hydroxide.In above-mentioned reactions steps, form the solution contain Sodium Persulfate, it is concentrated and separate by vacuumizing crystallization, centrifuging etc. subsequently, then obtain the Sodium Persulfate crystal.As mentioned above, react the method for producing Sodium Persulfate by ammonium persulfate and sodium hydroxide and must need quite long and considerable production stage, so just reduced the productivity based on the Sodium Persulfate object of ammonium persulfate, therefore, it lacks advantage economically.
In this case, people have carried out some trials in the hope of need not to produce Sodium Persulfate by ammonium persulfate by direct electrolysis.For example, a kind of method by sodium pyrosulfate is produced Sodium Persulfate as starting raw material has been described in Japanese patent application (special permission is open) 56395/1975 (clear-50), yet because the efficient of electric current is extremely low in electrolysis, this method does not gear to actual circumstances.
In addition, Japanese patent laid-open publication gazette 31190/1980 (clear-55) has been described a kind of anode and has been used neutral starting raw material to carry out the method that Sodium Persulfate is produced in electrolysis under the condition that ammonium ion exists, yet because current efficiency is low to moderate about 70-80% in electrolysis, this method of it is said also is uneconomic.In addition, the shortcoming that aforesaid method had is: the ammonium ion that is contained in the crystal object has increased nitrogen components contents in the Sodium Persulfate object, and then make this method must carry out careful and wholwe-hearted cleaning step to meet conventional specification of quality as the finished product that promptly purity is at least 99% and nitrogenous component mostly is 0.1% most to guarantee Sodium Persulfate.Though done many effort that improve production method so far, real situation is a kind of method of producing the economy of Sodium Persulfate that also do not work out so far.
Purpose of the present invention is exactly the existing problem of ordinary method that solves above-mentioned production Sodium Persulfate.And provide a kind of simultaneously and have the method that the mode of advantage is produced Sodium Persulfate with industrialization.
In the case, in order to overcome above-mentioned shortcoming, the result who attentively researches and develops as the applicant, the applicant has found a kind of method of producing Sodium Persulfate, this method may further comprise the steps, thereby thereby that is: anode forms ammonium persulfate in electrolysis under the condition that sodium ion exists, sodium hydroxide is directly joined form Sodium Persulfate (reactions steps) in the liquid that produces at the anode place, concentrate and the Sodium Persulfate of resulting separation.Now also find to obtain this starting raw material the astonishing current efficiency that is higher than not the ammonium persulfate that coexists with sodium ion of acquisition in the electrolysis of ammonium persulfate by using at anode with the starting raw material of sodium ion coexistence with by the crystallization mother liquor that mixes liquid that the negative electrode place forms and concentrate, forms behind the separating obtained Sodium Persulfate.Above-mentioned discovery makes the present invention be accomplished.
That is to say, the present invention relates to a kind of production method of Sodium Persulfate, this method comprises: step (1): the solution and the step (2) that contain ammonium persulfate at anode electrolysis: form Sodium Persulfate by the final liquid and the sodium hydroxide that produce at anode.
In following detailed description, will provide the inventive method, in electrolysis step, promptly in the step (1) of the inventive method, the solution that will contain sulfate of ammoniac is as the anode starting raw material, solution preferably contains sulfate of ammoniac and sodium ion, and particularly, solution comprises the sulfate of ammoniac of 15-35 weight %, the sodium sulfate of 5-20 weight % and the Sodium Persulfate of 5-20 weight %, more preferably, above-mentioned solution is higher than the aqueous solution form of sodium sulfate concentration for sulfate of ammoniac concentration.Preferably, the anodic starting raw material contains the polarization agent of some amount, and its typical example is thiocyanate-, prussiate, cyanate and fluorochemical.The anodic starting raw material not necessarily requires to be adjusted to neutrality, and it can contain free acid, and this can not influence current efficiency.It is that the aqueous sulfuric acid of sulfate of ammoniac of 0-35 weight % is as starting raw material that negative electrode contains concentration with 10-80 weight %.It is disadvantageous using the aqueous solution of concentration outside above-mentioned scope, because thus obtained current efficiency is lower.
That the used electrolyzer of the inventive method separates with the aluminum oxide barrier film and in industrial widely used barrier film pond, also but the pressure filter-type electrolyzer that separates with ion-exchange membrane.Anode is preferably made by platinum, also can use chemical-resistant material such as carbon dioxide process carbon electrode.Negative electrode is preferably made by lead or zirconium, also can use acid proof metal electrode such as stainless steel.The current density of anode surface is at least 40 peace/square decimeters.The electrolyzer temperature inside is 15-40 ℃.When temperature is lower than said scope, will produce the danger that from solution, is settled out salt.Salt solubility increases along with the raising of solution temperature, but wherein too high unreasonably temperature does not have benefit, because this moment, formed persulphate had the tendency of hydrolysis reaction.
The inventive method step (2) does not limit especially and is used to make the liquid of anode place generation and the reactor of aqueous sodium hydroxide solution reaction, as long as can use under reduced pressure, and it can be furnished with agitator.Join all positively charged ions that the quantity of the sodium hydroxide in the liquid that the anode place produces must make said liquid contain and change sodium ion into.Temperature of reaction is 15-60 ℃, is preferably 20-50 ℃.When temperature of reaction is lower than said scope, will produce as being settled out crystalline detrimentally affect such as ammonium persulfate, cause operation difficulty and reaction insufficient thus.On the contrary, when temperature of reaction is higher than said scope, will cause decomposition such as persulphate, and then cause the productivity of object Sodium Persulfate to reduce.
Reaction pressure is the 10-400 mmhg, preferred 20-100 mmhg.By under reduced pressure reacting, the removing of the ammonia that can promote in reaction to be produced.When reaction pressure is lower than said scope, there is not benefit economically, because vacuum electric load is bigger.On the contrary, when reaction pressure was higher than said scope, the solubleness of the ammonia that is produced in solution increased.The reaction times preferably approximately is 30-60 minute.Reaction times does not have benefit economically than said scope length.The ammonia that is produced is absorbed in the vitriolic aqueous solution and by the starting raw material of electrolysis step as negative electrode and recycles.
If desired, can remove the operation of sodium sulfate, its objective is and after reaction is finished, remove the sodium sulfate that comes from the coexistence in the reaction liquid.Above-mentioned operation of removing sodium sulfate is cooling and crystallization liquid and the operation that contains the sodium sulfate crystal of ten crystal water by precipitate and separate.By using above-mentioned operation of removing sodium sulfate in practice, can improve the purity of the Sodium Persulfate that in the next step (3) of concentrated and crystallization, obtains.Saidly manipulate a jar type crystallization device of being furnished with refrigerating unit, its typical example is widely used jar of type cooling crystallization device in the present industrial circle.The temperature of cooling crystallization is 5-30 ℃, preferred 15-25 ℃.The temperature of cooling crystallization is disadvantageous when being lower than said scope, because eutectic will take place Sodium Persulfate, and also is disadvantageous when temperature is higher than said scope, because the precipitation of sodium sulfate is insufficient, and then has reduced the purity of object Sodium Persulfate.Thereby introduce and carry out solid-liquid in solid-liquid separator such as the centrifugal filter and separate removing the slip that forms behind the sedimentary sodium sulfate.Thereby the sodium sulfate of a part of crystalline form is dissolved again as the anodic starting raw material, and recycle by reactive system.With the mother liquor after separating be incorporated into next concentrate and crystallization steps in.
After the step of removing sodium sulfate is finished,, can use a kind of being extensive use of and normally used jar of type crystallization device as liquid being concentrated and the crystallization device of crystallization steps (step (3)).The temperature of crystallization is 15-60 ℃, is preferably 20-50 ℃.Be disadvantageous economically when crystallization temperature is lower than said scope, because the temperature of condenser portion is low excessively, and also is disadvantageous when temperature is higher than said scope, because the object Sodium Persulfate decomposes, reduced its productivity thus, this is as the situation of above-mentioned reaction.For crystallization pressure, the pressure in the time of can adopting water in the said temperature scope, to seethe with excitement.By using solid-liquid separator such as centrifugal filter, the slip that contains Sodium Persulfate after the crystallization is separated into crystal and mother liquor.The crystal that drying so obtains in the powder for drying device also is made into finished product.On the other hand, with the liquid that produces in the sodium hydroxide and at catholyte, and subsequently with separate after mother liquor mix.Resulting mixing liquid has dissolved a part by the sodium sulfate of the step discharge of removing sodium sulfate and the polarization agent of some amount, and as the anodic starting raw material.To mixing used in this step and again dissolving vessel have no particular limits, as long as be furnished with agitator, but they can be selected from widely used stirred pot in industrial circle.
According to the inventive method, can produce the high-purity Sodium Persulfate that does not almost have the nitrogen component, current efficiency is higher in electrolysis simultaneously.
Below, describe the present invention in more detail with reference to comparative example and work embodiment, yet these embodiment are not limited to the present invention.Current efficiency general formula in comparative example and work embodiment: the expression of [the persulphate ion (mole) * 2 of formation]/[magnitude of current (F)] * 100%, that is exactly the ratio of formed Sodium Persulfate ion and unitary current quantity.The electromotive force of electrolyzer is the potential difference between the electrode.All concentration represent with weight, except as otherwise noted.
Embodiment 1
Step (1)-(3) that comprise electrolysis, react and remove sodium sulfate by the front form Sodium Persulfate.Electrolyzer used herein is to make with transparent polyvinyl chloride, and is made up of anolyte compartment that separates with diaphragm material and cathode compartment, and diaphragm material is by making with sealing agent fixed porous neutral alumina, and sealing agent is made by silicon rubber.Each chamber is furnished with surge tank, and it also plays cooling tank.With the pipe pump liquid starting raw material is fed in the electrode vessel by surge tank, get back in the surge chamber again through outlet by the liquid in the overflow electrode vessel.Make cooling water circulation by the cast water cooler of making by glass that is inserted in the surge tank.Anode used herein by two wide be that 1.8 centimetres, length are that the platinum foil of 16 centimetres (area is 28.8 square centimeters) is formed, negative electrode used herein is made by a lead flake.Anode and the negative electrode installed approximately respectively are 0.5 centimetre apart from barrier film.Provide direct current by variable rectifier to electrode.Under the current value of 44 peaces, electrolysis was carried out 4 hours by use chemical constitution starting raw material as described below.The quantity of the anode starting raw material of aqueous solution form is 2970.8 grams.
Project weight % quantity (gram)
Sodium Persulfate 11.0 326.4
Sodium sulfate 12.0 356.0
Ammonium sulfate 18.0 534.4
Sulfuric acid 0.03 2.8
Ammonium thiocyanate 0.03 0.89
The quantity of the negative electrode starting raw material of aqueous solution form is 1716.8 grams.
Project weight % quantity (gram)
Sulfuric acid 18.8 322.0
Ammonium sulfate 23.5 404.0
After the electrolysis, obtain 2886.3 grams and restrain the liquid that produces at negative electrode at the liquid and 1739.2 that anode produces.Chemical constitution by the resulting liquid of titrimetry.Provide analytical results and operational condition below.
Liquid in the anode generation
Project weight % quantity (gram)
Ammonium persulphate 22.7 654.0
Sodium Persulfate 11.3 326.4
Sodium sulfate 7.5 216.4
Ammonium sulfate 0.9 25.4
Sulfuric acid 1.1 31.2
Liquid in the negative electrode generation
Project weight % quantity (gram)
Sodium sulfate 7.8 140.0
Ammonium sulfate 29.8 534.4
Sulfuric acid 0.5 9.6
Operational condition
Current efficiency 87.3%
7.3 volts of medial temperatures of electrolyzer electromotive force: 29 ℃ of medial temperatures: 30 ℃ at the liquid of negative electrode at anodic liquid
The final liquid that anode is produced moves on in the reactor of being furnished with agitator, liquid and 562.8 gram concentration are that 48% aqueous sodium hydroxide solution mixes there, it is essential that this quantity changes sodium ion into for all positively charged ions that said liquid is contained, and simultaneously discharges ammonia fully under the vacuum tightness of 30 mmhg and room temperature condition.Thereby the reaction liquid after cooling and crystallization discharge ammonia fully under 18 ℃ forms the sodium sulfate that 445.2 grams contain ten crystal water by precipitate and separate.Filtration contains the sodium sulfate of ten crystal water.Isolating filtered liquid like this moved into be furnished with in jar type crystallization device of agitator and condenser, thereby and under the condition of the vacuum tightness of 20 mmhg and 30 ℃, vacuumize crystallization and precipitate Sodium Persulfate.
Thereby will in the Sodium Persulfate slip introducing centrifugal filter that so obtains slip be separated into crystal and mother liquor.Thereby complete drying isolating crystal like this obtains, and 676.9 gram purity are 99.8%, nitrogen content is 0.001% Sodium Persulfate crystal.So the productivity of the Sodium Persulfate that obtains is 99% (is benchmark with the contained ammonium persulphate of liquid in the anode generation).
Mother liquor in mixing again dissolving vessel after introducing 898.0 grams and the crystal separation; 1793.2 the liquid that gram obtains in aforementioned electrolysis in the negative electrode generation; A part aforementioned remove the sodium sulfate that obtains in the step of sodium sulfate (309.6 gram) thus obtain uniform solution.The polarization agent that adds some amount in resulting homogeneous solution makes 3009.7 gram anode starting raw materials.Thereby the ammonia that reactions steps produces reclaims with the vitriolic aqueous solution and makes 1716.8 gram negative electrode starting raw materials.Anode and negative electrode starting raw material with so preparation carries out electrolysis with aforementioned electrolyzer under condition as hereinbefore subsequently.The result is as follows:
Current efficiency: 87.4%
Electrolyzer electromotive force: 7.2 volts
Medial temperature at anodic liquid: 30 ℃
Medial temperature at the liquid of negative electrode: 29 ℃
The comparative example 1
According to the described method of Japanese patent laid-open publication gazette 31190/1980 (clear-55), thus with testing installation as testing with the used identical electrolyzer of embodiment 1 in case with the condition of ammonium ion coexistence under directly electrolysis form Sodium Persulfate.The starting raw material as described below with chemical constitution carried out electrolysis 2.5 hours under the current value condition of 44 peaces:
The anode starting raw material quantity of aqueous solution form is 3450 grams.
Project weight % quantity (gram)
Sodium Persulfate 20.5 707.3
Sodium sulfate 12.1 417.5
Ammonium sulfate 9.81 338.4
Sulfuric acid 00
Ammonium thiocyanate 0.03 1.04
The quantity of the negative electrode starting raw material of aqueous solution form is 950 grams.
Project weight % quantity (gram)
Sulfuric acid 29.7 282.2
After the electrolysis, obtain 3300 grams and restrain the liquid that produces at negative electrode at the liquid and 1000 that anode produces.Chemical constitution by titrimetry gained liquid.Provide analytical results and operational condition below:
Liquid in the anode generation
Project weight % quantity (gram)
Sodium Persulfate 34.5 1138.0
Sodium sulfate 0.5 16.5
Ammonium sulfate 8.1 267.3
Sulfuric acid 1.1 36.3
Liquid in the negative electrode generation
Project weight % quantity (gram)
Sodium sulfate 12.6 126.0
Ammonium sulfate 6.78 67.8
Sulfuric acid 6.2 62.0
Operational condition
Current efficiency: 80.3%
Electrolyzer electromotive force: 7.9 volts
Medial temperature at anodic liquid: 33 ℃
Medial temperature at the liquid of negative electrode: 38 ℃
Use and embodiment 1 used identical reactor, the liquid that anode is produced and concentration are that 48% aqueous sodium hydroxide solution mixes, and the quantity of aqueous sodium hydroxide solution must neutralize the sulfuric acid that liquid contained in the anode generation by the electrolysis acquisition.Thereby final neutral liquid vacuumizes crystallization and is settled out Sodium Persulfate under the vacuum tightness of 30 ℃ and 20 mmhg.
Thereby will in the Sodium Persulfate slip introducing centrifugal filter that so obtains slip be separated into crystal and mother liquor.Thereby the crystal that complete drying so obtains forms, and 450 gram purity are 98.0%, nitrogen content is 0.2% Sodium Persulfate crystal.
The result of direct electrolysis method shows that the crystalline purity that current efficiency is 80% approximately only, crystallization obtained is lower.And, in order to obtain purity and embodiment 1 the same high crystal, need to use saturated Sodium Persulfate solution to carry out careful and wholwe-hearted cleaning, make this saturated solution show slightly alkalescence with sodium hydroxide.In addition, the final production rate of electrolytic object Sodium Persulfate is 95%, cleans productivity is reduced.
The comparative example 2
Thereby, the reaction of ammonium persulphate and sodium hydroxide forms Sodium Persulfate by being tested with ordinary method.Thereby this method with not with the condition of sodium ion coexistence under the electrolysis method that forms Sodium Persulfate be equal to.Use chemical constitution starting raw material as described below under the current value condition of 44 peaces, to carry out electrolysis 3 hours:
The anode starting raw material quantity of aqueous solution form is 2300 grams.
Project weight % quantity (gram)
Ammonium persulphate 7.2 165.6
Ammonium sulfate 33.6 772.8
Sulfuric acid 5.8 133.4
Ammonium thiocyanate 0.03 0.69
The negative electrode starting raw material quantity of aqueous solution form is 1950 grams.
Project weight % quantity (gram)
Sulfuric acid 14.4 280.8
After the electrolysis, obtain 2600 grams and restrain the liquid that produces at negative electrode at the liquid and 1600 that anode produces.Chemical constitution by titrimetry gained liquid.Provide analytical results and operational condition below:
Liquid in the anode generation
Project weight % quantity (gram)
Ammonium persulphate 24.3 631.8
Ammonium sulfate 10.8 280.8
Sulfuric acid 6.5 169.0
Liquid in the negative electrode generation
Project weight % quantity (gram)
Ammonium sulfate 8.4 134.4
Sulfuric acid 3.4 54.4
Operational condition
Current efficiency: 81.8%
Electrolyzer electromotive force: 7.8 volts
Medial temperature at anodic liquid: 32 ℃
Medial temperature at the liquid of negative electrode: 34 ℃
Thereby the liquid that produces at anode that makes acquisition like this under the vacuum degree condition of 30 ℃ and 20 mmhg vacuumizes crystallization and is settled out ammonium persulphate.Thereby will in the ammonium persulphate slip introducing centrifugal filter that so obtains slip be separated into crystal and mother liquor.Thereby resulting hydrate crystal dissolved again and be that 48% aqueous sodium hydroxide solution mixes and reacts with concentration.The Sodium Persulfate crystal separates from solution and reclaims, subsequently with its complete drying.As a result, obtain 445 gram purity and be 99.5%, nitrogen content is 0.001% Sodium Persulfate crystal, its productivity is 95%.In a word, its current efficiency is lower than about 6% (87.4-81.8) of the inventive method, and the productivity (is benchmark with the ammonium persulphate) of the object Sodium Persulfate that electrolysis forms is lower than about 4% (99-95) of the inventive method.
Claims (11)
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP355148/1997 | 1997-12-24 | ||
| JP355148/97 | 1997-12-24 | ||
| JP35514897A JP3778238B2 (en) | 1997-12-24 | 1997-12-24 | Method for producing sodium persulfate |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1220969A true CN1220969A (en) | 1999-06-30 |
| CN1116439C CN1116439C (en) | 2003-07-30 |
Family
ID=18442229
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN98126033A Expired - Fee Related CN1116439C (en) | 1997-12-24 | 1998-12-24 | Process for producing sodium persulfate |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP3778238B2 (en) |
| CN (1) | CN1116439C (en) |
| DE (1) | DE19858544B4 (en) |
| TW (1) | TW384318B (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102825023A (en) * | 2012-09-14 | 2012-12-19 | 武汉钢铁(集团)公司 | Continuous belt-driven surface adsorption crystal purification process |
| CN102877085A (en) * | 2012-09-24 | 2013-01-16 | 山东东岳高分子材料有限公司 | Method for preparing high-purity peroxysulphate based on electrolytic oxidation through ion-exchange membrane electrolyzer for chlor-alkali production |
| CN103432974A (en) * | 2013-09-14 | 2013-12-11 | 河北冀衡集团有限公司 | Deaminizing and dewatering technology and special device for sodium persulfate (salt) synthetic fluid |
| CN108149274A (en) * | 2017-11-16 | 2018-06-12 | 铜陵泰富特种材料有限公司 | The method of novel ammonium sulfate production sodium peroxydisulfate |
| CN108220995A (en) * | 2017-11-16 | 2018-06-29 | 铜陵泰富特种材料有限公司 | The method of novel ammonium sulfate electrolysis production ammonium persulfate |
| CN113174604A (en) * | 2021-04-13 | 2021-07-27 | 浙江工业大学 | Method for preparing sodium persulfate through direct electrooxidation |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20220251714A1 (en) | 2019-07-30 | 2022-08-11 | Mitsubishi Gas Chemical Company, Inc. | Composition, method for roughening stainless steel surface using same, roughened stainless steel, and method for producing said roughened stainless steel |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE2837118C2 (en) * | 1978-08-25 | 1982-05-19 | Dornier System Gmbh, 7990 Friedrichshafen | Porous oxide electrodes for high temperature electrochemical cells |
| JP3029712B2 (en) * | 1991-08-22 | 2000-04-04 | 株式会社東芝 | RF modulator circuit |
-
1997
- 1997-12-24 JP JP35514897A patent/JP3778238B2/en not_active Expired - Fee Related
-
1998
- 1998-12-18 DE DE19858544A patent/DE19858544B4/en not_active Expired - Fee Related
- 1998-12-19 TW TW087121262A patent/TW384318B/en not_active IP Right Cessation
- 1998-12-24 CN CN98126033A patent/CN1116439C/en not_active Expired - Fee Related
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102825023A (en) * | 2012-09-14 | 2012-12-19 | 武汉钢铁(集团)公司 | Continuous belt-driven surface adsorption crystal purification process |
| CN102877085A (en) * | 2012-09-24 | 2013-01-16 | 山东东岳高分子材料有限公司 | Method for preparing high-purity peroxysulphate based on electrolytic oxidation through ion-exchange membrane electrolyzer for chlor-alkali production |
| CN102877085B (en) * | 2012-09-24 | 2015-06-17 | 山东东岳高分子材料有限公司 | Method for preparing high-purity peroxysulphate based on electrolytic oxidation through ion-exchange membrane electrolyzer for chlor-alkali production |
| CN103432974A (en) * | 2013-09-14 | 2013-12-11 | 河北冀衡集团有限公司 | Deaminizing and dewatering technology and special device for sodium persulfate (salt) synthetic fluid |
| CN108149274A (en) * | 2017-11-16 | 2018-06-12 | 铜陵泰富特种材料有限公司 | The method of novel ammonium sulfate production sodium peroxydisulfate |
| CN108220995A (en) * | 2017-11-16 | 2018-06-29 | 铜陵泰富特种材料有限公司 | The method of novel ammonium sulfate electrolysis production ammonium persulfate |
| CN113174604A (en) * | 2021-04-13 | 2021-07-27 | 浙江工业大学 | Method for preparing sodium persulfate through direct electrooxidation |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1116439C (en) | 2003-07-30 |
| DE19858544B4 (en) | 2007-08-02 |
| JP3778238B2 (en) | 2006-05-24 |
| TW384318B (en) | 2000-03-11 |
| JPH11189888A (en) | 1999-07-13 |
| DE19858544A1 (en) | 1999-07-01 |
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