EP2649010A1 - Procédé de production d'oxyde de chrome(iii) - Google Patents

Procédé de production d'oxyde de chrome(iii)

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Publication number
EP2649010A1
EP2649010A1 EP11791295.6A EP11791295A EP2649010A1 EP 2649010 A1 EP2649010 A1 EP 2649010A1 EP 11791295 A EP11791295 A EP 11791295A EP 2649010 A1 EP2649010 A1 EP 2649010A1
Authority
EP
European Patent Office
Prior art keywords
sodium
chromium
oxide
hydrolysis
iii
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.)
Withdrawn
Application number
EP11791295.6A
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German (de)
English (en)
Inventor
Holger Friedrich
Matthias Boll
Rainer Ortmann
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lanxess Deutschland GmbH
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Lanxess Deutschland GmbH
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Priority claimed from EP11180086A external-priority patent/EP2565162A1/fr
Application filed by Lanxess Deutschland GmbH filed Critical Lanxess Deutschland GmbH
Priority to EP11791295.6A priority Critical patent/EP2649010A1/fr
Publication of EP2649010A1 publication Critical patent/EP2649010A1/fr
Withdrawn legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G37/00—Compounds of chromium
    • C01G37/02—Oxides or hydrates thereof
    • C01G37/033—Chromium trioxide; Chromic acid
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
    • C01G37/00—Compounds of chromium
    • C—CHEMISTRY; METALLURGY
    • C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
    • C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK  ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
    • C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
    • C09C1/34—Compounds of chromium
    • C09C1/346—Chromium oxides
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
    • C01P2006/00—Physical properties of inorganic compounds
    • C01P2006/80—Compositional purity

Definitions

  • the invention relates to a process for the preparation of chromium (III) oxide starting from sodium monochromate and gaseous ammonia, as well as the use of the produced chromium (III) oxide for various applications.
  • Chromium (III) oxide is a versatile product with a wide range of uses. Thus, it can be used as a pigment for coloring different application media, such as, for example, building materials, plastics, paints and varnishes, glasses or ceramics. For this application, the lowest possible content of water-soluble impurities is required.
  • chromium (III) oxide is also used in abrasives and high-temperature resistant materials.
  • chromium (III) oxide For the use of chromium (III) oxide in high-temperature-resistant materials, the lowest possible alkali metal content is desired in order to maximize the oxidation of Cr (ill) to alkali metal chromate promoted at high temperatures and in the presence of alkali metal ions suppress.
  • Another important industrial application for chromium (III) oxide is its use as starting material for the production of chromium metal and / or chromium-containing high-performance alloys.
  • chromium (II) oxides can be used here, which are characterized by a low sulfur content and a low carbon content.
  • the term "sulfur-poor chromium (III) oxide” is therefore often used as a synonym for "chromium (III) oxide for metallurgical purposes".
  • Chromium (II) oxide can be prepared in the prior art by various methods. Usually, it is produced at higher temperatures from hexavalent chromium compounds, whereby different degrees of purity can be achieved.
  • As starting compounds of the hexavalent chromium chromic acid, ammonium chromates or alkali chromates are used.
  • the reaction can be carried out with or without the addition of a reducing agent.
  • Reducing agents are organic or inorganic reducing agents such as sawdust, molasses, cellulose blues, acetylene, methane, sulfur and its compounds, phosphorus, carbon, hydrogen and the like.
  • Such methods are described in numerous patents. By way of example, only US Pat. No.
  • US 1,893,761 discloses the preparation of chromium (III) oxide by the reduction of alkali metal chromates with organic substances. When using carbon or organic compounds as reducing agents, the process can be conducted so that sodium carbonate is finally obtained as a by-product, as already mentioned in US Pat. No. 1,893,761. This may optionally be in the production process of Sodium dichromate can be recycled when the sodium dichromate is prepared via an oxidative alkaline digestion from chrome ore.
  • the chromium (III) oxide thus obtained contains a high proportion of carbon which renders it unsuitable for metallurgical use.
  • DE-A-20 30 510 describes a process for the continuous production of very pure, low-sulfur chromium (III) oxide, by reduction of alkali chromates with hydrogen at higher temperatures and a device suitable for this purpose.
  • the reaction temperature is between 1000-1800 ° C, advantageously between 1 100-1400 ° C, and the product obtained is separated from the exhaust gas by means of an alkaline dispersion.
  • DE-A-24 16 203 and US Pat. No. 4,052,225 describe processes in which hydrogen is also used for the reduction of alkali metal chromates.
  • the alkali metal chromate is reduced in fine distribution in a heated hydrogen-containing reaction zone at temperatures between 900 and 1600 ° C, wherein the reduction is also in the presence of a gas which binds the alkali metal ions in the reduction of the alkali metal chromate with salt formation and wherein the formed Chromium (Ili) oxide deposits in the form of an alkaline dispersion.
  • the salt-forming gases used are preferably chlorine or hydrogen chloride, which forms sodium chloride. However, since the melting point of sodium chloride is at 800 ° C, melting in the reactor is to be expected, which will form clumps and caking during prolonged campaigns.
  • the thermal decomposition of pure ammonium dichromate itself does not lead to any significant forced formation of a by-product, since in the ideal case it proceeds according to the reaction equation (H 4 ) 2 Cr 2 O 7 - * Cr 2 O 3 + N 2 + 4 H 2 O (1) and expires at a temperature of about 200 ° C.
  • the technical methods used today for the production of ammonium dichromate are based on alkali metal dichromates, usually sodium dichromate. The sodium dichromate is reacted with ammonium chloride or ammonium sulfate to give ammonium dichromate and sodium chloride or to ammonium dichromate and sodium sulfate.
  • Metallurgical chromium (IH) oxide was previously industrially produced by calcining in an oven a mixture of ammonium dichromate and sodium chloride obtained by in situ reaction of sodium dichromate and ammonium chloride in virtually stoichiometric equivalent amounts.
  • the calcination temperature should be above 700 ° C to ensure that the reaction mixture has a high chromium (hi) oxide content; at too high a
  • temperature increases the risk of slag formation in the oven, and the temperature is therefore generally kept below 850 ° C.
  • ammonium sulfate instead of ammonium chloride is often preferred, since the ammonium chloride, due to its low sublimation temperature, can be sublimated as NH 3 and HCl during the calcining and can thus pass into the exhaust air. For this reason, the use of ammonium chloride has no economic significance today.
  • the "disadvantage of the use of ammonium sulfate is, however, that is onsrea introduced in this way, sulfur in the product! Although a chromium (III) oxide is desired, with the lowest possible sulfur content.
  • alkali metal dichroate present due to the excess decomposes thermally to alkali chromate, chromium (II) oxide and oxygen.
  • alkali metal sulphate for example sodium sulphate
  • alkali metal chromate for example sodium chromate
  • the mother liquor then also contains the forced accumulation of alkali metal sulphate, which must be lavishly purified, since it is always contaminated with alkali chromate.
  • US Pat. No. 4,296,076 discloses a process in which, inter alia, sodium dichromate and ammonium choride or sodium dichromate and ammonium sulfate are used. In contrast to DE-A-26 35 086 essentially selects a stoichiometric ratio or preferably uses an excess of the ammonium compound.
  • a first reaction step the starting compounds are converted to ammonium dichromate and sodium chloride or ammonium dichromate and sodium sulfate. In the disclosed examples, this reaction step takes place at 400 to 800 ° C, followed by the aqueous work-up and then a second annealing process at a temperature above 1100 ° C.
  • chromic acid as a starting material for the production of chromium (III) oxide are usually reacted in a first step alkali chromates with sulfuric acid and / or hydrogen sulfate containing compounds to Alkalidichromaten (3) and then converted with further sulfuric acid in chromic acid (4 ).
  • Amnion iumchromat is prepared by reacting sodium chromate in the presence of carbon dioxide and ammonia.
  • the ammonium chromate produced by this process should be able to be used for the production of chromium (Ii) oxide.
  • the disclosed process for the production of ammonium chromate has several disadvantages.
  • the sodium chromate solution used must be initially recrystallised and filtered. So it is a - only incompletely described - cleaning step required in which sodium chloride is obtained as a byproduct.
  • the reaction with carbon dioxide and ammonia takes place in two process steps, in which carbon dioxide and ammonia are added in each case.
  • the separation of the sodium bicarbonate formed after the first reaction is carried out by cooling crystallization, wherein the cooling rate is 1 ° C / h to 4 ° C / h.
  • the crystallization is a very slow and time-consuming process, especially since in all the examples disclosed before the filtration also takes place a two-hour aging step.
  • the conditions under which chromium (II) oxide is obtained from the obtained ammonium chromate are not disclosed in CN-A-1310132.
  • the dust also does not contain unreacted proportions of Cr (VI in CN-A-1418822
  • GB 748,610 generally describes the reduction of Aikalimetallchromaten with hydrogen and subsequent conversion to Cr 2 0 3rd
  • the yields in such a reduction are very low.
  • the yield of Cr 2 0 3 starting from alkali-free sodium monochromate is less than 67%, which makes this process for the reaction with such reactive starting materials in an industrial scale uninteresting.
  • CN 1 07865 A discloses a method for the production of chromium oxide, wherein reacting a chromate salt as a starting material and a reducing gas such as hydrogen, natural gas, coal gas or mixtures thereof as a reducing agent at 300-850 ° C for 0.5 to 3 hours. After cooling, the reaction mixture is washed with water and calcined after drying at 400-1 100 ° C for 1 to 3 hours.
  • a reducing gas such as hydrogen, natural gas, coal gas or mixtures thereof
  • the object of the invention was to find a process for the production of chromium oxide, which is more economical to use and also produces a chromium oxide which can be used for metallurgical purposes, ie in particular a low sulfur content and alkali metal content, in particular sodium content, and has as few by-products as possible.
  • the invention therefore relates to a process for the preparation of chromium (III) oxide, comprising the steps: a) reaction of sodium nonochromate with gaseous ammonia, in particular at a temperature of from 200 to 800 ° C., b) hydrolysis of the reaction product obtained according to step a) in which the pH of the water for the hydrolysis before the hydrolysis or that of the alkaline mother liquor during or after the hydrolysis is lowered to a value of 4 to 11, preferably of 5 to 10 by means of an acid, c) separation of the after step b ) precipitated Hydro lyse economics, preferably at a pH of 4 to 1 1, in particular from 5 to 10, and optionally washing and optionally drying and d) calcining the obtained after step c) hydrolysis at a
  • the starting material for the production of chromium (HI) oxide is sodium monochromate. It is irrelevant whether the sodium monochromate is used as anhydrous compounds or in the form of its hydrates.
  • the sodium monochromate can be used either as a solution, in particular as an aqueous solution, or as a suspension or as a solid. Solids are particularly preferably used for the process according to the invention, these preferably having a residual moisture content of less than 4.0% by weight, particularly preferably less than 2.0% by weight.
  • the sodium monochromate used has a content of alkali metal hydroxide of less than 2 wt .-%, particularly preferably less than 1 wt .-%, in particular less than 0.5 wt .-%.
  • the sodium monochromate used in step a) does not necessarily have to be used in pure form. It can also be advantageously used in a mixture. Thus, the process according to the invention is preferred in which sodium monochromate is used as the only chromium compound or sodium monochromate in mixture with other Cr (III) and / or CrfVI) -containing compounds in step a).
  • mixtures of sodium monochromate and other Cr (IIl) or Cr (VI) -containing compounds are particularly advantageous.
  • the sodium monochromate is preferably used in the form of mixtures with other Cr (III) or Cr (VI) -containing compounds.
  • Such Cr (III) or Cr (VI) -containing compounds as mixed components with sodium monochromate are preferably chromium (III) oxide, sodium chromite, sodium ammonium chromate double salts, ammonium monochromate, ammonium dichromate or sodium chromium chromate.
  • the process according to the invention is preferred in which sodium monochromate is mixed in step a) with a mixture of chromium (III) oxide, sodium chromite, sodium ammonium chromate double salt, ammonium monochromate, ammonium dichromate and / or sodium chromium chromate.
  • chromium (III) oxide chromium oxide
  • sodium chromite sodium ammonium chromate double salt
  • ammonium monochromate ammonium dichromate and / or sodium chromium chromate
  • Such mixtures can be prepared synthetically by mixing the components, but they can also be prepared by other means, for example a solid-state reaction.
  • the solid state reaction between sodium chromite and sodium dichromate preferably takes place at a temperature above 300 ° C. Then formed from the two components sodium monochromate and chromium (III) oxide.
  • sodium chromium chromates are compounds in which chromium not only occurs in the oxidation state + VI (in the form of chromate) but is also present in the oxidation state + III at the same time.
  • sodium ammonium chromate double salts are compounds having the ideal composition 3 or NaNH 4 Cr0 4 * 2H 2 0 or NaNH 4 Cr0 4 in its anhydrous form.
  • the molar fraction of Nairium monochromate in the mixture is preferably at least 30%, particularly preferably at least 40%, completely particularly preferably at least 50%, based on all chromium-containing compounds of the mixture.
  • such a mixture contains less than 20, preferably less than 10, in particular less than 5 mol% of sodium dichromate, based on all chromium-containing compounds of the mixture.
  • the reaction of the sodium monochromate with gaseous ammonia is preferably carried out at a temperature of 200 to 800 ° C, more preferably from 200 to 650 ° C, most preferably from 300 to 600 ° C. It has been found that the reduction of sodium monochromate with ammonia is complete even when the reaction temperature is well below the melting point of sodium monochromate. As a result, the risk of melting and sticking of sodium monochromate during the reduction can be excluded.
  • the reaction does not necessarily have to occur at only one temperature. It has proved to be advantageous if the temperature is raised in the course of the reaction. Preferably, the reaction is started at a temperature of 200 to 400 ° C and held this temperature until a temperature increase can be observed. For further implementation, the temperature can then be increased, this increase can be continuous or stepwise.
  • reaction of the sodium monochromate with gaseous ammonia is preferably carried out in an indirectly heated reactor, in particular in a rotary kiln or in a fluidized bed.
  • the reaction time is usually 0.5 to 10 hours and depends inter alia on the reaction temperature, the sodium monochromate used and the size of the sodium monochromatic crystals used. For this reason, it may be advantageous if the sodium monochromate used is comminuted before it is fed to step a). Preference is given to particles smaller than 1000 ⁇ m, more preferably smaller than 500 ⁇ m, very particularly preferably smaller than 300 ⁇ m.
  • the reaction of the sodium monochromate with gaseous ammonia finally leads inter alia to the formation of sodium chromite as the reaction product.
  • the sodium chromite NaCr0 2 formed could be detected in the reaction product by means of an X-ray powder absorption from one of the examples described below.
  • the gaseous ammonia is advantageously not used in the exact stoichiometric ratio, but in excess.
  • the excess of ammonia is at least 5%, particularly preferably at least 10%, in particular 10 to 30%, based on the stoichiometric amount of sodium monochromate.
  • the reaction according to step a) is terminated until the reaction product in the hydrolysis with four times the amount of water, a suspension having a pH of at least 1 1, more preferably of at least 12, most preferably of at least 13 results ,
  • a suspension having a pH of at least 1 1, more preferably of at least 12, most preferably of at least 13 results preferably samples are taken from the reaction, subjected to hydrolysis with water as described, and the pH of the resulting suspension is determined.
  • reaction product obtained after step a) can, before it is fed to step b), be comminuted in order to ensure as rapid and complete hydrolysis as possible.
  • Step V) The reaction product obtained after step a) is hydrolyzed with water to give a ⁇ & ⁇ & ⁇ 3 ⁇ ⁇ and a mother liquor.
  • the hydrolysis can be carried out at room temperature or else at elevated temperatures.
  • chromium (III) hydroxide and / or chromium (III) oxide hydroxide and sodium hydroxide solution are formed as precipitates, so that the resulting mother liquor has a very high pH when pure water is used.
  • the hydrolysis of sodium chromite NaCr0 2 can be formally described by the following two reaction equations:
  • the precipitating hydrolysis is rö 'ntgenamorph so that its precise structure determination was not possible.
  • based on the reaction product obtained after step a) at least the same Gewichismenge of water used for the hydrolysis.
  • the viscosity of the suspension obtained can be very high, it is advantageous for the hydrolysis to use at least twice the amount by weight of water, based on the reaction product obtained after step a).
  • the hydrolysis product is suspended using pure water in a strongly alkaline mother liquor.
  • the hydrolysis product is usually very finely divided, but it shows significantly better filtration properties (significantly shorter Fiitration devis) in comparison to the hydrolysis product, which was obtained from the reduction of Natriumdi chromate with ammonia.
  • the pH is lowered at a temperature of 20 to 140 ° C, preferably from 40 to 100 ° C.
  • Very particular preference is given to lowering the pH during or after the hydrolysis.
  • the pH is lowered before the separation of the precipitated hydrolysis product taking place in step c) takes place.
  • preference is given to using inorganic acids or organic acids.
  • Inorganic acids within the meaning of this invention also include acidic gases, such as carbon dioxide, in water. These acidic gases can be introduced either under atmospheric pressure or under elevated pressure in the mother liquor.
  • organic acids in particular organic low molecular weight acids such as, for example, formic acid or acetic acid.
  • the pH is preferably in the range from 4 to 11, more preferably in the range from 5 to 10.
  • the adjustment of the pH can be carried out in one or more steps.
  • the advantage of using C0 2 to adjust the pH is that in this way sodium carbonate or sodium bicarbonate can be obtained from the alkaline mother liquor.
  • the sodium carbonate or sodium bicarbonate can be separated off by means of various continuous or batchwise solid-liquid separation processes.
  • continuously operating units for example, vacuum drum filters or vacuum belt filters or centrifuges are particularly preferred.
  • Sodium carbonate can be used directly for the production of sodium monochromate or dichromate via the oxidative digestion of chromium iron.
  • sodium bicarbonate this can still be converted by calcination into sodium carbonate and then used for the preparation of sodium monochromats or dichromates via the oxidative decomposition of chromium iron.
  • the released during the annealing of sodium bicarbonate to sodium carbonate carbon dioxide can be recycled back into the process for the purpose of pH reduction.
  • the precipitated Cr-containing hydrolysis product obtained after step b) is now separated from the mother liquor.
  • the skilled person knows a variety of suitable units and methods. It does not matter whether the solid / liquid separation and optionally subsequent washing done continuously or discontinuously. It is also irrelevant whether they are carried out under increased or reduced pressure.
  • the continuous filtration and washing units for example, vacuum drum filters or vacuum belt filters are particularly preferred.
  • filter presses are particularly preferred.
  • the separated, preferably filtered off hydrolysis product can now be washed or - optionally after drying - the step d) are supplied.
  • suitable aggregates Only channel, belt, stacker, drum, drum, tube, blade, spray dryer (atomizing dryer with discs or nozzles), fluidized bed dryer or discontinuous chamber hoppers are mentioned at this point.
  • the wet fiiter cake is fed directly to the calcination in step d), in particular without washing.
  • the separated hydrolysis product can also be washed in one or more stages.
  • the laundry can be done directly with water.
  • the wash water is preferably reacted with an acid before or during the wash to lower the pH.
  • preference is given to using inorganic acids or organic acids or carbon dioxide, as already described above.
  • organic acids in particular organic low molecular weight acids such as, for example, formic acid or acetic acid.
  • very particular preference is given to using carbon dioxide to adjust the pH, which can be introduced into the wash water either under atmospheric pressure or under elevated pressure.
  • the pH of the wash water after washing is in the range of 4 to 11, more preferably in the range of 5 to 10.
  • the adjustment of the pH can be carried out in one or more steps.
  • flocculants or flocculants are used prior to filtration or before washing.
  • the use of organic flocculants or flocculants is particularly preferred because they are decomposed by oxidation without residue in the subsequent calcination in step d) and do not remain as an impurity in the calcined product.
  • Preferred flocculants are anionic polyelectrolytes, for example the basis of polyacrylate, polyactylamide, polyethyleneimine and polyethylene oxide in different chain length.
  • nonionic synthetic and natural (for example, starch or glue) compounds can be used as flocculants.
  • the wet filter cake of the hydrolysis product obtained after the separation and, if appropriate, the washing can either be fed directly to the calcination according to step d) or else dried beforehand.
  • the drying step those skilled in the art will recognize a variety of suitable aggregates already mentioned above.
  • step c) can also be used to obtain sodium carbonate or sodium bicarbonate, as already described in step b).
  • the mother liquor from step b) and the washings from step c) can also be used together, if appropriate after concentration, for the recovery of sodium carbonate or sodium bicarbonate.
  • this procedure entails the risk that sodium bicarbonate crystallizes out of the mother liquor if it is concentrated too much, since the mother liquor always has a very high sodium concentration.
  • Step d) The thermal treatment at elevated temperature, so the calcination, according to step d) is carried out at a temperature of 700 to 1400 ° C, more preferably from 800 to 1300 ° C, preferably in a period of more than 20 minutes, more preferably more than 30 minutes, especially 30 minutes to 4 hours.
  • a temperature of 700 to 1400 ° C more preferably from 800 to 1300 ° C, preferably in a period of more than 20 minutes, more preferably more than 30 minutes, especially 30 minutes to 4 hours.
  • the calcination at such high temperatures the skilled person knows a variety of suitable apparatus. At this point, only ring hearth furnaces, rotary kilns, fluidized bed reactors or discontinuously operating chamber furnaces are mentioned.
  • the calcination is carried out in a directly heated rotary kiln, the residence time of the material to be calcined is depending on the configuration and length of the furnace preferably at 30 minutes to 4 hours.
  • the calcination is preferably carried out in
  • the hydrolysis product obtained after step c) and optionally washed, which is calcined in step d), does not tend to stick during the calcination, so that the calcination is possible without problems.
  • one or more alkali metal halides or ammonium halides or alkaline earth metal halides in particular the fluorides, chlorides, bromides or iodides of sodium or potassium or ammonium, or AikaJimetaUhydroxide, in particular sodium hydroxide, or potassium hydroxide, or chromic acid in in an amount of from 0.01% by weight to 3.0% by weight, particularly preferably from 0.02% by weight to 1.0% by weight, based on the hydrolysis product used for the calcination.
  • the performance properties, in particular the increase in the bulk density of the obtained chromium (II) oxide can be influenced. It is likewise preferred to dispense with addition of such additives before or during the calcination
  • chromium (lII) oxide is preferably cooled and optionally ground.
  • the calcined product is suspended in water after step d), resulting in a mother liquor and optionally washed with water in one or more stages and then dried again.
  • water-soluble impurities water-soluble salts
  • essentially alkali metal chromate for example sodium chromate, which has been formed by oxidation of chromium (II) oxide at high temperatures
  • the preferred embodiments for the washing apply, as already indicated under step c).
  • the chromium (III) oxide generally has good filtration and washing properties, so that the adjustment of the pH or the addition of a flocculant or flocculant is no longer necessary.
  • the moist chromium (IIl) oxide obtained after the solid / liquid separation is subsequently dried.
  • the dried chromium (IV) oxide is then preferably filled directly or optionally ground before bottling.
  • the already mentioned aggregates can be used.
  • a grinding can be advantageous.
  • the calcined and optionally suspended in water and washed and dried product is still subjected to grinding.
  • grinders of different types are suitable, such as roll mills, edge mills, pendulum mills, hammer mills, pin mills, turbo mills, ball mills or jet mills.
  • a milling dryer in which the drying and grinding in only one step.
  • the choice of suitable grinding unit depends, inter alia, on the particular field of application for the chromium (III) oxide produced.
  • the respective mother liquor and the washing water in both cases essentially contain alkali metal chromate and / or alkali metal dichromate.
  • alkali metal chromate and / or alkali metal dichromate These two valuable substances can be recycled back into the production process, for example by being used again for the preparation of alkali metal dichromate or, for example, an alkali metal ammomum chromate double salt.
  • mother liquors and washing waters, which are obtained during the washing of the calcined product are used again for the preparation of alkali metal dichromate or, for example, an alkali metal ammonium chromate double salt.
  • the chromium (III) oxide produced by the process according to the invention is highly pure. It is therefore eminently suitable for metallurgical purposes such as the production of chromium metal or chromium-containing high performance alloys, in particular by reduction in the presence of Aluminiummetalf on the aluminothermic process, and for the production of high temperature resistant materials, but it can also be used as a color pigment for pigmentary applications, as it also has a low content of water-soluble salts.
  • the invention also encompasses the use of chromium (III) oxide prepared by the process according to the invention, as a color pigment, abrasive and as starting material for the production of high-temperature resistant materials, chromium metal or chromium-containing high-performance alloys, in particular by reduction in the presence of aluminum metal via the aluminothermic process ,
  • the process according to the invention for producing high-purity, low-sulfur chromium (III) oxide has some significant advantages over the processes described in the prior art.
  • An advantage of the process according to the invention is that alkali metal chromate and / or alkali metal dichromate forms as by-products, which can be recycled back into the manufacturing process without problems.
  • the strongly alkaline mother liquor formed during the hydrolysis can be acidified with carbon dioxide and thus either converted directly into sodium carbonate or first converted into sodium bicarbonate, which is then calcined to sodium carbonate.
  • the sodium carbonate can be used again for the oxidative digestion of chromium iron to form sodium chromate.
  • a great advantage over the method described in CN 1907865A is that the yield is improved and in particular in the case of pH reduction, the yield and purity of the resulting chromium oxide can be further increased.
  • the inventive method provides significantly higher yields of chromium (HI) oxide.
  • the process according to the invention for the preparation of chromium (III) oxide from sodium monochromate has further advantages in comparison with the processes described in the prior art, which are based on the reaction of sodium dichromate with ammonia at elevated temperatures.
  • the melting point of sodium dichromate is only 357 ° C.
  • the reduction with ammonia involves the risk that the sodium dichromate melts during the exothermic reaction and thus tends to stick together.
  • the sodium monochromate at 792 ° C has a much higher melting point, the risk of melting when using sodium monochromate is not given.
  • the hydrolysis product obtained from the reaction of sodium monochromate with ammonia has significantly better filtration properties (significantly shorter filtration times) compared to the hydrolysis product obtained from the reduction of sodium dichromate with ammonia.
  • the obtained by the novel chromium (iII) oxide is highly pure. It is low in sulfur per se, because no sulfur compounds are introduced into the production process. Furthermore, it is low in alkali metal.
  • Chromium (III) oxides which have a sulfur content of less than 200 ppm, preferably less than 50 ppm, very particularly preferably less than 40 ppm, are considered to be "low in sulfur” for the purposes of this invention
  • Chromium (oxides) which have an alkali metal content - calculated as alkali metal - of less than 1500 ppm, preferably less than 500 ppm.
  • the coarsely crushed reaction product was slurried in 200 ml of water and hydrolyzed to give a suspension having a pH of 13.2. Then, carbon dioxide was introduced into the suspension under normal pressure until a pH of 9.8 resulted, which could not be further lowered.
  • the suspension was then briefly heated to 85 ° C and filtered through a suction filter (filtration time 2 minutes).
  • the mother liquor contained only 180 mg / kg Cr.
  • the filter cake was resuspended in 200 ml of water and the pH of the suspension was adjusted to 7.1 by passing carbon dioxide under atmospheric pressure. Further lowering of the pH was not possible. Then the suspension was heated again briefly to 85 ° C and filtered through a suction filter (filtration time 30 seconds).
  • the mother liquor contained only 25 mg kg Cr.
  • the filter cake was dried at 120 ° C. Then it was annealed at 1250 ° C for 2 hours.
  • the calcined chromium (III) oxide was suspended in water, washed with water and finally dried at 120 ° C.
  • the chromium (III) oxide obtained in this way had a Na content - calculated as Na metal - of 430 ppm.
  • Example 4 Crushed sodium chromite NaCrO 2 and comminuted sodium dichromate Na 2 Cr 2 O 7 are mixed in a molar Cr (III): Cr (VI) ratio of 1: 1 and heated to 350 ° C. under an inert gas atmosphere. After one hour, the temperature is raised at 3 ° C / min to 450 ° C and held at 450 ° C for a further 30 min. The resulting reaction product is dark green. According to a powder X-ray recording, it is composed of chromium (III) oxide and sodium monochromate Na 2 Cr0 4: 2 NaCr0 2 + Na 2 Cr 2 0 7 -> 2 Na 2 Cr0 4 + Cr 2 0 3 (10)
  • reaction product was reacted with gaseous ammonia, which was used as a mixture of 13.6% by volume of ammonia and an inert gas at 500 ° C, with the reduction already starting at about 350 ° C in motion.
  • gaseous ammonia which was used as a mixture of 13.6% by volume of ammonia and an inert gas at 500 ° C, with the reduction already starting at about 350 ° C in motion.
  • reducing a weight loss of 10.65% occurs, which is in good agreement with the expected reaction to form sodium chromite: 2 Na 2 Cr0 4 + Cr 2 0 3 + 2 NH 3 -> 4 NaCr0 2 + 3 H 2 0 + N 2 (1 1)
  • the sodium chromite NaCrO 2 obtained after the reaction with ammonia according to equation (11 ) can be worked up as described in Example I.

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Abstract

L'invention concerne un procédé de production d'oxyde de chrome(III), comprenant les étapes suivantes : a) réaction du monochromate de sodium avec de l'ammoniac gazeux, en particulier à une température de 200 à 800°C, b) hydrolyse du produit réactionnel obtenu à l'étape a), en abaissant le pH de l'eau pour l'hydrolyse, avant l'hydrolyse, ou celui de la lessive-mère alcaline, pendant ou après l'hydrolyse, à une valeur de 4 à 11, de préférence de 5 à 10, au moyen d'un acide, c) séparation du produit d'hydrolyse résultant de l'étape b), de préférence à un pH de 4 à 11, en particulier de 5 à 10, et éventuellement lavage, et éventuellement séchage, et d) calcination du produit d'hydrolyse obtenu à l'étape c), à une température de 700 à 1400°C, en particulier de 800 à 1300°C.
EP11791295.6A 2010-12-08 2011-12-07 Procédé de production d'oxyde de chrome(iii) Withdrawn EP2649010A1 (fr)

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EP11791295.6A EP2649010A1 (fr) 2010-12-08 2011-12-07 Procédé de production d'oxyde de chrome(iii)

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EP10194157 2010-12-08
EP11180086A EP2565162A1 (fr) 2011-09-05 2011-09-05 Procédé de fabrication d'oxyde de chrome (III)
EP11791295.6A EP2649010A1 (fr) 2010-12-08 2011-12-07 Procédé de production d'oxyde de chrome(iii)
PCT/EP2011/071997 WO2012076564A1 (fr) 2010-12-08 2011-12-07 Procédé de production d'oxyde de chrome(iii)

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EP (1) EP2649010A1 (fr)
CN (1) CN103249677B (fr)
AR (1) AR084183A1 (fr)
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EP3020690A1 (fr) * 2014-11-13 2016-05-18 LANXESS Deutschland GmbH Procédé de réduction de chrome hexavalent dans des matières solides oxydées
CN109401438A (zh) * 2018-10-31 2019-03-01 江苏拜富科技有限公司 陶瓷喷墨用绿色颜料及其制备方法
CN110436521A (zh) * 2019-09-11 2019-11-12 攀钢集团攀枝花钢铁研究院有限公司 铬酸钠制备三氧化二铬的方法
CN113620345B (zh) * 2021-10-12 2022-03-11 中国科学院过程工程研究所 一种亚铬酸钠材料及其制备方法与应用
CN114180627B (zh) * 2021-12-22 2024-04-26 广东工业大学 一种钠离子电池正极材料及其制备方法以及钠离子电池
CN114784270B (zh) * 2022-03-05 2023-09-19 四川龙蟒磷化工有限公司 一种钠离子电池材料的制备方法

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RU2591245C2 (ru) 2016-07-20
CN103249677A (zh) 2013-08-14
RU2013130866A (ru) 2015-04-10
CN103249677B (zh) 2016-08-17
US20140105812A1 (en) 2014-04-17
AR084183A1 (es) 2013-04-24
US9580333B2 (en) 2017-02-28
WO2012076564A1 (fr) 2012-06-14
ZA201304161B (en) 2014-02-26

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