WO2010135856A1 - 一种拜耳法氢氧化铝或氧化铝的生产工艺 - Google Patents

一种拜耳法氢氧化铝或氧化铝的生产工艺 Download PDF

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WO2010135856A1
WO2010135856A1 PCT/CN2009/070631 CN2009070631W WO2010135856A1 WO 2010135856 A1 WO2010135856 A1 WO 2010135856A1 CN 2009070631 W CN2009070631 W CN 2009070631W WO 2010135856 A1 WO2010135856 A1 WO 2010135856A1
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decomposition
liquid
aluminum hydroxide
composite catalyst
catalytic decomposition
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PCT/CN2009/070631
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English (en)
French (fr)
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李民菁
史智慧
王志勇
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河南未来铝业（集团）有限公司
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Publication of WO2010135856A1 publication Critical patent/WO2010135856A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/14—Aluminium oxide or hydroxide from alkali metal aluminates
    • C01F7/144—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by precipitation due to cooling, e.g. as part of the Bayer process
    • C01F7/145—Aluminium oxide or hydroxide from alkali metal aluminates from aqueous aluminate solutions by precipitation due to cooling, e.g. as part of the Bayer process characterised by the use of a crystal growth modifying agent other than aluminium hydroxide seed

Definitions

  • the invention belongs to the technical field of production technology of aluminum hydroxide or aluminum oxide, and particularly relates to a production process of Bayer process aluminum hydroxide or aluminum oxide. Background technique
  • the 2 O k concentration is 180 ⁇ 300g/l, and the caustic ratio a k of circulating mother liquor is 2.5 ⁇ 3.5.
  • the traditional Bayer process for the production of aluminum hydroxide or aluminum oxide uses a conventional seed crystal decomposition process.
  • the concentration of A1 2 0 3 in the semen is 120-190 g/l, the caustic ratio a k is 1.45 1.70, and the silicon content index is 200 or more.
  • the initial temperature of decomposition is 50 ⁇ 75 °C, the decomposition time is generally 30 ⁇ 72h, no catalyst is added, only additives such as phosphorus pentoxide are added when the particle size is emphasized, and the concentration of decomposition mother liquor A1 2 0 3 at the end of decomposition is 70 ⁇ 120g/l.
  • the caustic ratio a k is between 2.0 and 3.5, the decomposition final temperature is 30 to 50 ° C, the decomposition rate is generally 30 to 55%, and the aluminum hydroxide product particle size D 5Q is generally 1 to 80 ⁇ sand or surface.
  • the traditional Bayer process aluminum hydroxide or alumina production process not only has the disadvantages of high requirements for bauxite ore, low decomposition rate, poor controllability of the particle size of the aluminum hydroxide product, and decomposition of the alumina content in the mother liquor,
  • the high silica content limits the increase of evaporation efficiency, and the degree of crusting of the mother liquid evaporation is serious, which is not conducive to the normal operation of the system, the improvement of production capacity and the reduction of energy consumption.
  • the object of the present invention is to provide a production process of Bayer process aluminum hydroxide or aluminum oxide, which reduces the batching requirements of bauxite, greatly improves the decomposition rate, and the aluminum hydroxide product.
  • the particle size is controllable, and the alumina content in the decomposed mother liquor is greatly reduced, and the silica content is also decreased, so that the evaporation efficiency is significantly improved, and the degree of crusting of the mother liquid evaporation is reduced, which is beneficial to the normal operation of the system and the improvement of the production capacity. Reduce energy consumption.
  • a production process of Bayer process aluminum hydroxide or aluminum oxide including crushing of bauxite, preparation of raw ore pulp, dissolution, dilution of dissolved pulp, separation and washing of red mud , sodium aluminate crude liquid refining, sodium aluminate semen decomposition, aluminum hydroxide treatment, mother liquor evaporation, aluminum hydroxide roasting, which is special in that: the sodium aluminate semen is decomposed by using sodium aluminate semen as a catalytic decomposition liquid.
  • a composite catalyst YHC formed by mixing and compounding YHA and composite catalyst YHB is added to the catalytic decomposition solution at a ratio of 1 to 300% of its volume for catalytic decomposition, and the initial temperature of decomposition is 30-80 ° C, and the decomposition temperature is finalized.
  • the decomposition time is from 1 to 80 hours, and the decomposition time is from 1.5 to 80 hours, wherein the composite catalyst YHA is formed by mixing one or more of a surfactant, an alcohol, and an ester in an arbitrary ratio, wherein the The composite catalyst YHB is formed by mixing one or two of a saccharide or an inorganic one in an arbitrary ratio.
  • the mixing process for preparing the composite catalysts YHA, YHB and YHC belongs to the prior art, and the mixing ratio between the various preparations of the composite catalysts YHA and YHB and the composite catalyst YHA and the composite catalyst YHB when preparing the composite catalyst YHC are
  • the mixing ratio can be adjusted according to the composition of the slurry combined with the decomposition system to achieve the decomposition rate of the production demand, the particle size of the aluminum hydroxide product, and the impurity content of the aluminum hydroxide product.
  • the production process of the aluminum hydroxide or aluminum oxide is carried out according to the following steps: bauxite, lime, and lye are first subjected to raw material grinding to form a raw ore slurry, and the raw ore slurry is pre-desiliconized and then subjected to pipeline dissolution. After dilution, the red mud is separated, the red mud separated bottom stream is washed by red mud, the washed solid phase is red mud, the washed liquid phase is returned for dilution, and the red mud separation overflow is sodium aluminate crude liquid.
  • the solid phase returns to continue the red mud separation, and the liquid phase is the sodium aluminate semen, and the catalytic decomposition solution is used, and the composite catalyst YHA and the composite are added to the catalytic decomposition liquid at a ratio of 1 to 300% of the volume.
  • the composite catalyst YHC formed by mixing YHB catalysts is catalytically decomposed, the initial temperature of decomposition is 30-80 ° C, the final decomposition temperature is 20-70 ° C, the decomposition is carried out for 1.5-80 h, and the separated liquid filtrate is used for catalyst recovery.
  • the specific recovery method of the catalyst can select conventional solid-liquid, solid-solid separation processes such as separation, distillation or evaporation according to different properties of the medicament, and the recovered reagents are composite catalyst YHA and composite catalyst respectively.
  • the agent YHB is returned to the recycling process, and the recovered residual liquid is sent to the mother liquid evaporation process as a catalytic decomposition mother liquid, and the separated solid phase filter cake is washed into a finished aluminum hydroxide product, dried to obtain a dried aluminum hydroxide finished product, and calcined to obtain an alumina finished product.
  • the washing liquid produced by the solid phase filter cake washing also passes through the catalyst recovery step, and the recovered composite catalyst YHA and the composite catalyst YHB are also returned to the recycling, and the residual liquid is also used as the catalytic decomposition mother.
  • the liquid is sent to the mother liquid evaporation process, and the water is evaporated back to the red mud washing process.
  • the mother liquid is evaporated, the liquid alkali mixing process is returned to continue the grinding of the original ore.
  • the sodium aluminate semen can be first decomposed by the seed crystal, and then the seed mother liquor is used as a catalytic decomposition liquid to carry out catalytic decomposition.
  • the sodium aluminate fine liquid crystal is decomposed and classified, and the classified overflow and the underflow are respectively separated, and the two separated liquid phases are seed mother liquids, and simultaneously used as catalytic decomposition liquid to carry out catalytic decomposition and subsequent treatment processes.
  • the solid phase return of the overflow separation continues the decomposition of the seed crystal, and the solid phase separated by the underflow is washed to become the finished aluminum hydroxide, and a part of the washing liquid produced by the washing is washed by the red mud, and the other part is separated from the mother liquor of the catalytic decomposition liquid to evaporate.
  • the surfactant is cetylpyridinium bromide, ethyl(1-alkylaminoethylimidazoline), sodium dodecyl benzoate or sodium di-decyl sulfonate;
  • the alcohol The class is decyl alcohol, ethanol, glycerol, n-hexadecanol or n-butanol;
  • the ester is ethyl acetate, phenyl acetate or decyl benzoate;
  • the saccharide is sucrose, glucose, Fructose or maltose;
  • the inorganic class is aluminum hydroxide, aluminum fluoride or aluminum oxide.
  • the concentration of A1 2 0 3 is 40-200 g/l
  • the caustic ratio a k is 1.3-4.5
  • Na 2 O c 3 ⁇ 4 degree
  • the concentration of Si0 2 is 0.2 ⁇ 5g/l.
  • A1 2 0 3 concentration is 5 ⁇ 150g/l
  • caustic ratio a k is 1.5-100
  • Na 2 O c concentration is 0.5 ⁇ 40g/l
  • Si0 2 concentration is 0.004 ⁇ 4.5g /l.
  • the original bauxite pulp a solids content of 200 ⁇ 1000g / l, calcium ingredient concentration ratio of CaO f l ⁇ 50g / l, Na 2 O k circulating liquor concentration of 150 ⁇ 400g / l, caustic liquor circulation Than a k is 1.30 ⁇ mess
  • the decomposition rate of the catalytic decomposition is 20 to 95%, and under normal conditions are more than 60%; the particle size D 5 () of the aluminum hydroxide product is 0.3 to 110 ⁇ , which can be controlled in a certain section according to production requirements; In terms of percentage, the impurity content of the aluminum hydroxide product is: Si0 2 0.005-5%, Fe 2 0 3 0.002-0.02%, Na 2 O 0.10 ⁇ 3.0%.
  • the process principle of the present invention is also the basic process principle of Bayer process for the production of aluminum hydroxide or alumina:
  • the basic process principle of the production of Bayer process aluminum hydroxide or alumina of the present invention is that the process from left to right of the equation is the dissolution process of bauxite, and the process from the right to the left of the equation is the catalytic decomposition process of sodium aluminate solution (semen). Or seed decomposition + catalytic decomposition process.
  • the invention has the advantages that: the method of the invention can be recycled due to the addition of the catalyst, the batching requirement of the bauxite is reduced, the decomposition rate is greatly improved, and the decomposition mother liquid also occurs.
  • the fundamental change the alumina content in the decomposition mother liquor is greatly reduced, the silica content is also decreased, so that the evaporation efficiency is significantly improved, the degree of crusting of the mother liquor evaporation is reduced, which is beneficial to the normal operation of the system, the improvement of the production capacity and the reduction.
  • Energy consumption The particle size of aluminum hydroxide or alumina is controllable, and it can be controlled within a certain interval according to production requirements, and the economic benefits will change significantly.
  • the content of impurities in aluminum hydroxide or alumina can be decomposed according to catalytic decomposition - aluminate
  • the quality of the sodium semen or seed mother liquor, the decomposition system, and the proportion of the composite catalyst are effectively controlled.
  • Fig. 1 is a flow chart showing the production process of a conventional seed crystal decomposition Bayer process aluminum hydroxide or aluminum oxide
  • Fig. 2 is a flow chart showing the production process of catalytic decomposition of Bayer process aluminum hydroxide or aluminum oxide according to Examples 1 to 6 of the present invention
  • Fig. 3 is a flow chart showing the production process of seed crystal decomposition + catalytic decomposition of Bayer process aluminum hydroxide or aluminum oxide according to Example 7 of the present invention. detailed description
  • catalytic decomposition of Bayer process aluminum hydroxide or alumina production process flow chart bauxite, lime, lye first material grinding, to make the original slurry, the original slurry pre-desiliconization
  • the pipeline is dissolved, diluted and red mud separated.
  • the bottom of the red mud is washed by red mud.
  • the washed solid phase is red mud, the washed liquid phase is returned for dilution, and the red mud separation is aluminum.
  • the composite catalyst YHC was added for catalytic decomposition.
  • the composite catalyst YHC was mixed by the composite catalyst YHA (80% by weight, 20% ethanol, 20% ethanol) and the composite catalyst YHB (aluminum hydroxide) at 10%: 90% by weight.
  • the liquid composite catalyst formed by the preparation has a decomposition initial temperature of 40 ° C, a decomposition final temperature of 20 ° C, separation after 60 hours, separation, and separation of the liquid phase filtrate for catalyst recovery.
  • the recovered reagents are composite catalyst YHA and composite catalyst YHB. , returning to the recycling, the recovered residual liquid is sent to the mother liquid evaporation process as the catalytic decomposition mother liquid, and the separated solid phase filter cake is washed into a finished aluminum hydroxide product, and dried to obtain a dried aluminum hydroxide finished product.
  • the calcined product is obtained by calcination, and the washing liquid produced by the solid phase filter cake washing is also subjected to a catalyst recovery step, and the recovered composite catalyst YHA and the composite catalyst YHB are also recycled for recycling, and the liquid phase is also sent to the mother liquid evaporation step as a catalytic decomposition mother liquid, and evaporated.
  • the catalytic decomposition liquid is: the concentration of A1 2 0 3 is 100-180 g/l, and the caustic ratio a k is 1.3-1.6.
  • the concentration of Na 2 O c is 10 ⁇ 50g/l, the concentration of Si0 2 is 0.2 ⁇ 0.8g/l; in the catalytic decomposition mother liquor: the concentration of A1 2 0 3 is 60 ⁇ 120g/l, the caustic ratio a k is 2.5 ⁇ 4.5 , Na 2 O c concentration is 5 ⁇ 40g/l, Si0 2 concentration is 0.1 ⁇ 0.7g/l; bauxite ore slurry: solid content is 250 ⁇ 400g/l, and the ratio of calcium to CaO f is l ⁇ 50g/l circulating mother liquor Na 2 O k concentration of 250 ⁇ 350g / l, a k circulating liquor caustic ratio of 1.3 1.6; decomposition catalytic decomposition of 30 to 60%; product of aluminum hydroxide particle size D 50 of 0.3 ⁇ 50 ⁇ ; by weight Percentage, aluminum hydroxide product impurity content: Si0 2 0.05-2%, Fe 2 0 3 0.005-0.02%, Na 2 0 0.15 ⁇ 0.6
  • the composite catalyst YHC is added to the catalytic decomposition at a ratio of 50% of its volume.
  • the composite catalyst YHC is composed of the composite catalyst YHA (ethanol) and the composite catalyst YHB (alumina) at 50%: 50%.
  • the other processes and procedures are the same as in the first embodiment.
  • the catalytic decomposition of the stock solution A1 2 0 3 concentration of 40 ⁇ 200g / l, caustic ratio a k is 1.3 ⁇ 4.5, Na 2 O c concentration of 10 ⁇ 50g / l, Si0 2 concentration of 0.2 ⁇ 5g / l;
  • Catalytic decomposition of mother liquor A1 2 0 3 concentration is 10 ⁇ 50g/l, caustic ratio a k is 4.5 ⁇ 40, Na 2 O c concentration is 2 ⁇ 10g/l, Si0 2 concentration is 0.1 ⁇ 2g/l; original slurry ore: a solids content of 300 ⁇ 500g / l, the ingredients calcium ratio of CaO f concentration of l ⁇ 50g / l, cycle mother liquor Na 2 O k concentration of 280 ⁇ 400g / l, circulating liquor caustic ratio of a k 4.5 40
  • the decomposition rate of catalytic decomposition is 70 ⁇ 85%; the particle size D 5Q of aluminum
  • the composite catalyst YHC was added to catalytic decomposition at a ratio of 130% by volume.
  • the composite catalyst YHC was composed of composite catalyst YHA (ethanol) and composite catalyst YHB (aluminum hydroxide) at 40%: 60
  • the liquid composite catalyst formed by mixing and mixing % by weight has a decomposition initial temperature of 60 ° C, a decomposition final temperature of 50 ° C, and decomposition after 80 hours of decomposition.
  • the other processes and procedures are the same as in the first embodiment.
  • the catalytic decomposition of the stock solution A1 2 0 3 concentration of 40 ⁇ 200g / l, caustic ratio a k is 1.3 ⁇ 4.5, Na 2 O c concentration of 10 ⁇ 50g / l, Si0 2 concentration of 0.2 ⁇ 5g / l;
  • Catalytic decomposition of mother liquor A1 2 0 3 concentration is 10 ⁇ 50g/l, caustic ratio a k is 6.5 ⁇ 60, Na 2 O c concentration is l ⁇ 15g/l, Si0 2 concentration is 0.1 ⁇ lg/l; original slurry ore: a solids content of 300 ⁇ 500g / l, the ingredients calcium ratio of CaO f concentration of l ⁇ 50g / l, cycle mother liquor Na 2 O k concentration of 280 ⁇ 400g / l, circulating liquor caustic ratio of a k 6.5 60
  • the decomposition rate of catalytic decomposition is 70 ⁇ 85%; the particle size D 5Q of aluminum
  • the composite catalyst YHC was added to catalytic decomposition at a ratio of 230% by volume.
  • the composite catalyst YHC was composed of composite catalyst YHA (ethanol) and composite catalyst YHB (aluminum hydroxide) at 80%: 20
  • the liquid composite catalyst formed by mixing and mixing % by weight has a decomposition initial temperature of 65 ° C, a decomposition final temperature of 60 ° C, and separation after 50 hours of decomposition.
  • the other processes and procedures are the same as in the first embodiment.
  • the catalytic decomposition of the stock solution A1 2 0 3 concentration of 40 ⁇ 200g / l, caustic ratio a k is 1.3 ⁇ 4.5, Na 2 O c concentration of 10 ⁇ 50g / l, Si0 2 concentration of 0.2 ⁇ 5g / l;
  • Catalytic decomposition of mother liquor A1 2 0 3 concentration is 5 ⁇ 30g/l, caustic ratio a k is 10 100, Na 2 O c concentration is 0.5 ⁇ 10g/l, Si0 2 concentration is 0.004 ⁇ 0.5g/l;
  • solid content is 300 ⁇ 550g / l, calcium ingredient concentration ratio of CaO f l ⁇ 50g / l, Na 2 O k circulating liquor concentration of 280 ⁇ 400g / l, a k ratio of the caustic liquor cycles of 10 100;
  • the composite catalyst YHC is catalytically decomposed at a ratio of 300% of its volume.
  • the composite catalyst YHC is composed of a composite catalyst YHA (sterol) and a composite catalyst YHB (alumina) at 10%: 90
  • the liquid composite catalyst formed by mixing and mixing % by weight has a decomposition initial temperature of 80 ° C, a decomposition final temperature of 70 ° C, and a separation after 1.5 hours of decomposition.
  • the other processes and procedures are the same as in the first embodiment.
  • the catalytic decomposition of the stock solution A1 2 0 3 concentration of 40 ⁇ 200g / l, caustic ratio a k is 1.3 ⁇ 4.5, Na 2 O c concentration of 10 ⁇ 50g / l, Si0 2 concentration of 0.2 ⁇ 5g / l;
  • Catalytic decomposition of the mother A1 2 0 3 concentration is 32 ⁇ : lOOg/1, caustic ratio a k is 2 ⁇ 5.65, Na 2 O c concentration is 5 ⁇ 40g/l, Si0 2 concentration is 0.15 ⁇ 4.5g/l;
  • bauxite raw pulp a solids content of 200 ⁇ 300g / l, the concentration of the ingredients calcium ratio CaOf l ⁇ 50g / l, Na 2 O k circulating liquor concentration of 150 ⁇ 250g / l, a k ratio of the caustic liquor cycle 2 ⁇ 2.65;
  • the decomposition rate of catalytic decomposition is 20 ⁇ 50%; the particle size D
  • the composite catalyst YHC is catalytically decomposed at a ratio of 120% of its volume.
  • the composite catalyst YHC is composed of composite catalyst YHA (ethanol) and composite catalyst YHB (alumina) at 60%: 40
  • the liquid composite catalyst formed by mixing and mixing % by weight has a decomposition initial temperature of 30 ° C, a decomposition final temperature of 20 ° C, and decomposition after 20 hours of decomposition.
  • the other processes and procedures are the same as in the first embodiment.
  • the catalytic decomposition of the stock solution A1 2 0 3 concentration of 100 ⁇ 160g / l, caustic ratio a k is 1.3-1.8, Na 2 O c concentration of 10 ⁇ 50g / l, Si0 2 concentration of 0.2 ⁇ 5g / l;
  • Catalytic decomposition of mother liquor A1 2 0 3 concentration is 15 ⁇ 60g/l, caustic ratio a k is 4.5 ⁇ 40, Na 2 O c concentration is 2 ⁇ 20g/l, Si0 2 concentration is 0.1 ⁇ 2g/l; original slurry ore: a solids content of 300 ⁇ 1000g / l, the ingredients calcium ratio CaOf concentration of l ⁇ 50g / l, cycle mother liquor Na 2 O k concentration of 280 ⁇ 400g / l, circulating liquor caustic ratio of a k of 4.5 40;
  • the decomposition rate of catalytic decomposition is 70 ⁇ 95%;
  • the seed crystal decomposition + catalytic decomposition of Bayer process aluminum hydroxide or alumina production process sodium aluminate semen first seed crystal decomposition, followed by classification, graded overflow, underflow separation, two separation
  • the liquid phase is the seed mother liquid, and as the catalytic decomposition liquid solution, the catalytic decomposition and the subsequent process are continued, the solid phase return of the overflow separation continues the seed decomposition, and the solid phase of the underflow separation is washed to become the finished aluminum hydroxide, and the washing is performed.
  • Part of the generated washing liquid is washed to the red mud, and the other part is combined with the catalytic decomposition mother liquid to the mother liquid evaporation process, a part of the water is evaporated back to the red mud washing process, and the other part is returned to the washing process of the classified bottom flow branch of the seed crystal decomposition, and the evaporation mother liquid is evaporated. Return to the liquid alkali mixing process to continue the grinding of the ore.
  • the composite catalyst YHC is a liquid composite catalyst formed by mixing a composite catalyst YHA (sterol) and a composite catalyst YHB (aluminum hydroxide) in a weight percentage of 15%: 85%; catalytic decomposition decomposition liquid: A1 2 0 3 concentration 40 ⁇ 200g/l, caustic ratio a k is 1.3 4.5, Na 2 O c concentration is 10 ⁇ 50g/l, Si0 2 concentration is 0.2 ⁇ 5g/l; catalytic decomposition mother liquor: A1 2 0 3 concentration is 50 ⁇ 150g/l, caustic ratio a k is 2.5 ⁇ 5, Na 2 O c concentration is 10 ⁇ 40g/l, Si0 2 concentration is 0.15 ⁇ 4g/l; bauxite ore slurry: solid content is 200 ⁇ 300g/l ingredients calcium ratio of CaO f concentration of l ⁇ 50g / l, cycle mother liquor Na 2 O k concentration of 200 ⁇ 250g / l, circulating liquor caustic ratio of
  • the decomposition rate of catalytic decomposition is 30 ⁇ 50%; the particle size D 5Q of aluminum hydroxide product is 70 ⁇ 105 ⁇ ; the content of impurities of aluminum hydroxide product by weight percentage: Si0 2 0.005-5%, Fe 2 0 3 0.002-0.02% , Na 2 0 0.10 ⁇ 3.0%.

Description

一种拜耳法氢氧化铝或氧化铝的生产工艺 技术领域
本发明属于氢氧化铝或氧化铝的生产工艺技术领域， 具体涉及了一种 拜耳法氢氧化铝或氧化铝的生产工艺。 背景技术
传统的拜耳法氢氧化铝或氧化铝的生产工艺， 整个生产过程包括铝土 矿的破碎、 原矿浆的制备、 溶出、 溶出矿浆稀释、 赤泥分离洗涤、 粗液精 制、 精液晶种分解、 氢氧化铝处理、 母液蒸发、 氢氧化铝焙烧等， 生产工 艺流程见图 1。传统的拜耳法氢氧化铝或氧化铝的生产工艺中，铝土矿配料 固含量一般为 150~400g/l , 配料钙比为 1.0~2.0(CaOf约 7~70g/l) , 循环母液 的 Na2Ok浓度为 180~300g/l , 循环母液的苛性比 ak为 2.5~3.5。 传统的拜耳 法氢氧化铝或氧化铝的生产工艺釆用传统的晶种分解工艺， 精液中 A1203 浓度为 120~190g/l , 苛性比 ak为 1.45 1.70, 硅量指数 200以上， 分解初温 为 50~75 °C , 分解时间一般 30~72h, 不加催化剂， 只在强调粒度时添加五 氧化二磷等添加剂， 分解终点的分解母液 A1203浓度为 70~120g/l , 苛性比 ak为 2.0~3.5之间， 分解终温 30~50°C , 分解率一般为 30~55%, 氢氧化铝 产品粒度 D5Q—般为 1~80μπι的砂状或面状。 因此，传统的拜耳法氢氧化铝 或氧化铝的生产工艺不仅存在着铝土矿配料要求高、 分解率偏低、 氢氧化 铝产品粒度可控性差的缺陷， 而且分解母液中的氧化铝含量、 二氧化硅含 量偏高， 限制了蒸发效率的提高， 母液蒸发的结疤程度严重， 不利于系统 的正常运转、 产能的提高及能耗的降低。 发明内容
为克服现有技术的不足， 本发明的目的就是在于提供一种拜耳法氢氧 化铝或氧化铝的生产工艺， 该工艺降低了铝土矿的配料要求、 分解率大幅 度提高、 氢氧化铝产品粒度粗细可控， 同时分解母液中的氧化铝含量大幅 度下降， 二氧化硅含量也有所下降， 从而使蒸发效率明显提高， 母液蒸发 的结疤程度减轻， 有利于系统的正常运转、 产能提高及降低能耗。 为实现上述目的， 本发明釆取的技术方案如下： 一种拜耳法氢氧化铝 或氧化铝的生产工艺， 包括铝土矿的破碎、 原矿浆的制备、 溶出、 溶出矿 浆稀释、 赤泥分离洗涤、 铝酸钠粗液精制、 铝酸钠精液分解、 氢氧化铝处 理、 母液蒸发、 氢氧化铝焙烧， 其特别之处在于： 所述的铝酸钠精液分解 以铝酸钠精液为催化分解原液，并以其体积的 1~300%的比例在催化分解原 液中加入由复合催化剂 YHA和复合催化剂 YHB混合调配形成的复合催化 剂 YHC进行催化分解， 分解初温为 30~80°C , 分解终温为 20~70°C , 分解 时间为 1.5~80h, 其中所述的复合催化剂 YHA由表面活性剂、 醇类、 酯类 之其中一种或两种以上以任意比例混合而成， 其中所述的复合催化剂 YHB 由糖类、 无机类之其中一种或两种以任意比例混合而成。 制备复合催化剂 YHA、 YHB、 YHC时的混合工艺均属于现有技术，且制备复合催化剂 YHA、 YHB 时各种之间的混合比例以及制备复合催化剂 YHC 时的复合催化剂 YHA和复合催化剂 YHB之间的混合比例均可根据料浆的成分不同结合分 解制度进行调整， 以达到所生产需求的分解率、 氢氧化铝产品的粒度、 氢 氧化铝产品的杂质含量为准。
具体地， 所述的氢氧化铝或氧化铝的生产工艺按以下步骤进行： 铝土 矿、 石灰、 碱液首先进行原料磨矿， 制成原矿浆， 原矿浆预脱硅后进行管 道化溶出， 稀释后进行赤泥分离， 赤泥分离的底流进行赤泥洗涤， 洗涤的 固相为赤泥弃之， 洗涤的液相则返回用于稀释， 赤泥分离的溢流为铝酸钠 粗液， 叶滤后， 固相返回继续赤泥分离， 液相则为铝酸钠精液， 并以其为 催化分解原液且以其体积的 1~300%的比例在催化分解原液中加入复合催 化剂 YHA和复合催化剂 YHB混合调配形成的复合催化剂 YHC进行催化 分解， 分解初温为 30~80°C , 分解终温为 20~70°C , 分解 1.5~80h后进行分 离， 分离的液相滤液进行催化剂回收， 催化剂的具体回收方法可以依据药 剂的不同性质分别选择分离、 蒸馏或蒸发等常规固 -液、 固-固分离工艺， 回 收的药剂分别为复合催化剂 YHA和复合催化剂 YHB, 返回循环使用， 回 收后的残液作为催化分解母液送去母液蒸发工序， 分离的固相滤饼经洗涤 成为氢氧化铝成品， 干燥得到干燥氢氧化铝成品， 焙烧得到氧化铝成品， 同时固相滤饼洗涤产生的洗液同样经过催化剂回收工序， 回收的复合催化 剂 YHA和复合催化剂 YHB同样返回循环使用， 残液同样作为催化分解母 液送去母液蒸发工序， 蒸发回水去赤泥洗涤工序， 蒸发母液则返回液碱调 配工序继续原矿的磨制。
进一步地， 铝酸钠精液还可以先晶种分解， 而后以种分母液作为催化 分解原液进行催化分解。
具体地， 铝酸钠精液晶种分解之后进行分级， 分级的溢流、 底流分别 进行分离， 两次分离的液相均为种分母液， 同时作为催化分解原液进行催 化分解和后续的处理工序， 溢流分离的固相返回继续晶种分解， 底流分离 的固相经洗涤成为氢氧化铝成品， 而洗涤产生的洗液一部分去赤泥洗涤， 另一部分与催化分解母液共去母液蒸发工序， 蒸发回水一部分去赤泥洗涤 工序， 另一部分返回晶种分解的分级底流支路的洗涤工序， 蒸发母液则返 回液碱调配工序继续原矿的磨制。
进一步地， 所述的表面活性剂为溴代十六烷基吡啶、 乙一烷基氨基乙 基咪唑啉、 十二烷基苯横酸钠或琥珀酸二乙辞酯磺酸钠； 所述的醇类为曱 醇、 乙醇、 丙三醇、 正十六醇或正丁醇； 所述的酯类为乙酸乙酯、 乙酸苯 酯或苯曱酸曱酯； 所述的糖类为蔗糖、 葡萄糖、 果糖或麦芽糖； 所述的无 机类为氢氧化铝、 氟化铝或氧化铝。
再进一步地， 催化分解原液中： A1203浓度为 40~200g/l, 苛性比 ak为 1.3-4.5, Na2Oc ;¾度为 10~50g/l, Si02浓度为 0.2~5g/l。
再进一步地， 催化分解母液中： A1203浓度为 5~150g/l, 苛性比 ak为 1.5-100, Na2Oc浓度为 0.5~40g/l, Si02浓度为 0.004~4.5g/l。
更进一步地， 铝土矿原矿浆中： 固含量为 200~1000g/l, 配料钙比 CaOf 浓度为 l~50g/l, 循环母液 Na2Ok浓度为 150~400g/l, 循环母液苛性比 ak为 1.30〜亂
所述催化分解的分解率为 20~95%, 正常情况下都在 60%以上； 氢氧化 铝产品粒度 D5()为 0.3~110μπι, 可以根据生产要求控制在某一区段内； 按重 量百分比计，氢氧化铝产品杂质含量为： Si02 0.005-5%, Fe203 0.002-0.02%, Na2O 0.10~3.0%。
本发明的工艺原理也是拜耳法氢氧化铝或氧化铝生产的基本工艺原 理：
Α1203·(1或
Figure imgf000005_0001
2NaAl (OH) 4+aq 与传统拜耳法氢氧化铝或氧化铝生产的基本工艺原理相比：
传统拜耳法氢氧化铝或氧化铝生产的基本工艺原理其方程式从左边到 右边的过程是铝土矿的溶出过程， 方程式从右边到左边的过程是铝酸钠溶 液（精液） 的种子分解过程。
本发明拜耳法氢氧化铝或氧化铝生产的基本工艺原理其方程式从左边 到右边的过程是铝土矿的溶出过程， 方程式从右边到左边的过程是铝酸钠 溶液（精液） 的催化分解过程或种子分解 +催化分解过程。
相对于现有技术， 本发明的优点在于： 本发明的方法由于催化剂的加 入， 同时催化剂可以循环使用， 降低了铝土矿的配料要求， 分解率得到了 大幅度的提高， 分解母液也发生了根本性的变化， 分解母液中的氧化铝含 量大幅度下降， 二氧化硅含量也有所下降， 从而使蒸发效率明显提高， 母 液蒸发的结疤程度减轻， 有利于系统的正常运转、 产能提高及降低能耗； 氢氧化铝或氧化铝成品粒度粗细可控， 可以根据生产要求控制在某一区间 内， 经济效益发生重大变化； 氢氧化铝或氧化铝成品杂质含量可以根据催 化分解原液——铝酸钠精液或种分母液的质量、 分解制度、 复合催化剂的 添加比例进行有效地控制。 附图说明
图 1 : 传统的晶种分解拜耳法氢氧化铝或氧化铝的生产工艺流程图； 图 2: 本发明实施例 1~6的催化分解拜耳法氢氧化铝或氧化铝的生产 工艺流程图；
图 3: 本发明实施例 7的晶种分解 +催化分解拜耳法氢氧化铝或氧化铝 的生产工艺流程图。 具体实施方式
以下结合具体实施例和附图对本发明作进一步的详细说明， 但本发明 的保护范围并不局限于此：
实施例 1
如图 2所示的催化分解拜耳法氢氧化铝或氧化铝的生产工艺流程图： 铝土矿、 石灰、 碱液首先进行原料磨矿， 制成原矿浆， 原矿浆预脱硅后进 行管道化溶出， 稀释后进行赤泥分离， 赤泥分离的底流进行赤泥洗涤， 洗 涤的固相为赤泥弃之， 洗涤的液相则返回用于稀释， 赤泥分离的溢流为铝 酸钠粗液， 叶滤后， 固相返回继续赤泥分离， 液相则为铝酸钠^"液， 并以 其为催化分解原液，且以其体积的 1%的比例在催化分解原液中加入复合催 化剂 YHC进行催化分解， 复合催化剂 YHC是由复合催化剂 YHA (按重量 百分比计， 曱醇 80%, 乙醇 20% )和复合催化剂 YHB (氢氧化铝）以 10%: 90%的重量百分比混合调配形成的液态复合催化剂， 分解初温为 40°C , 分 解终温为 20 °C , 分解 60h后进行分离， 分离的液相滤液进行催化剂回收， 回收的药剂分别为复合催化剂 YHA和复合催化剂 YHB, 返回循环使用， 回收的残液作为催化分解母液送去母液蒸发工序， 分离的固相滤饼经洗涤 成为氢氧化铝成品， 干燥得到干燥氢氧化铝成品， 焙烧得到氧化铝成品， 同时固相滤饼洗涤产生的洗液同样经过催化剂回收工序， 回收的复合催化 剂 YHA和复合催化剂 YHB同样返回循环使用， 液相同样作为催化分解母 液送去母液蒸发工序， 蒸发回水去赤泥洗涤工序， 蒸发母液则返回液碱调 配工序继续原矿的磨制。其中，催化分解原液中： A1203浓度为 100~180g/l , 苛性比 ak为 1.3~1.6, Na2Oc浓度为 10~50g/l , Si02浓度为 0.2~0.8g/l; 催化 分解母液中： A1203浓度为 60~120g/l , 苛性比 ak为 2.5~4.5 , Na2Oc浓度为 5~40g/l , Si02浓度为 0.1~0.7g/l; 铝土矿原矿浆中： 固含量为 250~400g/l , 配料钙比 CaOf浓度为 l~50g/l ,循环母液 Na2Ok浓度为 250~350g/l ,循环母 液苛性比 ak为 1.3 1.6; 催化分解的分解率为 30~60%； 氢氧化铝产品粒度 D50为 0.3~50μπι;按重量百分比计，氢氧化铝产品杂质含量： Si02 0.05-2%, Fe203 0.005-0.02%, Na20 0.15~0.60%。 实施例 2
在铝酸钠精液催化分解原液中， 以其体积的 50%的比例加入复合催化 剂 YHC进行催化分解， 复合催化剂 YHC由复合催化剂 YHA (乙醇）和复 合催化剂 YHB (氧化铝） 以 50%: 50%的重量百分比混合调配形成的液态 复合催化剂， 分解初温为 50°C , 分解终温为 40°C , 分解 60h后进行分离， 其它工序及流程均同实施例 1。 其中， 催化分解原液中： A1203浓度为 40~200g/l ,苛性比 ak为 1.3~4.5 , Na2Oc浓度为 10~50g/l , Si02浓度为 0.2~5g/l; 催化分解母液中： A1203浓度为 10~50g/l, 苛性比 ak为 4.5~40, Na2Oc浓度 为 2~10g/l, Si02浓度为 0.1~2g/l; 铝土矿原矿浆中： 固含量为 300~500g/l, 配料钙比 CaOf浓度为 l~50g/l,循环母液 Na2Ok浓度为 280~400g/l,循环母 液苛性比 ak为 4.5 40; 催化分解的分解率为 70~85%； 氢氧化铝产品粒度 D5Q为 20~80μπι;按重量百分比计，氢氧化铝产品杂质含量： Si02 0.005-5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。 实施例 3
在铝酸钠精液催化分解原液中，以其体积的 130%的比例加入复合催化 剂 YHC进行催化分解， 复合催化剂 YHC由复合催化剂 YHA (乙醇）和复 合催化剂 YHB (氢氧化铝） 以 40%: 60%的重量百分比混合调配形成的液 态复合催化剂，分解初温为 60 °C ,分解终温为 50°C ,分解 80h后进行分离， 其它工序及流程均同实施例 1。 其中， 催化分解原液中： A1203浓度为 40~200g/l,苛性比 ak为 1.3~4.5,Na2Oc浓度为 10~50g/l, Si02浓度为 0.2~5g/l; 催化分解母液中： A1203浓度为 10~50g/l, 苛性比 ak为 6.5~60, Na2Oc浓度 为 l~15g/l, Si02浓度为 0.1~lg/l; 铝土矿原矿浆中： 固含量为 300~500g/l, 配料钙比 CaOf浓度为 l~50g/l, 循环母液 Na2Ok 浓度为 280~400g/l, 循环 母液苛性比 ak为 6.5 60; 催化分解的分解率为 70~85%； 氢氧化铝产品粒 度 D5Q为 20~80μπι; 按重量百分比计， 氢氧化铝产品杂质含量： Si02 0.005-5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。 实施例 4
在铝酸钠精液催化分解原液中，以其体积的 230%的比例加入复合催化 剂 YHC进行催化分解， 复合催化剂 YHC由复合催化剂 YHA (乙醇）和复 合催化剂 YHB (氢氧化铝） 以 80%: 20%的重量百分比混合调配形成的液 态复合催化剂，分解初温为 65°C ,分解终温为 60°C ,分解 50h后进行分离， 其它工序及流程均同实施例 1。 其中， 催化分解原液中： A1203浓度为 40~200g/l,苛性比 ak为 1.3~4.5,Na2Oc浓度为 10~50g/l, Si02浓度为 0.2~5g/l; 催化分解母液中： A1203浓度为 5~30g/l, 苛性比 ak为 10 100, Na2Oc浓度 为 0.5~10g/l , Si02浓度为 0.004~0.5g/l ; 铝土矿原矿浆中： 固含量为 300~550g/l , 配料钙比 CaOf 浓度为 l~50g/l , 循环母液 Na2Ok浓度为 280~400g/l, 循环母液苛性比 ak为 10 100; 催化分解的分解率为 70~90%； 氢氧化铝产品粒度 D5Q为 1~80μπι; 按重量百分比计， 氢氧化铝产品杂质含 量： Si02 0.005 5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。 实施例 5
在铝酸钠精液催化分解原液中，以其体积的 300%的比例加入复合催化 剂 YHC进行催化分解， 复合催化剂 YHC由复合催化剂 YHA (曱醇）和复 合催化剂 YHB (氧化铝） 以 10%: 90%的重量百分比混合调配形成的液态 复合催化剂， 分解初温为 80°C , 分解终温为 70°C , 分解 1.5h后进行分离， 其它工序及流程均同实施例 1。 其中， 催化分解原液中： A1203浓度为 40~200g/l,苛性比 ak为 1.3~4.5,Na2Oc浓度为 10~50g/l, Si02浓度为 0.2~5g/l; 催化分解母中： A1203浓度为 32〜： lOOg/1, 苛性比 ak为 2~5.65, Na2Oc浓度 为 5~40g/l, Si02浓度为 0.15~4.5g/l;铝土矿原矿浆中：固含量为 200~300g/l, 配料钙比 CaOf浓度为 l~50g/l,循环母液 Na2Ok浓度为 150~250g/l,循环母 液苛性比 ak为 2~2.65； 催化分解的分解率为 20~50%； 氢氧化铝产品粒度 D50为 70~110μπι;按重量百分比计，氢氧化铝产品杂质含量： Si02 0.005-5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。 实施例 6
在铝酸钠精液催化分解原液中，以其体积的 120%的比例加入复合催化 剂 YHC进行催化分解， 复合催化剂 YHC是由复合催化剂 YHA (乙醇）和 复合催化剂 YHB (氧化铝） 以 60%: 40%的重量百分比混合调配形成的液 态复合催化剂，分解初温为 30°C ,分解终温为 20°C ,分解 20h后进行分离， 其它工序及流程均同实施例 1。 其中， 催化分解原液中： A1203浓度为 100~160g/l, 苛性比 ak为 1.3-1.8 , Na2Oc浓度为 10~50g/l, Si02浓度为 0.2~5g/l; 催化分解母液中： A1203浓度为 15~60g/l, 苛性比 ak为 4.5~40, Na2Oc浓度为 2~20g/l, Si02浓度为 0.1~2g/l; 铝土矿原矿浆中： 固含量为 300~1000g/l , 配料钙比 CaOf 浓度为 l~50g/l , 循环母液 Na2Ok浓度为 280~400g/l, 循环母液苛性比 ak为 4.5 40; 催化分解的分解率为 70~95%； 氢氧化铝产品粒度 D5Q为 0.3~80μπι; 按重量百分比计， 氢氧化铝产品杂质 含量： Si02 0.05-2%, Fe203 0.005-0.02%, Na20 0.15~3.0%„ 实施例 7
如图 3 所示的晶种分解 +催化分解拜耳法氢氧化铝或氧化铝的生产工 艺： 铝酸钠精液首先晶种分解， 之后进行分级， 分级的溢流、 底流分别进 行分离， 两次分离的液相均为种分母液， 并作为催化分解原液继续进行催 化分解和后续的工序， 溢流分离的固相返回继续晶种分解， 底流分离的固 相经洗涤成为氢氧化铝成品， 而洗涤产生的洗液一部分去赤泥洗涤， 另一 部分与催化分解母液共去母液蒸发工序，蒸发回水一部分去赤泥洗涤工序， 另一部分返回晶种分解的分级底流支路的洗涤工序， 蒸发母液则返回液碱 调配工序继续原矿的磨制。 其中， 复合催化剂 YHC是由复合催化剂 YHA (曱醇）和复合催化剂 YHB (氢氧化铝） 以 15%: 85%的重量百分比混合 调配形成的液态复合催化剂； 催化分解原液中： A1203浓度为 40~200g/l , 苛性比 ak为 1.3 4.5 , Na2Oc浓度为 10~50g/l , Si02浓度为 0.2~5g/l; 催化分 解母液中： A1203浓度为 50~150g/l , 苛性比 ak为 2.5~5 , Na2Oc浓度为 10~40g/l , Si02浓度为 0.15~4g/l; 铝土矿原矿浆中： 固含量为 200~300g/l , 配料钙比 CaOf浓度为 l~50g/l ,循环母液 Na2Ok浓度为 200~250g/l ,循环母 液苛性比 ak为 2.5~5； 其它工艺参数和工序均同实施例 3。 催化分解的分解 率为 30~50%； 氢氧化铝产品粒度 D5Q为 70~105μπι; 按重量百分比计， 氢 氧化铝产品杂质含量： Si02 0.005-5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。

Claims

权利要求书
1. 一种拜耳法氢氧化铝或氧化铝的生产工艺， 包括铝土矿的破碎、 原 矿浆的制备、 溶出、 溶出矿浆稀释、 赤泥分离洗涤、 铝酸钠粗液精制、 铝 酸钠精液分解、 氢氧化铝处理、 母液蒸发、 氢氧化铝焙烧， 其特征在于： 所述的铝酸钠精液分解以铝酸钠精液为催化分解原液， 并以其体积的 1~300%的比例在催化分解原液中加入由复合催化剂 YHA和复合催化剂 YHB 混合调配形成的复合催化剂 YHC 进行催化分解， 分解初温为 30-80 °C , 分解终温为 20~70°C , 分解时间为 1.5~80h, 其中所述的复合催 化剂 YHA由表面活性剂、 醇类、 酯类之其中一种或两种以上混合而成， 其 中所述的复合催化剂 YHB由糖类、 无机类之其中一种或两种混合而成。
2. 如权利要求 1所述的拜耳法氢氧化铝或氧化铝的生产工艺， 其特征 在于所述的氢氧化铝或氧化铝的生产工艺按以下具体步骤进行： 铝土矿、 石灰、 碱液首先进行原料磨矿， 制成原矿浆， 原矿浆预脱硅后进行管道化 溶出， 稀释后进行赤泥分离， 赤泥分离的底流进行赤泥洗涤， 洗涤的固相 为赤泥弃之， 洗涤的液相则返回用于稀释， 赤泥分离的溢流为铝酸钠粗液， 叶滤后， 固相返回继续赤泥分离， 液相则为铝酸钠精液， 并以其为催化分 解原液且以其体积的 1 ~300%的比例在催化分解原液中加入由复合催化剂 YHA和复合催化剂 YHB混合调配形成的复合催化剂 YHC进行催化分解， 分解初温为 30~80°C , 分解终温为 20~70°C , 分解 1.5~80h后进行分离， 分 离的液相滤液进行催化剂回收，回收的药剂分别为复合催化剂 YHA和复合 催化剂 YHB, 返回循环使用， 回收后的残液作为催化分解母液送去母液蒸 发工序， 分离的固相滤饼经洗涤成为氢氧化铝成品， 干燥得到干燥氢氧化 铝成品， 焙烧得到氧化铝成品， 同时固相滤饼洗涤产生的洗液同样经过催 化剂回收工序， 回收的复合催化剂 YHA和复合催化剂 YHB同样返回循环 使用， 残液同样作为催化分解母液送去母液蒸发工序， 蒸发回水去赤泥洗 涤工序， 蒸发母液则返回液碱调配工序继续原矿的磨制。
3. 如权利要求 1所述的拜耳法氢氧化铝或氧化铝的生产工艺， 其特征 在于： 铝酸钠精液先晶种分解， 而后以种分母液作为催化分解原液进行催 化分解。
4. 如权利要求 2所述的拜耳法氢氧化铝或氧化铝的生产工艺， 其特征 在于： 铝酸钠精液先晶种分解， 而后以种分母液作为催化分解原液进行催 化分解。
5. 如权利要求 4所述的拜耳法氢氧化铝或氧化铝的生产工艺， 其特征 在于： 铝酸钠精液晶种分解之后进行分级， 分级的溢流、 底流分别进行分 离， 两次分离的液相均为种分母液， 同时作为催化分解原液进行催化分解 和后续的处理工序， 溢流分离的固相返回继续晶种分解， 底流分离的固相 经洗涤成为氢氧化铝成品， 而洗涤产生的洗液一部分去赤泥洗涤， 另一部 分与催化分解母液共去母液蒸发工序， 蒸发回水一部分去赤泥洗涤工序， 另一部分返回晶种分解的分级底流支路的洗涤工序， 蒸发母液则返回液碱 调配工序继续原矿的磨制。
6. 如权利要求 1~5之任意一项所述的拜耳法氢氧化铝或氧化铝的生产 工艺， 其特征在于： 所述的表面活性剂为溴代十六烷基吡啶、 乙一烷基氨 基乙基咪唑啉、 十二烷基苯横酸钠或琥珀酸二乙辞酯磺酸钠； 所述的醇类 为曱醇、 乙醇、 丙三醇、 正十六醇或正丁醇； 所述的酯类为乙酸乙酯、 乙 酸苯酯或苯曱酸曱酯； 所述的糖类为蔗糖、 葡萄糖、 果糖或麦芽糖； 所述 的无机类为氢氧化铝、 氟化铝或氧化铝。
7. 如权利要求 1~5之任意一项所述的拜耳法氢氧化铝或氧化铝的生产 工艺， 其特征在于： 催化分解原液中： A1203浓度为 40~200g/l, 苛性比 ak 为 1.3~4.5, Na2Oc ;¾度为 10~50g/l, Si02浓度为 0.2~5g/l。
8. 如权利要求 2或 4或 5所述的拜耳法氢氧化铝或氧化铝的生产工艺， 其特征在于：催化分解母液中： A1203浓度为 5~150g/l,苛性比 ak为 1.5 100, Na2Oc浓度为 0.5~40g/l, Si02浓度为 0.004~4.5g/l。
9. 如权利要求 1~5之任意一项所述的拜耳法氢氧化铝或氧化铝的生产 工艺， 其特征在于： 铝土矿原矿浆中： 固含量为 200~1000g/l, 配料钙比 CaOf 浓度为 l~50g/l,循环母液 Na2Ok浓度为 150~400g/l,循环母液苛性比 ak为 1.30 100。
10. 如权利要求 1~5之任意一项所述的拜耳法氢氧化铝或氧化铝的生 产工艺， 其特征在于： 催化分解的分解率为 20~95%； 氢氧化铝产品粒度 D50为 0.3~110μπι ; 按重量百分比计， 氢氧化铝产品杂质含量： Si02 0.005-5%, Fe203 0.002-0.02%, Na20 0.10~3.0%。
PCT/CN2009/070631 2009-02-24 2009-03-04 一种拜耳法氢氧化铝或氧化铝的生产工艺 WO2010135856A1 (zh)

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