CN109704376B - Bayer process production method for co-producing chemical aluminum oxide - Google Patents
Bayer process production method for co-producing chemical aluminum oxide Download PDFInfo
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Abstract
The invention relates to the technical field of alumina production, and particularly discloses a method for producing alumina by a Bayer process and co-producing chemicals. The method is characterized in that causticized liquid obtained by a pseudo-boehmite production system or superfine aluminum hydroxide product washing liquid in a superfine aluminum hydroxide production system is sent to the middle of a mud layer of a red mud separation settling tank to any position between the upper parts of red mud primary washing settling tanks, and the causticized liquid or the superfine aluminum hydroxide product washing liquid enters the red mud primary washing settling tank along with the red mud underflow of the red mud separation settling tank. The causticized liquid or the ultrafine aluminum hydroxide product washing liquid is digested and absorbed in a Bayer process production system, so that the evaporation steam consumption is saved. The method can also effectively solve the problem of sodium aluminate solution hydrolysis in the Bayer process production system, and the digestion step can further reduce the molecular ratio of the digested slurry and improve the cycle efficiency, so that the bottleneck problem of low yield of the Bayer process production system can be effectively solved, and an ideal way for energy conservation, consumption reduction and cycle efficiency improvement of the Bayer process is found.
Description
Technical Field
The invention relates to the technical field of alumina production, in particular to a method for producing alumina by Bayer process co-production chemicals, and especially relates to a method for producing pseudoboehmite by Bayer process co-production or a method for producing superfine aluminum hydroxide by Bayer process co-production.
Background
Chemical alumina means aluminum hydroxide, alumina and aluminum-containing compounds other than alumina for producing aluminum ingots, including, for example, ultrafine aluminum hydroxide and pseudo-boehmite. By taking pseudo-boehmite as an example, the pseudo-boehmite is also called pseudo-boehmite and is also called monohydrate alumina, which is an aluminum hydroxide series chemical product and is thixotropic gel in a water-containing state. The space structure of the pseudo-boehmite is a net shape, and the single degree of the microstructure phase of the crystal is relatively high; at the same time, it is also strongerPeptity and cohesiveness; in addition, it has the characteristics of high specific surface area, large pore volume and the like. Due to the physical properties of the pseudoboehmite, the pseudoboehmite is mostly used as a drying agent, a catalyst and a carrier raw material in life, and a derivative product thereof can be widely used in petrochemical industry, nitrogen fertilizer, environmental protection, medicine manufacturing and fire-proof technical materials. The pseudoboehmite is an important intermediate product for preparing active alumina and belongs to a special alumina. Gamma-Al converted from pseudoboehmite by heating2O3The catalyst and the carrier thereof are commonly used as the catalyst and the carrier thereof, which are the most widely used catalyst and carrier raw materials thereof, and account for about 70 percent of the industrial supported catalyst. At present, manufacturers for producing pseudoboehmite mainly comprise Shandong branch of China aluminum thigh (Shandong Zibo), Shanxi aluminum factory (Shanxi river jin), Zhongai Guizhou branch (Guizhou Guiyang) and Wenzhou Jing alumina Co., and the total capacity is 5.5 million tons/year. The annual demand of the actual domestic pseudo-boehmite market is about 7.5 ten thousand tons, the gap is about 2.5 ten thousand tons, and the market prospect of the pseudo-boehmite is wide.
The manufacturing method of chemical alumina is more, at present, China mostly relies on alumina enterprises to produce chemical alumina, such as pseudoboehmite products, and figure 1 shows a flow chart of a production and preparation process for distributing partial Bayer process concentrate liquid from Bayer process concentrate liquid to be used for the pseudoboehmite products. In the existing technological process for producing pseudoboehmite by relying on alumina enterprises, most Bayer process refined solution enters a seed precipitation decomposition tank, alumina for aluminum ingots is produced according to the conventional Bayer process, and a small part of Bayer process refined solution enters a carbon precipitation decomposition tank for carbon precipitation to prepare the pseudoboehmite. The neutralizer for decomposing carbon component is industrial CO2A gas. The pseudo-boehmite product is produced by depending on alumina enterprises, the operation is simple, the cost is lower, zero emission and no pollution in environmental protection can be realized, and the produced product is a common pseudo-boehmite product. The pseudoboehmite production process mainly adopts the technical conditions of low temperature, low concentration and rapid carbon decomposition, wherein the decomposed pseudoboehmite needs a large amount of water washing, and each 1 ton of the pseudoboehmite is produced by 49 tons of water washing. As shown in figure 1, washing in a filtering and washing tank to obtain a pseudo-boehmite product, and sending primary washing water with Nk (caustic alkali concentration) of 7-9 g/L to prepare lime milk; part of the secondary washing water with Nk of about 0.5g/L is used for diluting Bayer process refined liquid from a Bayer process system, and the other part of the secondary washing water is used as red mud washing water of the Bayer process system. The filtered mother liquor after the carbonization mainly contains carbon alkali, lime milk is needed to causticize until Nk is 20-40 g/L, then the filtered mother liquor is introduced into a Bayer process system, the filtered mother liquor enters the Bayer process system and is sent to an evaporation system, and the filtered mother liquor needs to be evaporated until Nk is 230-250 g/L, so that the evaporation steam consumption is greatly increased, and the production cost is increased. Similarly, when the superfine aluminum hydroxide is co-produced by the bayer process, the superfine aluminum hydroxide product obtained by production also needs a large amount of water for washing, a large amount of superfine aluminum hydroxide product washing liquor can be generated, and the superfine aluminum hydroxide product washing liquor also enters an evaporation system at present, so that the evaporation steam consumption is increased, and the production cost is increased, as shown in fig. 2.
For a Bayer process system, the ore pulp after high-pressure dissolution needs to be settled and separated out of red mud after being diluted by a dilution desilication tank, and the step is completed in a red mud separation settling tank. The overflow of the red mud separation settling tank is crude liquid, and the Bayer process refined liquid is obtained by refining through a leaf filter. It has been found during the production process that the molecular ratio of the bayer process liquor (i.e. the molar ratio of sodium oxide to alumina in the liquor) tends to be higher than that of the digestion slurry, due to hydrolysis of the sodium aluminate liquor. The hydrolysis products of the sodium aluminate solution are aluminum hydroxide and sodium hydroxide, the aluminum hydroxide enters the red mud to be discharged, and the sodium hydroxide is left in the refined liquor of the Bayer process, so that the molecular ratio of the refined liquor is increased; the aluminum hydroxide entering the discharged red mud causes the loss of aluminum hydroxide products. Hydrolysis of the low molecular ratio, medium concentration sodium aluminate solution is inevitable because of the high degree of supersaturation of the solution and the poor stability of the solution. The hydrolysis mainly occurs in the underflow part of the red mud separation and sedimentation tank, the molecular ratio of the washing liquid of the red mud is increased after the red mud is washed, and the molecular ratio of the liquid phase is increased when the washing liquid is used for diluting the digestion slurry. In the alumina industry, in order to solve the hydrolysis problem of a settling system, the molecular ratio of dissolved slurry in a dissolving step cannot be too low so as to reduce hydrolysis, but the molecular ratio of the dissolved slurry can seriously influence the yield increase and the circulation efficiency of a Bayer process, and the contradiction becomes the bottleneck problem of low yield increase of an alumina Bayer process production system.
Disclosure of Invention
The invention mainly solves the technical problem of providing a method for producing Bayer process co-production chemical alumina, wherein the chemical alumina can be pseudoboehmite or superfine aluminum hydroxide.
In order to solve the technical problems, the invention adopts the technical scheme that: a method for producing aluminum oxide by Bayer process with chemicals comprises making aluminum oxide into pseudoboehmite or superfine aluminum hydroxide;
when the produced chemical alumina is pseudo-boehmite, causticizing a filtering mother liquor subjected to carbon decomposition in a pseudo-boehmite production system to Nk of 20-50 g/L by lime emulsion to obtain causticized liquor, then sending the causticized liquor to any position between the middle part of a mud layer of a red mud separation settling tank and the upper part of a red mud primary washing settling tank, and sending the causticized liquor into the red mud primary washing settling tank along with the red mud underflow of the red mud separation settling tank;
when the produced chemical aluminum oxide is superfine aluminum hydroxide, the superfine aluminum hydroxide product washing liquid is sent to the middle of the mud layer of the red mud separation settling tank to any position between the upper parts of the red mud primary washing settling tanks, and the superfine aluminum hydroxide product washing liquid enters the red mud primary washing settling tank along with the red mud underflow of the red mud separation settling tank.
Furthermore, the Nk of the superfine aluminum hydroxide product washing liquid is 30-70 g/L.
Preferably, the causticized liquid is sent to the middle lower part of a mud layer of the red mud separation and sedimentation tank. Because the hydrolysis of the sodium aluminate solution mainly occurs in the underflow part of the red mud separation and sedimentation tank, the causticized liquid is sent to the middle lower part of the mud layer of the red mud separation and sedimentation tank, the molecular ratio of the liquid phase in the underflow part of the red mud separation and sedimentation tank can be improved, and the hydrolysis occurrence is effectively reduced.
Preferably, the washing liquid of the superfine aluminum hydroxide product is sent to the middle lower part of the mud layer of the red mud separation and sedimentation tank. Similarly, the hydrolysis of the sodium aluminate solution mainly occurs in the underflow part of the red mud separation and sedimentation tank, and the ultrafine aluminum hydroxide product washing liquid is sent to the middle lower part of the mud layer of the red mud separation and sedimentation tank, so that the molecular ratio of the liquid phase in the underflow part of the red mud separation and sedimentation tank can be improved, and the hydrolysis occurrence can be effectively reduced.
Preferably, after the causticized solution enters the red mud separation and sedimentation tank, slurry distribution of a sodium aluminate solution crude solution with an upper molecular ratio of 1.3-1.6 and a lower liquid phase molecular ratio of 1.6-2.5 is formed in the red mud separation and sedimentation tank.
Preferably, after the superfine aluminum hydroxide product washing liquor enters the red mud separation and sedimentation tank, slurry distribution of a sodium aluminate solution crude liquid with an upper molecular ratio of 1.3-1.6 and a lower liquid phase molecular ratio of 1.6-2.5 is formed in the red mud separation and sedimentation tank.
The red mud separating and settling tank is used for settling and separating out red mud, supernatant in the red mud separating and settling tank overflows to a sodium aluminate solution collecting container, the supernatant is sent to decompose and separate out aluminum hydroxide through leaf filtration, and concentrated red mud discharged from a slag discharging port is underflow. The upper part in the red mud separation and sedimentation tank is a sodium aluminate solution crude liquid layer, and the lower part is a concentrated red mud slurry layer containing the red mud and the sodium aluminate solution crude liquid, namely a mud layer. After the causticized liquid or the superfine aluminum hydroxide product washing liquid enters the red mud separation and sedimentation tank, the molecular ratio of a sodium aluminate solution crude liquid layer at the upper part in the red mud separation and sedimentation tank is 1.3-1.6, and the molecular ratio of a concentrated red mud slurry layer liquid phase containing the red mud and the sodium aluminate solution crude liquid at the lower part is 1.6-2.5.
More preferably, in the red mud separation and sedimentation tank, the molecular ratio of the sodium aluminate solution region from the liquid level position at the top of the red mud separation and sedimentation tank to 1 m below the liquid level is 1.3-1.6, and the molecular ratio of the liquid phase from the discharge port at the bottom of the red mud separation and sedimentation tank to the slurry region 1 m upwards along the vertical height direction is 1.6-2.5.
The liquid-phase molecular ratio of the red mud layer at the lower part of the red mud separation and sedimentation tank is increased, namely the liquid-phase molecular ratio of the underflow is increased, and the hydrolysis of the sodium aluminate solution is effectively inhibited.
The invention provides a production method for coproducing chemical alumina by a Bayer process, which is characterized in that causticized liquid or superfine aluminum hydroxide product washing liquid is sent into a red mud separation and sedimentation tank of a Bayer process production system, enters the middle lower part of a mud layer of the red mud separation and sedimentation tank, and reaches a red mud primary washing and sedimentation tank after being washed with diluted underflow. On one hand, the causticized liquid or the ultrafine aluminum hydroxide product washing liquid is digested and absorbed in a Bayer process production system, evaporation and concentration are not needed, and evaporation steam consumption is saved. On the other hand, the causticized liquid or the superfine aluminum hydroxide product washing liquid enters the red mud one-time washing and settling tank, and the hydrolysis of the sodium aluminate solution in a Bayer process settling system can be effectively inhibited. The bottom flow of the original red mud separation and sedimentation tank (the bottom flow of the sodium aluminate solution in the bottom flow) is low-molecular-ratio and medium-supersaturated sodium aluminate solution, has high solid content, low temperature and poor stability, is very easy to hydrolyze to separate out aluminum hydroxide, and the separated aluminum hydroxide enters the red mud to cause the loss of the aluminum hydroxide. Before the washing liquid or the causticized liquid of the superfine aluminum hydroxide product is sent to the bottom of a mud layer of a red mud separation and sedimentation tank, the causticized alkali concentration of the slurry in the red mud separation and sedimentation tank is 80-180 g/L, the solid content of the red mud is 30-900 g/L, the solid aluminum-silicon ratio is 1.0-1.5, the solid content is high, and the stability is poor. The causticizing liquid or the superfine aluminum hydroxide product washing liquid is sent into the red mud separation and sedimentation tank of the Bayer process production system and enters the middle lower part of the mud layer of the red mud separation and sedimentation tank, so that the supersaturation degree and the solid content of the bottom flow liquid of the red mud separation and sedimentation tank can be reduced, the molecular ratio can be improved by mixing the causticizing liquid or the superfine aluminum hydroxide product washing liquid mainly containing caustic alkali with the mud layer or the bottom flow of the red mud separation and sedimentation tank, and the hydrolysis is effectively inhibited. The method can effectively solve the problem of hydrolysis of the sodium aluminate solution, so that the molecular ratio of the dissolved slurry can be further reduced in the dissolving step, and the circulation efficiency is improved. Therefore, the bottleneck problem of the yield increase and the weakness of the Bayer process production system can be effectively solved, and an ideal way for the Bayer process to save energy, reduce consumption and improve the cycle efficiency is found.
Drawings
FIG. 1 is a flow chart of a process for producing pseudo-boehmite by an existing alumina enterprise;
FIG. 2 is a flow chart of a process for producing ultrafine aluminum hydroxide by an existing alumina enterprise;
FIG. 3 is a flow chart of the process for producing pseudo-boehmite by an improved alumina enterprise according to the present invention;
FIG. 4 is a flow chart of the process for producing ultra-fine aluminum hydroxide by the improved alumina enterprises of the present invention.
Detailed Description
The technical solution of the present invention will be described in detail by specific examples.
Example 1
Some alumina manufacturing company a carries out the production according to the process flow shown in fig. 1. The technological parameters are as follows:
dissolving slurry: 200m3Nk 260g/L, alpha k 1.41, red mud A/S1.21;
primary washing liquid of red mud: nk 58g/L,. alpha.k 1.59, 180m3/h；
Diluting desilication tank slurry: nk 165g/L, α k 1.45;
bottom flow of red mud separation settling tank: nk 166g/L,. alpha.k 1.55;
discarding the red mud: A/S1.25;
bayer process concentrate liquid: α k 1.48.
The method is improved, and the improved process flow chart is shown in figure 3, and the specific improvement is as follows:
causticizing the filtered mother liquor after decomposing carbon in the pseudoboehmite production system to Nk of 21g/L by lime milk to obtain causticized liquid, then sending the causticized liquid to the middle lower part of a mud layer of a red mud separation and sedimentation tank, and adding the causticized liquid 40m in 5 parts3Then, the red mud underflow of the red mud separation settling tank enters a red mud primary washing settling tank, the red mud primary washing liquid overflowing from the red mud primary washing settling tank enters the red mud separation settling tank through a dilution desiliconization tank, and slurry distribution of a sodium aluminate solution crude liquid with an upper molecular ratio of 1.46 and a lower molecular ratio of 1.71 is formed in the red mud separation settling tank; wherein, before the causticized liquid is sent to the lower part of a mud layer of the red mud separation and sedimentation tank, the causticized alkali concentration of the slurry in the red mud separation and sedimentation tank is 165g/L, the solid content of the red mud is 800g/L, and the solid aluminum-silicon ratio is 1.23.
The improved process is adopted, and the process parameters are as follows:
underflow of the red mud separation settling tank: nk 110g/L, α k 1.71;
primary washing liquid of red mud: nk 50g/L, α k 1.72;
diluting desilication tank slurry: nk 164g/L,. alpha.k 1.46;
discarding the red mud: A/S1.22;
bayer process concentrate liquid: α k 1.48.
Obviously, it can be seen from the underflow liquid phase of the red mud separation settling tank, the red mud primary washing liquid α k and the red mud a/S:
the alpha k of the original red mud primary washing liquid is 1.59, the alpha k value is changed into 1.72 after improvement, the alpha k value is obviously increased, the molecular ratio alpha k value is actively improved by the intervention of pure caustic alkali solution, the stability of the solution is increased, and the loss of alumina caused by passive hydrolysis is avoided;
underflow liquid phase of the original red mud separation settling tank: nk 166g/L and alpha k 1.55, which are Nk 110g/L and alpha k 1.71 after improvement, the Nk value is reduced, the alpha k value is increased, the solution concentration is reduced, the underflow dilution effect is realized, and good conditions are created for the subsequent washing and sedimentation of the red mud;
the red mud A/S of the digestion slurry is 1.21, the original abandoned red mud A/S is 1.25, the improved abandoned red mud A/S is 1.22, which is obviously reduced compared with the original abandoned red mud and is close to the aluminum-silicon ratio of the red mud of the digestion slurry, and further shows that the value of the molecular ratio alpha k of the bottom flow solution of the red mud separation and sedimentation tank is actively improved, and the increase of the abandoned red mud A/S caused by the hydrolysis of alumina in the solution entering the red mud is inhibited.
The analysis shows that the hydrolysis of the sodium aluminate solution in the Bayer process production system is inhibited after the improvement, the hydrolysis loss is saved, the bottom flow of the red mud separation settling tank is diluted, the red mud settling and washing efficiency is improved, 35 tons of water are evaporated less per hour by evaporation, and the evaporation energy consumption is obviously reduced.
Example 2
Some alumina manufacturing company B performs the manufacturing according to the process flow shown in fig. 1. The technological parameters are as follows:
dissolving slurry: 320m3H, Nk 280g/L, alpha k 1.38, red mud A/S1.18;
primary washing liquid of red mud: nk 61g/L,. alpha.k 1.57, 300m3/h；
Diluting desilication tank slurry: nk 168g/L, α k 1.42;
bottom flow of red mud separation settling tank: nk 165g/L,. alpha.k 1.53;
discarding the red mud: A/S1.21;
bayer process concentrate liquid: α k 1.45.
The method is improved, and the improved process flow chart is shown in figure 3, and the specific improvement is as follows:
causticizing the filtered mother liquor after decomposing carbon in the pseudoboehmite production system to Nk of 50g/L by lime milk to obtain causticized liquid, then sending the causticized liquid to the middle lower part of a mud layer of a red mud separation and sedimentation tank, and adding the causticized liquid 60m in 6 parts3Then, the red mud underflow of the red mud separation settling tank enters a red mud primary washing settling tank, the red mud primary washing liquid overflowing from the red mud primary washing settling tank enters the red mud separation settling tank through a dilution desiliconization tank, and slurry distribution of a sodium aluminate solution crude liquid with an upper molecular ratio of 1.49 and a lower molecular ratio of 2.21 is formed in the red mud separation settling tank; wherein, before the causticized liquid is sent to the lower part of a mud layer of the red mud separation and sedimentation tank, the concentration of causticization alkali in the slurry in the red mud separation and sedimentation tank is 167g/L, the solid content of the red mud is 750g/L, and the solid aluminum-silicon ratio is 1.05.
The improved process is adopted, and the process parameters are as follows:
underflow of the red mud separation settling tank: nk 120g/L, α k 1.70;
primary washing liquid of red mud: nk 56g/L,. alpha.k 1.72;
diluting desilication tank slurry: nk 169g/L, α k 1.43;
discarding the red mud: A/S1.19;
bayer process concentrate liquid: α k 1.45.
Similarly, as can be seen from the underflow liquid phase of the red mud separation settling tank, the red mud primary washing liquid alpha k and the red mud A/S, the hydrolysis of the sodium aluminate solution in the Bayer process production system is inhibited after the improvement, the hydrolysis loss is saved, the underflow pre-dilution of the red mud separation settling tank improves the red mud settling and washing efficiency, 52 tons of water are evaporated less per hour by evaporation, and the evaporation energy consumption is obviously reduced.
Example 3
Some alumina manufacturing company C performs the manufacturing according to the process flow shown in fig. 2. The parameters are as follows:
ultra-fine aluminum hydroxide washing liquid: nk 60g/L,. alpha.k 2.95, 80m3/h；
Dissolving slurry: 520m3H, Nk 280g/L, alpha k 1.38, red mud A/S1.20;
primary washing liquid of red mud: nk 61g/L,. alpha.k 1.57, 300m3/h；
Diluting desilication tank slurry: nk 165g/L, α k 1.40;
bottom flow of red mud separation settling tank: nk 165g/L,. alpha.k 1.53;
discarding the red mud: A/S1.23;
bayer process concentrate liquid: α k 1.46.
The method is improved, and the improved process flow chart is shown in figure 4, and the specific improvement is as follows:
the superfine aluminum hydroxide lotion in the superfine aluminum hydroxide production system is sent to the middle-lower part of a mud layer of a red mud separation and sedimentation tank, and the superfine aluminum hydroxide lotion 80m is added in 8 parts3Then, the red mud underflow of the red mud separation settling tank enters a red mud primary washing settling tank, the red mud primary washing liquid overflowing from the red mud primary washing settling tank enters the red mud separation settling tank through a dilution desiliconization tank, and slurry distribution of a sodium aluminate solution crude liquid with an upper molecular ratio of 1.45 and a lower molecular ratio of 2.11 is formed in the red mud separation settling tank; wherein, before the superfine aluminum hydroxide washing liquor is sent to the lower part of the mud layer of the red mud separation and sedimentation tank, the concentration of caustic soda in the slurry in the red mud separation and sedimentation tank is 158g/L, the solid content of the red mud is 550g/L, and the solid aluminum-silicon ratio is 1.15.
The improved process is adopted, and the process parameters are as follows:
underflow of the red mud separation settling tank: nk 129g/L, α k 1.71;
primary washing liquid of red mud: nk 56g/L,. alpha.k 1.72;
diluting desilication tank slurry: nk 166g/L,. alpha.k 1.41;
discarding the red mud: A/S1.21;
bayer process concentrate liquid: α k 1.45.
Similarly, as can be seen from the underflow liquid phase of the red mud separation and sedimentation tank, the red mud primary washing liquid alpha k and the red mud A/S, the hydrolysis of the sodium aluminate solution in the Bayer process production system is inhibited after the improvement, the hydrolysis loss is saved, the underflow pre-dilution of the red mud separation and sedimentation tank improves the red mud sedimentation and washing efficiency, the evaporated water is reduced, and the evaporation energy consumption is obviously reduced.
Claims (3)
1. A production method for coproducing chemical alumina by a Bayer process is characterized in that the chemical alumina is pseudoboehmite or superfine aluminum hydroxide; the coproduction is realized by that a part of Bayer process refined solution in a Bayer process production system enters a seed precipitation decomposition tank of the Bayer process production system, and a part of Bayer process refined solution enters a carbon precipitation decomposition tank in a pseudoboehmite production system or a decomposition tank in a superfine aluminum hydroxide production system;
when the produced chemical alumina is pseudo-boehmite, causticizing a filtering mother liquor subjected to carbon decomposition in a pseudo-boehmite production system to Nk of 20-50 g/L by lime emulsion to obtain causticized liquor, then sending the causticized liquor to any position between the middle part of a mud layer of a red mud separation settling tank and the upper part of a red mud primary washing settling tank, and sending the causticized liquor into the red mud primary washing settling tank along with the red mud underflow of the red mud separation settling tank; after the causticized solution enters a red mud separation and sedimentation tank, slurry distribution of a sodium aluminate solution crude solution with an upper molecular ratio of 1.3-1.6 and a lower liquid phase molecular ratio of 1.6-2.5 is formed in the red mud separation and sedimentation tank;
when the produced chemical aluminum oxide is superfine aluminum hydroxide, sending a superfine aluminum hydroxide product washing liquid to the middle of a mud layer of a red mud separation settling tank to any position between the upper parts of red mud primary washing settling tanks, wherein the Nk of the superfine aluminum hydroxide product washing liquid is 30-70 g/L, and the superfine aluminum hydroxide product washing liquid enters the red mud primary washing settling tank along with the red mud underflow of the red mud separation settling tank; after the superfine aluminum hydroxide product washing liquor enters the red mud separation and sedimentation tank, slurry distribution of a sodium aluminate solution crude liquid with an upper molecular ratio of 1.3-1.6 and a lower liquid phase molecular ratio of 1.6-2.5 is formed in the red mud separation and sedimentation tank.
2. The method for producing alumina coproduced with chemicals by the Bayer process as claimed in claim 1, wherein the causticized liquid is sent to the middle lower part of a mud layer of a red mud separation and sedimentation tank.
3. The method for producing aluminum oxide by coproducing chemicals through the Bayer process according to claim 1, wherein the ultrafine aluminum hydroxide product washing liquid is sent to the middle lower part of a mud layer of a red mud separation and sedimentation tank.
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| CN108910923A (en) * | 2018-08-06 | 2018-11-30 | 湖南绿脉环保科技有限公司 | A kind of method of alumina producing Bayer process |
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