CN87103497A - 由分解铝酸钠溶液生产氧化铝的工艺和装置 - Google Patents

由分解铝酸钠溶液生产氧化铝的工艺和装置 Download PDF

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Publication number
CN87103497A
CN87103497A CN87103497.2A CN87103497A CN87103497A CN 87103497 A CN87103497 A CN 87103497A CN 87103497 A CN87103497 A CN 87103497A CN 87103497 A CN87103497 A CN 87103497A
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Prior art keywords
splitter
suspension
sorting
liquid stream
technology
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Expired - Lifetime
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CN87103497.2A
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English (en)
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CN1007516B (zh
Inventor
尚特里奥·埃利克
格罗贝尔尼·亨利
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Rio Tinto France SAS
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Aluminium Pechiney SA
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Publication of CN87103497A publication Critical patent/CN87103497A/zh
Publication of CN1007516B publication Critical patent/CN1007516B/zh
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    • B22D—CASTING OF METALS; CASTING OF OTHER SUBSTANCES BY THE SAME PROCESSES OR DEVICES
    • B22D11/00—Continuous casting of metals, i.e. casting in indefinite lengths
    • B22D11/06—Continuous casting of metals, i.e. casting in indefinite lengths into moulds with travelling walls, e.g. with rolls, plates, belts, caterpillars
    • B22D11/0605—Continuous casting of metals, i.e. casting in indefinite lengths into moulds with travelling walls, e.g. with rolls, plates, belts, caterpillars formed by two belts, e.g. Hazelett-process
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    • B22D11/06—Continuous casting of metals, i.e. casting in indefinite lengths into moulds with travelling walls, e.g. with rolls, plates, belts, caterpillars
    • B22D11/0637—Accessories therefor
    • B22D11/068—Accessories therefor for cooling the cast product during its passage through the mould surfaces
    • B22D11/0685—Accessories therefor for cooling the cast product during its passage through the mould surfaces by cooling the casting belts
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    • B29C48/305—Extrusion nozzles or dies having a wide opening, e.g. for forming sheets
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Abstract

一种在氢氧化铝晶种剂存在下连续分解铝酸钠过饱和溶液形成悬浮液的工艺和装置，其特征在于：
a)在一个不搅拌的分选分解器中，使由这种悬浮液组成的进料液流同由分解器底流区带走的再循环液流相接触；
b)在同样的底流区同时抽走产物液流；
c)在分选分解器的溢流区排走溢流液流；
d)根据进料液流的流速，适当地控制再循环液流速度、底流区悬浮液液流的排放速度以及溢流区悬浮液的上升速度。

Description

本发明涉及一种不用搅拌铝酸钠过饱和溶液的分解工艺和装置，采用Bayer法生产氧化铝，产物主要用来经熔融电解转化成铝。
该方法用合适浓度的氢氧化钠水溶液，将铝土矿（红泥）进行热处理，使氧化铝溶解，生成铝酸钠的过饱和溶液。把未受侵蚀的矿渣固相分离掉，余下的铝酸钠过饱和溶液里放入氢氧化铝晶种剂，使氢氧化铝沉淀。
精于此行者一般把那种操作称之为“分解”，该操作通常在许多连续的装置里进行，它们的区别主要在于温度、放入的晶种剂的粒度和数量、连续罐里母液循环的流程布局以及任何再循环过程。
生产氧化铝的工艺装置，大多也是在称之为搅拌分解器的反应器里进行上述的分解操作。其目的是为了避免因分解器底部颗粒积聚而导致物料的任何损失，尤其是尽可能保持悬浮液的均匀度。因此，除了可提高由于分解反应的固体量以外，还可得到对分解器里悬浮液特性来说完全相同的条件，即固体的浓度以及这种固体的粒度。搅拌作用起的另外一个效果是不管颗粒大小如何，溶液本身和固体颗粒在分解器里停留时间的分布状态一致。
分解器生产技术改变了悬浮态的固体和溶液的循环，因此需用相当量的搅拌能，它同时改进了控制化学分解反应过程的某些参数，因此改进了溶液的生产能力以及沉淀固体的质量，尤其是它们最终的粒度。
如今，为了工业规模生产出特定质量的氧化铝，如规定其粒度，同时又要保持高水平的生产能力和限定能耗，专于此行者会对某些参数能彼此独立保持控制发生兴趣，这些参数在涉及搅拌分解器的工艺中彼此不能相互无关，因此，难以选定最佳的参数数值，即：
分解器里固含量的浓度;
这种固体的粒度;
溶液在分解器里停留时间的分布状态;
固体颗粒在分解器里停留时间的分布状态，与上述分布状态要有所不同，相异的固体颗粒，也随其粒度大小而不同。
现在，已经开发出一些生产大颗粒氧化铝状态的颗粒，其粒度大小45微米的最多不超过10%（重量），同时每立方米过饱和溶液生产沉淀氧化铝的能力高于80公斤。
在晶种剂存在下由分解铝酸钠过饱和溶液沉淀氧化铝的某些方法，通过延长分解器里晶种颗粒同再生母液接触的停留时间，为提高其粒度提供了手段。因此，采用限制和甚至抑制搅拌的方法，由于晶种颗粒的沉降，氧化铝的沉淀以及所述颗粒的粒度因与高固含量区域的母液接触而增加，在分解器的下层产生了一个固体颗粒含量高的区域。
这些分解方法是属于靠晶种积累或保留的浓相分解方法之列。
美国专利3，607，113和3，649，184于是采用了以二个分隔间的分解器来分解铝酸钠过饱和溶液的一步分解法。其中第一个搅拌分隔间是用来接受母液和细的晶种剂，在室内进行氢氧化铝颗粒的凝聚，随着凝聚物粒度的增加，凝聚物积累到分解器的下层，并间断地从分隔间内抽走，与此同时，部分分解了的溶液通过分解器第二个非搅拌分隔间，在那里颗粒发生选择性保留，然后溢流入下一个分解器。
颗粒积累在每个分解器的底部，在其上面均匀地进行溶液的沉淀，这种颗粒因此间断地被抽走，经旋风分离段分离，构成生产过程;旋风分离段对除去最细的颗粒是必不可少的，这类颗粒同部分消耗的溶液一起再循环到每个分解器的第一分隔间。
美国专利4，364，919实现分解铝酸钠溶液的方法分两个不同的步骤。第一步凝聚是在少量选过了的晶种剂存在下于搅拌罐里进行的。第二步养育和增大凝聚物粒度是在慢搅拌的罐里进行的，固体颗粒在罐里停留的时间比消耗的母液要长得多，母液用溢流方法排出罐外。固体颗粒含量可达到400至1500克/升。
同样，美国专利4，511，542在氢氧化铝颗粒存在少量选过了的晶种剂于第一阶段成核和凝聚后，采用在一系列分解器里积聚沉淀氧化铝的方法，给悬浮液的固体物又提供一种增浓作用。氢氧化铝颗粒的停留时间在30至90小时范围内变动，固含量为250至700克/升。高固含量的悬浮液从最后的分解器放出，按总体分类供给产物和细的晶种剂，后者经洗涤再循环使用。
事实上，这些方法在分解阶段过程中的共同特点是为颗粒的停留提供了条件，从铝酸钠分解中，氧化铝无区别地沉淀在所有氢氧化铝颗粒的上面，而不论它们的颗粒大小如何。因此它表现在氧化铝沉淀在细的颗粒上面和母液的过早枯竭，只是在最后特定的阶段，必须完全靠悬浮液的分选操作，才把产物同晶种剂分开。因此，在分解作业过程中，没有把颗粒按其粒度大小分选，这就有可能在一个给定的限度内，有选择地调节粗颗粒的停留时间，并很快从反应介质里消除细的颗粒。
法国专利1，187，352所述的流化床沉淀方法可认为能解决此问题。其中，结晶体或固体颗粒的悬浮液在一种上升的液态里保持平衡状态。在这种流化床中，固体颗粒的含量和大小从底向上渐减，而流化床的高度则决定于这种液态向上移动的速度。这样就有可能根据颗粒的直径精确地调节颗粒停留的限度，从而只需改变液体的上升速度，便可精确调节颗粒在反应剂里的停留时间，这里液体的特性必须保持不变。如果液体本身便构成反应介质，并在介质中存在液固物料传递，液体就必须不断进行更新。
事实上，在流化床的工业应用中，尤其在用于分解铝酸钠溶液时，众所周知，使用并随后连续控制那种流化床是很艰难。由于流化床既使在稳态操作方式时也是高度不稳定的，它对控制液体的流体动力学流动以及沉淀过程的参数：温度，密度，粘度，颗粒的大小和形状等敏感。
我们的法国专利申请书84-18135表明，以工业规模采用流化床工艺来分解铝酸钠饱和溶液，从而按粒度大小正确选择氢氧化铝颗粒的保留长短以控制它们的停留时间，然而是不大可能的。为此，适宜在很多显然不同的工序中进行分解作业。首先的工序是在一个不搅拌的罐里进行凝聚，未分类的晶种剂从上向下通过含有过饱和母液的不搅拌罐。粗颗粒在其中有一个停留时间，从而有一个同细颗粒相比含量变小的数值，加上没有任何搅拌装置，它便按一个十分适合凝聚和调节凝聚物粒度的方向移动。在第二个工序中，使用并稳化稠密床，在这个过程中进行粗颗粒的选择性停留和养育，该作业由于上面的工序而变得更为方便。从第一个分解工序放出的悬浮液被投入不搅拌的分解器下层，溶液慢速循环使粗凝聚物颗粒停留在悬浮液进料区，随着氧化铝的沉淀，粗颗粒的粒度增加并最终沉降下来，将它们不断从分解器底部取走，直接形成产品。
没有凝聚或粘接不足的细颗粒级分很快通过溢流方法随未消耗完的溶液一起带走。在第三个也就是最后一个工序中，在加有补充量再循环细晶种剂的情况下，用沉淀耗尽上面的溶液。
掌握氧化铝从铝酸钠过饱和溶液里沉淀的定量和定性参数，在这方面实际上也意味着，在进行和同时控制三个分解工序，尤其是头两个工序时，掌握了十分精确和微妙的控制指标，其中头两个工序操纵着流化床的稳定性和选择保留的效果。
为了给从铝酸钠过饱和溶液分解沉淀氧化铝提供较好的独特控制，从而选定最佳的条件，本发明人开发了一种实施有效的工艺和装置，它能同时进行氢氧化铝颗粒的分类，选择保留和养育，因而避免颗粒分解后分选产物的晶种剂，采用的办法是生长选留的粗颗粒，在溢流装置里带走有害的细颗粒或不需要专门进行颗粒分选的三步工序的分解工艺，只要在第一步骤聚工序非常准确的调节流化床，以同时进行颗粒的养育和选留。
更确切地说，本发明的一个首要目的是一种连续分解铝酸钠溶液的工艺，溶液相对于氧化铝处于过饱和状态，它是采用Bayer法将铝土矿经碱侵蚀而制得，并在氢氧化铝晶种剂存在下形成悬浮液，该工艺特征在于以下的措施：
a）所述组成进料液流的悬浮液从一个不搅拌的分选分解器或反应器的上部进入器内，在器内的平静区，所述进料液流同一种固体颗粒含量高的悬浮液的级份产生接触;温度介于45到70℃，在分选分解器下部被称之为底流区的地方形成再循环液流而被带走。
b）同时，直接组成产物液流的另一部分固体颗粒含量高的悬浮液，从不搅拌分选分解器的底流区被抽走。
c）组成溢流液流的低固含量悬浮液，在分选分解器的上层被提走，以及
d）对预先确定的一个有关进料液流的流速来说，再循环液流的流速可按这样一种方法来调节：
再循环流速为进料流速的2到7倍;
底流区悬浮液的排出速度每小时介于1至10米;
溢流区悬浮液的上升速度每小时介于0.5至5米。
本发明的第二个目的是一种供进行分解作业的装置，它被称之为分选分解器，其特征包括：
a）一个圆锥形罐，它的上部圆柱形部分装备有进料区和评静区的溢流区它是由例如一根部分浸没在被处理的悬浮液里的中心轴所组成，罐下部的圆锥形部分配置在被称之为底流区的位置，在其未端配有一根泄流导管，该导管本身又同产物液流的出口导管相连结;
b）悬浮液从底流区传送到位于分选分解器上部进料区和平静区的设备内。
这样，按照本发明，就有可能彼此独立地调节铝酸钠溶液在氢氧化铝晶种存在下分解所涉及的基本参数。
1.进入分解器的颗粒在其中停留时间的分布状态，决定产物最终的粒度，因此，经调节可大大提高粗颗粒对较细颗粒的停留时间的相对值（5至10倍），较细的颗粒通过溢流方式随部分分解的液体一起流出。颗粒的停留时间也比它同样在搅拌分解器中理应呆的时间要长。粗颗粒在底流区的保留时间，只要达到充分选择的程度，便有可能通过周围溶液的分解反应，优先提高其粒度，并通过采用合适的连续提取设备，直接得到所要求粒度的产物。
通过结合两种现象和有关的装置，可以达到晶种剂的选择性保留效果：
a）通过悬浮液的沉降，将颗粒按其粒度分选。分选作用是在一个圆锥形分解器里进行的，该分解器装有一个沉降容器，其中没有搅拌，容器里存在一个进料和再循环液流的平静区。颗粒是沿介于含颗粒的底流液流再循环液流和产物液流向的分界区进行分选。
分选效果的质量受进料液流中的固含量所控制，该含量按氢氧化铝表示要低于200克/升，最好介于110和180克/升之间，同时铝酸钠溶液以Na2O钠碱浓度表示，介于100和200克/升之间;而所述溶液中含的Al2O3同苟性Na2O的重量比WR，则介于0.5和1.2之间。
分选效果也受底流液流中固含量控制，该含量按氢氧化铝表示要介于300和900克/升之间，同时溢流区悬浮液的上升速度要介于每小时0.5和5米之间，最好在每小时1和3米之间。
b）在底流区悬浮液里固体的增稠作用。如果没有这种增稠作用，底流区将含有一种悬浮液，其中的固含量会同进料液流的固含量没有多大差别，这样，以底流方式流出的平均停留时间会等于底流区所含固体物质的质量同以底流方式流出的固体物质流速的比值，换句话说，等于在一个搅拌分解器里的停留时间。为了显著延长颗粒的停留时间，采用体积恒定的分解器和流速恒定的底流液流，就必须提高分解器里固体物质的量。按照本发明就可以达到这个目标，其方法是利用一台分解器内或分解器外的泵，将再循环液流重新通入分解器;再循环液流从底流区抽走，在分解器中心轴位置具有高的固含量（300至900克/升）。此再循环导致在底流区达到一个平衡的固含量，其数值更靠近以底流方式放出的产物液流的值，因此，当底流区悬浮排出液流的流速增大，此数值更高。
对直径一定的分解器来说，再循环液流因而是决定性的因素。底流体区悬浮液的排放液流速度要介于每小时1和10米之间，最好在3和8米之间。再循环液流在进料液流的2和7倍之间，最好在2和3.5倍之间。
2.有关溶液在分解器里停留时间的分布状态;控制着此溶液的总的生产能力;它可以被调整到这样一种状况，使溢流液和底流液的溢流时间相近，由此，使溶液总的生产能力达到最大值，为此，采用了两种方法：
a）选择溢流区和底流区各自的体积，这在设计装置时便已决定下来。溢流区与底流区的体积比一般在0.1和0.5之间。
b）进入分解器底流区的再循环液流要达到进料液流的2至7倍。
5.附图说明
图1和2是实施本发明用的装置的纵截面示意图。
图3是在被人称作三阶段工艺的分解过程中实施本发明的总示意图2，该工艺在应用实例3和4里加以说明。
图1表示一种利用一台离心泵（12）作外循环的分选分解器，以及
图2表示另一种利用一台螺旋（13）泵作内循环的分选分解器。
这种分选分解器是一个圆锥形罐（1），它是由圆柱形上部（2）的锥形底部（3）所组成，它带有一个溢流装置（4）和一根中心管或轴（5）;后者浸在氢氧化铝溶液中。
罐的上部因此给分成两个区域：
介于轴（5）和圆柱体外壳间的溢流区（A）;
位于轴（5）内的进料区（B）。
分解器的下部被称作底流区（C）。罐的运行同四种不同的液流有关：
-进料液流（6）;
-溢流液流（7）;
-再循环液流（8）;
-产物液流（9）。
进料导管（6）和再循环导管（8）通入中心轴（5），液流在（B）区混合并组成罐的喂料。
在中心轴（5）下面的位置（D）;由进料液流（6）和再循环液流（8）的混合物产生的液流分成二股，喂入溢流区（A）和底流区（C）。
通入轴（5）的两根导管浸入（B）区，以避免任何乳化事故，并在缓慢排出悬浮液流进入（D）区时避免扰动。为了遮断喷嘴，在中心轴（5）内的（B）区，浸入一块水平板（11）或任何其它的固定分散器装置，其位置在进料液流（8）的两根导管进口下面约10厘米的地方，这两根管的进口也浸在液体里。
在底流区，两种液流从锥部的底下抽走：
-再循环液流（8）;
-产物液流（9）。
在图1中，这两种液流是利用泄料导管（10）从分解器流走;再循环导管8配有一台离心泵（12），把液流输送到进料区（B）。
在图2中，再循环回路位于分解器内，其中为悬浮液流动提供一台螺旋泵（13），靠一根插入管（14）将分解器底部泄出的料吸入同样的区域（B）。
以上所述的不同液流，即进料液流，溢流液流，再循环液流以及产物液流，在“堵塞流动”型的缓慢流动形式时，达到流体动力学平衡状态，这种类型流动的特征，在于底流区和溢流区的固含量和粒度以及固体和溶液的停留时间。
在停留喂料的情况下，采用关闭装置（15），以及关掉再循环泵（12）（图1），或螺旋泵（13）（图2），中断产物液流（9）分选罐隔开，这样可以为底流区（C）提供足够的流速，以保持悬浮溶液固含量均匀，从而防止产生任何沉积和堵塞事故。
6.应用实例
本发明开始的两个应用实例是涉及严格按两种不同的操作规则的分解器，这些规则是从一个生产氧化铝的工业装置中实现的。
分解器的特性：
罐的直径：9米
轴的直径：3.15米
有效体积：1000米3
轴浸入深度：3米
溢流区体积/底流区体积：0.2
加入晶种前溶液的特性：
铝酸钠（含有145克/升苟性钠）
温度：65℃
不同悬浮液液流的特性：
第一实例：（第一种操作规则）
进料液流;流速：154米3/小时
固含量：158克/升
WR：1.06
粒度：35%＜48微米
溢流液流;流速：132米3/小时
固含量：138克/米
WR：0.95
粒度：47%＜48微米
再循环液流;流速：455米3/小时
产物液流;流速：22米3/小时
固含量：460克/升
WR：0.93
粒度：9%＜48微米
溢流区悬浮液的上升速度：2.4米/小时
底流区悬浮液的排出流速：7.48米/小时
颗粒粒度范围的增加：经48微米筛，颗粒掉落2%（介于进料液流和溢流液流与产物液流的混合物之间粒度＜48μ颗粒的重量百分之差）
第二实施例：（第二种操作条件）
进料液流;流速：112米3/小时
固含量：165克/升
WR：1.3
粒度：38%＜48微米
溢流液流;流速：98米3/小时
固含量：137.5克/升
WR：0.877
粒度：54%＜48微米
再循环液流;流速：355米3/小时
产物液流;流速：14米3/小时
固含量：625克/升
WR：0.860
粒度：5.5%＜48微米
溢流区悬浮液上升速度：1.75米/小时
底流区悬浮液的排出流速：5.8米/小时
颗粒粒度范围的增加：经48微米筛，颗粒掉落6%。
下面三个采用本发明的实施例，是涉及在一个分解回路中分选分解器的使用。
其中第三和第四个实施例，分选分解器是用在一种包含三个阶段的叫作“ACSPE”法的工艺中，参照图3，该方法包括：
一个因固体的浓缩、颗粒在悬浮液里凝聚的阶段“A”（参照阶段1），
一个颗粒胶接和产物排放的阶段“CSP”，在这个阶段中，粗颗粒的选择停留，使得从“A”阶段放出的凝聚体可以优先增加其粒度固结合和分选，这就使其排放液形成产物液流（参照阶段2），
一个溶液消耗阶段“E”在这个阶段中，采用高浓度细颗粒溶液，对其生产率大小是特别重要的（参照阶段3）。
值得指出的是，根据从凝聚阶段1放出的要被处理的悬浮液的体积，按分解器的容量可采用一个或多个分选分解器，它们可以串联和（或）平行布置。
第三实例：（三个阶段-A，CSP    E）
阶段1需每小时通入437米的铝酸钠溶液，温度为70℃，每升160克Na2O，WR：1.13，并每小时通入56吨来自阶段3的氢氧化铝晶种，从而获得每升含120克晶种剂的悬浮液，晶种剂是由占40%（重量）、粒度＜48微米的颗粒所组成。悬浮液在第一个凝聚阶段停留的时间为8小时;由此，悬浮液固含量达到140克/升。
然后，将悬浮液输入由三个与例1，2所述相同的分选分解器所组成的阶段，这三个分解器按并联布置。悬浮液给分成三股相等的液流，并保持温度65℃，在三个分解器里停留18小时。在此第二阶段的过程中，每个分选分解器的平均参数的设置使悬浮液进料流速控制在462/3＝154米3/小时：
-再循环流速：462米3/小时
-底流区悬浮液排放流速：7.8米/小时
-溢流区悬浮液上升速度：2.1米/小时
将不断抽出的分选产物加以洗涤，其中颗粒＜48微米的颗粒不到10%（重量）;与此同时，分选分解器的溢流液流喂入第三阶段，该阶段还得到补充量的晶种剂，使每升悬浮液的固含量达到730克。分解继续进行16小时，直到所得的重量比为0.60，然后把晶种剂从分解的溶液里分离出来。
第四个实例：（三个阶段-A，CPS    E）
在阶段1需每小时通入194米3与例3同样特性的铝酸钠溶液，并每小时通入7.5吨氢氧化铝晶种;从而获得每升含38克固体颗粒的悬浮液;固体颗粒的40%（重量），其粒度＜48微米。悬浮液在第一个凝聚阶段停留的时间为10小时，由此，悬浮液固含量达到60克/升。
然后，将悬浮液输入一个与例1和例2相同的分选分解器，在分解器里保持65%，停留24小时。在这个第二阶段的过程中，分选分解器的参数设置使悬浮液进料流速控制在197米/小时：
-再循环流速：591米3/小时
-底流区悬浮用排放流速：7.25米/小时
-溢流区悬浮液上升速度：1.8米/小时
将不断抽出的分选产物加以洗涤，其中粒度＜48微米的颗粒不到8%（重量），而分解器里含有20克/升固体颗粒的溢流液流排入第三阶段，该阶段还得到补充量的晶种剂，使每升悬浮液的固含量达到750克。分解继续再进行10小时，直到重量比约为0.60;然后把晶种剂从分解的溶液里分离出来。
实施例3和例4表明，在少于50小时的这段溶液分解时期内，每立方米铝酸钠溶液的生产能力可达到约85公斤，而且，40%（重量）颗粒的粒度＜48微米的大量细晶种，并不直接影响获得10%（重量）颗粒的粒度＜48微米的产物。至今还没有别的生产Al2O3的工业方法，可以不用特殊的分选系统达到这样的结果，这种分选系统供分解用途总是累赘的。
在第五个实例中，分选分解器是按二个阶段方法操作的，其中，第一个凝聚阶段仍保持不变，而涉及颗粒胶接、产物排放以及溶液消耗的阶段，则在同一个工序里进行。
第五实施例：（二个阶段-A，CSPE）
在阶段1需每小时通入500米3铝酸钠溶液和66吨氢氧化铝晶种;它们的特性与实例3和4所用相同。这种形成的悬浮液在第一阶段停留18小时，直到固含量达到150克/升。
然后，将该悬浮液输入由三个与例1、例2所述相同的分选分解器所组成的阶段，这三个分解器按并联布置;第一和第二分解器的溢流液流分别组成第二、第三分解器的进料液流。悬浮液保持在65℃，在三个分解器里总停留时间为42小时，在氢氧化铝颗粒胶接和固结之后，可从每个分解器直接抽取固含量至少有600克/升的悬浮液;构成粒度＜48微米不到6%（重量）的产物。这样，每小时总共可抽出110米3的悬浮液，而将由440米3/小时悬浮液（每升固含量150克）组成的最后一个分解器的溢流液流加以过滤。粒度＜48μ的颗粒占44%（重量）的固体组成通入阶段1的晶种，而溶液（WR进行＝0.6）进行再循环以侵蚀铝土矿。
由此看来，即使把分解回路系统减少到二个阶段，也可以免除分选操作而进行分解且仍能保持产物符合所要求的粒度质量，并在不超过50小时的全部分解时期内，每立方米过饱和溶液Al2O3的生产能力可以超过80公斤。
本发明利用分选分解器工业生产氧化铝，因此，从以下诸方面，提供了很多优点：产品的质量，生产能力，运行以及投资。
a）产品;质量：本发明可以工业生产有特定粒度特性的氧化铝，采用的办法是，单独调节和控制包括固体和溶液的停留时间的分解参数，并结合分解器里颗粒粒度的大小分选颗粒。
b）生产能力：在没有搅拌情况下，通过悬浮液的“堵塞流动”型的液流流动;分解作用过程接近于已知的、有规律的反应过程。而且，可以在分解器里按照比较均匀的方式调节溶液的停留时间，这样，溶液的生产能力处于最佳状态。
c）运行：由于分选分解器的体系惯性小，使它可以在稳态条件下直接修正或改正一个参数，不需破坏整个反应介质的平衡。所需要的功率仅用于泵出再循环液流，其数值（25-304瓦）远低于一个搅拌分解器作业所述需要的功率（有效体积3000米3的罐，为40-70千瓦），也远低于其它装置所需要的功率，这些装置是为了试图提供同样的质量特性水平，不过要求添置很多辅助设备。
悬浮液在装置里的循环最终使它可以避免产生任何不能进行分解反应的死区，并减少了在用搅拌分解器时遇到的形成残渣的危险。
d）投资：所用工艺使用多功能的单一型设备，精简了装置。

Claims (15)

1、一种连续分解铝酸钠溶液的工艺，该溶液对氧化铝来说处于过饱和状态，它是采用Bayer法将铝土矿经碱侵蚀而制得，并在氢氧化铝晶种剂存在下形成悬浮液，该工艺的特征在于以下的措施：
a)所述组成进料液流的悬浮液从一个不搅拌的分选分解器或反应器的上部分进入器内，在器内的平静区，所述进料液流与一种高固体颗粒含量的悬浮液的一部分发生接触，接触温度介于50和75℃之间，在分选分解器下部被称之为底流区的地方形成再循环液流而给带走。
b)同时，直接组成产物液流的另一部分高固体颗粒含量的悬浮液，从不搅拌分选分解器的底流区给抽走。
c)组成溢流液流的低固含量悬浮液在分选分解器的上层被提走。
d)对预先确定的一个进料液流的流速来说，再循环液流的流速可按照这样一种方法来调节：
再循环流速为进料流速的2至7倍；
底流区悬浮液的排出速度为每小时1至10米；
溢流区悬浮液的上升速度为每小时0.5至5米。
2、根据权利要求1的工艺，其特征在于进料液流的固含量按氢氧化铝来表示低于200克/升。
3、根据权利要求2的工艺，其特征在于进料液流的固含量按氢氧化铝来表示介于110和180克/升之间。
4、根据权利要求1-3的工艺，其特征在于用来分解的溶液中可溶性Al  O/苟性Na  O浓度的重量比WR为0.5至1.2。
5、根据权利要求1的工艺，其特征在于再循环液流的固含量按氢氧化铝表示介于300和900克/升之间。
6、根据权利要求1的工艺，其特征在于再循环液流最好是进料液流的2至3.5倍。
7、根据权利要求1的工艺，其特征在于分选分解器底流区悬浮液的排放速度最好是每小时3至8米。
8、根据权利要求1的工艺，其特征在于分选分解器溢流区的溢流速度最好是每小时1至3米。
9、根据1-8任何一项权利要求，一种供进行分解作用被称作分选分解器的装置，其特征在于这种装置包括：
一个园锥形罐（1），它的上部的圆柱体（2）备有溢流区（4），进料区和平静区（B）;其下部的锥体（3）配置在一个称作底流区（C）的位置，它配有一根泄流导管（10），该导管本身又同产物液流的出口导管（9）相连结，悬浮液从底流区（C）传送到进料和平静区（B）的设备内。
10、一种根据权利要求9的分选分解器，其特征在于，由部分浸没在要处理的悬浮液里的一根中心轴（5），构成进料和平静区（B），供进料液流的导管（6）和再循环液流的导管（8）进入轴内。
11、根据权利要求9和10的一种分选分解器，其特征在于，在其中心轴（5）内的进料和平静区（B）浸入一块水平板（11）或任何其它的固定分散器装置，其位置在通入进料液流（6）和再循环液流导管的进口也浸在液体里。
12、一种根据9-11任何一项权利要求的分选分解器，其特征在于溢流区（A）同底流区（C）的体积比为0.1至0.5。
13、一种根据权利要求9的分选分解器，其特征在于从底流区（C）带走悬浮液的传送设备是在所述的分选分解器外部分，它是由与泄料导管（10）相连接的一台离心泵（13）构成，并通过再循环液流导管（8）排放入进料和平静区（B）。
14、一种根据权利要求9的分选分解器，其特征在于从底流区（C）带走悬浮液的传送设备是在所述的分选分解器内部，它是由一台螺旋泵（13）构成，这种泵吸收分解器底部流区（C）的悬浮液，并通过再循环液流导管（8），排放入进料和平静区（B）。
15、一种根据权利要求9的分选分解器，其特征在于产物液流（9）的排放导管配置有一个关闭装置（15）。
CN87105401A 1986-05-15 1987-05-14 由分解铝酸钠溶液生产氧化铝的工艺和装置 Expired CN1007516B (zh)

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