JPS638730Y2 - - Google Patents
Info
- Publication number
- JPS638730Y2 JPS638730Y2 JP5229182U JP5229182U JPS638730Y2 JP S638730 Y2 JPS638730 Y2 JP S638730Y2 JP 5229182 U JP5229182 U JP 5229182U JP 5229182 U JP5229182 U JP 5229182U JP S638730 Y2 JPS638730 Y2 JP S638730Y2
- Authority
- JP
- Japan
- Prior art keywords
- alumina
- slurry
- bauxite
- line
- extraction process
- 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.)
- Expired
Links
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 76
- 238000000605 extraction Methods 0.000 claims description 59
- 239000002002 slurry Substances 0.000 claims description 50
- 229910001570 bauxite Inorganic materials 0.000 claims description 36
- 150000004684 trihydrates Chemical class 0.000 claims description 23
- 150000004682 monohydrates Chemical class 0.000 claims description 21
- 239000000243 solution Substances 0.000 claims description 11
- 239000012670 alkaline solution Substances 0.000 claims description 10
- 238000000034 method Methods 0.000 claims description 10
- 238000012545 processing Methods 0.000 claims description 8
- 150000004645 aluminates Chemical class 0.000 claims description 2
- 239000002994 raw material Substances 0.000 claims description 2
- 239000007788 liquid Substances 0.000 description 16
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 12
- 238000001816 cooling Methods 0.000 description 12
- 238000006243 chemical reaction Methods 0.000 description 11
- 238000000354 decomposition reaction Methods 0.000 description 8
- 239000003513 alkali Substances 0.000 description 5
- ANBBXQWFNXMHLD-UHFFFAOYSA-N aluminum;sodium;oxygen(2-) Chemical compound [O-2].[O-2].[Na+].[Al+3] ANBBXQWFNXMHLD-UHFFFAOYSA-N 0.000 description 5
- 239000000377 silicon dioxide Substances 0.000 description 5
- 229910001388 sodium aluminate Inorganic materials 0.000 description 5
- 239000012530 fluid Substances 0.000 description 4
- WNROFYMDJYEPJX-UHFFFAOYSA-K aluminium hydroxide Chemical compound [OH-].[OH-].[OH-].[Al+3] WNROFYMDJYEPJX-UHFFFAOYSA-K 0.000 description 3
- 238000010276 construction Methods 0.000 description 3
- 229910018072 Al 2 O 3 Inorganic materials 0.000 description 2
- 229910004298 SiO 2 Inorganic materials 0.000 description 2
- 239000002585 base Substances 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 239000000284 extract Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 239000010453 quartz Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 238000005406 washing Methods 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 238000004131 Bayer process Methods 0.000 description 1
- DGAQECJNVWCQMB-PUAWFVPOSA-M Ilexoside XXIX Chemical compound C[C@@H]1CC[C@@]2(CC[C@@]3(C(=CC[C@H]4[C@]3(CC[C@@H]5[C@@]4(CC[C@@H](C5(C)C)OS(=O)(=O)[O-])C)C)[C@@H]2[C@]1(C)O)C)C(=O)O[C@H]6[C@@H]([C@H]([C@@H]([C@H](O6)CO)O)O)O.[Na+] DGAQECJNVWCQMB-PUAWFVPOSA-M 0.000 description 1
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- FAHBNUUHRFUEAI-UHFFFAOYSA-M hydroxidooxidoaluminium Chemical compound O[Al]=O FAHBNUUHRFUEAI-UHFFFAOYSA-M 0.000 description 1
- 239000002244 precipitate Substances 0.000 description 1
- 239000010802 sludge Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Description
【考案の詳細な説明】
本考案は、３水和物型アルミナ成分と１水和物
型アルミナ成分を含むアルミナ含有鉱石（以下混
合型ボーキサイトと称する）をアルカリ液と混合
し、低濃度、低温の反応条件で予め３水和物型ア
ルミナ成分を抽出し、次いで高濃度、高温の反応
条件で１水和物型アルミナ成分を抽出する、所
謂、混合型ボーキサイトよりアルミナを２段階で
抽出する反応装置の改良に関するものであり、更
に詳細には、設備能力の拡張を考慮した極めて経
済的な混合型ボーキサイトからのアルミナの抽出
装置に関するものである。[Detailed description of the invention] The present invention is a method of mixing alumina-containing ore containing trihydrate-type alumina components and monohydrate-type alumina components (hereinafter referred to as mixed-type bauxite) with an alkali solution, and A reaction in which alumina is extracted from mixed bauxite in two stages, in which the trihydrate type alumina component is extracted in advance under the reaction conditions of , and then the monohydrate type alumina component is extracted under the reaction conditions of high concentration and high temperature. The present invention relates to improvements in equipment, and more particularly, to an extremely economical mixed-type bauxite extraction equipment for alumina that takes into account expansion of equipment capacity.
周知の如く、ボーキサイト中のアルミナは主と
して３水和物型アルミナ（Al2O3・3H2O）或は
１水和物型アルミナ（Al2O3・H2O）の形で存在
しており、通常その割合は有効アルミナ中３水和
物型アルミナが60〜90重量％、残部が１水和物型
アルミナである。 As is well known, alumina in bauxite mainly exists in the form of trihydrate type alumina (Al 2 O 3・3H 2 O) or monohydrate type alumina (Al 2 O 3・H 2 O). The ratio is usually 60 to 90% by weight of trihydrate alumina in the effective alumina, with the remainder being monohydrate alumina.
ボーキサイトにアルカリ溶液を添加し、アルミ
ナを抽出する場合３水和物型アルミナは１水和物
型アルミナに比較し、溶解度、溶解速度ともに高
いので低濃度、低温で抽出し得るが、１水和物型
アルミナは抽出し難く、低濃度、低温処理法にて
抽出を行なうならばボーキサイト中の３水和物型
アルミナが優先的に溶解し、それのみで溶解中の
アルミナ濃度が１水和物の溶解度を越えてしまう
ので１水和物型アルミナの溶液を期待することは
殆んどできず、従つて混合型ボーキサイトからア
ルミナを抽出する場合には低圧溶解し得る３水和
物を共含するにもかかわらず、エネルギー的に不
経済である１水和物型アルミナの抽出条件である
高濃度、高温処理方法を適用する必要があつた。 When alumina is extracted by adding an alkaline solution to bauxite, trihydrate alumina has higher solubility and dissolution rate than monohydrate alumina, so it can be extracted at low concentrations and low temperatures. It is difficult to extract solid-type alumina, and if extraction is performed using a low-concentration, low-temperature treatment method, trihydrate-type alumina in bauxite will be preferentially dissolved, and this alone will reduce the concentration of dissolved alumina to monohydrate. Since the solubility of alumina exceeds the solubility of monohydrate alumina, it is almost impossible to expect a solution of monohydrate-type alumina. Therefore, when extracting alumina from mixed-type bauxite, it is difficult to expect a solution of alumina containing trihydrate, which can be dissolved at low pressure. Despite this, it was necessary to apply a high-concentration, high-temperature treatment method, which is an energy-uneconomical extraction condition for monohydrate alumina.
２段階抽出装置はかかる不都合を解決したもの
で先ず混合型ボーキサイトに３水和物型アルミナ
を抽出するに必要なアルカリ量を添加し、低濃
度、低温度で３水和物型アルミナを抽出した後、
１水和物型アルミナを含む残渣とアルミン酸ソー
ダ溶液を分離し、次いで該分離後の残渣に１水和
物型アルミナを抽出するに十分なアルカリ量を添
加し、高濃度、高温処理するものである。この方
法に於いては３水和物型アルミナの抽出に必要以
上の高温度の条件を採用しないため、エネルギー
的に優れた方法である。 The two-stage extraction device solved this inconvenience; first, the amount of alkali necessary to extract trihydrate alumina was added to the mixed bauxite, and the trihydrate alumina was extracted at a low concentration and low temperature. rear,
A method in which a residue containing monohydrate alumina and a sodium aluminate solution are separated, and then an amount of alkali sufficient to extract monohydrate alumina is added to the residue after separation, and the residue is treated at high concentration and high temperature. It is. This method is energy-efficient because it does not require higher temperatures than necessary for extraction of trihydrate alumina.
しかしながら該装置は前述の如く３水和物型ア
ルミナ抽出工程と１水和物型アルミナ抽出工程の
２工程を必要とするため、建設時点に於いて将来
生産の拡張が予想されるにもかかわらず現状需要
量が少ない場合にあつては現状需要規模のプラン
トを設計するか、或は将来の需要増を見込んだ規
模のプラントを設計するか判断に苦しむ点であつ
た。 However, as mentioned above, this equipment requires two processes: a trihydrate type alumina extraction process and a monohydrate type alumina extraction process, so even though future production expansion is expected at the time of construction, When the current demand is small, it is difficult to decide whether to design a plant of the current demand scale or a plant of a scale that anticipates future demand increases.
前者の現状需要規模のプラントを建設する場合
には将来需要増時の増設のためには高価なプラン
ト建設費を必要とし、他方過剰能力のプラントを
建設した場合には需要が予想量に達する期間迄は
装置内にスラリーが沈積しない最低流速を保つた
め使用ボーキサイトに対し、必要以上に多量のア
ルカリ溶液を添加し操業する必要が生じるため、
循環液量が増加し、エネルギー的に不経済とな
る。 In the former case, if a plant is built to meet the current demand, expensive plant construction costs will be required for expansion when demand increases in the future, while if a plant with excess capacity is built, it will take a long time for demand to reach the expected amount. Until then, it was necessary to add a larger amount of alkaline solution than necessary to the bauxite used in order to maintain a minimum flow rate that would prevent slurry from depositing in the equipment.
The amount of circulating fluid increases, making it uneconomical in terms of energy.
かかる情況を鑑み本考案者らは、将来設備拡張
に於いて経済的なアルミナ製造装置を見出すべく
鋭意検討した結果、遂に本考案を完成するに至つ
た。すなわち本考案は３水和物型アルミナ成分と
１水和物型アルミナ成分とを含む混合型ボーキサ
イトにアルカリ溶液を加え、まず３水和物型アル
ミナを抽出処理し、得られたスラリーをアルミン
酸アルカリ溶液と１水和物型アルミナを含有する
溶解残渣の泥状物とに分離する第１段抽出工程
と、第１段抽出工程で分離された該泥状物にアル
カリ溶液を加え、１水和物型アルミナを抽出処理
する第２段抽出工程よりなる混合型ボーキサイト
からのアルミナの抽出装置に於いて、第２段抽出
工程に原料ボーキサイト供給手段を有し、かつ該
抽出工程の処理能力を少くとも第１段抽出工程よ
り導入される泥状物と新たに供給されるボーキサ
イトの総量を処理し得る能力に設定したことを特
徴とする混合型ボーサイトからのアルミナの抽出
装置を提供するにある。 In view of this situation, the inventors of the present invention conducted intensive studies to find an economical alumina manufacturing device for future facility expansion, and finally completed the present invention. That is, in the present invention, an alkaline solution is added to mixed bauxite containing a trihydrate type alumina component and a monohydrate type alumina component, the trihydrate type alumina is first extracted, and the resulting slurry is treated with aluminic acid. A first-stage extraction step in which an alkaline solution and a slurry of the dissolved residue containing monohydrate-type alumina are separated; and an alkaline solution is added to the slurry separated in the first-stage extraction step, and one water is added. In an apparatus for extracting alumina from mixed bauxite, which comprises a second stage extraction process for extracting hydrate type alumina, the second stage extraction process has a raw material bauxite supply means, and the processing capacity of the extraction process is increased. To provide an apparatus for extracting alumina from mixed bauxite, characterized in that the apparatus is set to a capacity capable of processing the total amount of mud introduced from at least the first stage extraction step and the total amount of bauxite newly supplied. be.
以下図面を用いて本考案を更に詳細に説明す
る。 The present invention will be explained in more detail below with reference to the drawings.
第１図は本考案装置の一実施形態を示し、図
中、５，３５はスラリー調整槽、７は予備脱硅
部、９，３７は管状予熱装置、１１，３９はオー
トクレーブ、１７，４７は固液分離機、１３，１
５，４１および４３は冷却用蒸発缶、２０，２４
および２６は熱交換機、２９，３０，５２は生蒸
気吹込管、４９は赤泥洗浄工程、その他の番号は
ラインを示す。 FIG. 1 shows an embodiment of the device of the present invention, in which 5 and 35 are slurry adjustment tanks, 7 is a preliminary desiliconization section, 9 and 37 are tubular preheating devices, 11 and 39 are autoclaves, and 17 and 47 are Solid-liquid separator, 13,1
5, 41 and 43 are cooling evaporators, 20, 24
and 26 are heat exchangers, 29, 30, and 52 are live steam blowing pipes, 49 is a red mud washing process, and other numbers indicate lines.
第１図において、ライン１からのアルカリ溶
液、分解液は二流体方式による３水和物型アルミ
ナ抽出工程の分解液主流（ライン２）と副流（ラ
イン３）、および１水和物型アルミナ抽出工程に
供給される分解液（ライン３４）に分割される。
ライン３により導入される分解液副流は混合型ボ
ーキサイト中の３水和物型アルミナ成分を抽出す
るには不十分であるが、反応性シリカ分を抽出す
るに十分な量のアルカリ溶液であり、ライン４か
ら供給されるボーキサイトと混合されスラリー調
整槽５において輸送可能なスラリーに調整され
る。調整されたスラリーはライン６を経て通常タ
ンク状の容器からなる予備脱硅反応処理槽７に導
入され、ここでライン２９から供給される熱によ
り約70℃以上、好ましくは約80℃以上スラリーの
沸点温度以下に加熱されスラリー中のシリカ分が
所望の量脱硅反応生成物となるまで保持される。 In Figure 1, the alkaline solution and decomposition liquid from line 1 are the main stream (line 2) and side stream (line 3) of the decomposition liquid in the trihydrate alumina extraction process using a two-fluid system, and the monohydrate alumina extraction process. It is divided into a decomposition liquid (line 34) which is fed to the extraction process.
The decomposition liquid substream introduced by line 3 is an alkaline solution in an amount that is insufficient to extract the trihydrate type alumina component in the mixed bauxite, but is sufficient to extract the reactive silica component. , and mixed with bauxite supplied from line 4, and adjusted in slurry adjustment tank 5 into a slurry that can be transported. The adjusted slurry is introduced into a preliminary desiliconization reaction treatment tank 7 which is usually a tank-shaped container through a line 6, where the slurry is heated to a temperature of about 70°C or more, preferably about 80°C or more by heat supplied from a line 29. The slurry is heated to a temperature below the boiling point and maintained until the desired amount of silica in the slurry becomes a desiliconization reaction product.
ライン２９から予備脱硅反応処理槽７に供給さ
れる熱源はバイヤープロセス内で回収される蒸気
であつてもよいし、また系外部からの熱源であつ
てもよい。予備脱硅処理後のスラリーはライン８
を経て３水和物型アルミナの予熱抽出処理のため
の管状予熱器９に供給される。管状予熱器にはラ
イン１８、およびライン２２を経てアルミナ抽出
後のスラリー冷却用蒸発缶１５および１３で回収
される蒸気が導入されスラリーは順次予熱され、
アルミナ抽出用の熱量が不足する場合にはさらに
ライン３０より生蒸気の吹込みにより３水和物型
アルミナの抽出温度条件である110〜180℃に予熱
されてアルミナの抽出が行なわれる。管状予熱器
９で予熱処理されたスラリーはライン１０を経て
抽出および脱硅反応処理容器１１に供給される。 The heat source supplied to the preliminary desiliconization reaction treatment tank 7 from the line 29 may be steam recovered within the Bayer process, or may be a heat source from outside the system. Slurry after preliminary desiliconization treatment is on line 8
It is then supplied to a tubular preheater 9 for preheating and extraction treatment of trihydrate type alumina. The steam recovered in the evaporators 15 and 13 for cooling the slurry after alumina extraction is introduced into the tubular preheater via line 18 and line 22, and the slurry is sequentially preheated.
If the amount of heat for alumina extraction is insufficient, live steam is further blown through line 30 to preheat to 110 to 180°C, which is the extraction temperature condition for trihydrate type alumina, and alumina extraction is performed. The slurry preheated in the tubular preheater 9 is supplied to an extraction and desiliconization reaction treatment vessel 11 via a line 10.
他方ライン２を経て導入される分解液主流は冷
却用蒸発缶１５で回収され、ライン１９を経て供
給される熱と熱交換器２０で熱交換され、さらに
熱交換器２４で冷却用蒸発缶１３で回収され、ラ
イン２３を経て供給される熱と熱交換されて予熱
され、必要によりライン２５を経て予熱された分
解液主流は熱交換器２６により外部からライン２
７を介して供給される生蒸気により所要の温度に
予熱され、ライン２８を経て抽出および脱硅反応
処理槽１１に供給され、前述の予熱されたスラリ
ーと混合されてボーキサイトとボーキサイト中の
３水和物型アルミナ成分を抽出するに十分なアル
カリ溶液とからなるスラリーとされた状態で保持
され、抽出および脱硅反応処理を行なわせるとと
もに３水和物型アルミナの抽出処理を完了する。 On the other hand, the main stream of the decomposition liquid introduced through line 2 is recovered by the cooling evaporator 15, heat exchanged with the heat supplied through the line 19 by the heat exchanger 20, and further transferred to the cooling evaporator 13 by the heat exchanger 24. The main stream of the decomposition liquid, which has been preheated by heat exchange with the heat supplied via line 23 and is preheated via line 25 if necessary, is transferred from the outside to line 2 by a heat exchanger 26.
It is preheated to the required temperature by live steam supplied through line 28, and is supplied to the extraction and desiliconization reaction treatment tank 11 through line 28, where it is mixed with the preheated slurry described above to form bauxite and the 3 water in bauxite. The slurry is maintained in a slurry containing sufficient alkaline solution to extract the hydrate type alumina component, and the extraction process and desiliconization reaction process are carried out, and the extraction process of the trihydrate type alumina is completed.
かくして脱硅反応処理されて、３水和物型アル
ミナ成分の抽出処理を完了したスラリーはライン
１２から抜き出し、ライン１４を通り、スラリー
の冷却用蒸発缶１３および１５で冷却されライン
１６により固液分離装置１７に送られる。冷却用
蒸発缶１３および１５で回収される蒸気は一般に
分解液主流、混合型ボーキサイトと分解液副流と
からなる供給スラリーの予熱用熱源として利用さ
れる。 The slurry that has been subjected to the desiliconization reaction treatment and has completed the extraction treatment of the trihydrate type alumina component is extracted from line 12, passes through line 14, is cooled in slurry cooling evaporators 13 and 15, and is converted into solid-liquid through line 16. It is sent to a separation device 17. The steam recovered in the cooling evaporators 13 and 15 is generally used as a heat source for preheating a feed slurry consisting of a main decomposition liquid, mixed bauxite, and a substream decomposition liquid.
ライン１６より固液分離装置１７に導入される
３水和物型アルミナ抽出処理後のスラリーは、主
としてボーキサイト中より３水和物型アルミナを
抽出してなるアルミン酸ソーダ溶液と、脱硅反応
生成物および１水和物型アルミナを含有する溶解
残渣の泥状物とに分離され、アルミン酸ソーダ溶
液はライン３１および５３を経て図示しない析出
工程に供給され、他方泥状物はライン３２を経て
次工程である１水和物型アルミナ抽出のためのス
ラリー調整槽３５に導入される。 The slurry after the trihydrate type alumina extraction treatment introduced into the solid-liquid separator 17 from the line 16 is mainly composed of a sodium aluminate solution obtained by extracting trihydrate type alumina from bauxite, and a desiliconization reaction product. The sodium aluminate solution is fed to a precipitation step (not shown) via lines 31 and 53, while the slurry is fed via line 32 to a slurry of dissolved residue containing monohydrate type alumina. The slurry is introduced into a slurry adjustment tank 35 for the next step, monohydrate type alumina extraction.
該調整槽３５において１水和物型アルミナ含有
の泥状物はライン１より１水和物型アルミナ抽出
用として分割され、ライン３４を経て導入される
分離液にて該泥状物中のアルミナとライン３３よ
り新たに供給されるボーキサイト中のアルミナを
抽出するに十分なアルカリ濃度および輸送可能な
スラリー状となした後ライン３６を経て管状予熱
装置３７に供給され、１水和物型アルミナの抽出
処理温度に近い温度（通常約200℃またはそれ以
上）に予熱される。管状予熱装置３７の熱源とし
ては第２段抽出工程を出るスラリーの冷却用蒸発
缶、４１，４３で回収され、ライン４４，４５を
経て供給される蒸気が使われる。 In the adjustment tank 35, the slurry containing monohydrate alumina is divided through line 1 for extraction of monohydrate alumina, and the alumina in the slurry is separated by the separated liquid introduced via line 34. The bauxite freshly supplied from the line 33 is made into a slurry with sufficient alkali concentration to extract the alumina and can be transported, and is then supplied to the tubular preheating device 37 via the line 36 to form monohydrate alumina. It is preheated to a temperature close to the extraction processing temperature (usually around 200°C or higher). As a heat source for the tubular preheating device 37, steam is used which is recovered in the cooling evaporators 41, 43 of the slurry exiting the second stage extraction process and supplied via lines 44, 45.
該管状予熱装置３７で予熱されたスラリーは次
いでライン３８を経て単管式、多管式等に管型ま
たはオートクレーブ等の加圧容器で構成される抽
出装置３９内に供給され、ボーキサイト中のアル
ミナ分および３水和物抽出後の泥状物中の残余の
アルミナ分が実質的に抽出するに足る時間滞留さ
せる。図においては熱源としてライン５２より生
蒸気を吹込む槽型の加圧容器を想定して示したが
もちろん連続した管型抽出装置で構成することも
できる。 The slurry preheated in the tubular preheating device 37 is then fed through a line 38 into an extraction device 39 constructed of a pressurized container such as a single tube type, multi-tube type, or an autoclave, and extracts the alumina in the bauxite. The slurry is allowed to remain for a sufficient period of time to substantially extract the remaining alumina content in the slurry after extraction of the alumina and trihydrate. In the figure, a tank-type pressurized container into which live steam is blown from the line 52 as a heat source is assumed, but of course it can also be constructed with a continuous pipe-type extraction device.
抽出装置３９において、ボーキサイト中のアル
ミナ分をアルミン酸ソーダとして抽出したスラリ
ーは、ライン４０により抜き出し、スラリーの冷
却用蒸発缶４１、さらにライン４２を経てスラリ
ーの冷却用蒸発缶４３で冷却され、ライン４６に
より次工程に移送される。冷却用蒸発缶４１，４
３で回収された蒸気は一般に前述のスラリーの予
熱用の熱源として利用される。冷却されたスラリ
ーはライン４６を経て図示しないブローオフタン
クに送られ、系の圧力を大気圧に戻した後固液分
離装置４７に導入され、泥状物とアルミン酸ソー
ダ溶液とに分離され、アルミン酸ソーダ溶液はラ
イン５１を経てライン５３により３水和物型アル
ミナの抽出処理で得たアルミン酸ソーダ溶液同様
に図示しない析出工程に供給され、常法により水
酸化アルミニウムを析出、分離し、分離された水
酸化アルミニウムは焙焼し、析出水酸化アルミニ
ウムを分離後の分解液は適宜必要に応じ濃縮およ
び／または消費されたアルカリ分を添加補充後ラ
イン１に循環される。 In the extraction device 39, the slurry obtained by extracting the alumina content in bauxite as sodium aluminate is extracted through a line 40, passes through a slurry cooling evaporator 41, further passes through a line 42, and is cooled in a slurry cooling evaporator 43. 46, it is transferred to the next process. Cooling evaporator 41, 4
The steam recovered in step 3 is generally utilized as a heat source for preheating the aforementioned slurry. The cooled slurry is sent to a blow-off tank (not shown) via a line 46, and after returning the pressure of the system to atmospheric pressure, it is introduced into a solid-liquid separator 47, where it is separated into a slurry and a sodium aluminate solution. The acid soda solution is supplied through line 51 and through line 53 to a precipitation step (not shown) in the same manner as the aluminate sodium solution obtained in the extraction process of trihydrate type alumina, and aluminum hydroxide is precipitated, separated, and separated by a conventional method. The resulting aluminum hydroxide is roasted, and the decomposed liquid after separating the precipitated aluminum hydroxide is recycled to the line 1 after being concentrated and/or supplemented with the consumed alkali content as required.
一方固液分離器４７で分離された泥状物は洗浄
工程４９に送られ、有効成分を回収した後、ライ
ン５０を経て放棄される。 On the other hand, the sludge separated by the solid-liquid separator 47 is sent to a washing step 49, and after recovering the active ingredients, is discarded via a line 50.
尚図において、第１段抽出工程を二流体方式で
記載したが、一流体方式を用いてもよく、又予熱
器として管状反応器の例を示したがオートクレー
ブ形式でもよい。さらに、それぞれの冷却用蒸発
缶、スラリーの管状予熱抽出反応器を特定基数を
挙げて説明を試みたが、これらは勿論任意の基数
で構成することが可能である。 In the figures, the first stage extraction process is shown as a two-fluid system, but a one-fluid system may also be used.Although a tubular reactor is shown as an example of a preheater, an autoclave system may also be used. Furthermore, although an attempt has been made to explain the respective cooling evaporators and tubular preheating extraction reactors for slurry by citing a specific number of bases, it is of course possible to configure these with any number of bases.
又本装置は第２段抽出工程にボーキサイトを導
入するため、該工程の予熱抽出部にシリカに起因
するスケールが生成、壁面に沈着するため、伝熱
面の熱伝導性を低下することがあるので、第２段
抽出工程の予熱工程３７の間で、かつスラリーが
130〜160℃に予熱される部分に脱硅反応処理部を
設け、液中のSiO2濃度が1.0g／以下となるよう
に処理することが好ましく、更に必要によりライ
ン３３のボーキサイトに一部アルカリ溶液（ライ
ン３４の分流）を混合、処理する予備脱硅処理部
をスラリー調整槽３５に至る間に設けてもよい。 In addition, since this device introduces bauxite into the second stage extraction process, scale caused by silica is generated in the preheating extraction part of this process and deposited on the wall surface, which may reduce the thermal conductivity of the heat transfer surface. Therefore, during the preheating step 37 of the second stage extraction step, the slurry
It is preferable to provide a desiliconization reaction treatment section in the part that is preheated to 130 to 160°C, and perform treatment so that the SiO 2 concentration in the liquid is 1.0 g/or less. A preliminary desiliconization processing section for mixing and processing the solution (separate flow of the line 34) may be provided between the slurry adjustment tank 35 and the slurry adjustment tank 35.
第２段抽出工程にボーキサイトを導入しない場
合には第１段抽出工程よりの泥状物中の石英（Ｆ
−SiO2）に起因するスケールの生成はわずかで
あるが、第２段抽出工程にボーキサイトを導入
し、かつボーキサイト中のシリカ成分が高い場合
にはライン３２よりの泥状物中の石英とライン３
３よりのボーキサイト中の反応性シリカ（Ｒ−
SiO2）とが第２段抽出工程の予熱部域で160℃を
越える部分において急激に析出し、スケール化す
る。 When bauxite is not introduced into the second stage extraction process, quartz (F) in the slurry from the first stage extraction process is
However, if bauxite is introduced into the second extraction process and the silica content in bauxite is high, the quartz in the slurry from line 32 and the line 3
Reactive silica (R-
SiO 2 ) rapidly precipitates and scales in the preheating region of the second stage extraction step where the temperature exceeds 160°C.
以上詳細したごとく本考案の装置における特徴
は第２段抽出工程にあり、従来の２段階抽出装置
に比較して、１水和物型アルミナ抽出工程にボー
キサイト供給手段を新たに設けること、及び抽出
装置容量が単に第１段抽出工程より導入されるア
ルミナ含有泥状物の処理能力よりも高く設定され
ている所にある。この余剰能力量は将来設備拡張
が予想される量であり、ボーキサイトの供給手段
はかかる余剰設備能力を有効に利用することを可
能ならしめるもので、第１段抽出工程及び第２段
抽出工程の全工程を予め過剰量で建設したものに
比較し経済的操業が可能であり、他方将来拡張時
の新規プラント建設に比較し、第２段抽出工程の
建設費が著しく廉価にすみ、極めて経済的である
とともにボーキサイト中の１水和物型アルミナ含
有量が変動した場合においても、第２段抽出工程
へ装入するボーキサイト量を調整するのみで、そ
の変動吸収がきわめて容易に対応できるというメ
リツトを有し、その工業的価値は頗る大なるもの
である。 As detailed above, the features of the device of the present invention are in the second-stage extraction process, and compared to the conventional two-stage extraction device, a bauxite supply means is newly provided in the monohydrate type alumina extraction process, and the extraction The equipment capacity is simply set higher than the processing capacity of the alumina-containing slurry introduced from the first stage extraction process. This amount of surplus capacity is the amount that is expected to be expanded in the future, and the means of supplying bauxite makes it possible to effectively utilize this surplus capacity. It is possible to operate economically compared to a system in which all processes are constructed in advance with excess capacity, and on the other hand, compared to constructing a new plant for future expansion, the construction cost of the second stage extraction process is significantly lower, making it extremely economical. In addition, even if the monohydrate alumina content in bauxite fluctuates, it has the advantage of being able to absorb the fluctuation extremely easily by simply adjusting the amount of bauxite charged to the second stage extraction process. Its industrial value is enormous.
第１図は本考案の装置の一実施態様を示す概略
構成図であつて５，３５はスラリー調整槽、７は
予備脱硅部、９，３７は管状予熱装置、１１は抽
出、脱硅反応処理用オートクレーブ、１３，１
５，４１，４３は冷却用蒸発缶、２０，２４，２
６は熱交換機、３９は１水和物型アルミナ抽出装
置を示す。
FIG. 1 is a schematic configuration diagram showing one embodiment of the apparatus of the present invention, in which 5 and 35 are slurry adjustment tanks, 7 is a preliminary desiliconization section, 9 and 37 are tubular preheating devices, and 11 is an extraction and desiliconization reaction. Processing autoclave, 13,1
5, 41, 43 are cooling evaporators, 20, 24, 2
6 is a heat exchanger, and 39 is a monohydrate type alumina extractor.
Claims (1)
成分とを含む混合型ボーキサイトにアルカリ溶液
を加え、まず３水和物型アルミナを抽出処理し、
得られたスラリーをアルミン酸アルカリ溶液と１
水和物型アルミナを含有する溶解残渣の泥状物と
に分離する第１段抽出工程と、第１段抽出工程で
分離された該泥状物にアルカリ溶液を加え、１水
和物型アルミナを抽出処理する第２段抽出工程よ
りなる混合型ボーキサイトからのアルミナの抽出
装置に於いて、第２段抽出工程に原料ボーキサイ
トの供給手段を有し、かつ該抽出工程の処理能力
を少なくとも第１段抽出工程より導入される泥状
物と新たに供給されるボーキサイトの総量を処理
し得る能力に設定したことを特徴とする混合型ボ
ーキサイトからのアルミナの抽出装置。 An alkaline solution is added to mixed bauxite containing a trihydrate type alumina component and a monohydrate type alumina component, and the trihydrate type alumina is first extracted.
The obtained slurry was mixed with an alkaline aluminate solution.
A first extraction step in which the dissolved residue is separated into a slurry containing hydrated alumina, and an alkaline solution is added to the slurry separated in the first extraction step to extract monohydrated alumina. In an apparatus for extracting alumina from mixed bauxite, which comprises a second stage extraction process, the second stage extraction process has means for supplying raw material bauxite, and the processing capacity of the extraction process is increased to at least the first level. An apparatus for extracting alumina from mixed bauxite, characterized in that the capacity is set to be able to process the total amount of mud introduced from a stage extraction process and the total amount of bauxite newly supplied.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5229182U JPS58155345U (en) | 1982-04-09 | 1982-04-09 | Alumina extraction equipment from mixed bauxite |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5229182U JPS58155345U (en) | 1982-04-09 | 1982-04-09 | Alumina extraction equipment from mixed bauxite |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58155345U JPS58155345U (en) | 1983-10-17 |
| JPS638730Y2 true JPS638730Y2 (en) | 1988-03-16 |
Family
ID=30062999
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5229182U Granted JPS58155345U (en) | 1982-04-09 | 1982-04-09 | Alumina extraction equipment from mixed bauxite |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58155345U (en) |
-
1982
- 1982-04-09 JP JP5229182U patent/JPS58155345U/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58155345U (en) | 1983-10-17 |
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