CN103101947A - Digesting process for aluminum oxide production process - Google Patents
Digesting process for aluminum oxide production process Download PDFInfo
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- CN103101947A CN103101947A CN2013100768488A CN201310076848A CN103101947A CN 103101947 A CN103101947 A CN 103101947A CN 2013100768488 A CN2013100768488 A CN 2013100768488A CN 201310076848 A CN201310076848 A CN 201310076848A CN 103101947 A CN103101947 A CN 103101947A
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Abstract
The invention discloses a digesting process for an aluminum oxide production process. By using the digesting process, the concentration of caustic alkali of a digesting system for producing aluminum oxide is effectively increased, the steam addition of the digesting system is reduced, and the production cost of the aluminum oxide is reduced. The digesting process comprises the following steps of: (1) pre-desiliconizing ores; (2) adding a blending liquid, blending the ores into ore pulp, and delivering the ore pulp to a double-tube preheater for preheating; (3) respectively placing the preheated ore pulp into two ore pulp buffers, and respectively enabling the ore pulp in the two ore pulp buffers to flow into two sets of digesters; (4) introducing high-pressure steam to the digesters, heating the pulp to 255-270 DEG C, and keeping the temperature for 50-60min; (5) enabling the two paths of pulp to enter a flash tank through a mixer to naturally evaporate, and enabling dead steam evaporated by the flash tank to return to the double-tube preheater; and (6) enabling the flashed ore pulp to enter a diluting tank, delivering the diluted ore pulp to a settlement separation tank by a diluting pump, enabling settlement overflow to circularly flow into the diluting tank, mixing the settlement overflow and the ore pulp, and then, delivering the diluted ore pulp to the settlement separation tank by the diluting pump, wherein the settlement overflow is obtained after red mud at the bottom of the settlement separation tank is cleaned for the first time.
Description
Technical field
The present invention relates to a kind of production technique of aluminum oxide, be specifically related to the dissolving-out process in a kind of aluminum oxide production process.
Background technology
Produce the topmost consumption of aluminum oxide and comprise steam, in producing the alumina leaching process, under the condition that guarantees the stripping index, reduce as much as possible the add-on of steam, reduce the steam consumption and be very important.Steam direct heating ore pulp dissolving-out technology particularly more should reduce the intake of steam, reduces and causes the reduction of the severe alkali concn of digestion series because passing into too much steam.Therefore, improve the severe alkali concn of digestion series, can yet be regarded as and improve a kind of good method of aluminum oxide output.
Summary of the invention
The objective of the invention is provides the dissolving-out process in a kind of aluminum oxide production process for overcoming above-mentioned the deficiencies in the prior art.Effectively improve and produce the severe alkali concn of alumina leaching system, reduce digestion series steam add-on, reduce alumina production cost.
For achieving the above object, the present invention adopts following technical proposals:
Dissolving-out process in a kind of aluminum oxide production process comprises the following steps:
1) with the ore pre-desiliconizing;
2) allocate mixed liquid into, ore is deployed into ore pulp, and deliver to the cannula primary heater preheating;
3) ore pulp after preheating is divided into two groups and enters two ore pulp snubbers, two interior ore pulps of ore pulp snubber flow into respectively two groups of digesters;
4) pass into high pressure steam in digester, slip is heated to 255～270 ℃, and be incubated 50～60 minutes;
5) two stock material slurries enter flash drum self-evaporatint n. by mixing tank, and cannula primary heater is returned in the exhaust steam of flash drum evaporation; Flash drum one is that slip pressure is unloaded to normal pressure, the 2nd, and the preheating temperature of assurance high pressure digestion canalization guarantees thermal equilibrium;
6) enter dilution trap through the ore pulp after flash distillation, to dilute ore pulp with dilution pumps and deliver to precipitation separation tank, the sedimentation overflow circulating of the underflow red mud of precipitation separation tank after through washing for the first time flows into dilution trap, and again will dilute ore pulp with dilution pumps after ore pulp mixes and deliver to precipitation separation tank.
The concrete grammar of described step 1) is: send the pre-desiliconizing groove with ore mill, utilize the ore pulp pre-desiliconizing of pre-desiliconizing, so that the kaolin in ore is dissolved out, thereby reduce silicon-dioxide scabbing in pipeline.
The ore pulp of described pre-desiliconizing is a water soft mineral ore pulp or a hydraulic ore ore pulp.
Described step 2) concrete grammar is: allocate mixed liquid in the pre-desiliconizing groove, be deployed into ore pulp, pass through feeding pump, ore pulp is sent into surge pump, to the cannula primary heater preheating, steam is from flash drum with pulp conveying for surge pump, and the water of condensation of generation enters the sedimentation hot water tank.
Described surge pump is four, and surge pump is delivered to ore pulp respectively four canalization preheatings of cannula primary heater.
Described mixed liquid is that the mother liquor after the seed precipitation solution evaporation concentration is allocated into liquid caustic soda again and be get final product, and the severe alkali concn of described mixed liquid is 237～243g/l, ak＞3.0.
The described ore pulp of step 3) under the pressure of surge pump promotes, heats pulp conveying after snubber mixes in different digesters.
Ore pulp ak after described step 6) flash distillation is 1.40～1.48, and the dilution ore pulp contains admittedly less than 70g/l.
The invention has the beneficial effects as follows:
Solubility rate of the present invention is 83～85%, and in the situation that alumina same feedstock amount, quantity of steam saves 7～8% than transformation is front, and the unit inlet amount improves 10%, and energy-saving effect is remarkable.The present invention improves the severe alkali concn of production alumina leaching system effectively, reduces digestion series steam add-on, reduces alumina production cost.Because the raw material of ore of using is a hydraulic ore, approximately 255～270 ℃ of needed temperature, dissolution time 50～60 minutes, after digester originally is together in series, except front 3 digesters pass into steam always, other digester needs in order to prevent the slip precipitation steam that passes into that is interrupted, and causes the steam that passes in digester to increase.Digester is divided into two groups, the charging resistance reduces, slip enters through after improved flash system, the exhaust steam of flash distillation measures raising, the ore pulp temperature out of canalization heating is improved, reheat required 255～270 ℃ of ore pulp, the quantity of steam that passes in digester is just few, so the quantity of steam that uses reduces.
Description of drawings
Fig. 1 is process flow sheet of the present invention.
Embodiment
The present invention will be further elaborated below in conjunction with drawings and Examples, should be noted that following explanation is only in order to explain the present invention, its content not to be limited.
Embodiment 1:
Dissolving-out process in a kind of aluminum oxide production process comprises the following steps:
1) send the pre-desiliconizing groove with ore mill, utilize diaspore ore pulp pre-desiliconizing, so that the kaolin in ore is dissolved out, thereby reduce silicon-dioxide scabbing in pipeline;
2) allocate the mother liquor after the seed precipitation solution evaporation concentration into liquid caustic soda again and namely get mixed liquid, the severe alkali concn of mixed liquid is 238g/l, and ak 2.9; Allocate mixed liquid in the pre-desiliconizing groove, be deployed into ore pulp, by feeding pump, ore pulp is sent into four surge pumps, surge pump is delivered to ore pulp respectively four canalization preheatings of cannula primary heater, and steam is from flash drum, and the water of condensation of generation enters the sedimentation hot water tank;
3) ore pulp after preheating is divided into two groups and enters two ore pulp snubbers, the ore pulp in two ore pulp snubbers is delivered to respectively in two groups of digesters and heats under the pressure of surge pump promotes;
4) pass into high pressure steam in digester, slip is heated to 255 ℃, and be incubated 55 minutes;
5) two stock material slurries enter flash drum self-evaporatint n. by mixing tank, and cannula primary heater is returned in the exhaust steam of flash drum evaporation; Flash drum one is that slip pressure is unloaded to normal pressure, the 2nd, and the preheating temperature of assurance high pressure digestion canalization guarantees thermal equilibrium;
6) enter dilution trap through the ore pulp after flash distillation, to dilute ore pulp with dilution pumps and deliver to precipitation separation tank, the sedimentation overflow circulating of the underflow red mud of precipitation separation tank after through washing for the first time flows into dilution trap, and again will dilute ore pulp with dilution pumps after ore pulp mixes and deliver to precipitation separation tank; Ore pulp ak after flash distillation is 1.42, and the dilution ore pulp contains admittedly less than 70g/l.Exsolution red mud A/S 1.15.
Embodiment 2:
Dissolving-out process in a kind of aluminum oxide production process comprises the following steps:
1) send the pre-desiliconizing groove with ore mill, utilize diaspore ore pulp pre-desiliconizing, so that the kaolin in ore is dissolved out, thereby reduce silicon-dioxide scabbing in pipeline;
2) allocate the mother liquor after the seed precipitation solution evaporation concentration into liquid caustic soda again and namely get mixed liquid, the severe alkali concn of mixed liquid is 239g/l, and ak 3.0; Allocate mixed liquid in the pre-desiliconizing groove, be deployed into ore pulp, by feeding pump, ore pulp is sent into four surge pumps, surge pump is delivered to ore pulp respectively four canalization preheatings of cannula primary heater, and steam is from flash drum, and the water of condensation of generation enters the sedimentation hot water tank;
3) ore pulp after preheating is divided into two groups and enters two ore pulp snubbers, the ore pulp in two ore pulp snubbers is delivered to respectively in two groups of digesters and heats under the pressure of surge pump promotes;
4) pass into high pressure steam in digester, slip is heated to 265 ℃, and be incubated 50 minutes;
5) two stock material slurries enter flash drum self-evaporatint n. by mixing tank, and cannula primary heater is returned in the exhaust steam of flash drum evaporation; Flash drum one is that slip pressure is unloaded to normal pressure, the 2nd, and the preheating temperature of assurance high pressure digestion canalization guarantees thermal equilibrium;
6) enter dilution trap through the ore pulp after flash distillation, to dilute ore pulp with dilution pumps and deliver to precipitation separation tank, the sedimentation overflow circulating of the underflow red mud of precipitation separation tank after through washing for the first time flows into dilution trap, and again will dilute ore pulp with dilution pumps after ore pulp mixes and deliver to precipitation separation tank; Ore pulp ak after flash distillation is 1.43, and the dilution ore pulp contains admittedly less than 70g/l.Exsolution red mud A/S 1.13.
Embodiment 3:
Dissolving-out process in a kind of aluminum oxide production process comprises the following steps:
1) send the pre-desiliconizing groove with ore mill, utilize diaspore ore pulp pre-desiliconizing, so that the kaolin in ore is dissolved out, thereby reduce silicon-dioxide scabbing in pipeline;
2) allocate the mother liquor after the seed precipitation solution evaporation concentration into liquid caustic soda again and namely get mixed liquid, the severe alkali concn of mixed liquid is 240g/l, and ak 3.05; Allocate mixed liquid in the pre-desiliconizing groove, be deployed into ore pulp, by feeding pump, ore pulp is sent into four surge pumps, surge pump is delivered to ore pulp respectively four canalization preheatings of cannula primary heater, and steam is from flash drum, and the water of condensation of generation enters the sedimentation hot water tank;
3) ore pulp after preheating is divided into two groups and enters two ore pulp snubbers, the ore pulp in two ore pulp snubbers is delivered to respectively in two groups of digesters and heats under the pressure of surge pump promotes;
4) pass into high pressure steam in digester, slip is heated to 270 ℃, and be incubated 55 minutes;
5) two stock material slurries enter flash drum self-evaporatint n. by mixing tank, and cannula primary heater is returned in the exhaust steam of flash drum evaporation; Flash drum one is that slip pressure is unloaded to normal pressure, the 2nd, and the preheating temperature of assurance high pressure digestion canalization guarantees thermal equilibrium;
6) enter dilution trap through the ore pulp after flash distillation, to dilute ore pulp with dilution pumps and deliver to precipitation separation tank, the sedimentation overflow circulating of the underflow red mud of precipitation separation tank after through washing for the first time flows into dilution trap, and again will dilute ore pulp with dilution pumps after ore pulp mixes and deliver to precipitation separation tank; Ore pulp ak after flash distillation is 1.44, and the dilution ore pulp contains admittedly less than 70g/l.Exsolution red mud A/S 1.12.
Although above-mentionedly by reference to the accompanying drawings the specific embodiment of the present invention is described; but be not limiting the scope of the invention; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various modifications that creative work can make or distortion still in protection scope of the present invention.
Claims (8)
1. the dissolving-out process in an aluminum oxide production process, is characterized in that, comprises the following steps:
1) with the ore pre-desiliconizing;
2) allocate mixed liquid into, ore is deployed into ore pulp, and deliver to the cannula primary heater preheating;
3) ore pulp after preheating is divided into two groups and enters two ore pulp snubbers, two interior ore pulps of ore pulp snubber flow into respectively two groups of digesters;
4) pass into high pressure steam in digester, slip is heated to 255-270 ℃, and be incubated 50-60 minute;
5) two groups of digester discharging slips enter flash drum self-evaporatint n. by mixing tank, and cannula primary heater is returned in the exhaust steam of flash drum evaporation;
6) enter dilution trap through the ore pulp after flash distillation, to dilute ore pulp with dilution pumps and deliver to precipitation separation tank, the sedimentation overflow circulating of the underflow red mud of precipitation separation tank after through washing for the first time flows into dilution trap, and again will dilute ore pulp with dilution pumps after ore pulp mixes and deliver to precipitation separation tank.
2. dissolving-out process according to claim 1, is characterized in that, the concrete grammar of described step 1) is: send the pre-desiliconizing groove with the ore mill, utilize the ore pulp pre-desiliconizing of pre-desiliconizing, so that the kaolin in ore is dissolved out.
3. dissolving-out process according to claim 2, is characterized in that, the ore pulp of described pre-desiliconizing is a water soft mineral ore pulp or a hydraulic ore ore pulp.
4. dissolving-out process according to claim 1, it is characterized in that, described step 2) concrete grammar is: allocate mixed liquid in the pre-desiliconizing groove, be deployed into ore pulp, by feeding pump, ore pulp is sent into surge pump, surge pump carries out preheating with pulp conveying to cannula primary heater, steam is from flash drum, and the water of condensation of generation enters the sedimentation hot water tank.
5. dissolving-out process according to claim 4, is characterized in that, described surge pump is four, and surge pump is delivered to ore pulp respectively four canalization preheatings of cannula primary heater.
6. according to claim 4 or 5 described dissolving-out process, is characterized in that, described mixed liquid is that the mother liquor after the seed precipitation solution evaporation concentration is allocated into liquid caustic soda again and be get final product, and the severe alkali concn of described mixed liquid is 238～240g/l, ak2.8-3.0.
7. dissolving-out process according to claim 1, is characterized in that, the described ore pulp of step 3) under the pressure of surge pump promotes, heats pulp conveying after snubber mixes in different digesters.
8. dissolving-out process according to claim 1, is characterized in that, the ore pulp ak after described step 6) flash distillation is 1.40～1.45, and the dilution ore pulp contains admittedly less than 70g/l.
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104692425A (en) * | 2013-12-10 | 2015-06-10 | 沈阳铝镁设计研究院有限公司 | Method for reducing smoking of dissolution dilution tank |
| CN107764850A (en) * | 2016-08-23 | 2018-03-06 | 沈阳铝镁设计研究院有限公司 | A kind of method of aluminum oxide high-pressure dissolved mineral slurry molecular proportion on-line checking |
| CN111732116A (en) * | 2020-08-14 | 2020-10-02 | 中铝山东工程技术有限公司 | Aluminium hydroxide redissolution system |
| CN112209414A (en) * | 2020-09-01 | 2021-01-12 | 靖西天桂铝业有限公司 | Linkage hot test process before production of aluminum oxide |
| CN117069130A (en) * | 2023-07-12 | 2023-11-17 | 沈阳铝镁设计研究院有限公司 | Method for reducing new steam consumption in alumina production |
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| US2852343A (en) * | 1954-09-30 | 1958-09-16 | Kaiser Aluminium Chem Corp | Process for treating aluminous ores |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104692425A (en) * | 2013-12-10 | 2015-06-10 | 沈阳铝镁设计研究院有限公司 | Method for reducing smoking of dissolution dilution tank |
| CN107764850A (en) * | 2016-08-23 | 2018-03-06 | 沈阳铝镁设计研究院有限公司 | A kind of method of aluminum oxide high-pressure dissolved mineral slurry molecular proportion on-line checking |
| CN111732116A (en) * | 2020-08-14 | 2020-10-02 | 中铝山东工程技术有限公司 | Aluminium hydroxide redissolution system |
| CN112209414A (en) * | 2020-09-01 | 2021-01-12 | 靖西天桂铝业有限公司 | Linkage hot test process before production of aluminum oxide |
| CN112209414B (en) * | 2020-09-01 | 2022-11-11 | 靖西天桂铝业有限公司 | Linkage hot test process before alumina production |
| CN117069130A (en) * | 2023-07-12 | 2023-11-17 | 沈阳铝镁设计研究院有限公司 | Method for reducing new steam consumption in alumina production |
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Effective date of registration: 20170417 Address after: 533821 Jingxi the Guangxi Zhuang Autonomous Region canal town Patentee after: Guangxi Xinfa Aluminum Co. Ltd. Address before: 252100 Shandong County of Chiping city in Liaocheng Province, seven kilometers west of the city Patentee before: Chiping Xinfa Huayu Alumina Co., Ltd. |
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Effective date of registration: 20180608 Address after: 032300 Xiaoyi City, Lvliang, Shanxi Patentee after: Shanxi Xin hair Chemical Co., Ltd. Address before: 533821 the Guangxi Zhuang Autonomous Region Jingxi city canal town Patentee before: Guangxi Xinfa Aluminum Co. Ltd. |