WO2007045154A1 - Appareil de digestion d'alumine - Google Patents

Appareil de digestion d'alumine Download PDF

Info

Publication number
WO2007045154A1
WO2007045154A1 PCT/CN2006/002701 CN2006002701W WO2007045154A1 WO 2007045154 A1 WO2007045154 A1 WO 2007045154A1 CN 2006002701 W CN2006002701 W CN 2006002701W WO 2007045154 A1 WO2007045154 A1 WO 2007045154A1
Authority
WO
WIPO (PCT)
Prior art keywords
pressure
dissolution
specifications
flasher
alumina
Prior art date
Application number
PCT/CN2006/002701
Other languages
English (en)
Chinese (zh)
Inventor
De Chen
Original Assignee
China Aluminum International Engineering Corporation Limited
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by China Aluminum International Engineering Corporation Limited filed Critical China Aluminum International Engineering Corporation Limited
Priority to BRPI0617714-0B1A priority Critical patent/BRPI0617714B1/pt
Publication of WO2007045154A1 publication Critical patent/WO2007045154A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/02—Apparatus therefor
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
    • C01F7/00—Compounds of aluminium
    • C01F7/02—Aluminium oxide; Aluminium hydroxide; Aluminates
    • C01F7/04—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom
    • C01F7/06—Preparation of alkali metal aluminates; Aluminium oxide or hydroxide therefrom by treating aluminous minerals or waste-like raw materials with alkali hydroxide, e.g. leaching of bauxite according to the Bayer process
    • C01F7/062—Digestion
    • C01F7/064—Apparatus for digestion, e.g. digestor vessels or heat exchangers
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B21/00—Obtaining aluminium
    • C22B21/0015—Obtaining aluminium by wet processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • This invention relates to alumina production equipment, and more particularly to dissolution apparatus for alumina production.
  • the large-scale equipment is the development trend of the alumina industry at home and abroad. It can increase the alumina plant capacity, automation equipment level and labor productivity, improve technical and economic indicators, and reduce consumption.
  • the Bayer process alumina plant which is newly built using Sanshui bauxite as a raw material, has a production capacity of 700-900 kt/year alumina.
  • Dissolution is the core process in the alumina production process.
  • the domestic alumina plant Bayer process production system uses a maximum capacity of 450kt/year.
  • a set of original pulp by volume dissolution apparatus is 460 ⁇ 470m 3 / h, the two dissolution apparatus for producing alumina a year, more than 900,000 Tuen p.
  • alumina plant can be further developed in the direction of large-scale is the key to whether the dissolution device can be further enlarged.
  • the invention combines the current alumina production situation and the development trend of the alumina industry, studies the dissolution device, and proposes a new large-scale dissolution device and a matching scheme, and the raw slurry amount that the dissolution device can pass is 52 0 ⁇ 550 m 3 /h, can increase alumina production capacity to 500kt / year.
  • the object of the present invention is to provide a new large-scale dissolution apparatus which can increase the existing dissolution apparatus having an alumina capacity of 450 kt/year to 500 kt/year, thereby further increasing the size of the dissolution apparatus.
  • the invention is implemented as follows: It comprises the following equipment:
  • heating tube bundle cooker 15 or 16 units (with 13 or 14 units, 2 units), design pressure 5.2Mpa, pressure cooker specifications: ⁇ 3 X 18m;
  • cooker 4 or 5 sets, design pressure 5.2Mpa, cooker specifications: ⁇ 3> ⁇ 18 ⁇ ;
  • the above equipment is connected by pipes in the order of the dissolution process.
  • the equipment given above contains the necessary equipment for the process, including: 1 high-pressure diaphragm pump; 2 sets of boilers with heating tube bundles, 2 sets of flashers (so 2 sets of 12 flashers) Form a ten-level flash process).
  • the main technical indicators of the new dissolution apparatus are: circulating mother liquor: Na 2 0 K 230 ⁇ 250g/l, R P 0.53 - 0.60; raw pulp temperature: 85 ⁇ 96 dissolution temperature: 255-262 °C; dissolution time: 30 ⁇ 60min; Alumina dissolution rate: >93%; Eluent R P : 1.15- 1.20; Dissolution red mud-base ratio: 0.28 ⁇ 0.40; Last stage self-evaporation temperature: 127-135; Dissolution apparatus operating rate: >9 3 %; Diluent The residence time of the tank after dissolution: 3.5 ⁇ 4.5h.
  • the alumina capacity can reach 450 kt / year. If the raw slurry of the dissolution device passes With a capacity of 525 m 3 /h, the alumina capacity can reach 500 kt/year.
  • the novel dissolution apparatus of the invention can pass the raw slurry of 5 2 5 ⁇ 5 50 m 3 / h, and the basis thereof is as follows:
  • high-pressure diaphragm pump the domestic alumina industry in the Netherlands GEHO this process usually produced by high pressure diaphragm pumps, now the company's new diaphragm pump its maximum flow up to 550m 3 / h, can meet this primary section Pulp flow requirements; diaphragm pumps with flow rates of 250 ⁇ 300m 3 /h can also be used, and two pumps can be used to feed the dissolution device at the same time; domestic pumps of the same type can also be used.
  • casing preheater ⁇ , inner casing diameter D325xl3, when passing 525 ⁇ 550m 3 /h raw slurry, the slurry flow rate is 2.08 ⁇ 2.18m / s, according to the principles of fluid mechanics and Industry experience, when the original slurry in the tube flow rate is in the range of 2.0 ⁇ 2.5m / s, the casing preheater can achieve the best heat transfer effect, and it is not easy to generate scars in the pipe.
  • the heat transfer area, the jacket preheater, the total heat transfer area (calculated as the inner diameter of the inner tube) is 3174 m 2 , and the total heat transfer area of the original 450 kt / year casing preheater is 2595 m 2 , increasing The size is 22.3%, so the heat transfer area is sufficient to meet the 500kt/year alumina scale.
  • pulse buffer The volume increased by 17.3%, which can meet the 500kt/year alumina production requirements.
  • the volume of the cooker is 100m 3 /set
  • the volume of the existing cooker is 8:3 m 3 /set
  • each volume increases by 20.5%.
  • the heat transfer area of the cooker with heating tube is 540m 2
  • the heat transfer area of the cooker is 610m 2
  • the volume of the cooker and the heat transfer area are both Can meet the 500kt / year alumina production requirements.
  • Flash evaporator There are 12 flash evaporators in this dissolution apparatus.
  • the existing 450kt/year dissolution apparatus has a flasher size of (
  • the flasher of this dissolution apparatus adjusts it to ⁇ 3.5 ⁇ 5.5 9.7m, the cross-sectional area of each flasher increased by 21.0 - 36.1%, which can meet the 500kt / year alumina production requirements.
  • the main equipment of the novel dissolution apparatus of the present invention is subjected to capacity review, and its alumina production capacity can fully meet the needs of 500 kt/year.
  • the raw slurry from the raw material mill or atmospheric desiliconization process is pumped into the high pressure diaphragm pump, and the raw slurry is sent to the first pulse buffer through the high pressure diaphragm pump, and then into the 5-6 stage casing preheater.
  • the original slurry enters the 4 ⁇ 5 preheating cooker, preheating the original slurry temperature to about 200 ,, and then heating it into the reaction digester with new steam, and the temperature is raised to 255 ⁇ 262 ⁇ normal dissolution temperature requirements, followed by thermal insulation dissolution residence time 30 ⁇ 60min, after the dissolution, the slurry enters the slurry from the evaporator, and the temperature is reduced from 255 ⁇ 260 "C to 127 ⁇ 135 ⁇ , and then the temperature is from 255 ⁇ 260 "C to 127 ⁇ 135 ⁇ , and then sent to the dilution tank, and the red mud washing liquid from the sedimentation workshop.
  • the post-dissolution trough is sent, and the diluted slurry is left in the trough after the dissolution for about 4 hours to remove impurities such as silicon and iron in the solution, and then sent to the sedimentation workshop.
  • connection mode of each device of the dissolution device is:
  • the high pressure diaphragm pump is connected with the first pulse buffer (pressure 7.0Mpa)
  • the first pulse buffer is connected with the casing preheater
  • the casing preheater and the second buffers pulse (pressure 5 .2Mpa) is connected
  • a second set of buffers pulse tube bundle with a heating boiler pressure connection with a tube bundle heat Autoclave Autoclave connected with, autoclaving with a set of flash
  • the steamer and the flasher outlet are connected to the dilution tank.
  • the invention has the beneficial effects of: increasing the 450kt/year alumina production scale of each existing dissolution device to 500kt/year or more, which makes the alumina industry of China take a big step forward in the large-scale equipment, further improving China Alumina technical equipment level.
  • Figure 1 is a schematic view of the process flow of the present invention.
  • Embodiments of the invention The following equipment is selected according to the alumina capacity of 500 kt/year:
  • casing preheater preheating with six-stage casing, six per stage, each casing length is 90m, the total length of casing is 3240m; inner casing specification is: D325 x l3 ⁇ 14, outer casing specification is: D402 9 ⁇ 10;
  • pulse buffer 2 sets, the pressure is 5.2Mpa and 7.0Mpa respectively, equipment specifications: ⁇ 2.6 10m, volume 42m 3 ;
  • heating tube bundle cooker 16 sets, design pressure 5.2Mpa, pressure cooker specifications: ⁇ 3 X 18m, volume 100m 3 , heating area 610m 2 ;
  • 5 pressure cooker 5 sets, design pressure 5.2Mpa, cooker specifications: ⁇ 3 ⁇ 18 ⁇ , volume 100m 3 ;
  • the above equipment is connected in series according to the dissolution process sequence to form a complete process of the dissolution process.
  • the main technical indicators of the new dissolution apparatus are: circulating mother liquor: Na 2 0 K 235 ⁇ 245g/l, R P 0.53 - 0.55; raw pulp temperature: 90 ⁇ ; dissolution temperature: 258 ⁇ 262 ⁇ ; dissolution time: 40min; alumina dissolution rate : 93% ⁇ 95%; eluent R P : 1.18 ⁇ 1.20; dissolution ratio of red mud to alkali: 0.28 - 0.38;
  • the final stage self-evaporation temperature 130 ⁇ i: 32°C; the dissolution rate of the dissolution device: 93 % ⁇ 9 6%; the residence time of the solution after the dissolution of the diluent: 4h.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Organic Chemistry (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Geology (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Mechanical Engineering (AREA)
  • Manufacturing & Machinery (AREA)
  • General Health & Medical Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Nutrition Science (AREA)
  • Inorganic Chemistry (AREA)
  • Environmental & Geological Engineering (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)
  • Paper (AREA)

Abstract

La présente invention a trait à un appareil de digestion d'alumine, comportant les dispositifs suivants: des pompes à membrane haute pression, des dispositif de préchauffage à double conduite, des amortisseurs d'impulsions, des autoclaves avec des faisceaux de tubes de chauffage, des autoclaves et des évaporateurs à détente. Les dispositifs sont reliés successivement par des conduites selon le procédé de lessivation. L'appareil améliore le rendement d'alumine de 450kt/année par un appareil existant à 500kt/année, permettant ainsi une amélioration de la productivité.
PCT/CN2006/002701 2005-10-19 2006-10-13 Appareil de digestion d'alumine WO2007045154A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
BRPI0617714-0B1A BRPI0617714B1 (pt) 2005-10-19 2006-10-13 Aparelho de digestão de alumina

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CNB2005102006200A CN1295354C (zh) 2005-10-19 2005-10-19 氧化铝溶出装置及工艺
CN200510200620.0 2005-10-19

Publications (1)

Publication Number Publication Date
WO2007045154A1 true WO2007045154A1 (fr) 2007-04-26

Family

ID=36679236

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2006/002701 WO2007045154A1 (fr) 2005-10-19 2006-10-13 Appareil de digestion d'alumine

Country Status (3)

Country Link
CN (1) CN1295354C (fr)
BR (1) BRPI0617714B1 (fr)
WO (1) WO2007045154A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102531011A (zh) * 2011-12-22 2012-07-04 东北大学设计研究院（有限公司） 可实现高低温两种溶出方式的氧化铝溶出装置及方法
CN109437265A (zh) * 2018-12-25 2019-03-08 中铝视拓智能科技有限公司 高压溶出闪蒸系统效率优化方法和效率优化系统

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1295354C (zh) * 2005-10-19 2007-01-17 贵阳铝镁设计研究院 氧化铝溶出装置及工艺
CN101264912B (zh) * 2007-03-14 2011-05-04 贵阳铝镁设计研究院 氧化铝高压溶出工段的加热及保温溶出方法
CN102531004B (zh) * 2010-12-21 2014-09-10 贵阳铝镁设计研究院有限公司 一种一水硬铝石高压溶出方法及装置
CN103101947B (zh) * 2013-03-11 2014-08-27 茌平信发华宇氧化铝有限公司 一种氧化铝生产过程中的溶出工艺

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2033968C1 (ru) * 1992-07-21 1995-04-30 Акционерное общество открытого типа "Уральский научно-исследовательский и проектный институт алюминиевой промышленности" Установка для выщелачивания боксита
RU2117632C1 (ru) * 1996-08-07 1998-08-20 Акционерное общество "Богословский алюминиевый завод" Способ выщелачивания боксита
CN1620405A (zh) * 2002-01-21 2005-05-25 皮奇尼铝公司 在压力浸煮－水合铝土矿过程中,通过回收利用冷凝物溶解碳酸盐
RU2256614C2 (ru) * 2003-10-16 2005-07-20 Открытое акционерное общество "Сибирско-Уральская алюминиевая компания" Способ выщелачивания боксита
WO2005066378A1 (fr) * 2004-01-07 2005-07-21 Grenvil Marquis Dunn Circuits d'autoclave de lixiviation sous pression exothermique
CN1752231A (zh) * 2005-10-19 2006-03-29 贵阳铝镁设计研究院 氧化铝溶出装置

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
HU201276B (en) * 1988-10-27 1990-10-28 Magyar Aluminium Process for producing alum earth from bauxite containing gibbsite
CN1528669A (zh) * 2003-09-26 2004-09-15 中国铝业股份有限公司 氧化铝高压釜溶出系统的闪蒸器注水方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
RU2033968C1 (ru) * 1992-07-21 1995-04-30 Акционерное общество открытого типа "Уральский научно-исследовательский и проектный институт алюминиевой промышленности" Установка для выщелачивания боксита
RU2117632C1 (ru) * 1996-08-07 1998-08-20 Акционерное общество "Богословский алюминиевый завод" Способ выщелачивания боксита
CN1620405A (zh) * 2002-01-21 2005-05-25 皮奇尼铝公司 在压力浸煮－水合铝土矿过程中,通过回收利用冷凝物溶解碳酸盐
RU2256614C2 (ru) * 2003-10-16 2005-07-20 Открытое акционерное общество "Сибирско-Уральская алюминиевая компания" Способ выщелачивания боксита
WO2005066378A1 (fr) * 2004-01-07 2005-07-21 Grenvil Marquis Dunn Circuits d'autoclave de lixiviation sous pression exothermique
CN1752231A (zh) * 2005-10-19 2006-03-29 贵阳铝镁设计研究院 氧化铝溶出装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
LI X. AND FAN W.: "Problems in High-pressure Leaching and its Improving Method", LIGHT METAL, no. 6, 2002, pages 11 - 13, XP008080139 *

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102531011A (zh) * 2011-12-22 2012-07-04 东北大学设计研究院（有限公司） 可实现高低温两种溶出方式的氧化铝溶出装置及方法
CN102531011B (zh) * 2011-12-22 2013-11-06 东北大学设计研究院（有限公司） 可实现高低温两种溶出方式的氧化铝溶出装置及方法
CN109437265A (zh) * 2018-12-25 2019-03-08 中铝视拓智能科技有限公司 高压溶出闪蒸系统效率优化方法和效率优化系统
CN109437265B (zh) * 2018-12-25 2021-03-23 中铝视拓智能科技有限公司 高压溶出闪蒸系统效率优化方法和效率优化系统

Also Published As

Publication number Publication date
CN1752231A (zh) 2006-03-29
CN1295354C (zh) 2007-01-17
BRPI0617714A2 (pt) 2011-08-02
BRPI0617714B1 (pt) 2014-01-21

Similar Documents

Publication Publication Date Title
WO2007045154A1 (fr) Appareil de digestion d'alumine
CN101445256A (zh) 一种一水硬铝石型铝土矿的大型管道加停留罐溶出工艺
CN101767806B (zh) 一种一水硬铝石型铝土矿的大型管道加停留罐的溶出工艺
CN105692665B (zh) 三水铝石型铝土矿的并联列管加停留罐溶出系统及方法
CN102249271B (zh) 一种三水铝石型铝土矿的列管加停留罐溶出系统及方法
CN211920887U (zh) 一种用于三水铝石与一水软铝石混合铝土矿溶出的装置
CN107399870B (zh) 一种德士古气化炉黑水热回收处理系统
CN210632117U (zh) 一种连续反应装置
CN102583461B (zh) 氧化铝高压溶出工艺利用蒸汽冷凝水预热的装置及方法
CN107790072A (zh) 费托浆态床反应系统和费托合成反应的方法
CN107915244A (zh) 一种三水铝石型铝土矿双流法溶出的工艺装置和方法
CN106145166B (zh) 一种氧化铝生产中高压溶出热量综合利用方法及装置
CN205235931U (zh) 一种连续化生产大分子不饱和聚醚反应装置
CN202099075U (zh) 一种三水铝石型铝土矿的列管加停留罐溶出系统
CN1915827B (zh) 氧化铝生产工艺中铝酸钠溶液全闪蒸的蒸发方法及设备
CN214936100U (zh) 一种拜耳法高低温联合溶出机组
CN103408681A (zh) 一种大幅度提高聚氯乙烯产能的方法
CN207845172U (zh) 一种三水铝石型铝土矿双流法溶出的工艺装置
CN103101942B (zh) 一种高效利用溶出工序二次蒸汽的工艺
CN102515225B (zh) 一种双套管预热免搅拌停留保温的氧化铝溶出方法
CN106830026A (zh) 氧化铝生产中高压溶出的方法
CN108067167A (zh) 浆态床反应系统和费托合成反应的方法
CN109556414B (zh) 一种氢氧化铝焙烧炉产品的余热利用方法及装置
CN201634445U (zh) 一种氧化铝管道化溶出装置
CN109126640A (zh) 浆态床反应系统和费托合成反应的方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application
NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 06791261

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: PI0617714

Country of ref document: BR

Kind code of ref document: A2

Effective date: 20080422