WO2011041956A1 - 利用中低品位MnO2矿进行烟气脱硫制备MnSO4·H2O的方法 - Google Patents
利用中低品位MnO2矿进行烟气脱硫制备MnSO4·H2O的方法 Download PDFInfo
- Publication number
- WO2011041956A1 WO2011041956A1 PCT/CN2010/075314 CN2010075314W WO2011041956A1 WO 2011041956 A1 WO2011041956 A1 WO 2011041956A1 CN 2010075314 W CN2010075314 W CN 2010075314W WO 2011041956 A1 WO2011041956 A1 WO 2011041956A1
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- flue gas
- mns0
- slurry
- preparing
- stage
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G45/00—Compounds of manganese
- C01G45/10—Sulfates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/80—Semi-solid phase processes, i.e. by using slurries
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/60—Inorganic bases or salts
Definitions
- the invention relates to a method for preparing MnS0 4 ⁇ H 2 0 by using flue gas desulfurization with medium and low grade Mn0 2 ore.
- CN1824 372A mentions a microwave-catalyzed flue gas desulfurization technology, which has a high desulfurization efficiency for simulating flue gas, but requires special equipment, and the desulfurized gas still needs dilute acid absorption; the reaction catalyst bed needs to be continuously regenerated. It is not conducive to the smooth operation of continuous large industrial production equipment.
- CN188 3764A uses its own high-value chemical manganese dioxide, electrolytic manganese dioxide for desulfurization treatment, high cost and complicated operation, which does not meet China's national conditions, and the subsequent treatment of manganese sulfate solution produced by desulfurization is not involved. .
- the invention provides a method for preparing MnS0 4 ⁇ H 2 0 by using flue gas desulfurization with medium and low grade Mn0 2 ore, the method involving the following chemical reactions:
- the invention relates to a method for preparing MnS0 4 ⁇ H 2 0 by flue gas desulfurization using medium and low grade Mn0 2 ore as follows:
- a First select the treated Mn0 2 ore fines with a fineness of 80-1 00. Use wet ball milling or rod grinding, water or circulating mother liquor or washing slag to prepare the initial solid-liquid ratio (% by weight). 5% ⁇ The 5% by weight of the slurry, and the Mn0 2 content of the slurry reached 1.5% (% by weight) or more.
- the sieve is sieved by a Taylor sieve, that is, a particle size range corresponding to 80 - 100 mesh It is 1 50- 18 0 ⁇ ⁇ .
- a sulfur-containing flue gas is introduced into the absorption device, and the flue gas may be a coal-fired converter tail gas, a boiler exhaust gas or other S0 2- containing exhaust gas, and the gas velocity is generally controlled at Q. 5-4 m/s ec, and the gas-liquid ratio is generally Controlled at 10-40L/m 3 .
- the slurry of Mn0 2 is added to the absorption device, and the reverse flow is controlled with respect to the sulfur-containing flue gas. After the action of the Mn0 2 is completed, the separation process is performed, and the flue gas after the desulfurization is discharged from the absorption device.
- the singular solid-liquid ratio is 25-30%, and the superficial velocity is 1. 5 ⁇ 0. 2m/ s ec , if the mineral powder having a total manganese content of 15% by weight or less is used as the raw material.
- the ratio of gas to liquid is 15-25 L/m 3 .
- the gas outlet temperature is controlled to > 60 ° C to maintain a certain amount of solution evaporation to ensure a thickening effect.
- step C The Mn0 2 slurry discharged from step B is subjected to pressure filtration separation, and the mother liquid separated by pressure filtration is returned to the absorption device, and the specific position is in the slurry circulation pool, and the evaporation is carried out by using the heat of the flue gas to continue the introduction.
- the operation was carried out until the concentration of MnS0 4 in the mother liquor was > 200 g/L.
- the absorption device in the steps B and C can select a tertiary absorption device.
- the steps B and C are specifically:
- the B firstly introduces flue gas in the first stage of the absorption device, the gas velocity is controlled at 0. 5-4 m / s ec, the gas-liquid ratio is controlled at 10-40 L/m 3 , and then in the absorption device
- the Mn0 2 slurry is added to the third stage, and the counter-flow is controlled relative to the flue gas.
- the three stages of the three-stage absorption device are simultaneously self-circulating, that is, the first-stage absorption slurry is continuously from the second stage.
- the third stage continuously replenishes the slurry to the second stage, and the newly prepared Mn0 2 slurry is continuously replenished to the third stage.
- the first stage enters the separation process, and the de-stone-filled smoke is removed.
- the Mn0 2 slurry discharged from the step B is subjected to pressure filtration separation, and the mother liquid separated by the pressure filtration is returned to the circulating water tank of the first stage of the absorption device, and concentrated by the evaporation of the heat of the flue gas, and the operation is continued until the operation is continued.
- the concentration of MnS0 4 in the mother liquor was > 200 g/L.
- the third-stage absorption device is a conventional experimental device in the field, and is used in the present invention, which is intended to fully utilize the raw materials, save costs, improve reaction efficiency, and continuously carry out the reaction, and optimize the present invention, and it is emphasized that other The method of optimizing the absorption device can also serve to optimize the present invention, for example, a secondary or multi-stage absorption device can also implement the present invention.
- step D adjust the pH of the clear solution according to the concentration requirement obtained by pressure filtration in step C to 2-4.
- the pH is 3. 0-3. 5
- lime milk or dilute gram acid can be used, and the temperature is controlled at room temperature (25 ° C) to 95 ° C, preferably 50-70 ° C, and manganese sulfide is added under stirring to carry out the reaction.
- the industrial grade manganese sulphide produced by Guizhou Red Star Development Co., Ltd. can be used, and the impurities are removed by filtration.
- the membrane is sprayed with 0.5 ⁇ m ⁇ , and continuously stirred for 1-1. 5 hours, and then separated by pressure filtration, and the obtained clarified filtrate is subjected to filtration.
- Evaporation preferably multi-effect evaporation, after drying the gas stream, MnS0 4 . ⁇ 2 0 product can be obtained, and the obtained filter residue is mainly metal sulfide, and the valuable metal can be recovered by using the same.
- the multi-effect evaporation is a conventional method for reducing steam consumption in the art, and the low-temperature solution is heated by the secondary steam generated by evaporation, thereby achieving the purpose of saving.
- the step of preparing the filter cake obtained in the step C is stirred with water for 1 - 1. 5 hours, and the ratio of the control water to the water is 1: 4-1 : 5 range.
- a method of washing a high concentration slag with a low concentration of water may be employed, which increases the number of washings, increases the washing efficiency, and reduces the volume of the solution.
- Mn0 2 ore powder residue is obtained, which can be used for making building materials or directly for harmless landfill treatment, and the obtained mother liquor can be used as a preparation slurry.
- the invention discloses a method for preparing MnS0 4 ⁇ ⁇ 2 0 by using flue gas desulfurization with medium and low grade Mn0 2 ore, directly utilizing medium and low grade manganese oxide ore powder slurry spraying and absorbing desulfurization treatment, without special equipment, and The resulting MnS0 4 solution is concentrated, decontaminated and valuable metal recovered, making full use of resources, and is operable and implementable.
- the invention utilizes the redox reaction to perform multi-stage spraying of medium and low grade manganese oxide ore powder on the flue gas desulfurization under the wet condition, thereby solving the problem of desulfurization efficiency and stable operation.
- the invention reduces the concentration of the MnS0 4 solution produced by the desulfurization by using the flue gas energy to solve the problem of the production cost of the manganese sulfate product.
- the invention improves the total manganese recovery rate by multi-stage countercurrent treatment.
- the invention utilizes a special impurity removing agent to obtain high-efficiency recovery of valuable metals while purifying and removing the MnS0 4 solution.
- Example 1 Sulfur-containing flue gas is produced by the carbon reduction method to prepare industrial grade cesium carbonate kiln exhaust gas, the average gas volume
- the average S0 2 content is 1 3400mg/m 3
- the cyclone dust removal outlet temperature is about 170 °C.
- the sulfur-containing flue gas is introduced into the first stage of the absorption device, and the gas velocity of the empty column is controlled at 1.5 m/sec.
- the liquid-gas circulation spray ratio gas-liquid ratio
- the Mn0 2 slurry prepared in the step A is added, and the reverse flow is controlled with respect to the sulfur-containing flue gas, and the three stages of the third-stage absorption device are simultaneously self-circulating, that is, the first-stage absorption.
- the slurry is continuously replenished from the second stage, and the third stage continuously replenishes the slurry to the second stage, and the newly prepared Mn0 2 slurry is continuously replenished to the third stage, and is separated from the first stage after the Mn0 2 is completed.
- the flue gas after desulfurization is discharged from the third stage of the absorption device, the third stage desulfurization flue gas outlet temperature is 65 ° C, and the S0 2 content is 21 3_402 mg/m 3 .
- the discharged Mn0 2 slurry is subjected to pressure filtration separation, and the mother liquid separated by the pressure filtration is returned to the circulating water tank of the first stage of the absorption device, and concentrated by the evaporation of the flue gas, and the conduction operation is continued three times.
- the concentration of MnS0 4 in the mother liquor reached 317 g/L.
- the polysulfide filter cake obtained during the purification treatment of the manganese sulfate solution is dried to obtain the MS sample 1 # .
- Example 2 was carried out in the same manner as in Example 1 to obtain MnS0 4 .
- the mother liquor MnS0 4 concentration was determined to be 289 g/L, and the resulting clear solution was utilized.
- the polysulfide filter cake obtained during the purification of the manganese sulfate solution is dried to obtain an MS sample 2*.
- the sulfur-containing flue gas is prepared by the carbon reduction method to prepare industrial strontium kiln exhaust gas, the average gas volume is 17000NM7H, the average S0 2 content is 11500mg/m 3 , and the cyclone dust removal outlet temperature is 150°C.
- the Mn0 2 content in the obtained Mn0 2 slurry is 4.92%
- the liquid-gas circulation spray ratio is about 25L/m 3
- the empty tower speed is 1.7m/sec
- the third-stage outlet temperature is 60°C
- the third-stage outlet The S0 2 content is in the range of 114-322 mg/m 3 .
- the method of high concentration slag was washed for 1 hour, and the ratio of the feed water to the ratio of 1:4 was used, and the obtained mother liquid was used as a formulation slurry.
- the polysulfide filter cake obtained during the purification of the manganese sulfate solution is dried to obtain an MS sample 3 # .
- Example 4 was carried out in the same manner as in Example 1 to obtain MS sample 1 # :
- the sulfur-containing flue gas adopts coal-fired boiler exhaust gas, the average gas volume is 31000 ⁇ 7H, the average S0 2 content is 4800 mg/m 3 , and the cyclone dust removal outlet temperature is about 170 °C.
- the Mn0 2 wet base total manganese content is 9.10%
- the slurry initial solid-liquid ratio is 25%
- the Mn0 2 content in the obtained Mn0 2 slurry is 2.88%
- the liquid-gas circulation spray ratio is about 20L/m 3
- the empty tower speed It is 1.5 m/sec
- the third stage outlet temperature is 75 °C
- the tertiary outlet S0 2 content is 74_162 mg/m 3 .
- the polysulfide filter cake obtained during the purification treatment of the manganese sulfate solution is dried to obtain an MS sample 4 # .
- the main component contents (% by weight) of the MnS0 4 ⁇ H 2 0 samples obtained in the respective examples were measured as follows:
- the main component content (% by weight) of the MS samples obtained in the respective examples was measured as follows.
Description
Claims
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/514,397 US9018119B2 (en) | 2009-10-10 | 2010-07-20 | Method for preparing manganese sulfate monohydrate by desulfurizing fume with middle-low grade manganese dioxide ore |
EP10821565.8A EP2487137B1 (en) | 2009-10-10 | 2010-07-20 | Method for preparing manganese sulfate monohydrate by desulfurizing fume with middle-low grade manganese dioxide ore |
KR1020127012029A KR101321317B1 (ko) | 2009-10-10 | 2010-07-20 | 중저품질의 NnO2 광석을 사용한 배연탈황으로 MnSO4ㆍH2O를 제조하는 방법 |
AU2010305218A AU2010305218B2 (en) | 2009-10-10 | 2010-07-20 | Method for preparing manganese sulfate monohydrate by desulfurizing fume with middle-low grade manganese dioxide ore |
ZA2012/03392A ZA201203392B (en) | 2009-10-10 | 2012-05-09 | Method for preparing manganese sulfate monohydrate by desulfurizing fume with middle-low grade manganese dioxide ore |
HK13100089.7A HK1172883A1 (zh) | 2009-10-10 | 2013-01-03 | 利用中低品位 礦進行烟氣脫硫製備 的方法 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN200910179944.9 | 2009-10-10 | ||
CN2009101799449A CN101723466B (zh) | 2009-10-10 | 2009-10-10 | 利用中低品位MnO2矿进行烟气脱硫制备MnSO4·H2O的方法 |
Publications (1)
Publication Number | Publication Date |
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WO2011041956A1 true WO2011041956A1 (zh) | 2011-04-14 |
Family
ID=42445122
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/CN2010/075314 WO2011041956A1 (zh) | 2009-10-10 | 2010-07-20 | 利用中低品位MnO2矿进行烟气脱硫制备MnSO4·H2O的方法 |
Country Status (8)
Country | Link |
---|---|
US (1) | US9018119B2 (zh) |
EP (1) | EP2487137B1 (zh) |
KR (1) | KR101321317B1 (zh) |
CN (1) | CN101723466B (zh) |
AU (1) | AU2010305218B2 (zh) |
HK (1) | HK1172883A1 (zh) |
WO (1) | WO2011041956A1 (zh) |
ZA (1) | ZA201203392B (zh) |
Cited By (2)
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WO2013165071A1 (ko) * | 2012-04-30 | 2013-11-07 | 전남대학교산학협력단 | 고순도 황산망간일수화물의 제조방법 및 그 제조방법에 의하여 제조된 고순도 황산망간일수화물 |
JP2013245159A (ja) * | 2012-05-28 | 2013-12-09 | Guizhou Redstar Developing Co Ltd | クラウス法テールガスを包括的に処理するとともに硫酸マンガンを製造する方法 |
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- 2009-10-10 CN CN2009101799449A patent/CN101723466B/zh active Active
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- 2010-07-20 AU AU2010305218A patent/AU2010305218B2/en not_active Ceased
- 2010-07-20 EP EP10821565.8A patent/EP2487137B1/en not_active Not-in-force
- 2010-07-20 US US13/514,397 patent/US9018119B2/en not_active Expired - Fee Related
- 2010-07-20 WO PCT/CN2010/075314 patent/WO2011041956A1/zh active Application Filing
- 2010-07-20 KR KR1020127012029A patent/KR101321317B1/ko active IP Right Grant
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2012
- 2012-05-09 ZA ZA2012/03392A patent/ZA201203392B/en unknown
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Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2013165071A1 (ko) * | 2012-04-30 | 2013-11-07 | 전남대학교산학협력단 | 고순도 황산망간일수화물의 제조방법 및 그 제조방법에 의하여 제조된 고순도 황산망간일수화물 |
US9365912B2 (en) | 2012-04-30 | 2016-06-14 | Industry Foundation Of Chonnam National University | Method for producing high-purity manganese sulfate monohydrate and high-purity manganese sulfate monohydrate produced by the method |
JP2013245159A (ja) * | 2012-05-28 | 2013-12-09 | Guizhou Redstar Developing Co Ltd | クラウス法テールガスを包括的に処理するとともに硫酸マンガンを製造する方法 |
Also Published As
Publication number | Publication date |
---|---|
KR20120093948A (ko) | 2012-08-23 |
EP2487137A4 (en) | 2013-05-22 |
AU2010305218B2 (en) | 2014-02-06 |
CN101723466A (zh) | 2010-06-09 |
KR101321317B1 (ko) | 2013-10-30 |
CN101723466B (zh) | 2011-11-30 |
US9018119B2 (en) | 2015-04-28 |
ZA201203392B (en) | 2013-01-30 |
US20120328495A1 (en) | 2012-12-27 |
EP2487137B1 (en) | 2015-03-25 |
EP2487137A1 (en) | 2012-08-15 |
HK1172883A1 (zh) | 2013-05-03 |
AU2010305218A1 (en) | 2012-05-31 |
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