CN105154918A - Electrolytic manganese production system capable of saving energy and reducing consumption - Google Patents
Electrolytic manganese production system capable of saving energy and reducing consumption Download PDFInfo
- Publication number
- CN105154918A CN105154918A CN201510741339.1A CN201510741339A CN105154918A CN 105154918 A CN105154918 A CN 105154918A CN 201510741339 A CN201510741339 A CN 201510741339A CN 105154918 A CN105154918 A CN 105154918A
- Authority
- CN
- China
- Prior art keywords
- pump
- production system
- catholyte
- energy
- saving
- 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.)
- Granted
Links
Landscapes
- Electrolytic Production Of Non-Metals, Compounds, Apparatuses Therefor (AREA)
Abstract
The invention discloses an electrolytic manganese production system capable of saving energy and reducing consumption. The electrolytic manganese production system capable of saving the energy and reducing the consumption mainly comprises an electrolyzer, a balance buffer tank, a heat exchanger, a continuous crystallizing tank, a water source heat pump, a dying oven, a centrifugal filter, a filter press, a pulp barrel and a leaching barrel. The electrolytic manganese production system is composed of a main circulation loop of electrolytic production, a catholyte small circulation loop of manganese slag extraction and a catholyte cooling loop of tank liquor cooling, and efficient recycling of soluble manganese of manganese slags and efficient conversion and full utilization of joule heat produced through electrolysis are achieved. By means of the electrolytic manganese production system capable of saving the energy and reducing the consumption, energy and material consumption of the electrolytic production is greatly reduced, the benefit is significant, and the important role in solving the problems of saving the energy and reducing emission in the industry is played.
Description
Technical field
The present invention relates to hydrometallurgy electrolytic metal production system, be related specifically to a kind of energy-saving and cost-reducing electrolytic metal Mn production system.
Background technology
Traditional electrolytic metal Mn is produced: electrolytic solution flows into anolyte compartment by cathode compartment through diaphragm bag, produce the anolyte remittance anode false end in anolyte compartment after, flow out through channel isolation edge from electrolyzer again, anolyte enters leaching barrel, add sulfuric acid leaching manganese mineral powder, leach liquor, after purification and impurity removal filters, returns electrolysis.Mn in electrolytic process
2+precipitating metal manganese on cathode compartment inner cathode plate, and produce electrocaloric effect releasing joule heating, take away except anolyte and evaporate with groove face, outside cell body heat radiation, also has a large amount of heat storages in groove, " nation manganese industry technology " the 20 chapter gives surveys by Theoretical Calculation and production plant the data drawn: often separate out 1Kg manganese metal and need derive 4.6 × 103KJ heat (the summer high-temperature earning in a day), because in traditional slot, the shortcoming of heat existence is derived in cooling: heat transfer efficiency is poor, cooling water inflow is large (often to be produced 1 ton of product and needs cooling water inflow 200 ~ 250m3, it is 4 ~ 5 times of circulation of elecrolyte amount), water evaporates, blowing, the loss such as seepage many (often producing one ton of product manganese loss 1.5 ~ 2m3 water coolant), groove electrolyte inside impurity easily accumulates, fouling is fast, affect electrolytic efficiency and quality product, many drawbacks, make numerous producer attempt groove to cool outward, but the technological achievement that it is not yet seen, there are the cooling of a patent CN01111708.3(manganese electrolysis cathode liquid and the recovery method of magnesium in one's early years), also industrial implementation is not obtained, there is following shortcoming: 1. enter tank liquor manganese concentration low, enter tank liquor temperature relatively high, the exchange capacity of heat and the exchange capacity of matter (manganese) in groove will be met simultaneously, be difficult to operation control, and catholyte internal circulating load is large, it is more than 3 times of the electrolytic solution amount of following, consume energy high, 2. by catholyte self evaporative heat loss, restrict by envrionment temperature, not easily realize the accurate control (41 ~ 43 DEG C) of groove temperature, 3. crystallisate in evaporator tower, can occur in chute and collecting tank in a large number, cleaning trouble.
The electrolytic manganese output of China is large, account for more than 95% of the whole world, the manganese ore consumed is except a part of import, residue Dou Shi China has ore by oneself, and the manganese ore grade of China is low, along with a large amount of exploitation, the grade entering chemical combination bucket manganese powder from original 14 ~ 18% dropped to that 10 ~ 13%(has also through magnetic concentration), qualifying liquid processed containing manganese concentration also from original containing Mn
2+36 ~ 38g/L drops to containing Mn
2+34 ~ 35g/L, qualifying liquid is containing Mn
2+measure low, the consumption liquid measure of ton product manganese will be increased, thus increase the internal circulating load of electrolysis liquid, certainly will increase the leaching in liquid process processed, the load of filtration and auxiliary material to consume, cause feed flow difficulty sometimes, production can not normally be carried out, although the production line working rate of numerous producer is not high, abundant production line can deal with production, but production cost is high, so far also not with containing Mn
2+the qualifying liquid of below 34g/L is produced and obtains the producer of good economic benefit; To low-grade manganese powder high density liquid, manganese slag takes manganese amount out of greatly, and the yield of manganese declines, and also do not have economic benefit, this is all an application difficult problem for low grade ore.
Summary of the invention
The object of the present invention is to provide a kind of reduction energy and material consumption, can low Mn be adapted to
2+qualifying liquid produce the system of electrolytic manganese.
Object of the present invention realizes by the following technical solutions: a kind of energy-saving and cost-reducing electrolytic manganese production system, mainly comprise electrolyzer, equalizing and buffering groove, interchanger, continuous crystallizing tank, water resource heat pump, baking oven, centrifugal filter, pressure filter, change slurry bucket, leaching barrel, described electrolyzer, equalizing and buffering groove, negative electrode liquid pump, interchanger, continuous crystallizing tank are connected to ring successively by pipeline, form loop line; Described electrolyzer and balance dashpot with change starch bucket, mortar pump, pressure filter, rich manganese negative electrode liquid pool be connected to ring successively by pipeline, formation loop line; Described electrolyzer, anode liquid pool, anode pump, heating coil, leaching barrel, mortar pump, pressure filter, qualified liquid pool are connected to ring successively by pipeline, form loop line; Described continuous crystallizing tank, centrifugal filter, pump are connected to ring successively by pipeline, form loop line; Described water pot, water pump, interchanger, water resource heat pump are connected to ring successively by pipeline, form loop line, described water resource heat pump has water source (hot blast) heat pump and water source (hot water) heat pump, described water source (hot blast) heat pump is connected with baking oven, and described water source (hot water) heat pump is connected by pipeline with hot water barrel.
Further, described electrolyzer is primarily of cell body, negative plate, positive plate, diaphragm bag, division board of the false end, anolyte upflow tube, catholyte upflow tube, adapter, division board composition of the false end, polylith negative plate and positive plate is provided with in described cell body, described anode sleeve-board has diaphragm bag, described diaphragm bag end opening is connected with division board of the false end, more than division board of the described false end and diaphragm bag take exterior domain as cathode compartment, be anolyte compartment in described diaphragm bag, described anolyte compartment is communicated with false bottom compartment, described false bottom compartment is communicated with anolyte upflow tube, described anolyte upflow tube adjustment height, and anolyte is overflowed from cell body top, the catholyte upflow tube height adjustable that described cathode compartment top is arranged, and make the overflow port of overflow port higher than anolyte of catholyte.
Further, described equalizing and buffering groove is made up of cell body, balance communicating pipe, drain pipe, upflow tube, adapter, the upflow tube height adjustable that described cell body top is arranged, described upflow tube is connected with adapter, described balance communicating pipe is connected with electric tank cathode room, and described drain pipe is connected with negative electrode liquid pump.
Further, described electrolyzer and balance dashpot two groove face keep same level, and overflow port also keeps same level.
Further, described interchanger adopts plate-type heat exchanger or tubular heat exchanger.
Further, described heating coil also can adopt plate-type heat exchanger or tubular heat exchanger.
Beneficial effect of the present invention:
1, the joule heating thermal-pump unit that the electrocaloric effect in electrolytic process produces is converted to hot blast, not only cool cell liquid but also save existing electric heating drying electric cost, because the thermal efficiency of water resource heat pump can reach 4.5, the installed power of water resource heat pump dries installed power lower than electrothermal tube, add new cooling system power electric power far below existing hydrologic cycle cooling system power used, COMPREHENSIVE CALCULATING often produces 1 ton of electrolytic manganese power saving more than 120 degree.
2, water coolant storage significantly reduces, only need original 5% ~ 10%, cooling water circulation amount only needs original 20% ~ 25%, save in existing water cycle process simultaneously and evaporate, blowing loss, supplement new water in product manganese minimizing per ton 1.5 ~ 2m3, by electrolytic manganese industry clean production standard (HJ/T357-2007), a ton product can be made to consume the fresh water yield and to rise an index grade.
3, directly supplement electrolysis after catholyte washery slag concentrate, eliminate that major cycle Anodic immersion goes out, the isometric link consuming time of removal of impurities, circulation is fast, and internal circulating load is few, when qualifying liquid in major cycle is on the low side containing manganese (containing Mn
2+32 ~ 34g/L), major cycle amount can not be increased, increase cost (catholyte cyclic permutation cost) and be less than that Footwall drift amount is contained to be worth, still have an economic benefit; When major cycle qualifying liquid concentration normal value (containing Mn
2+34 ~ 38g/L), major cycle fluid volume can be reduced, consume and reduce, then can obtain higher economic benefit.
4, electrolyzer concentration adjustment and temperature regulate relatively independent, and groove temperature is easy to control, even concentration in groove, and calcium magnesium ammonium salt crystallization and impurity are concentrated, and easily process, clear groove cycle stretch-out, good product quality, and leaching efficiency improves, and comprehensive benefit is good.
5, because groove concentrates cooling and dosing outward, apply for a patent unit vat in 201510541317.0 and continuous automatic drier in conjunction with the present inventor, larger benefit will be played.
Accompanying drawing explanation
Fig. 1 is equipment connection schematic diagram of the present invention.
Fig. 2 is electrolyzer of the present invention and balance dashpot structural representation.
Embodiment
Technical scheme of the present invention is further illustrated by embodiment below in conjunction with accompanying drawing,
As shown in Figure 1, this energy-saving and cost-reducing electrolytic manganese production system provided by the invention, mainly comprise electrolyzer 1, equalizing and buffering groove 2, interchanger 4, continuous crystallizing tank 5, water resource heat pump 8,10, baking oven 9, centrifugal filter 13, pressure filter 18,19, change slurry bucket 17, leaching barrel 14, described electrolyzer 1, equalizing and buffering groove 2, negative electrode liquid pump 3, interchanger 4, continuous crystallizing tank 5 are connected to ring successively by pipeline, form loop line; Described electrolyzer 1 and balance dashpot 2 with change starch bucket 16, mortar pump 17, pressure filter 18, rich manganese negative electrode liquid pool 21 be connected to ring successively by pipeline, formation loop line; Described electrolyzer 1, anode liquid pool 22, anode pump 23, heating coil 11, leaching barrel 14, mortar pump 15, pressure filter 19, qualified liquid pool 20 are connected to ring successively by pipeline, form loop line; Described continuous crystallizing tank 5, centrifugal filter 13, pump 24 are connected to ring successively by pipeline, form loop line; Described water pot 6, water pump 7, interchanger 4, water resource heat pump 8,10 are connected to ring successively by pipeline, form loop line, described water resource heat pump has water source (hot blast) heat pump 8 and water source (hot water) heat pump 10, be parallel to loop line, described water source (hot blast) heat pump 8 is connected with baking oven 9, described water source (hot water) heat pump 10 is connected by pipeline with hot water barrel 12, and described electrolyzer 1 and balance dashpot 2 two groove face keep same level, and overflow port also keeps same level.
As shown in Figure 2, electrolyzer 1 is primarily of cell body 112, positive plate 101, negative plate 102, diaphragm bag 103, division board of the false end 109, anolyte upflow tube 104, catholyte upflow tube 111, adapter 110, 105 compositions, polylith positive plate 101 and polylith negative plate 102 is provided with in described cell body 112, described positive plate 101 cover has diaphragm bag 103, described diaphragm bag 103 end opening is connected with division board of the false end 109, division board of the described false end more than 109 and diaphragm bag 103 take exterior domain as cathode compartment 106, be anolyte compartment 107 in described diaphragm bag 103, described anolyte compartment 107 is communicated with false bottom compartment 108, described false bottom compartment 108 is communicated with anolyte upflow tube 104, described anolyte upflow tube 104 adjustment height, and make anolyte enter adapter 105 from the overflow of cell body top, catholyte upflow tube 111 height adjustable that described cathode compartment 106 top is arranged, catholyte overflow is made to enter adapter 110, and keep catholyte overflow port higher than the overflow port of anolyte.
As Fig. 1, shown in Fig. 2, described equalizing and buffering groove 2 is made up of cell body 205, balance communicating pipe 203, drain pipe 204, upflow tube 201, adapter 202, upflow tube 201 height adjustable that described cell body 205 top is arranged, described upflow tube 201 is connected with adapter 202, described balance communicating pipe 203 is connected with electric tank cathode room 106, and described drain pipe 204 is connected with negative electrode liquid pump 3.
As technological selection scheme, described interchanger 4 adopts plate-type heat exchanger or tubular heat exchanger.
As technological selection scheme, described heating coil 11 can adopt plate-type heat exchanger or tubular heat exchanger.
The principle of work of present system is as follows:
1, the former electrolytic manganese production recycle system is maintained, and transformed, ring is connected to successively by pipeline primarily of electrolyzer 1, anode liquid pool 22, anode pump 23, heating coil 11, leaching barrel 14, mortar pump 15, pressure filter 19, qualified liquid pool 20, the loop line formed is major cycle, is the major way of electrolysis production.
2, catholyte washery slag partial circulating is set up, primarily of electrolyzer 1 and balance dashpot 2 with change starch bucket 16, mortar pump 17, pressure filter 18, rich manganese negative electrode liquid pool 21 be connected to ring successively by pipeline, the loop line formed is catholyte washery slag partial circulating, with the qualifying liquid in catholyte displacement manganese slag, replenish electrolyzer amount of metal, qualifying liquid consumption can be reduced, also can use lower concentration qualifying liquid, as the supplementary mode of electrolysis production.
3, catholyte cooling partial circulating is set up, ring is connected to successively by pipeline primarily of electrolyzer 1, equalizing and buffering groove 2, negative electrode liquid pump 3, interchanger 4, continuous crystallizing tank 5, the loop line formed is catholyte cooling partial circulating, remove original hydrologic cycle cooling system, directly mix cell liquid with the outer cooled catholyte of groove and realize groove temperature control.To be connected successively by pipeline by continuous crystallizing tank 5, centrifugal filter 13, pump 24 simultaneously and to form the device that loop line formed, the groove realizing catholyte cools outward, and the calcium magnesium ammonium salt compound crystal formed in process of cooling is also focused on.
4, set up heat utilization device, form primarily of water pot 6, water pump 7, interchanger 4, water source (hot blast) heat pump 8 and water source (hot water) heat pump 10, water source (hot blast) heat pump 8 is connected with baking oven 9, the heat of catholyte is converted to hot blast and dries for manganese sheet; Water source (hot water) heat pump 10 is connected by pipeline with hot water barrel 12, and the heat of catholyte is become hot water, and improve extraction temperature for heating anolyte, hot water also can be used as bath water.
Lower two tables are technical solution of the present invention and prior art power consumption, material consumption contrast table
Table one, power consumption contrast table (ton product manganese meter) is dried in 10,000 tons of electrolytic manganese production line coolings
As can be seen from Table I, compared to prior art, the present invention often produces one ton of product can economize on electricity 139 degree, and 10,000 tons of production lines can save 1,390,000 degree of electricity every year.
Table two, 10,000 tons of electrolytic manganese production line material consumption contrast tables (ton product manganese meter)
As can be seen from Table II, embodiments of the invention product per ton can save 2 tons of new water yields, and from recovery manganese with reduce circulation fluid cost savings and consume in a large number: product net income per ton 170 yuan, and 10,000 tons of production lines every year can income 1,700,000 yuan, remarkable benefit.
Claims (5)
1. an energy-saving and cost-reducing electrolytic manganese production system, mainly comprise electrolyzer (1), equalizing and buffering groove (2), interchanger (4), continuous crystallizing tank (5), water resource heat pump (8, 10), baking oven (9), centrifugal filter (13), pressure filter (18, 19), change slurry bucket (17), it is characterized in that: described electrolyzer (1), anode liquid pool (22), anode pump (23), heating coil (11), leaching barrel (14), mortar pump (15), pressure filter (19), qualified liquid pool (20) is connected to ring successively by pipeline, forming loop line is electrolysis major cycle, described electrolyzer (1) and balance dashpot (2) with change starch bucket (16), mortar pump (17), pressure filter (18), rich manganese negative electrode liquid pool (21) be connected to ring successively by pipeline, forming loop line is electrolysis auxiliary circulation, for the qualifying liquid of catholyte displacement manganese slag, described electrolyzer (1), equalizing and buffering groove (2), negative electrode liquid pump (3), interchanger (4), continuous crystallizing tank (5) are connected to ring successively by pipeline, form loop line, for catholyte control flume temperature, described continuous crystallizing tank (5), centrifugal filter (13), pump (24) are connected to ring successively by pipeline, and form loop line, for separating of crystallisation by cooling, described water pot (6), water pump (7), interchanger (4), water resource heat pump (8,10) are connected to ring successively by pipeline, form loop line, utilize for thermal power transfer,
Described water resource heat pump has water source (hot blast) heat pump (8) and water source (hot water) heat pump (10), is parallel to loop line;
Described water source (hot blast) heat pump (8) is connected with baking oven (9);
Described water source (hot water) heat pump (10) is connected by pipeline with hot water barrel (12);
Described electrolyzer (1) and balance dashpot (2) two groove face keep same level, and overflow port also keeps same level.
2. energy-saving and cost-reducing electrolytic manganese production system according to claim 1, it is characterized in that, electrolyzer (1) is primarily of cell body (112), positive plate 101), negative plate (102), diaphragm bag (103), false end division board (109), anolyte upflow tube (104), catholyte upflow tube (111), adapter (110, 105) form, polylith positive plate (101) and negative plate (102) is provided with in described cell body (112), described positive plate (101) cover has diaphragm bag (103), described diaphragm bag (103) end opening is connected with false end division board (109), more than described false end division board (109) and diaphragm bag (103) take exterior domain as cathode compartment (106), be anolyte compartment (107) in described diaphragm bag (103), described anolyte compartment (107) is communicated with false bottom compartment (108), described false bottom compartment (108) is communicated with anolyte upflow tube (104), described anolyte upflow tube (104) adjustment height, and make anolyte enter adapter (105) from the overflow of cell body top, catholyte upflow tube (111) height adjustable that described cathode compartment (106) top is arranged, catholyte overflow is made to enter adapter (110), and keep catholyte overflow port higher than the overflow port of anolyte.
3. energy-saving and cost-reducing electrolytic manganese production system according to claim 1, it is characterized in that, described equalizing and buffering groove (2) is made up of cell body (205), balance communicating pipe (203), drain pipe (204), upflow tube (201), adapter (202), upflow tube (201) height adjustable that described cell body (205) top is arranged, described upflow tube (201) is connected with adapter (202), described balance communicating pipe (203) is connected with electric tank cathode room (106), and described drain pipe (204) is connected with negative electrode liquid pump (3).
4. energy-saving and cost-reducing electrolytic manganese production system according to claim 1, is characterized in that, described interchanger (4) adopts plate-type heat exchanger or tubular heat exchanger.
5. energy-saving and cost-reducing electrolytic manganese production system according to claim 1, is characterized in that, described heating coil (11) can adopt plate-type heat exchanger or tubular heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510741339.1A CN105154918B (en) | 2015-11-04 | 2015-11-04 | A kind of energy-saving electrolytic manganese production system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510741339.1A CN105154918B (en) | 2015-11-04 | 2015-11-04 | A kind of energy-saving electrolytic manganese production system |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN105154918A true CN105154918A (en) | 2015-12-16 |
| CN105154918B CN105154918B (en) | 2017-10-24 |
Family
ID=54795953
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510741339.1A Active CN105154918B (en) | 2015-11-04 | 2015-11-04 | A kind of energy-saving electrolytic manganese production system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN105154918B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105671597A (en) * | 2016-02-04 | 2016-06-15 | 周勇 | Turbulent electrolytic cell and turbulent electrolytic production system consisting of turbulent electrolytic cell |
| CN105696026A (en) * | 2016-04-28 | 2016-06-22 | 中国科学院上海高等研究院 | Zinc powder electrolysis device and method |
| CN113957489A (en) * | 2021-12-01 | 2022-01-21 | 贵州省新材料研究开发基地 | Method and device for stabilizing working condition of electrolytic manganese electrolytic cell |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2446313A (en) * | 1945-08-18 | 1948-08-03 | Vedensky Dmitri | Process for production of electrolytic manganese |
| US3563868A (en) * | 1968-02-15 | 1971-02-16 | Canadian Patents Dev | Process for extracting and recovering manganese from ores |
| CN1377994A (en) * | 2001-03-29 | 2002-11-06 | 中南大学 | Method for cooling manganese electrolyzing cathode liquid outside tank and recovering magnesium |
| CN101608322A (en) * | 2009-07-13 | 2009-12-23 | 林建平 | A kind of manganese electrolytic cell equipment |
| CN201678739U (en) * | 2010-05-07 | 2010-12-22 | 周治平 | Manganese circulating electrolyzer |
| CN103118990A (en) * | 2010-09-30 | 2013-05-22 | 大金工业株式会社 | Electrolysis device and heat-pump-type water heater provided with same |
| CN205152356U (en) * | 2015-11-04 | 2016-04-13 | 王兆兵 | Energy saving and consumption reduction's electrolytic manganese production system |
-
2015
- 2015-11-04 CN CN201510741339.1A patent/CN105154918B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2446313A (en) * | 1945-08-18 | 1948-08-03 | Vedensky Dmitri | Process for production of electrolytic manganese |
| US3563868A (en) * | 1968-02-15 | 1971-02-16 | Canadian Patents Dev | Process for extracting and recovering manganese from ores |
| CN1377994A (en) * | 2001-03-29 | 2002-11-06 | 中南大学 | Method for cooling manganese electrolyzing cathode liquid outside tank and recovering magnesium |
| CN101608322A (en) * | 2009-07-13 | 2009-12-23 | 林建平 | A kind of manganese electrolytic cell equipment |
| CN201678739U (en) * | 2010-05-07 | 2010-12-22 | 周治平 | Manganese circulating electrolyzer |
| CN103118990A (en) * | 2010-09-30 | 2013-05-22 | 大金工业株式会社 | Electrolysis device and heat-pump-type water heater provided with same |
| CN205152356U (en) * | 2015-11-04 | 2016-04-13 | 王兆兵 | Energy saving and consumption reduction's electrolytic manganese production system |
Non-Patent Citations (1)
| Title |
|---|
| 曾昭盛: ""金属锰电解能耗分析及节能措施"", 《冶金能源》 * |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105671597A (en) * | 2016-02-04 | 2016-06-15 | 周勇 | Turbulent electrolytic cell and turbulent electrolytic production system consisting of turbulent electrolytic cell |
| CN105671597B (en) * | 2016-02-04 | 2018-06-22 | 周勇 | A kind of turbulent flow electrolytic cell, the turbulent flow electrolysis production system being made of turbulent flow electrolytic cell |
| CN105696026A (en) * | 2016-04-28 | 2016-06-22 | 中国科学院上海高等研究院 | Zinc powder electrolysis device and method |
| CN105696026B (en) * | 2016-04-28 | 2017-11-21 | 中国科学院上海高等研究院 | A kind of zinc powder electrolysis device and electrolytic method |
| CN113957489A (en) * | 2021-12-01 | 2022-01-21 | 贵州省新材料研究开发基地 | Method and device for stabilizing working condition of electrolytic manganese electrolytic cell |
| CN113957489B (en) * | 2021-12-01 | 2023-10-13 | 贵州省新材料研究开发基地 | Method and device for stabilizing working condition of electrolytic manganese cell |
Also Published As
| Publication number | Publication date |
|---|---|
| CN105154918B (en) | 2017-10-24 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109650415B (en) | Method for extracting lithium carbonate from scrapped lithium iron phosphate battery positive electrode powder | |
| CN105347364A (en) | Method for closed-loop recycling of lithium precipitation mother liquor in lithium carbonate production | |
| CN103911651A (en) | Process for recovering aluminum ions and sulfuric acid from aluminum alloy anodic oxidation tank | |
| CN109650413B (en) | Method and system for enriching lithium from sodium aluminate solution in alumina plant | |
| CN103397348B (en) | A kind of method utilizing the cyclone electrolytic cell process anode sludge | |
| CN105154918A (en) | Electrolytic manganese production system capable of saving energy and reducing consumption | |
| CN106367790B (en) | Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition and cooling and energy conserving system | |
| CN104495925B (en) | The preparation method of sodium metavanadate | |
| CN108359813B (en) | A kind of energy-saving and environment-friendly salt lake bittern proposes lithium technique | |
| CN204873906U (en) | Anti - technology evaporation crystallization device that circulates | |
| US20160221833A1 (en) | Method and System for Preparing High Purity Lithium Carbonate | |
| CN205152356U (en) | Energy saving and consumption reduction's electrolytic manganese production system | |
| CN105177622B (en) | A kind of energy-saving electrolytic manganese production new technique | |
| CN218665442U (en) | Device for extracting high-purity lithium chloride and sodium chloride from lithium-rich salt lake | |
| CN104018185A (en) | Compound technology for removing As, Sb, Bi by utilizing copper electrolyte | |
| CN107416880A (en) | Utilize the method for lepidolite waste residue one-step method continuous production caesium, rubidium salt | |
| CN103710732A (en) | Waste copper sulfate electrolyte purification system and method | |
| CN206986289U (en) | A kind of copper sulfate bath liquid circulating device | |
| CN106757258B (en) | Oxidation trough aluminium ion and retrieval of sulfuric acid and oxidation solution inhibition energy saver and technique | |
| CN110422827A (en) | A kind of the Waste Sulfuric Acid recycling device and technique of dry chlorine gas | |
| CN101445255B (en) | Technology with sea water as raw material for producing fresh water and sodium chloride | |
| CN210595271U (en) | Waste sulfuric acid recycling device for drying chlorine | |
| CN107858731B (en) | A kind of oxidized aluminum alloy liquid recycling and cooling equipment crystallization removing system and technique | |
| CN108130577B (en) | A kind of oxidized aluminum alloy liquid recycling configuration system compatible with slot is coloured and technique | |
| CN106185991B (en) | The apparatus and method of high purity potassium chloride are extracted from bittern using solar thermal energy |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| CB03 | Change of inventor or designer information | ||
| CB03 | Change of inventor or designer information |
Inventor after: Long Haitao Inventor after: Zheng Anjun Inventor after: Wang Zhenhua Inventor before: Wang Zhaobing Inventor before: Yao Fayan |
|
| TA01 | Transfer of patent application right | ||
| TA01 | Transfer of patent application right |
Effective date of registration: 20170816 Address after: 225300, 2 standard factory buildings, No. 818 Longfeng Road, new energy industrial park, Jiangsu, Taizhou Applicant after: Jiangsu Haitao Amperex Technology Limited Address before: 416400, No. 51 police village, Huayuan Town, Huayuan County, Xiangxi Tujia and Miao Autonomous Prefecture, Hunan Province Applicant before: Wang Zhaobing |
|
| GR01 | Patent grant | ||
| GR01 | Patent grant |