CN201038237Y - Selective volatilization recovery system for waste zinc-manganese battery - Google Patents
Selective volatilization recovery system for waste zinc-manganese battery Download PDFInfo
- Publication number
- CN201038237Y CN201038237Y CNU2007201193149U CN200720119314U CN201038237Y CN 201038237 Y CN201038237 Y CN 201038237Y CN U2007201193149 U CNU2007201193149 U CN U2007201193149U CN 200720119314 U CN200720119314 U CN 200720119314U CN 201038237 Y CN201038237 Y CN 201038237Y
- Authority
- CN
- China
- Prior art keywords
- zinc
- battery
- gas
- roasting furnace
- temperature
- 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 - Lifetime
Links
Images
Classifications
-
- 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
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W30/00—Technologies for solid waste management
- Y02W30/50—Reuse, recycling or recovery technologies
- Y02W30/84—Recycling of batteries or fuel cells
Landscapes
- Manufacture And Refinement Of Metals (AREA)
- Primary Cells (AREA)
Abstract
The utility model relates to a selective volatilization recovery system of waste zinc-manganese batteries, which comprises a classification conveying device, a liquid filter, a battery shell breaking machine, a rinsing bath, a selective volatilization roasting furnace, a condensation recoverer, an acid dissolution tank and a heating concentrator which are arranged in sequence; the battery shell breaking machine axially breaks the shells of the waste batteries; energizing and rinsing in a rinsing bath; the roasting furnace is subjected to segmented temperature rise and fractionation to obtain flue gas with different temperature sections; condensing by a condensation recoverer to respectively obtain ammonium chloride particles and zinc/zinc oxide powder; carrying out acid dissolution and alkali precipitation in an acid dissolution tank; filtering and purifying by a liquid filter; and heating and concentrating the purified acid-soluble tank solution by a heating concentrator to obtain purified manganese sulfate particles. The utility model discloses recovery system can retrieve comprehensively to the bulk content in the zinc-manganese cell, and the result purity that the recovery obtained is higher, and recovery operation and relevant equipment are simpler moreover, do not produce secondary pollution basically.
Description
Technical Field
The utility model relates to an environmental protection and resource recovery equipment, more specifically say, the utility model relates to a recovery plant system of abandonment chemical power supply.
Background
Modern society is stepping into the electronic era, and the more and more the varieties of electromechanical products and electronic equipment in modern society are, and the quantity is more and more huge, and among these products/equipment, the chemical power supply-battery that conveniently carries and the removal is used obtains wide application. Among them, the conventional batteries used in common appliances and vehicles mainly include primary batteries represented by zinc-manganese batteries. The zinc-manganese battery comprises a coating surface material and an electrochemically active content, wherein the coating surface material comprises: iron casing, sealing material asphalt, plastic, paper and other materials; the contents of electrochemical activity comprise positive active materials, negative active materials and electrolyte, wherein the positive active materials mainly comprise manganese dioxide, and the rest materials comprise carbon rods, acetylene black, graphite and the like; the negative electrode active material is mainly zinc, and the balance is a small amount of mercury, cadmium and lead which are added for reducing the corrosion speed of the zinc electrode; the electrolyte is ammonium chloride and zinc chloride for neutral zinc-manganese batteries, and potassium hydroxide for alkaline zinc-manganese batteries.
Dozens of thousands of tons of waste zinc-manganese batteries are discarded every year in China, most of substances such as heavy metals containing zinc, mercury, cadmium, copper, manganese and the like and organic matters, inorganic matters and the like of ammonium salts contained in the waste zinc-manganese batteries are difficult to degrade in the natural environment, and if the heavy metals are discarded at will, the environment is easily seriously damaged, for example, the residual heavy metals such as mercury and the like can be gradually enriched in natural water and a biological chain to pollute the environment. On the contrary, if the substances can be completely recycled, tens of thousands of tons to tens of thousands of tons of unequal manganese, zinc, copper and the like can be regenerated, and the method is a considerable resource. However, the recycling technology is a key problem, and if the recycling technology is not feasible, the pollution cannot be avoided or the recycling technology cannot be economically operated, and if the recycling technology is not feasible, secondary environmental pollution and resource waste can be caused.
Chinese patent application No. 200410026573.8 discloses a method for extracting zinc and manganese dioxide from waste dry batteries, which sequentially comprises: (A) The pretreatment of the waste dry batteries sequentially comprises the following steps: (A1) Waste dry battery in heatCarrying out anaerobic pyrolysis in the dissolving furnace to decompose organic matters and reduce manganese dioxide in the battery into low-valent oxide which is easy to dissolve and extract, wherein the pyrolysis temperature is 450-550 ℃, and the pyrolysis time is 1.5-3.5 hours; (A2) crushing and magnetic separation of waste dry batteries to pick out iron; (B) Carrying out acid dissolution and purification on the waste dry batteries after the pretreatment; (C) Electrolyzing the purified acid solution by zinc-manganese one-bath electrolysis with cathode current density of 250-1200A/m 2 The current density of the anode is 30-100A/m 2 . The method and the equipment system thereof have the following defects: the method adopts the strong acid electrolyte, the preparation process is more complex, the labor condition is worse, and the acid mist secondary pollution can be caused.
Disclosure of Invention
To the above disadvantage of the prior art, the utility model aims to provide a selective volatilization recovery system of abandonment zinc-manganese dioxide battery, it has following advantage: can comprehensively recycle a large amount of contents in the zinc-manganese battery, the purity of the recycled product is high, the recycling operation and related equipment are simple, and secondary pollution is basically not generated.
Therefore, the technical scheme of the utility model is that the selective volatilization recovery system of the waste zinc-manganese battery comprises a classification conveying device and a liquid filter, and the recovery system comprises a battery shell breaking machine, a rinsing bath, a selective volatilization roasting furnace, a condensation recoverer, an acid dissolving bath and a heating concentrator which are arranged according to the following procedures; the battery shell breaking machine comprises a battery through hole with a wall surface blade and a battery propeller, and is used for axially breaking the shells of the waste batteries; the washing tank is provided with a water energizer which energizes and rinses surface materials and contents after the battery is broken; the roasting furnace carries out sectional heating fractionation on the washed battery surface layer objects and the washed battery contents to obtain flue gas with different temperature sections; the condensation recoverer condenses the flue gas of each temperature section to respectively obtain ammonium chloride particles and zinc/zinc oxide powder; the acid dissolving tank is used for carrying out acid dissolving and alkali precipitation on solid residues which are subjected to high-temperature fractionation and left in the roasting furnace; the liquid filter is used for filtering and purifying the bath solution of the rinsing bath and the alkali precipitation solution in the acid dissolving bath; and heating and concentrating the purified acid-soluble tank solution by the heating concentrator to obtain purified manganese sulfate particles.
The selective volatilization recovery system of the utility model firstly uses the battery shell breaking machine with the wall surface cutting edge to axially break the shells of the waste batteries; and then thoroughly cleaning electrochemically active contents in the battery by using a rinsing bath, so that alkaline electrolyte with complex components is basically left in cleaning liquid, and the components of the solid electrochemically active contents are greatly simplified into three main components: inorganic carbon and carbon-containing organic matter, zinc and zinc compounds, manganese oxides; then the solid electrochemical active content with simplified components is placed in a selective volatilization roasting furnace for stage heating recovery/extraction, in a properly closed furnace with a high temperature range of 1000 ℃, inorganic carbon and carbon-containing organic matters can be combusted to release chemical energy and can generate carbon-containing reducing furnace atmosphere, and the reducibility of the carbon-containing furnace gas can be different along with the difference of temperature and air quantity, so that the reducibility strength of the furnace atmosphere is correspondingly changed, and the adjustable reducing atmosphere has positive effect on the extraction of zinc and manganese compounds in the furnace; the evaporation temperature of the elemental zinc is 419 ℃, and the boiling temperature of the elemental zinc is not very high and is 910 ℃; the original zinc compound ZnCl2 is hydrolyzed into attached solid Zn (OH) after the water washing step 2 Zn (OH) 2 can be converted into ZnO at a lower temperature (100-200 ℃) in the furnace, znO can be converted into metal zinc in a reducing atmosphere, znO or Zn can be volatilized into gas at a high temperature, and high-purity ZnO or Zn powder products can be obtained by condensation at a lower temperature of 100-300 ℃; under the reducing atmosphere in the selective volatile roaster, the oxides in the valence states of 2 and 4 of manganese (III) will be converted into oxides in the valence states of 2 of manganese completely or mostlyThe oxide in a state is beneficial to the subsequent acid dissolution recovery, the 2-valent manganese oxide powder is subjected to acid dissolution and alkali precipitation in an acid dissolution tank, a purified manganese sulfate solution is obtained by filtering, clarifying and purifying by a liquid filter, and then a purified manganese sulfate particle product is obtained by drying, and(IV) NH for the main species remaining in the cleaning liquid 4 Cl, the utility model discloses a technological method also borrows the middle temperature heat source that easily obtains in same roaster, and the sublimation obtains pure ammonium chloride gas at 340-390 ℃ within range, cools down the ammonium chloride gas and collects or liquid absorption, obtains the ammonium chloride solution of high-purity and reaches the crystallization.
In addition, although the control is increasingly strict due to the addition of mercury harmful substances to the battery in China, considering that some small-sized battery factories can still produce mercury-containing zinc-manganese batteries or can not completely cancel the application of mercury, for the sake of strict environmental protection and making the harm as good as possible, the system of the utility model can also use a selective volatilization roasting furnace, a condensation recoverer and the like to perform the following operations: firstly, controlling the temperature in the roasting furnace within the range of 50-600 ℃, carrying out medium-temperature dry distillation on the obtained surface layer substances and the obtained contents, sequentially passing the distilled medium-temperature gas through a condensation recoverer, a cyclone separator and a bag filter for gravity separation and filtration, and collecting the obtained mercury liquid so as to prevent mercury pollution.
It can be seen from the above analysis that the utility model discloses a process adopts five kinds of main equipment such as modified battery rejuvenator, the wash bowl, the selective volatilization roaster furnace, the condensation recoverer, sour dissolving tank, liquid filter can just can be extracted the bulk waste material in the zinc-manganese cell completely and retrieve the reuse, wherein the roaster furnace is main power consumption equipment, except being favorable to comprehensively, the bulk waste material is retrieved to high purity, improve follow-up solution separation's efficiency, compare the electrolysis trough, the roaster furnace can adopt electric auxiliary heating and coal coke or oil gas heating multiple mode to bake, the energy is replaced in a flexible way, can well adapt to domestic energy industry policy, each unit operation of overall process carries out or obtains alkaline product fast under alkaline environment, and suitable confined roaster furnace all has more advantages to energy-conservation, avoid secondary pollution, can greatly improve the separation effect, can also reduce energy consumption and secondary pollution.
The utility model discloses concrete institutional advancement still includes: .
In order to improve the washing efficiency of the rinsing bath and promote the optimization of subsequent treatment, the rinsing bath comprises one or more than one of a heat exchanger coil, an ultrasonic vibrator and a mechanical stirrer for applying heat energy.
In order to improve the energy efficiency, operational flexibility, automation degree and environmental protection level of main energy consumption and volatile gas equipment in the system, the roasting furnace comprises a combustion chamber for generating high-temperature flue gas or is additionally provided with an electric heater, a horizontally arranged middle-temperature chamber, a high-temperature chamber, a cooling chamber and a tubular material channel communicated with the chambers in sequence, a separating device is arranged among the chambers and is properly sealed and not communicated with the outside of the furnace body, a series of material pushing boats and a vibration type propelling device thereof are accommodated in the material channel, a high-temperature flue gas inlet, an air outlet, a temperature detection device and an air pipe system are arranged in each chamber, the air pipe system comprises a fan and a control valve, a cooling heat exchanger is arranged in the cooling chamber and comprises an air pipe heat exchanger for preheating the inlet air and a liquid medium heat exchanger for heating the liquid medium, gas sensors for detecting gas components are respectively arranged at the air inlet and the air outlet of each chamber, and an output line of each gas sensor is connected with a secondary instrument and a control circuit.
As important equipment of the system for recovering products with higher purity and preventing secondary pollution, the condensation recoverer comprises an air inlet and an air outlet of flue gas, and a cooler coil pipe distributed along the wall surface of a folded plate type settling chamber, wherein the settling chamber comprises a plurality of upper folded plates and lower folded plates which are alternately distributed, the folded plates are of hollow structures, the cooler coil pipe is closely distributed on the inner wall surface of the folded plate, a collecting port of the settling chamber is arranged below the upper folded plate, and the air outlet of the condensation recoverer is communicated with a bag type and/or electrostatic and/or cyclone dust remover.
In order to improve the recovery efficiency of the system, the purity of the recovered product and prevent secondary pollution, the condensation recoverer comprises an ammonium chloride condensation recoverer, a mercury liquid condensation recoverer and a zinc-powder-containing condensation recoverer which respectively condense and separate ammonium chloride particles, residual mercury liquid and zinc/zinc oxide powder, wherein the air inlets of the ammonium chloride condensation recoverer and the mercury liquid condensation recoverer are connected with the air outlet of the medium-temperature cavity of the roasting furnace, and the air inlet of the zinc-powder-containing condensation recoverer is connected with the air outlet of the high-temperature cavity of the roasting furnace.
In order to save energy, reduce pollution and increase recovery varieties, the inlet and the outlet of a heat exchanger coil in the rinsing bath are connected with a liquid medium heat exchanger arranged in a cooling chamber of the roasting furnace.
In order to save energy, reduce pollution and increase the operation elasticity of the roasting furnace, the air outlet of the condensation recoverer is communicated with the air inlet of an air pipe heat exchanger arranged in a cooling chamber of the roasting furnace, and the air outlet of the air pipe heat exchanger is communicated with the air inlet of each chamber of the roasting furnace through an air pipe system. The air pipe system comprises a circulating input pipeline communicated with the air outlet of the condensation recoverer and a circulating output pipeline communicated with the exhaust port of the roasting furnace, and the circulating control device comprises a gas sensor, a secondary instrument, a control circuit and a control valve.
In order to save energy and reduce pollution of the system, the heating concentrator comprises a heat exchanger coil for applying heat energy, and an inlet and an outlet of the heat exchanger coil are connected with a liquid medium heat exchanger arranged in a cooling chamber of the roasting furnace.
In order to improve the system efficiency, the liquid filter comprises an alkali liquid filter for separating and filtering the bath solution in the washing tank and the alkali precipitation solution, and an acid liquid filter for filtering the acid solution; the classification conveying equipment is arranged among the main equipment.
The invention is further described with reference to the following drawings and specific embodiments.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the recycling system of the present invention.
Detailed Description
Fig. 1 shows a schematic structural diagram of an embodiment of the system for selectively volatilizing and recycling waste zn-mn batteries according to the present invention. The recovery system comprises classified conveying equipment (not shown in detail) arranged among main equipment, an alkali liquor filter for filtering alkali precipitation solution, an acid liquor filter for filtering acid solution (not shown in detail), and the recovery system further comprises a battery shell breaking machine 100, a water washing tank 110, a selective volatilization roasting furnace 120, a condensation recoverer 150, an acid dissolving tank 180 and a heating concentrator 190 which are arranged according to the following procedures; the battery shell breaking machine 100 comprises a battery through hole 102 with a wall surface blade 101 and a battery pusher (not shown in detail), and the battery through hole and the battery pusher axially break the shells of the waste batteries Bt; the rinsing bath 110 is provided with a water body energizer such as a heat exchanger coil 113, an ultrasonic vibrator 112, a mechanical stirrer 111 and the like, and is used for energizing and rinsing surface layer substances and contents after the shells of the batteries Bt are broken; the roasting furnace 120 is used for raising the washed surface materials and the washed contents of the battery in stages by Wen Fenliu to obtain flue gas with different temperature sections; one or more condensing recoverers 150 condense the flue gas in each temperature section to respectively obtain ammonium chloride particles and zinc/zinc oxide powder; the acid-dissolving tank 180 is used for carrying out acid dissolution and alkali precipitation on solid residues which are subjected to high-temperature fractionation and are left in the roasting furnace; the liquid filter is used for filtering and purifying the tank liquor of the rinsing tank and the alkali precipitation solution in the acid dissolving tank; the heating concentrator 190 heats and concentrates the purified solution in the acid-soluble tank 180 by using the waste heat from the volatilization roasting furnace 120 to obtain purified manganese sulfate particles.
And heating and concentrating the purified acid solution in the acid dissolving tank by the heating concentrator 190 to obtain purified manganese sulfate particles. Heating concentrator 190 includes jacketed heat exchanger coil 191 for applying heat energy, and inlet and outlet of heat exchanger coil 191 are connected to liquid medium heat exchanger 136 disposed in cooling chamber 124 of roaster 120.
The air pipe system comprises a circulating input pipeline 141 communicated with the air outlet of the condensation recoverer 150 and a circulating output pipeline 142 communicated with the air outlet 131 of the roasting furnace, and the circulating control device comprises a gas sensor 137, a secondary instrument 138, a control circuit and a control valve 134.
The calcinator 120 is used for placing the washed battery surface layer objects and the washed battery contents into the material pushing boat 127 for segmented heating and fractionation to obtain flue gas with different temperature segments; the roasting furnace 120 comprises a combustion chamber 121A for generating high-temperature flue gas, an attached electric heater 121B, a middle-temperature chamber 122, a high-temperature chamber 123, a cooling chamber 124 and a tubular material channel 125 which penetrates through the chambers, wherein the middle-temperature chamber 122, the high-temperature chamber 123, the cooling chamber 124 and the tubular material channel 125 are horizontally arranged and are sequentially communicated, a separating device 126 is arranged among the chambers, the chambers are properly sealed and are not directly communicated with the outside of the furnace body, a series of material pushing boats 127 and a vibration type propelling device 128 thereof are accommodated in the material channel 125, a high-temperature flue gas inlet 129, a high-temperature gas inlet 130, a high-temperature outlet 131, a temperature detecting device 132 and an air duct system are arranged in each chamber, the air duct system comprises a fan 133 and a control valve 134, a cooling heat exchanger is arranged in the cooling chamber 124, the cooling heat exchanger comprises an air duct heat exchanger 135 for preheating inlet air and a liquid medium heat exchanger 136 for heating liquid medium, gas sensors 137 for detecting gas components are respectively arranged at the air inlet and the air outlet of each chamber, and output lines (indicated by dotted lines and indicated by control lines) of the gas sensors 137 are connected with a secondary instrument and a control circuit 138.
The condensation recoverer 150 includes an ammonium chloride condensation recoverer for respectively condensing and separating ammonium chloride particles, a mercury liquid condensation recoverer for condensing and separating residual mercury liquid, and a zinc powder-containing condensation recoverer for condensing and separating zinc/zinc oxide powder (only one of which is shown in the figure), wherein air inlets of the ammonium chloride condensation recoverer and the mercury liquid condensation recoverer are connected to an exhaust port of the medium-temperature chamber 122 of the roasting furnace 120 through a pipeline controlled by an electric valve, an air inlet of the zinc powder-containing condensation recoverer is connected to an exhaust port of the high-temperature chamber 123 of the roasting furnace 120, and flue gas at each temperature section is condensed to respectively obtain ammonium chloride particles and zinc/zinc oxide powder; the air outlets of the condensation recoverers 150 are all communicated to the air inlets of the air pipe heat exchangers 135 arranged in the cooling chamber 124 of the roasting furnace 120 through air/solid or air/liquid separation, and the air outlets of the air pipe heat exchangers 135 are communicated to the air inlets of the chambers of the roasting furnace 120 through air pipe systems. Each condensation recoverer 150 comprises a vertical folding plate type settling chamber 151, the settling chamber 151 comprises a plurality of upper folding plates 153 and lower folding plates 154 which are arranged alternately, the folding plates 153 and 154 are of hollow structures, cooler coils 152 are distributed on the inner wall surfaces of the folding plates 153 and 154 in a close fit manner, a collection port 155 of the settling chamber is arranged below the upper folding plate 153, and an air outlet of the condensation recoverer 150 is communicated with a cyclone dust collector 171 and an electrostatic dust collector 172.
Claims (10)
1. The utility model provides a selective volatilization recovery system of abandonment zinc-manganese dioxide battery, its characterized in that including categorised conveying equipment, liquid filter: the recovery system comprises a battery shell breaking machine, a washing tank, a selective volatilization roasting furnace, a condensation recoverer, an acid dissolving tank and a heating concentrator which are arranged according to the following procedures; the battery shell breaking machine comprises a battery through hole with a wall surface blade and a battery propeller, and is used for axially breaking the shells of the waste batteries; the washing tank is provided with a water energizer which is used for energizing and rinsing surface materials and contents after the battery is broken; the roasting furnace carries out sectional heating and fractionation on the washed battery surface layer objects and the washed battery contents to obtain flue gas with different temperature sections; the condensation recoverer condenses the flue gas of each temperature section to respectively obtain ammonium chloride particles and zinc/zinc oxide powder; the acid dissolving tank is used for carrying out acid dissolving and alkali precipitation on solid residues which are subjected to high-temperature fractionation and left in the roasting furnace; the liquid filter is used for filtering and purifying the bath solution of the rinsing bath and the alkali precipitation solution in the acid dissolving bath; and the heating concentrator heats and concentrates the purified acid solution in the dissolution tank to obtain purified manganese sulfate particles.
2. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 1, wherein: the rinsing bath comprises one or more than one of a heat exchanger coil pipe applying heat energy, an ultrasonic vibrator and a mechanical stirrer.
3. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 1, wherein: the roasting furnace comprises a combustion chamber for generating high-temperature flue gas or is additionally provided with an electric heater, a middle-temperature chamber, a high-temperature chamber, a cooling chamber and a tubular material channel communicated with the chambers in sequence, wherein the chambers are horizontally arranged, the middle-temperature chamber, the high-temperature chamber, the cooling chamber and the tubular material channel are properly sealed and not communicated with the outside of the furnace body, a series of material pushing boats and vibrating propelling devices thereof are accommodated in the material channel, a high-temperature flue gas inlet, a high-temperature flue gas outlet, a temperature detection device and an air pipe system are arranged in each chamber, the air pipe system comprises a fan and a control valve, a cooling heat exchanger is arranged in the cooling chamber, the cooling heat exchanger comprises an air pipe heat exchanger for preheating inlet air and a liquid medium heat exchanger for heating liquid medium, gas sensors for detecting gas components are respectively arranged at the air inlet and the air outlet of each chamber, and the output circuit of the gas sensors is connected with a secondary instrument and a control circuit.
4. The system for selective recovery of spent zinc manganese dioxide batteries of claim 1, further comprising: the condensation recoverer comprises a gas inlet, a gas outlet and cooler coils, wherein the cooler coils are distributed along the wall surface of a vertical folded plate type settling chamber, the settling chamber comprises a plurality of upper folded plates and lower folded plates which are arranged alternately, the folded plates are of hollow structures, the cooler coils are distributed on the inner wall surfaces of the folded plates in a clinging mode, a collecting port of the settling chamber is arranged below the upper folded plates, and the gas outlet of the condensation recoverer is communicated with a bag type and/or electrostatic and/or cyclone dust collector.
5. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 2, wherein: and the inlet and the outlet of a heat exchanger coil in the rinsing bath are connected with a liquid medium heat exchanger arranged in a cooling chamber of the roasting furnace.
6. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 3, wherein: the condensation recoverer comprises an ammonium chloride condensation recoverer, a mercury liquid condensation recoverer and a zinc-powder-containing condensation recoverer, wherein the ammonium chloride condensation recoverer and the mercury liquid condensation recoverer are respectively used for condensation separation of ammonium chloride particles, residual mercury liquid and zinc/zinc oxide powder, air inlets of the ammonium chloride condensation recoverer and the mercury liquid condensation recoverer are connected with an air outlet of a medium-temperature cavity of the roasting furnace, and an air inlet of the zinc-powder-containing condensation recoverer is connected with an air outlet of a high-temperature cavity of the roasting furnace.
7. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 3, wherein: the gas outlets of the condensation recoverers are communicated with gas inlets of gas pipe heat exchangers arranged in the cooling chambers of the roasting furnace, and the gas outlets of the gas pipe heat exchangers are communicated with gas inlets of the chambers of the roasting furnace through a gas pipe system.
8. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 3, wherein: the air pipe system comprises a circulating input pipeline communicated with the air outlet of the condensation recoverer and a circulating output pipeline communicated with the air outlet of the roasting furnace, and the circulating control device comprises a gas sensor, a secondary instrument, a control circuit and a control valve.
9. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 3, wherein: the heating concentrator comprises a heat exchanger coil for applying heat energy, and an inlet and an outlet of the heat exchanger coil are connected with a liquid medium heat exchanger arranged in a cooling chamber of the roasting furnace.
10. The system for selectively volatilizing and recovering the discarded zinc-manganese battery as recited in claim 1, wherein: the liquid filter comprises an alkali liquid filter for separating and filtering the bath solution in the rinsing bath, filtering the alkali precipitation solution and an acid liquid filter for filtering the acid dissolution solution; the sorting and conveying equipment is arranged among the main equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201193149U CN201038237Y (en) | 2007-04-03 | 2007-04-03 | Selective volatilization recovery system for waste zinc-manganese battery |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNU2007201193149U CN201038237Y (en) | 2007-04-03 | 2007-04-03 | Selective volatilization recovery system for waste zinc-manganese battery |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN201038237Y true CN201038237Y (en) | 2008-03-19 |
Family
ID=39210757
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNU2007201193149U Expired - Lifetime CN201038237Y (en) | 2007-04-03 | 2007-04-03 | Selective volatilization recovery system for waste zinc-manganese battery |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN201038237Y (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100480184C (en) * | 2007-04-03 | 2009-04-22 | 深圳市格林美高新技术股份有限公司 | Selective volatilization recovery process for waste zinc-manganese battery |
| CN107437626A (en) * | 2017-07-31 | 2017-12-05 | 蒋央芳 | Method for preparing carbon-coated manganese phosphate from waste zinc-manganese battery |
| CN107804876A (en) * | 2017-12-05 | 2018-03-16 | 王龙 | Manganese dioxide and ammonium chloride extraction element in a kind of waste battery |
| CN109326841A (en) * | 2018-09-03 | 2019-02-12 | 丁柳朋 | One kind, which is recycled used batteries, uses vacuum heating apparatus |
| CN109433783A (en) * | 2018-10-16 | 2019-03-08 | 黄勇 | A kind of Waste battery treatment equipment convenient for pumping |
| CN111628234A (en) * | 2020-05-27 | 2020-09-04 | 云南省能源研究院有限公司 | Waste battery recovery system and recovery method thereof |
-
2007
- 2007-04-03 CN CNU2007201193149U patent/CN201038237Y/en not_active Expired - Lifetime
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100480184C (en) * | 2007-04-03 | 2009-04-22 | 深圳市格林美高新技术股份有限公司 | Selective volatilization recovery process for waste zinc-manganese battery |
| CN107437626A (en) * | 2017-07-31 | 2017-12-05 | 蒋央芳 | Method for preparing carbon-coated manganese phosphate from waste zinc-manganese battery |
| CN107437626B (en) * | 2017-07-31 | 2019-08-13 | 蒋央芳 | Method for preparing carbon-coated manganese phosphate from waste zinc-manganese battery |
| CN107804876A (en) * | 2017-12-05 | 2018-03-16 | 王龙 | Manganese dioxide and ammonium chloride extraction element in a kind of waste battery |
| CN109326841A (en) * | 2018-09-03 | 2019-02-12 | 丁柳朋 | One kind, which is recycled used batteries, uses vacuum heating apparatus |
| CN110629026A (en) * | 2018-09-03 | 2019-12-31 | 丁柳朋 | Vacuum heating equipment for waste battery recovery processing |
| CN109433783A (en) * | 2018-10-16 | 2019-03-08 | 黄勇 | A kind of Waste battery treatment equipment convenient for pumping |
| CN111628234A (en) * | 2020-05-27 | 2020-09-04 | 云南省能源研究院有限公司 | Waste battery recovery system and recovery method thereof |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100480184C (en) | Selective volatilization recovery process for waste zinc-manganese battery | |
| CN201038237Y (en) | Selective volatilization recovery system for waste zinc-manganese battery | |
| CN109193064A (en) | A kind of method of waste power lithium battery valuable constituent sorting recycling | |
| CN104282962B (en) | The recovery method of waste and old lithium ionic cell electrolyte | |
| CN110783658A (en) | Ex-service power ternary lithium battery recovery demonstration process method | |
| CN101759158B (en) | Method for regenerating and recovering sulfuric acid from waste acid | |
| JPS63197592A (en) | Method of reutilizing battery, integrated circuit substrate and electronic part | |
| CN107282598A (en) | A kind of aluminium cell discards the recoverying and utilizing method of cathode carbon pieces | |
| CN201028540Y (en) | Selective volatilization roasting furnace for waste zinc-manganese battery | |
| CN112768796B (en) | Method for treating waste lithium battery | |
| CN112958588B (en) | Waste battery safety recycling and disassembling system and disassembling method thereof | |
| CN108134150A (en) | The method of valuable element in hydro-thermal synthetical recovery waste lithium iron phosphate positive electrode | |
| CN107196005A (en) | Method for recovering waste lead storage battery | |
| CN104009269B (en) | The recovery and treatment method of waste and old lithium ion battery | |
| CN105969992A (en) | Method for recycling fine tin from waste circuit board | |
| CN107706476A (en) | A kind of solvent sorting preprocess method of waste and old lithium ion battery | |
| CN107604383A (en) | A kind of method of electrolyte in smelting process extraction carbon slag | |
| CN109244582A (en) | A kind of technique of waste lead accumulator harmless treatment and resource utilization | |
| CN210045742U (en) | Resource disposal system for household garbage incineration fly ash | |
| CN202610337U (en) | Resourceful treatment device for metal pickling waste liquor | |
| CN110144462A (en) | A kind of mercury processing electrothermic retorting technique | |
| CN212041471U (en) | Device for recovering diaphragm paper in waste lithium ion battery | |
| CN113458114A (en) | Multistage sorting system and method for waste lithium batteries | |
| CN107293814B (en) | Method for ultrasonically separating electrode current collector and electrode material of lithium ion battery | |
| CN102618722B (en) | Clean recovery production method of copper-containing waste |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20080319 |