CN203820457U - System for recovering sulfur from sulfur-containing leach residue - Google Patents
System for recovering sulfur from sulfur-containing leach residue Download PDFInfo
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- CN203820457U CN203820457U CN201420197997.XU CN201420197997U CN203820457U CN 203820457 U CN203820457 U CN 203820457U CN 201420197997 U CN201420197997 U CN 201420197997U CN 203820457 U CN203820457 U CN 203820457U
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- sulfur
- sulphur
- bearing
- refrigerated separation
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 212
- 239000011593 sulfur Substances 0.000 title claims abstract description 107
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 107
- 239000000203 mixture Substances 0.000 claims abstract description 59
- 238000001816 cooling Methods 0.000 claims abstract description 50
- 238000000926 separation method Methods 0.000 claims abstract description 49
- 238000010438 heat treatment Methods 0.000 claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 26
- 239000007787 solid Substances 0.000 claims abstract description 26
- 239000012299 nitrogen atmosphere Substances 0.000 claims abstract description 9
- 239000007788 liquid Substances 0.000 claims abstract description 8
- 239000005864 Sulphur Substances 0.000 claims description 94
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 48
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 44
- 239000000498 cooling water Substances 0.000 claims description 39
- 238000000034 method Methods 0.000 claims description 29
- 238000007599 discharging Methods 0.000 claims description 23
- 229910052757 nitrogen Inorganic materials 0.000 claims description 22
- 239000000428 dust Substances 0.000 claims description 18
- 238000001914 filtration Methods 0.000 claims description 18
- 239000002893 slag Substances 0.000 claims description 17
- 239000002826 coolant Substances 0.000 claims description 16
- 238000006243 chemical reaction Methods 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 9
- 238000003723 Smelting Methods 0.000 claims description 8
- 238000000605 extraction Methods 0.000 claims description 8
- 229910052751 metal Inorganic materials 0.000 claims description 7
- 239000002184 metal Substances 0.000 claims description 7
- 239000000919 ceramic Substances 0.000 claims description 5
- 238000011084 recovery Methods 0.000 abstract description 17
- 238000003912 environmental pollution Methods 0.000 abstract description 9
- 238000012423 maintenance Methods 0.000 abstract description 6
- 238000005092 sublimation method Methods 0.000 abstract 1
- 238000005265 energy consumption Methods 0.000 description 13
- 238000009833 condensation Methods 0.000 description 10
- 230000005494 condensation Effects 0.000 description 10
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 description 9
- 229910052725 zinc Inorganic materials 0.000 description 9
- 239000011701 zinc Substances 0.000 description 9
- 238000004821 distillation Methods 0.000 description 7
- 238000002386 leaching Methods 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 230000008901 benefit Effects 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 239000012141 concentrate Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000004140 cleaning Methods 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 229910001882 dioxygen Inorganic materials 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000009776 industrial production Methods 0.000 description 3
- 230000003647 oxidation Effects 0.000 description 3
- 238000007254 oxidation reaction Methods 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 241001062472 Stokellia anisodon Species 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000859 sublimation Methods 0.000 description 2
- 230000008022 sublimation Effects 0.000 description 2
- 239000005083 Zinc sulfide Substances 0.000 description 1
- 238000012512 characterization method Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 239000010881 fly ash Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000005065 mining Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 229910052984 zinc sulfide Inorganic materials 0.000 description 1
- DRDVZXDWVBGGMH-UHFFFAOYSA-N zinc;sulfide Chemical compound [S-2].[Zn+2] DRDVZXDWVBGGMH-UHFFFAOYSA-N 0.000 description 1
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The utility model provides a system for recovering sulfur from sulfur-containing leach residue. The system comprises a heating treatment device which is used for heating the sulfur-containing leach residue to 400-500 DEG C under negative pressure conditions in a nitrogen atmosphere so as to obtain a sulfur-containing steam mixture and residual solid residue, and a first cooling and separation device which is used for performing first cooling separation on the sulfur-containing steam mixture so as to obtain liquid sulfur and a residual gas mixture, wherein the first cooling separation device is connected with the heating treatment device. By utilizing the system provided by the utility model, sulfur in the sulfur-containing leach residue can be fast and effectively separated and recovered through a direct sublimation method; furthermore, the recovery rate of sulfur is high, the environmental pollution is small, the operation load is small, the equipment maintenance rate is low, the system has no requirements about the content of elemental sulfur in the leach residue, the range of applications is wide, and the industrialization is easy to realize.
Description
Technical field
The utility model relates to chemical field, particularly, relates to the system that reclaims sulphur from sulfur-bearing leached mud.
Background technology
Oxygen is pressed in Leaching Zinc concentrate technique, and the elemental sulfur in zinc ore concentrate enters in leached mud with solid-state form, and elemental sulfur content can be up to 80% left and right.Elemental sulfur in leached mud is reclaimed, not only can create economic benefit, and can reduce the pollution to environment, realize Sustainable development.Research to leached mud recovery sulphur technique both at home and abroad, experiment are accompanied by zinc sulfide concentrates high pressure extract technology and start together.Bright Cotterell zinc factory of section of Canada is in 1981 the earliest by the industrialization of leached mud recovery sulphur technique, and the method for employing is hot filter method.Hudzon Ba Yi mining and metallurgy zinc factory of company of Canada hot filter method sulfur recovery system was also gone into operation in 1993.
The technical process of hot filter method is as follows: after the leaching pulp dewatering from flotation workshop, deliver to sulfur melting groove steam indirect heating to more than sulphur fusing point, then filter through molten sulfur strainer, after filtering, clean Molten sulphur is produced solid sulfur through granulating system.Domestic employing oxygen presses the example of leaching processing zinc ore concentrate few, and is operation recent years, construction, all adopts hot filter method in the zinc factory of going into operation, building.But the method has following several shortcoming: (1) maintenance of equipment rate is high: due to leached mud impure many (approximately 20%), molten sulfur filter operation load is large, faults frequent; (2) sulfur recovery rate is low: in the outer heat extraction filter residue of molten sulfur strainer, containing the sulphur of 50% left and right, affect the rate of recovery of sulphur, in leached mud, impurity is more, and the rate of recovery of sulphur is lower; (3) operating environment is poor: when molten sulphur process and molten sulfur strainer slag dumping, have a large amount of sulphur steam to overflow, operational condition is severe, and workman's operational load is large, and environmental pollution is also more serious; (4) narrow application range: the method requires in leached mud elemental sulfur content more than 70%, otherwise leached mud cannot form molten state, can not carry out follow-up molten sulfur and filter, narrow application range is higher to smelting technology and operational requirement.
Thereby, still have much room for improvement about the technique that reclaims sulphur from sulfur-bearing leached mud.
Utility model content
The utility model is intended at least solve one of technical problem existing in prior art.For this reason, it is high that an object of the present utility model is to propose a kind of sulfur recovery rate, and environmental pollution is little, and operational load is little, and maintenance rate is low, and to not requirement of elemental sulfur content in leached mud, the applied widely system that reclaims sulphur from sulfur-bearing leached mud.
Aspect one of the present utility model, the utility model provides a kind of system that reclaims sulphur from sulfur-bearing leached mud.According to embodiment of the present utility model, this system comprises: in nitrogen atmosphere, under condition of negative pressure, described sulfur-bearing leached mud is heated to 400-500 degree Celsius, to obtain the heat treatment apparatus of sulfur-bearing vapour mixture and remaining solid slag; And for described sulfur-bearing vapour mixture is carried out to the first refrigerated separation, to obtain the first refrigerated separation device of Molten sulphur and residual gas mixture, described the first refrigerated separation device is connected with described heat treatment apparatus.Utility model people finds, utilize this system of the present utility model, the method that can pass through directly distillation is fast and effectively by the sulphur Separation and Recovery in sulfur-bearing leached mud, and sulfur recovery rate is high, environmental pollution is little, and operational load is little, maintenance of equipment rate is low, and to not requirement of elemental sulfur content in leached mud, applied widely, be easy to realize industrialization.
According to embodiment of the present utility model, further comprise for before carrying out described heat treated, described sulfur-bearing leached mud is carried out to the filtration treatment device of filtration treatment, described filtration treatment device is connected with described heat treatment apparatus.Thus, can effectively reduce the water-content in sulfur-bearing leached mud, and then greatly reduce the energy consumption of heat treatment apparatus.
According to embodiment of the present utility model, described filtration treatment device is vertical filter.Thus, can effectively reduce the water-content in sulfur-bearing leached mud, obtain the lower sulfur-bearing leached mud of water content.
According to embodiment of the present utility model, described heat treatment apparatus is fluidizing furnace, and described fluidizing furnace comprises: body of heater, is limited with reaction compartment in described body of heater; For the opening for feed of described sulfur-bearing leached mud is provided to described body of heater, described opening for feed is arranged at described sidewall of the furnace body below; For to supplying nitrogen in described body of heater to form described nitrogen atmosphere, and discharge the inlet mouth of described remaining solid slag, described inlet mouth is arranged at described bottom of furnace body; For discharging the discharge port of described sulfur-bearing vapour mixture, described discharge port is arranged at described sidewall of the furnace body top.Utility model people finds, utilizes above-mentioned fluidizing furnace by distillation, sulphur simple substance to be separated from sulfur-bearing leached mud fast and effectively.In addition, this fluidizing furnace working pressure is negative pressure, and adopts nitrogen protection, can effectively prevent that sulphur is by airborne dioxygen oxidation.
According to embodiment of the present utility model, described fluidizing furnace further comprises for before carrying out described the first refrigerated separation, described sulfur-bearing vapour mixture is carried out to the dedusting treater of dust removal process, described dedusting treater is connected with described the first refrigerated separation device with described heat treatment apparatus respectively.Thus, can effectively make sulphur distil out from leached mud, ensure that the vapor partial pressure of sulphur is higher simultaneously, can discharge from fluidizing furnace top, enter cleaning apparatus.
According to embodiment of the present utility model, described dedusting treater is selected high temperature resistant dust collector, and according to an embodiment of the present utility model, described dedusting treater is Ceramic dust collector.Thus, dust removing effects is better.
According to embodiment of the present utility model, described the first refrigerated separation device has first end and the second end, the line of described first end and the second end and horizontal plane form angle α, wherein α is greater than 0 ° and be less than 30 °, and described first end is higher than described the second end, and described the first refrigerated separation device comprises: for the inner tube of the water coolant that circulates; Be used for forming the outer tube of cooling space for use in the described sulfur-bearing vapour mixture of circulation between described inner tube; For the cooling water inlet of water coolant is provided to described inner tube, described cooling water inlet is arranged at described outer tube bottom, and contiguous described the second end, is connected with described inner tube; For discharging the cooling water outlet of described water coolant, described cooling water outlet is arranged at described outer tube top, and contiguous described the second end, is connected with described inner tube; For the combi inlet port of described sulfur-bearing vapour mixture is provided to described cooling space, described combi inlet port is arranged at described outer tube top, and contiguous described the second end, is connected with described cooling space; For discharging the Molten sulphur outlet of described Molten sulphur, described Molten sulphur outlet is arranged at described outer tube bottom, and contiguous described the second end, is connected with described cooling space; And for discharging the residual gas mixture outlet of described residual gas mixture, described residual gas mixture outlet is arranged at described first end, be connected with described cooling space, wherein, described cooling water inlet and described Molten sulphur outlet interval arrange, and described cooling water outlet and described combi inlet port interval arrange.Thus, can be effectively Molten sulphur by high temperature sulphur vapor condensation, and due to the first end of the first cooling separator and the line of the second end and horizontal plane formation certain angle, the Molten sulphur of cooling acquisition can be by pipeline self to cooling separator bottom.
According to embodiment of the present utility model, further comprise for described residual gas mixture is carried out to the second refrigerated separation, to remove the second refrigerated separation device of water vapor acquisition nitrogen, described the second refrigerated separation device is connected with described the first refrigerated separation device, and has identical structure with described the first refrigerated separation device.Thus, can effectively remove the water vapour in nitrogen, thereby nitrogen is carried out to recycle, and then effectively reduce energy consumption, minimizing cost, and water of condensation can be by pipeline self to sewage collecting tank.
According to embodiment of the present utility model, further comprise for the feedwater of discharging through described cooling water outlet is returned to boiler, or will being delivered to the water shoot of deoxygenator through the de-mineralized water of described cooling water outlet discharge, described water shoot is connected with described cooling water outlet.Thus, can realize the recycle of feedwater and de-mineralized water, effectively reduce energy consumption, save cost.
According to embodiment of the present utility model, further comprise that to reclaim the Residue extraction pipeline of valuable metal, described Residue extraction pipeline is connected with described heat treatment apparatus for described remaining solid slag being carried out cooling and delivering to smelting shop.Thus, in by valuable metal recovery recycling, can avoid environmental pollution.
According to embodiment of the present utility model, further comprise for described Molten sulphur is delivered to described granulating system, to described Molten sulphur is prepared as to the liquid sulphur conveying pipe road of solid sulfur, described liquid sulphur conveying pipe road is connected and is connected with granulating system with described the first refrigerated separation device respectively.Thus, can effectively will reclaim the sulphur obtaining for industrial production.
Additional aspect of the present utility model and advantage in the following description part provide, and part will become obviously from the following description, or recognize by practice of the present utility model.
Brief description of the drawings
Above-mentioned and/or additional aspect of the present utility model and advantage accompanying drawing below combination is understood becoming the description of embodiment obviously and easily, wherein:
Fig. 1 has shown according to an embodiment of the present utility model, reclaims the structural representation of the system of sulphur from sulfur-bearing leached mud.
Embodiment
Describe embodiment of the present utility model below in detail, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has the element of identical or similar functions from start to finish.Be exemplary below by the embodiment being described with reference to the drawings, only for explaining the utility model, and can not be interpreted as restriction of the present utility model.
Aspect one of the present utility model, the utility model provides a kind of system 1000 that reclaims sulphur from sulfur-bearing leached mud.According to embodiment of the present utility model, with reference to Fig. 1, this system 1000 comprises: in nitrogen atmosphere, under condition of negative pressure, described sulfur-bearing leached mud is heated to 400-500 degree Celsius, after element sulphur distillation, mix and separate with solid slag with nitrogen, to obtain the heat treatment apparatus 100 of sulfur-bearing vapour mixture and remaining solid slag; And for described sulfur-bearing vapour mixture is carried out to the first refrigerated separation, to obtain the first refrigerated separation device 200 of Molten sulphur and residual gas mixture, described the first refrigerated separation device 200 is connected with described heat treatment apparatus 100.Utility model people finds, utilize this system of the present utility model, the method that can pass through directly distillation is fast and effectively by the sulphur Separation and Recovery in sulfur-bearing leached mud, and sulfur recovery rate is high, environmental pollution is little, and operational load is little, maintenance of equipment rate is low, and to not requirement of elemental sulfur content in leached mud, applied widely, be easy to realize industrialization.
According to embodiment of the present utility model, described sulfur-bearing leached mud is that oxygen presses Leaching Zinc to smelt leached mud.Thus, can reclaim elemental sulfur in leached mud, not only can create economic benefit, and can reduce the pollution to environment, realize Sustainable development.
According to embodiment of the present utility model, further comprise for before carrying out described heat treated, described sulfur-bearing leached mud is carried out to the filtration treatment device 300 of filtration treatment, described filtration treatment device 300 is connected with described heat treatment apparatus 100.Thus, can effectively reduce the water-content in sulfur-bearing leached mud, and then greatly reduce the energy consumption of heat treatment apparatus.
According to embodiment of the present utility model, described filtration treatment device 300 is vertical filter.Thus, can effectively reduce the water-content in sulfur-bearing leached mud, obtain the lower sulfur-bearing leached mud of water content.
According to embodiment of the present utility model, in described sulfur-bearing leached mud, solid content is 25%, through moisture lower than 15% in the sulfur-bearing leached mud of filtration treatment.Thus, can greatly reduce the energy consumption of heat treatment apparatus.
According to embodiment of the present utility model, described heat treatment apparatus 100 is fluidizing furnace, and described fluidizing furnace comprises: body of heater 101, is limited with reaction compartment (not shown) in described body of heater 101; For the opening for feed 102 of described sulfur-bearing leached mud is provided to described body of heater 101, described opening for feed 102 is arranged at described body of heater 101 sidewall belows; Be used for to the interior supplying nitrogen of described body of heater 101 to form described nitrogen atmosphere, and discharge the inlet mouth 103 of described remaining solid slag, described inlet mouth 103 is arranged at described body of heater 101 bottoms; For discharging the discharge port 104 of described sulfur-bearing vapour mixture, described discharge port 104 is arranged at described body of heater 101 sidewall tops.Utility model people finds, utilizes above-mentioned fluidizing furnace by distillation, sulphur simple substance to be separated from sulfur-bearing leached mud fast and effectively.In addition, this fluidizing furnace working pressure is negative pressure, and adopts nitrogen protection, can effectively prevent that sulphur is by airborne dioxygen oxidation.
According to embodiment of the present utility model, described fluidizing furnace further comprises that at least one is for making the temperature in described body of heater 101 remain the heating tube (not shown) of 400-500 degree Celsius, and described heating tube is arranged in described body of heater 101.Thus, can effectively make sulphur distil out from leached mud, ensure that the vapor partial pressure of sulphur is higher simultaneously, can discharge from fluidizing furnace top, enter cleaning apparatus.
According to embodiment of the present utility model, further comprise for before carrying out described the first refrigerated separation, described sulfur-bearing vapour mixture is carried out to the dedusting treater 400 of dust removal process, described dedusting treater 400 is connected with described the first refrigerated separation device 200 with described heat treatment apparatus 100 respectively.Thus, can effectively remove the impurity such as dust in sulphur steam, obtain the higher sulfur product of purity.
According to embodiment of the present utility model, described dedusting treater 400 is Ceramic dust collector.Thus, dust removing effects is better.
According to embodiment of the present utility model, the temperature in described Ceramic dust collector is 360-450 degree Celsius.Thus, can avoid sulphur vapor condensation to become Molten sulphur, cause equipment, line clogging.
According to embodiment of the present utility model, described the first refrigerated separation device 200 has first end and the second end, the line of described first end and the second end and horizontal plane form angle α, wherein α is greater than 0 ° and be less than 30 °, and described first end is higher than described the second end, and described the first refrigerated separation device 200 comprises: for the inner tube (not shown) of the water coolant that circulates; Outer tube 206, the cooling space (not shown) of the described sulfur-bearing vapour mixture that is formed between described outer tube 206 and described inner tube circulating; For the cooling water inlet 201 of described water coolant is provided to described inner tube, described cooling water inlet 201 is arranged at described outer tube 206 bottoms, and contiguous described the second end, is connected with described inner tube; For discharging the cooling water outlet 202 of described water coolant, described cooling water outlet 202 is arranged at described outer tube 206 tops, and contiguous described the second end, is connected with described inner tube; For the combi inlet port 203 of described sulfur-bearing vapour mixture is provided to described cooling space, described combi inlet port 203 is arranged at described outer tube 206 tops, and contiguous described the second end, is connected with described cooling space; For discharging the Molten sulphur outlet 204 of described Molten sulphur, described Molten sulphur outlet 204 is arranged at described outer tube 206 bottoms, and contiguous described the second end, is connected with described cooling space; And residual gas mixture outlet 205, described residual gas mixture outlet 205 is arranged at described first end, be connected with described cooling space, be used for discharging described residual gas mixture, wherein, described cooling water inlet 201 exports 204 intervals with described Molten sulphur and arranges, and described cooling water outlet 202 arranges with described combi inlet port 203 intervals.Thus, can be effectively Molten sulphur by high temperature sulphur vapor condensation, and due to the first end of the first cooling separator and the line of the second end and horizontal plane formation certain angle, the Molten sulphur of cooling acquisition can be by pipeline self to cooling separator bottom.
According to embodiment of the present utility model, further comprise for described residual gas mixture is carried out to the second refrigerated separation, to remove the second refrigerated separation device 500 of water vapor acquisition nitrogen, described the second refrigerated separation device 500 is connected with described the first refrigerated separation device 200, and has identical structure with described the first refrigerated separation device 200.Thus, can effectively remove the water vapour in nitrogen, thereby nitrogen is carried out to recycle, and then effectively reduce energy consumption, minimizing cost, and water of condensation can be by pipeline self to sewage collecting tank.
According to embodiment of the present utility model, described water coolant is feedwater or de-mineralized water.Thus, can realize the recycling of heat, effectively reduce energy consumption, save cost.
According to embodiment of the present utility model, further comprise for the feedwater of discharging through described cooling water outlet 202 is returned to boiler, or the de-mineralized water of discharging through described cooling water outlet 202 being delivered to the water shoot (not shown) of deoxygenator, described water shoot is connected with described cooling water outlet 202.Thus, can realize the recycle of feedwater and de-mineralized water, effectively reduce energy consumption, save cost.
According to embodiment of the present utility model, further comprise for described remaining solid slag being carried out cooling and delivering to smelting shop, to reclaim the Residue extraction pipeline (not shown) of valuable metal, described Residue extraction pipeline is connected with described heat treatment apparatus 100.Thus, in by valuable metal recovery recycling, can avoid environmental pollution.
According to embodiment of the present utility model, further comprise for described Molten sulphur is delivered to described granulating system, to described Molten sulphur is prepared as to the liquid sulphur conveying pipe road (not shown) of solid sulfur, described liquid sulphur conveying pipe road is connected and is connected with granulating system (not shown) with described the first refrigerated separation device 200 respectively.Thus, can effectively will reclaim the sulphur obtaining for industrial production.
In order better to understand the system that reclaims sulphur from sulfur-bearing leached mud of the present utility model, describe the method that reclaims sulphur from sulfur-bearing leached mud of utilizing this system below in detail:
Aspect one of the present utility model, the utility model provides a kind of method that reclaims sulphur from sulfur-bearing leached mud.According to embodiment of the present utility model, the method comprises the following steps: in nitrogen atmosphere, under condition of negative pressure, described sulfur-bearing leached mud is heated to 400-500 degree Celsius, to obtain sulfur-bearing vapour mixture and remaining solid slag; And described sulfur-bearing vapour mixture is carried out to the first refrigerated separation, to obtain Molten sulphur and residual gas mixture.Utility model people finds, utilize the method for the present utility model, can fast and effeciently reclaim the sulphur in sulfur-bearing leached mud, and the method is simple to operate, sulfur recovery rate is high, environmental pollution is little, operational load is little, and maintenance of equipment rate is low, and to not requirement of elemental sulfur content in leached mud, applied widely, be easy to realize industrialization.
According to the method that reclaims sulphur from sulfur-bearing leached mud of the utility model embodiment, can also there is following additional technical feature:
According to embodiment of the present utility model, described sulfur-bearing leached mud is that oxygen presses Leaching Zinc to smelt leached mud.Thus, can reclaim elemental sulfur in leached mud, not only can create economic benefit, and can reduce the pollution to environment, realize Sustainable development.
According to embodiment of the present utility model, before carrying out described heat treated, further comprise: described sulfur-bearing leached mud is carried out to filtration treatment.Thus, can effectively reduce the water-content in leached mud, and then greatly reduce the energy consumption of follow-up sublimation step.
According to embodiment of the present utility model, described filtration treatment adopts vertical filter to carry out.Thus, can effectively reduce the water-content in sulfur-bearing leached mud, obtain the lower sulfur-bearing leached mud of water content.
According to embodiment of the present utility model, in described sulfur-bearing leached mud, solid content is 25%, through moisture lower than 15% in the sulfur-bearing leached mud of filtration treatment.Thus, can effectively reduce the energy consumption in follow-up sublimation step.
According to embodiment of the present utility model, described heat treated adopts fluidizing furnace to carry out, and described fluidizing furnace comprises: body of heater, is limited with reaction compartment in described body of heater; Opening for feed, described opening for feed is arranged at described sidewall of the furnace body below, for providing and state sulfur-bearing leached mud to described body of heater; Inlet mouth, described inlet mouth is arranged at described bottom of furnace body, to form described nitrogen atmosphere, and discharges described remaining solid slag for supplying nitrogen in described body of heater; Discharge port, described discharge port is arranged at described sidewall of the furnace body top, for discharging described sulfur-bearing vapour mixture.Utility model people finds, utilizes above-mentioned fluidizing furnace by distillation, sulphur simple substance to be separated from sulfur-bearing leached mud fast and effectively.In addition, this fluidizing furnace working pressure is negative pressure, and adopts nitrogen protection, can effectively prevent that sulphur is by airborne dioxygen oxidation.
According to embodiment of the present utility model, described fluidizing furnace further comprises at least one heating tube, and described heating tube is arranged in described body of heater, for making the temperature in described body of heater remain 400-500 degree Celsius.Thus, can effectively make sulphur distil out from leached mud, ensure that the vapor partial pressure of sulphur is higher simultaneously, can discharge from fluidizing furnace top, enter cleaning apparatus.
According to embodiment of the present utility model, described sulfur-bearing leached mud is carried out to heat treated to 400 degree Celsius.Thus, can either ensure that sulphur effectively distils, can reduce again energy consumption, reduce costs.
According to embodiment of the present utility model, before carrying out described the first refrigerated separation, further comprise: described sulfur-bearing vapour mixture is carried out to dust removal process.Thus, can effectively remove the impurity such as dust in sulphur steam, obtain the higher sulfur product of purity.
According to embodiment of the present utility model, described dust removal process adopts Ceramic dust collector to carry out.Thus, dust removing effects is better.
According to embodiment of the present utility model, at the temperature of 360-450 degree Celsius, carry out described dust removal process.Thus, can avoid sulphur vapor condensation to become Molten sulphur, cause equipment, line clogging.
According to embodiment of the present utility model, utilize the first cooling separator to carry out described the first refrigerated separation, described the first cooling separator has first end and the second end, the line of described first end and the second end and horizontal plane form angle α, wherein α is greater than 0 ° and be less than 30 °, and described first end is higher than described the second end, and described the first cooling separator comprises: inner tube, and described inner tube is used for the water coolant that circulates; Outer tube, forms cooling space between described outer tube and described inner tube, the described cooling space described sulfur-bearing vapour mixture that is used for circulating; Cooling water inlet, described cooling water inlet is arranged at described outer tube bottom, and contiguous described the second end, is connected, for providing described water coolant to described inner tube with described inner tube; Cooling water outlet, described cooling water outlet is arranged at described outer tube top, and contiguous described the second end, is connected, for discharging described water coolant with described inner tube; Combi inlet port, described combi inlet port is arranged at described outer tube top, and contiguous described the second end, is connected, for described sulfur-bearing vapour mixture is provided to described cooling space with described cooling space; Molten sulphur outlet, described Molten sulphur outlet is arranged at described outer tube bottom, and contiguous described the second end, is connected, for discharging described Molten sulphur with described cooling space; And residual gas mixture outlet, described residual gas mixture outlet is arranged at described first end, be connected with described cooling space, be used for discharging described residual gas mixture, wherein, described cooling water inlet and described Molten sulphur outlet interval arrange, and described cooling water outlet and described combi inlet port interval arrange.Thus, can be effectively Molten sulphur by high temperature sulphur vapor condensation, and due to the first end of cooling separator and the line of the second end and horizontal plane formation certain angle, the Molten sulphur of cooling acquisition can be by pipeline self to cooling separator bottom.
According to embodiment of the present utility model, further comprise described residual gas mixture is carried out to the second refrigerated separation, obtain nitrogen to remove water vapor, wherein said the second refrigerated separation adopts the second cooling separator to carry out, and described the second cooling separator has identical structure with described the first cooling separator.Thus, can effectively remove the water vapour in nitrogen, thereby nitrogen is carried out to recycle, and then effectively reduce energy consumption, minimizing cost, and water of condensation can be by pipeline self to sewage collecting tank.
According to embodiment of the present utility model, described water coolant is feedwater or de-mineralized water.Thus, fully recovery waste heat, improves the heat utilization efficiency of whole technique.
According to embodiment of the present utility model, the feedwater of discharging through described cooling water outlet is returned to boiler, the de-mineralized water of discharging through described cooling water outlet is returned to deoxygenator.Thus, can realize the recycle of feedwater and de-mineralized water, effectively reduce energy consumption, save cost.
According to embodiment of the present utility model, described remaining solid slag is carried out cooling and delivers to smelting shop, to reclaim valuable metal.Thus, in by valuable metal recovery recycling, can avoid environmental pollution.
According to embodiment of the present utility model, by granulating system, described Molten sulphur is prepared as to solid sulfur.Thus, can effectively will reclaim the sulphur obtaining for industrial production.
Embodiment 1
Press solid content in Leaching Zinc smelting technology to be about 25% leached mud ore pulp oxygen and be delivered to vertical filter by ore pulp feeding pump, the impurity that filtration obtains etc. send smelting shop, the water content obtaining lower than 15% sulfur-bearing leached mud by constant feeder, be delivered in the reaction compartment of fluidizing furnace through opening for feed, in the reaction compartment of fluidizing furnace, under condition of negative pressure, sulfur-bearing leached mud is heated to be processed to 400-500 degree Celsius, simultaneously, by inlet mouth to supplying nitrogen in the reaction compartment of fluidizing furnace, and to heat by heating tube the temperature maintaining in reaction compartment be 400-500 degree Celsius, after element sulphur distillation in leached mud, mix and separate with solid slag with nitrogen, obtain thus sulfur-bearing vapour mixture and remaining solid slag, wherein, remaining solid slag is discharged reaction compartment by inlet mouth, carry smelting shop through Residue extraction pipeline, sulfur-bearing vapour mixture is discharged reaction compartment through discharge port, be transported to pyroceramic fly-ash separator, under 360-450 degree Celsius, carry out dust removal process, entered the cooling space of the first cooling separator by combi inlet port through the sulfur-bearing vapour mixture of dedusting, simultaneously, feedwater enters inner tube by cooling water inlet, make the condensation of sulfur-bearing vapour mixture by the heat exchange between water coolant and sulfur-bearing vapour mixture, to obtain Molten sulphur and residual gas mixture, the Molten sulphur obtaining is from the bottom that flow to cooling space, discharge cooling space by Molten sulphur outlet, be delivered to granulating system through liquid sulphur conveying pipe road and make solid sulfur, feedwater through heat exchange is discharged inner tube by cooling water outlet, be delivered to boiler systems, the residual gas mixture obtaining is discharged cooling space by residual gas mixture outlet, be transported to the cooling space of the second cooling separator, de-mineralized water enters inner tube by cooling water inlet simultaneously, make the water vapor condensation in residual gas mixture by the heat exchange between water coolant and residual gas mixture, so that acquisition nitrogen, the nitrogen obtaining is further transported to fluidizing furnace recycle, de-mineralized water through heat exchange is discharged inner tube by cooling water outlet, be delivered to deoxygenator.
In description of the present utility model, it will be appreciated that, term " " center ", " longitudinally ", " laterally ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", " outward ", " clockwise ", " counterclockwise ", " axially ", " radially ", orientation or the position relationship of instructions such as " circumferentially " are based on orientation shown in the drawings or position relationship, only the utility model and simplified characterization for convenience of description, instead of device or the element of instruction or hint indication must have specific orientation, with specific orientation structure and operation, therefore can not be interpreted as restriction of the present utility model.
In addition, term " first ", " second " be only for describing object, and can not be interpreted as instruction or hint relative importance or the implicit quantity that indicates indicated technical characterictic.Thus, one or more these features can be expressed or impliedly be comprised to the feature that is limited with " first ", " second ".In description of the present utility model, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the utility model, unless otherwise clearly defined and limited, the terms such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and for example, can be to be fixedly connected with, and can be also to removably connect, or integral; Can be mechanical connection, can be also electrical connection; Can be to be directly connected, also can indirectly be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, can understand as the case may be the concrete meaning of above-mentioned term in the utility model.
In the utility model, unless otherwise clearly defined and limited, First Characteristic Second Characteristic " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, First Characteristic Second Characteristic " on ", " top " and " above " but First Characteristic directly over Second Characteristic or oblique upper, or only represent that First Characteristic level height is higher than Second Characteristic.First Characteristic Second Characteristic " under ", " below " and " below " can be First Characteristic under Second Characteristic or tiltedly, or only represent that First Characteristic level height is less than Second Characteristic.
In the description of this specification sheets, the description of reference term " embodiment ", " some embodiment ", " example ", " concrete example " or " some examples " etc. means to be contained at least one embodiment of the present utility model or example in conjunction with specific features, structure, material or the feature of this embodiment or example description.In this manual, the schematic statement of above-mentioned term is not necessarily referred to identical embodiment or example.And specific features, structure, material or the feature of description can be with suitable mode combination in any one or more embodiment or example.
Although illustrated and described embodiment of the present utility model, those having ordinary skill in the art will appreciate that: in the situation that not departing from principle of the present utility model and aim, can carry out multiple variation, amendment, replacement and modification to these embodiment, scope of the present utility model is limited by claim and equivalent thereof.
Claims (12)
1. a system that reclaims sulphur from sulfur-bearing leached mud, is characterized in that, comprising:
For in nitrogen atmosphere, under condition of negative pressure, described sulfur-bearing leached mud is heated to 400-500 degree Celsius, to obtain the heat treatment apparatus of sulfur-bearing vapour mixture and remaining solid slag; And
For described sulfur-bearing vapour mixture is carried out to the first refrigerated separation, to obtain the first refrigerated separation device of Molten sulphur and residual gas mixture, described the first refrigerated separation device is connected with described heat treatment apparatus.
2. system according to claim 1, is characterized in that, further comprises for before carrying out described heat treated, and described sulfur-bearing leached mud is carried out to the filtration treatment device of filtration treatment, described filtration treatment device is connected with described heat treatment apparatus.
3. system according to claim 2, is characterized in that, described filtration treatment device is vertical filter.
4. system according to claim 1, is characterized in that, described heat treatment apparatus is fluidizing furnace, and described fluidizing furnace comprises:
Body of heater, is limited with reaction compartment in described body of heater;
For the opening for feed of described sulfur-bearing leached mud is provided to described body of heater, described opening for feed is arranged at described sidewall of the furnace body below;
For to supplying nitrogen in described body of heater to form described nitrogen atmosphere, and discharge the inlet mouth of described remaining solid slag, described inlet mouth is arranged at described bottom of furnace body;
For discharging the discharge port of described sulfur-bearing vapour mixture, described discharge port is arranged at described sidewall of the furnace body top.
5. system according to claim 4, is characterized in that, described fluidizing furnace further comprises that at least one is for making the temperature in described body of heater remain the heating tube of 400-500 degree Celsius, and described heating tube is arranged in described body of heater.
6. system according to claim 1, it is characterized in that, further comprise for before carrying out described the first refrigerated separation, described sulfur-bearing vapour mixture is carried out to the dedusting treater of dust removal process, described dedusting treater is connected with described the first refrigerated separation device with described heat treatment apparatus respectively.
7. system according to claim 6, is characterized in that, described dedusting treater is Ceramic dust collector.
8. system according to claim 1, it is characterized in that, described the first refrigerated separation device has first end and the second end, the line of described first end and the second end and horizontal plane form angle α, wherein α is greater than 0 ° and be less than 30 °, and described first end is higher than described the second end, and described the first refrigerated separation device comprises:
For the inner tube of the water coolant that circulates;
Be used for forming the outer tube of cooling space for use in the described sulfur-bearing vapour mixture of circulation between described inner tube;
For the cooling water inlet of water coolant is provided to described inner tube, described cooling water inlet is arranged at described outer tube bottom, and contiguous described the second end, is connected with described inner tube;
For discharging the cooling water outlet of described water coolant, described cooling water outlet is arranged at described outer tube top, and contiguous described the second end, is connected with described inner tube;
For the combi inlet port of described sulfur-bearing vapour mixture is provided to described cooling space, described combi inlet port is arranged at described outer tube top, and contiguous described the second end, is connected with described cooling space;
For discharging the Molten sulphur outlet of described Molten sulphur, described Molten sulphur outlet is arranged at described outer tube bottom, and contiguous described the second end, is connected with described cooling space; And
For discharging the residual gas mixture outlet of described residual gas mixture, described residual gas mixture outlet is arranged at described first end, be connected with described cooling space,
Wherein, described cooling water inlet and described Molten sulphur outlet interval arrange, and described cooling water outlet and described combi inlet port interval arrange.
9. system according to claim 8, it is characterized in that, further comprise for described residual gas mixture is carried out to the second refrigerated separation, to remove the second refrigerated separation device of water vapor acquisition nitrogen, described the second refrigerated separation device is connected with described the first refrigerated separation device, and has identical structure with described the first refrigerated separation device.
10. system according to claim 8, it is characterized in that, further comprise for the feedwater of discharging through described cooling water outlet is returned to boiler, or the de-mineralized water of discharging through described cooling water outlet is delivered to the water shoot of deoxygenator, described water shoot is connected with described cooling water outlet.
11. systems according to claim 1, is characterized in that, further comprise that to reclaim the Residue extraction pipeline of valuable metal, described Residue extraction pipeline is connected with described heat treatment apparatus for described remaining solid slag being carried out cooling and delivering to smelting shop.
12. systems according to claim 1, it is characterized in that, further comprise for described Molten sulphur is delivered to granulating system, to described Molten sulphur is prepared as to the liquid sulphur conveying pipe road of solid sulfur, described liquid sulphur conveying pipe road is connected and is connected with granulating system with described the first refrigerated separation device respectively.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420197997.XU CN203820457U (en) | 2014-04-22 | 2014-04-22 | System for recovering sulfur from sulfur-containing leach residue |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420197997.XU CN203820457U (en) | 2014-04-22 | 2014-04-22 | System for recovering sulfur from sulfur-containing leach residue |
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| CN203820457U true CN203820457U (en) | 2014-09-10 |
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| CN201420197997.XU Expired - Lifetime CN203820457U (en) | 2014-04-22 | 2014-04-22 | System for recovering sulfur from sulfur-containing leach residue |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964398A (en) * | 2014-04-22 | 2014-08-06 | 中国恩菲工程技术有限公司 | System for recovering sulfur from sulfur-containing leaching residue |
| CN112138855A (en) * | 2020-08-10 | 2020-12-29 | 西部矿业股份有限公司 | Method for recycling zinc oxygen pressure leaching sulfur flotation tailings |
| CN113086951A (en) * | 2021-03-24 | 2021-07-09 | 武汉科技大学 | Process for preparing high-purity sulfur by hot blowing desorption method |
-
2014
- 2014-04-22 CN CN201420197997.XU patent/CN203820457U/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964398A (en) * | 2014-04-22 | 2014-08-06 | 中国恩菲工程技术有限公司 | System for recovering sulfur from sulfur-containing leaching residue |
| CN112138855A (en) * | 2020-08-10 | 2020-12-29 | 西部矿业股份有限公司 | Method for recycling zinc oxygen pressure leaching sulfur flotation tailings |
| CN112138855B (en) * | 2020-08-10 | 2021-12-28 | 西部矿业股份有限公司 | Method for recycling zinc oxygen pressure leaching sulfur flotation tailings |
| CN113086951A (en) * | 2021-03-24 | 2021-07-09 | 武汉科技大学 | Process for preparing high-purity sulfur by hot blowing desorption method |
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