CN220959673U - Device for directly spraying liquid sulfur into fuming furnace for vulcanization and volatilization - Google Patents
Device for directly spraying liquid sulfur into fuming furnace for vulcanization and volatilization Download PDFInfo
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- CN220959673U CN220959673U CN202322824487.2U CN202322824487U CN220959673U CN 220959673 U CN220959673 U CN 220959673U CN 202322824487 U CN202322824487 U CN 202322824487U CN 220959673 U CN220959673 U CN 220959673U
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- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 346
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 344
- 239000011593 sulfur Substances 0.000 title claims abstract description 344
- 239000007788 liquid Substances 0.000 title claims abstract description 179
- 238000004073 vulcanization Methods 0.000 title claims abstract description 16
- 238000005507 spraying Methods 0.000 title abstract description 21
- 239000003245 coal Substances 0.000 claims abstract description 125
- 239000002893 slag Substances 0.000 claims abstract description 75
- 238000002347 injection Methods 0.000 claims abstract description 72
- 239000007924 injection Substances 0.000 claims abstract description 72
- 238000002844 melting Methods 0.000 claims abstract description 55
- 230000008018 melting Effects 0.000 claims abstract description 55
- 238000004321 preservation Methods 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 34
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 23
- 239000003546 flue gas Substances 0.000 claims abstract description 23
- 238000010791 quenching Methods 0.000 claims abstract description 23
- 230000000171 quenching effect Effects 0.000 claims abstract description 23
- 239000000428 dust Substances 0.000 claims abstract description 21
- 239000002918 waste heat Substances 0.000 claims abstract description 20
- 238000007664 blowing Methods 0.000 claims abstract description 14
- 238000012216 screening Methods 0.000 claims abstract description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 138
- 229910052757 nitrogen Inorganic materials 0.000 claims description 69
- 239000002245 particle Substances 0.000 claims description 31
- 238000010926 purge Methods 0.000 claims description 30
- 238000007599 discharging Methods 0.000 claims description 23
- 238000003860 storage Methods 0.000 claims description 19
- 238000010438 heat treatment Methods 0.000 claims description 11
- 238000005303 weighing Methods 0.000 claims description 7
- 239000000779 smoke Substances 0.000 claims description 4
- 238000005987 sulfurization reaction Methods 0.000 claims description 3
- 239000005864 Sulphur Substances 0.000 claims 1
- 239000007921 spray Substances 0.000 claims 1
- 230000008016 vaporization Effects 0.000 claims 1
- 238000009834 vaporization Methods 0.000 claims 1
- 238000006243 chemical reaction Methods 0.000 abstract description 33
- 239000003795 chemical substances by application Substances 0.000 abstract description 12
- 239000002699 waste material Substances 0.000 abstract description 7
- 238000002485 combustion reaction Methods 0.000 abstract description 5
- NIFIFKQPDTWWGU-UHFFFAOYSA-N pyrite Chemical compound [Fe+2].[S-][S-] NIFIFKQPDTWWGU-UHFFFAOYSA-N 0.000 description 45
- 229910052683 pyrite Inorganic materials 0.000 description 43
- ATJFFYVFTNAWJD-UHFFFAOYSA-N Tin Chemical compound [Sn] ATJFFYVFTNAWJD-UHFFFAOYSA-N 0.000 description 40
- 239000011028 pyrite Substances 0.000 description 38
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 32
- 238000000034 method Methods 0.000 description 16
- XOLBLPGZBRYERU-UHFFFAOYSA-N tin dioxide Chemical compound O=[Sn]=O XOLBLPGZBRYERU-UHFFFAOYSA-N 0.000 description 15
- 239000000463 material Substances 0.000 description 13
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 description 12
- 229910052681 coesite Inorganic materials 0.000 description 10
- 229910052906 cristobalite Inorganic materials 0.000 description 10
- 239000000155 melt Substances 0.000 description 10
- 239000000377 silicon dioxide Substances 0.000 description 10
- 229910052682 stishovite Inorganic materials 0.000 description 10
- 229910052905 tridymite Inorganic materials 0.000 description 10
- 238000004458 analytical method Methods 0.000 description 9
- 239000007789 gas Substances 0.000 description 9
- 238000006722 reduction reaction Methods 0.000 description 9
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 8
- 238000009413 insulation Methods 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 6
- 238000003723 Smelting Methods 0.000 description 6
- 238000003556 assay Methods 0.000 description 6
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 6
- 238000005070 sampling Methods 0.000 description 6
- 239000006004 Quartz sand Substances 0.000 description 5
- 235000013601 eggs Nutrition 0.000 description 5
- 238000004519 manufacturing process Methods 0.000 description 5
- 229910052960 marcasite Inorganic materials 0.000 description 5
- 238000004140 cleaning Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 229910052742 iron Inorganic materials 0.000 description 4
- 238000011946 reduction process Methods 0.000 description 4
- 230000000630 rising effect Effects 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- RYGMFSIKBFXOCR-UHFFFAOYSA-N Copper Chemical compound [Cu] RYGMFSIKBFXOCR-UHFFFAOYSA-N 0.000 description 3
- 229910004298 SiO 2 Inorganic materials 0.000 description 3
- 229910006404 SnO 2 Inorganic materials 0.000 description 3
- 230000001174 ascending effect Effects 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 230000000052 comparative effect Effects 0.000 description 3
- 229910052802 copper Inorganic materials 0.000 description 3
- 239000010949 copper Substances 0.000 description 3
- OMZSGWSJDCOLKM-UHFFFAOYSA-N copper(II) sulfide Chemical compound [S-2].[Cu+2] OMZSGWSJDCOLKM-UHFFFAOYSA-N 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000001514 detection method Methods 0.000 description 3
- 238000012544 monitoring process Methods 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 230000014233 sulfur utilization Effects 0.000 description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000002184 metal Substances 0.000 description 2
- 229910052751 metal Inorganic materials 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 239000013589 supplement Substances 0.000 description 2
- 229910001887 tin oxide Inorganic materials 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 229910052840 fayalite Inorganic materials 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 239000011521 glass Substances 0.000 description 1
- XLYOFNOQVPJJNP-ZSJDYOACSA-N heavy water Substances [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 239000003949 liquefied natural gas Substances 0.000 description 1
- 239000003915 liquefied petroleum gas Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 230000000750 progressive effect Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
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Abstract
The utility model discloses a device for directly spraying liquid sulfur into a fuming furnace for vulcanization and volatilization, which comprises: the device comprises a granular sulfur screening and belt conveying system, a granular sulfur melting heat preservation tank, a liquid sulfur suction pump, a liquid sulfur conveying pipeline, a pulverized coal conveying and blowing system, a fuming furnace, a slag water quenching system, a waste heat boiler, a surface cooler, a bag dust collector and a fuming furnace flue gas pipeline. The utility model can ensure smooth and unblocked pipeline transportation of the vulcanizing agent liquid sulfur, prepare and control the feeding speed of the liquid sulfur, avoid the technical problems of direct combustion waste of the granular sulfur and easy blockage of the pipeline caused by direct injection of the granular sulfur, ensure the full running of the vulcanization-reduction combined reaction and realize the control of the optimal economic index of the liquid sulfur and the pulverized coal by setting reasonable positions of the granular sulfur of the fuming furnace and the pulverized coal burner.
Description
Technical Field
The utility model relates to the technical field of vulcanization-reduction of a fuming furnace for tin-containing materials, in particular to a device for directly spraying liquid sulfur into the fuming furnace for vulcanization volatilization.
Background
With the gradual decrease of the tin-containing grade of the tin ore raw material and the increasing of the composition, the improvement of the treatment technology of the tin-containing material is also urgent. The fuming furnace is widely applied to the vulcanization and volatilization treatment of tin-containing materials, and has more than half of the world, and extremely mature and rich production operation experience is accumulated. In the industry, the vulcanizing and volatilizing agent for tin-containing materials is mainly pyrite (also called pyrite), which is mainly based on wide sources of pyrite and low purchase price.
The pyrite is taken as a fuming furnace vulcanization volatilizing agent, is generally put into a fuming furnace through a furnace top belt of the fuming furnace, and is subjected to vulcanization reaction with high-temperature melt in the furnace, sulfur in the pyrite is reacted with tin oxide (SnO 2 and SnO), and the main reactions are as follows:
2(FeS2)+O2＝2(FeO)+4(S) (1)
(SnO2)+2(S)＝SnS(g)+SO2(g) (2)
2(FeO)+SiO2＝2FeO·SiO2 (3)
the total reaction is ：2(FeS2)+O2+2(SnO2)+SiO2＝2FeO·SiO2+2SnS(g)+2SO2(g) (4)
2(SnO)+3(S)＝2SnS(g)+SO2(g) (5)
The total reaction is: 2 (FeS 2)+2O2+2(SnO)+SiO2＝2FeO·SiO2+2SnS(g)+2SO2 (g) (6)
The reaction (1) is high-temperature oxidation of pyrite, liquid elemental sulfur (S) and (FeO) are released, and the (FeO) and quartz sand SiO 2 are subjected to slag forming reaction (3) to generate fayalite phase 2 FeO.SiO 2; and the gaseous SnS (g) after vulcanization and volatilization enters the rising flue, and the gaseous SnS (g) is oxidized after secondary air supplement, namely the following reaction occurs:
SnS(g)+2O2＝SnO2(s)+SO2(g) (7)
The solid SnO 2(s) of tin dioxide is collected in a surface cooler and a bag dust collector and is used as a raw material for recycling in the subsequent smelting process.
However, as can be seen from the above total reactions (4) and (6), the sulfur utilization rate in the pyrite is not high, and 2 molecules of pyrite react with two different forms of tin oxide (SnO 2, snO) to release 2 molecules of sulfur dioxide gas SO 2 (g) respectively, SO that to further increase the sulfur utilization rate in the pyrite, the smelting plant often needs to supplement a certain amount of pulverized coal (i.e. carbon C), and the above total reactions (4) and (6) combine pulverized coal (i.e. carbon C) to react with the following reactions:
2(FeS2)+O2+4(SnO2)+SiO2+4C(s)＝2FeO·SiO2+4SnS(g)+4 CO2(g) (8)
2(FeS2)+2O2+4(SnO)+SiO2+3C(s)＝2FeO·SiO2+4SnS(g)+3CO2(g) (9)
The supplemented pulverized coal not only participates in the sulfuration volatilization reaction of the step (8) and the step (9) in the fuming furnace, but also partially performs combustion exothermic reaction with oxygen in the furnace, and the supplemented high-temperature melt keeps good fluidity and the heat required by the related chemical reaction, namely, the carbon in the pulverized coal plays a double role of participating in the sulfuration reaction and the combustion exothermic reaction.
However, the above reaction will occur in the process of vulcanizing and volatilizing the tin-containing material by the fuming furnace, but the pyrite purchased in the factory usually contains at least 10% by mass of water, which is difficult to be subjected to dehydration and drying treatment, otherwise, sulfur in the pyrite is entrained and lost by evaporated water, which is not economical to the smelting plant, and the following reaction will occur under the high temperature condition after the pyrite enters the fuming furnace:
(FeS2)+2H2O＝2H2S(g)+(FeO) (10)
The hydrogen sulfide gas H 2 S (g) released by the reaction can escape from the molten pool into the flue gas quickly, and besides a small amount of hydrogen sulfide gas H 2 S (g) is oxidized and combusted in a high temperature area to generate sulfur dioxide and water, most of hydrogen sulfide gas H 2 S (g) does not participate in other reactions, so that the sulfur utilization rate in the pyrite is not high, and as can be calculated from the reaction (10), the 10% mass fraction of water can consume 33.3% mass fraction of pyrite, which directly leads to the non-ideal smelting economic index. In addition, the residual hydrogen sulfide gas H 2 S (g) in the flue gas also affects the subsequent acid making or desulfurization treatment of the flue gas, and the tail gas is heavy in smell of smelly eggs and pollutes the atmosphere due to improper treatment.
Therefore, the utility model provides a method for volatilizing tin-containing materials in a fuming furnace by directly using liquid sulfur as a vulcanizing agent, so as to explore the use of sulfur as the vulcanizing agent to replace pyrite, avoid the technical problems, and solve the technical problem that the pipeline is easy to be blocked by using the pipeline to pneumatically convey powdery sulfur. According to inquiry, only crude tin refining, crude lead refining and crude nickel refining impurity removal processes in China are carried out at present, in order to remove copper impurities, most industries in China use particle sulfur to be added into high-temperature crude metal, sulfur in the sulfur reacts with impurity copper to generate insoluble solid copper sulfide, the solid copper sulfide is condensed in the cooling process, and the condensed copper sulfide is separated after slag dragging, so that the impurity copper removal is realized. However, the granular sulfur is basically added from the surface of the high-temperature crude metal melt, and is stirred and then is involved in the melt to participate in the reaction. However, in the process of vulcanizing and volatilizing tin-containing materials in a fuming furnace, sulfur is directly used as a vulcanizing agent to be added into a molten pool, if sulfur is added into the molten pool through a furnace top belt, the sulfur is easily burnt at 248 ℃ or above under the action of high temperature and oxidizing atmosphere in the process of falling into the molten pool, so that sulfur dioxide is directly generated, and only a small amount of granular sulfur can possibly fall into the molten pool to participate in vulcanization reaction, which directly leads to serious shortage of the effective utilization rate of the granular sulfur; particle sulfur is also used by a small number of domestic enterprises, is sprayed into a molten pool for vulcanization reaction through pneumatic conveying, but after the particle sulfur conveying pipeline is continuously used for a period of time, the fine particle sulfur is gradually adhered to the inner wall of the pipeline, so that the effective aperture of the particle sulfur conveying pipeline is smaller and smaller, the pipeline is not blocked, the conveying of the particle sulfur is unsmooth, normal production operation is influenced, in addition, the hardness of the fine particle sulfur adhered to the inner wall of the pipeline is higher, and the cleaning difficulty and the workload of the particle sulfur pipeline are increased. The research and industrial application of directly spraying liquid sulfur as vulcanizing agent into high temperature molten pool in fuming furnace smelting or other molten pool smelting technology and equipment have not been reported in relevant domestic and foreign industries.
Disclosure of utility model
The utility model aims to provide a device for directly spraying fuming and volatilizing tin-containing materials by using liquid sulfur, which ensures smooth and unblocked pipeline transportation of the liquid sulfur of vulcanizing agents, prepares and controls the feeding speed of the liquid sulfur, avoids the technical problems of direct combustion waste of granular sulfur and easy blockage of the pipeline by direct spraying of the granular sulfur, ensures the full running of the combined vulcanization-reduction reaction by the reasonable position arrangement of the granular sulfur of a fuming furnace and a pulverized coal burner, and realizes the control of the optimal economic index of the liquid sulfur and the pulverized coal.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
a device for directly spraying liquid sulfur into a fuming furnace for vulcanization and volatilization, which comprises:
The device comprises a granular sulfur screening and belt conveying system, a granular sulfur melting heat preservation tank, a liquid sulfur suction pump, a liquid sulfur conveying pipeline, a pulverized coal conveying and blowing system, a fuming furnace, a slag water quenching system, a waste heat boiler, a surface cooler, a bag dust collector and a fuming furnace flue gas pipeline;
The granular sulfur screening and belt conveying system is arranged on one side above the granular sulfur melting heat preservation tank;
The liquid sulfur suction pump is connected with the granular sulfur melting heat preservation tank and vertically penetrates into the granular sulfur melting heat preservation tank;
The liquid sulfur suction pump, the liquid sulfur conveying pipeline, the fuming furnace, the waste heat boiler, the surface cooler, the bag dust collector and the fuming furnace flue gas pipeline are connected in sequence;
The pulverized coal conveying and blowing system and the slag water quenching system are respectively connected with the fuming furnace.
Preferably, the granular sulfur screening and belt conveying system comprises:
The device comprises a particle sulfur conical hopper, a conical hopper vibrator, a primary screen, a secondary screen, a conical hopper blanking valve, an intermediate bin vibrator, an intermediate bin blanking valve, a differential weighing device, a particle sulfur storage bin, a storage bin blanking valve and a particle sulfur conveying belt;
The primary screen, the granular sulfur conical hopper, the secondary screen, the conical hopper blanking valve, the middle bin blanking valve, the differential weighing device, the granular sulfur storage bin and the storage bin blanking valve are sequentially connected from top to bottom;
The conical hopper vibrator is arranged on the side wall of the particle sulfur conical hopper; the intermediate bin vibrator is arranged on the side wall of the intermediate bin;
the feeding end of the granular sulfur conveying belt is arranged at the lower side of the discharging valve of the storage bin, and the discharging end of the granular sulfur conveying belt is arranged at one side above the granular sulfur melting heat preservation tank.
Preferably, the particle sulfur melting heat preservation tank is provided with a heat preservation tank thermometer, a liquid level meter, an infrared heating melter and a discharging hopper;
Wherein, the heat preservation tank thermometer and the liquid level meter are arranged above the granular sulfur melting heat preservation tank and penetrate into the granular sulfur melting heat preservation tank; the infrared heating melter is arranged in the wall body around the particle sulfur melting heat-preserving tank; the discharging hopper is arranged on one side above the granular sulfur melting heat preservation tank; the discharge end of the granular sulfur conveying belt is arranged above the discharging hopper;
the bottom of the liquid sulfur suction pump is provided with a suction pump filter screen.
Preferably, the outlet end of the liquid sulfur conveying pipeline is of an inverted V-shaped structure; the liquid sulfur conveying pipeline is provided with a liquid sulfur flowmeter, a conveying pipeline pressure gauge, an infrared heater, a nitrogen purging pipe, a check valve and a thermometer;
the infrared heater is arranged in the pipe wall of the liquid sulfur conveying pipeline;
the thermometer and the liquid sulfur flowmeter are arranged on the side wall of one side of the inlet end of the liquid sulfur conveying pipeline;
the conveying pipeline manometer is arranged in a pipeline at one side of the inlet end of the liquid sulfur conveying pipeline;
The nitrogen purging pipe is arranged at the top of the inverted V-shaped structure at the outlet end of the liquid sulfur conveying pipeline; a nitrogen purging pressure gauge and a nitrogen purging valve are arranged in the nitrogen purging pipe;
The check valve is arranged on one side of the outlet end of the liquid sulfur conveying pipeline.
Preferably, the pulverized coal conveying and blowing system comprises a pulverized coal tank and a pulverized coal conveying pipeline;
The pulverized coal tank is connected with the fuming furnace through a pulverized coal conveying pipeline;
the inlet end of the pulverized coal conveying pipeline is provided with a coal feeding conveying air valve, and one side of the inlet end is provided with a pulverized coal conveying flowmeter.
Preferably, the fuming furnace comprises: the device comprises a liquid sulfur injection burner, a pulverized coal injection burner, a furnace side liquid slag feeding chute, a furnace top feeding port, a fuming furnace body, a temperature monitor, an observation hole and a slag discharging port;
The liquid sulfur injection burner and the pulverized coal injection burner are respectively arranged at two sides of the bottom of the fuming furnace body; the pulverized coal injection burner is arranged at a position 100mm high from the bottom of the fuming furnace body, and the liquid sulfur injection burner is arranged at a position 100-150 mm high parallel to the upper part of the pulverized coal injection burner; the pulverized coal injection burner is connected with the pulverized coal conveying pipeline; the liquid sulfur injection burner is connected with the liquid sulfur conveying pipeline;
The slag discharge port is arranged at one side of the bottom of the fuming furnace body and is connected with the slag water quenching system;
The furnace side liquid slag feeding chute, the temperature monitor and the observation hole are respectively arranged on the side wall of the upper part of the fuming furnace body;
The furnace top feed inlet is arranged at one side of the top of the fuming furnace body; a furnace top belt feeding system matched with the furnace top feeding hole is arranged above the furnace top feeding hole;
The fuming furnace body is connected with the waste heat boiler, the surface cooler and the bag dust collector in sequence.
Preferably, the inlet end of the liquid sulfur injection burner is provided with a central pipeline nitrogen pipe; the central pipeline nitrogen pipe is communicated with the liquid sulfur injection burner;
The inlet end of the central pipeline nitrogen pipe is respectively provided with a central pipeline nitrogen pressure gauge, a central pipeline nitrogen flowmeter and a central pipeline nitrogen valve.
Preferably, the apparatus further comprises: a flue gas monitor, a secondary air valve and a dust remover;
the smoke monitor is arranged in the smoke pipeline of the fuming furnace;
the secondary air valve is arranged on the side wall of the bottom of the waste heat boiler;
The dust remover is arranged at the bottom between the waste heat boiler and the surface cooler and is connected with the waste heat boiler and the surface cooler.
Compared with the prior art, the utility model has the following beneficial effects:
① After the sulfur reaching the standard granularity after carefully selecting is conveyed into a granular sulfur melting heat preservation tank by a granular sulfur conveying belt, the optimal melting flow temperature of the sulfur is kept, the reasonable position of a liquid sulfur suction pump is kept, the continuous and smooth conveying process of the liquid sulfur pipeline can be ensured, and the situation that fine powder sulfur is easily stuck to the inner wall of a conveying pipeline due to direct pipeline conveying and blowing of fine granular sulfur is avoided;
② The pure nitrogen filtered by the dryer is used for conveying the granular sulfur, so that the waste of ineffective consumption of hydrogen sulfide pollution gas and sulfur generated by the reaction of liquid sulfur and water due to the moisture mixed in the pure nitrogen in a conveying gas medium can be avoided, the liquid sulfur can be used as inert gas for protecting the liquid sulfur and a jet burner thereof, and the safety risk of burning the liquid sulfur before the liquid sulfur is blown into a fuming furnace and the risk of burning loss of the jet burner are avoided;
③ The liquid sulfur is directly blown into a fuming furnace molten pool to complete the vulcanization-reduction process, so that the direct utilization rate of sulfur is remarkably improved, the waste that the existing height difference blanking process of adding the liquid sulfur into the molten pool through a furnace top belt is easy to burn directly is avoided, and the pollution problem of the tail gas hydrogen sulfide containing the odor of the smelly eggs to the atmosphere is avoided;
④ The method for fuming and volatilizing the tin-containing material by using liquid sulfur to replace the traditional pyrite or particle sulfur as a fuming furnace vulcanizing agent can avoid using the iron amount brought into the fuming furnace by pyrite, which not only can influence the PH value of slag, but also can avoid the problem that the particle sulfur is directly conveyed and blocked by a pipeline because quartz sand SiO 2 is matched to adjust the PH value of slag (see reaction 3), which can directly influence the effective hearth capacity of the fuming furnace, so that the treatment capacity of the fuming furnace is insufficient in unit time;
⑤ The positions of the liquid state vulcanization blowing nozzle and the pulverized coal blowing nozzle of the fuming furnace are reasonably set, so that the full operation of vulcanization-reduction combined reaction can be ensured, and the control of the optimal economic index of liquid state sulfur and pulverized coal is realized;
⑥ Besides the pulverized coal is used as a reducing agent and has a heat supply effect, the utility model can also use pipeline natural gas with equal combustion values, liquefied natural gas or liquefied petroleum gas and other fuel gases as substitutes for use, can achieve the purpose of the method for vulcanizing-reducing tin-containing materials by the same fuming furnace, and realizes the green use of clean energy.
Drawings
In order to more clearly illustrate the embodiments of the present utility model or the technical solutions in the prior art, the drawings that are required to be used in the embodiments or the description of the prior art will be briefly described below, and it is obvious that the drawings in the following description are only embodiments of the present utility model, and that other drawings can be obtained according to the provided drawings without inventive effort for a person skilled in the art.
FIG. 1 is a block diagram of an apparatus provided by the present utility model;
wherein, in the figure:
1. The device comprises a granular sulfur conical hopper, a conical hopper vibrator, a primary screen, a secondary screen, a conical hopper blanking valve, a middle bin, a 7-bin vibrator, a 8-bin blanking valve, a 9-differential weighing device, a 10-granular sulfur storage bin, a 11-bin blanking valve, a 12-granular sulfur conveying belt, a 13-bin, a 14-thermal insulation tank thermometer, a 15-liquid level meter, a 16-liquid sulfur suction pump, a 17-granular sulfur melting thermal insulation tank, a 18-granular sulfur melting thermal insulation tank, a 19-infrared heating melter, a 20-suction pump filter screen, a 21-liquid sulfur conveying pipeline, a 22-thermal insulation layer, a 23-liquid sulfur flowmeter, a 24-conveying pipeline pressure meter, a 25-infrared heating device, a 26-purging nitrogen pipe, a 27-purging nitrogen pressure meter, a 28-purging nitrogen valve, a liquid sulfur melting thermal insulation tank and a liquid sulfur discharge valve. 29, check valve, 30, center line nitrogen pipe, 31, liquid sulfur injection burner, 32, liquid sulfur injection burner orifice, 33, center line nitrogen pressure gauge, 34, center line nitrogen flow meter, 35, center line nitrogen valve, 36, pulverized coal tank, 37, coal feed air valve, 38, pulverized coal feed pipe, 39, pulverized coal feed flow meter, 40, pulverized coal injection burner, 41, pulverized coal injection burner orifice 42, furnace side liquid slag feed chute, 43, furnace top belt feed system, 44, furnace top feed port, 45, fuming furnace, 46, temperature monitor, 47, sight glass, 48, overgrate air valve, 49, waste heat boiler, 50, surface cooler, 51, bag collector, 52, flue gas monitor, 53, dust remover, 54, slag tap, 55 slag water quenching system, 56, fuming furnace flue gas pipe, and furnace bottom air duct, 57. A thermometer.
Detailed Description
The following description of the embodiments of the present utility model will be made clearly and completely with reference to the accompanying drawings, in which it is apparent that the embodiments described are only some embodiments of the present utility model, but not all embodiments. All other embodiments, which can be made by those skilled in the art based on the embodiments of the utility model without making any inventive effort, are intended to be within the scope of the utility model.
Example 1
The embodiment discloses a device for directly spraying liquid sulfur into a fuming furnace for vulcanization volatilization, which comprises:
The system comprises a granular sulfur screening and belt conveying system, a granular sulfur melting heat preservation tank 17, a liquid sulfur suction pump 16, a liquid sulfur conveying pipeline 21, a pulverized coal conveying and blowing system, a fuming furnace, a slag water quenching system 55, a waste heat boiler 49, a surface cooler 50, a bag dust collector 51 and a fuming furnace flue gas pipeline 56;
the liquid sulfur suction pump 16 is connected with the granular sulfur melting heat preservation tank 17 and vertically penetrates into the granular sulfur melting heat preservation tank 17;
The liquid sulfur suction pump 16, the liquid sulfur conveying pipeline 21, the fuming furnace, the waste heat boiler 49, the surface cooler 50, the bag dust collector 51 and the fuming furnace flue gas pipeline 56 are connected in sequence;
The pulverized coal conveying and blowing system and the slag water quenching system 55 are respectively connected with the fuming furnace;
In this embodiment, the particulate sulfur screening and belt conveyor system includes:
The device comprises a particle sulfur conical hopper 1, a conical hopper vibrator 2, a primary screen 3, a secondary screen 4, a conical hopper blanking valve 5, an intermediate bin 6, an intermediate bin vibrator 7, an intermediate bin blanking valve 8, a differential weighing device 9, a particle sulfur storage bin 10, a storage bin blanking valve 11 and a particle sulfur conveying belt 12;
The primary screen 3, the granular sulfur conical hopper 1, the secondary screen 4, the conical hopper blanking valve 5, the middle bin 6, the middle bin blanking valve 8, the differential weighing device 9, the granular sulfur storage bin 10 and the storage bin blanking valve 11 are sequentially connected from top to bottom;
The conical hopper vibrator 2 is arranged on the side wall of the particle sulfur conical hopper 1; the intermediate bin vibrator 7 is arranged on the side wall of the intermediate bin 6;
The feeding end of the particle sulfur conveying belt 12 is arranged at the lower side of the discharging valve 11 of the storage bin, and the discharging end is arranged at one side above the particle sulfur melting heat preservation tank 17.
The particle sulfur melting heat preservation tank 17 is provided with a heat preservation tank thermometer 14, a liquid level meter 15, an infrared heating melter 19 and a discharging hopper 13;
Wherein, the heat preservation tank thermometer 14 and the liquid level meter 15 are arranged above the granular sulfur melting heat preservation tank 17 and penetrate into the granular sulfur melting heat preservation tank 17; the infrared heating melter 19 is arranged in the wall body around the particle sulfur melting heat preservation tank 17; the discharging hopper 13 is arranged on one side above the granular sulfur melting heat preservation tank 17; the discharge end of the granular sulfur conveying belt 12 is arranged above the discharging hopper 13;
a passenger flow sulfur melting tank heat preservation layer 18 is formed above the liquid sulfur in the granular sulfur melting heat preservation tank 17;
the bottom of the liquid sulfur suction pump 16 is provided with a suction pump filter screen 20.
The outlet end of the liquid sulfur conveying pipeline 21 is of an inverted V-shaped structure; the liquid sulfur conveying pipeline 21 is provided with a liquid sulfur flowmeter 23, a conveying pipeline pressure gauge 24, an infrared heater 25, a purging nitrogen pipe 26, a check valve 29 and a thermometer 57;
The infrared heater 25 is arranged in the pipe wall of the liquid sulfur conveying pipeline 21 to form an insulating layer 22;
the thermometer 57 and the liquid sulfur flowmeter 23 are both provided on the side wall of the inlet end side of the liquid sulfur delivery pipe 21;
The delivery pipe pressure gauge 24 is arranged in the pipeline at one side of the inlet end of the liquid sulfur delivery pipe 21;
The nitrogen purging pipe 26 is arranged at the top of the inverted V-shaped structure at the outlet end of the liquid sulfur conveying pipeline 21; a nitrogen purging pressure gauge 27 and a nitrogen purging valve 28 are arranged in the nitrogen purging pipe 26;
The check valve 29 is provided on one side of the outlet end of the liquid sulfur delivery pipe 21.
Preferably, the pulverized coal conveying and injecting system comprises a pulverized coal tank 6 and a pulverized coal conveying pipeline 38;
The pulverized coal tank 36 is connected with the fuming furnace through a pulverized coal conveying pipeline 38;
The pulverized coal feed pipe 38 has a coal feed air valve 37 at its inlet end, and a pulverized coal flow meter 39 at its inlet end side.
Preferably, the fuming furnace comprises: liquid sulfur injection burner 31, liquid sulfur injection burner hole 32, pulverized coal injection burner 40, pulverized coal injection burner hole 41, furnace side liquid slag feed chute 42, furnace top feed port 44, fuming furnace body 45, temperature monitor 46, observation hole 47 and slag tap 54;
The liquid sulfur injection burner 31 and the pulverized coal injection burner 40 are respectively arranged at two sides of the bottom of the fuming furnace body 45 and are fixed through the liquid sulfur injection burner holes 32 and the pulverized coal injection burner holes 41; the pulverized coal injection burner 40 is arranged at a position 100mm high from the bottom of the fuming furnace body 45, and the liquid sulfur injection burner 31 is arranged at a position 100-150 mm high parallel to the upper part of the pulverized coal injection burner 41; the pulverized coal injection burner 40 is connected with the pulverized coal conveying pipeline 38; the liquid sulfur injection burner 31 is connected with the liquid sulfur conveying pipeline 21;
The slag discharging port is arranged at one side of the bottom of the fuming furnace body 45, and the slag discharging port 54 is connected with a slag water quenching system 55;
A furnace side liquid slag feeding chute 42, a temperature monitor 46 and a view port 47 are respectively provided on the side wall of the middle upper portion of the fuming furnace body 45;
The furnace top feed port 44 is arranged at one side of the top of the fuming furnace body 45; a furnace top belt feeding system 43 matched with the furnace top feed inlet 44 is arranged above the furnace top feed inlet;
the fuming furnace body 45 is connected with a waste heat boiler 49, a surface cooler 50 and a bag dust collector 51 in sequence.
The inlet end of the liquid sulfur injection burner 31 is provided with a central pipeline nitrogen pipe 30; the central pipeline nitrogen pipe 30 is communicated with the liquid sulfur injection burner 31;
The inlet end of the central pipe nitrogen pipe 30 is provided with a central pipe nitrogen pressure gauge 33, a central pipe nitrogen flow meter 34 and a central pipe nitrogen valve 35, respectively.
In this embodiment, the apparatus further includes: a flue gas monitor 52, a secondary air valve 48 and a dust unloader 53;
The flue gas monitor 52 is arranged inside a flue gas pipeline 56 of the fuming furnace;
The secondary air valve 48 is arranged on the side wall of the bottom of the waste heat boiler 49;
the dust discharger 53 is provided at the bottom between the waste heat boiler 49 and the surface cooler 50, and is connected to the waste heat boiler 49 and the surface cooler 50.
Example 2
Taking a 4m 2 fuming furnace as an object, processing tin-containing materials with tin content of 5%wt into 25 tons in a single furnace within 6 hours, calculating the sulfur content of the vulcanizing agent to be vulcanized into 25 tons multiplied by 5%wt multiplied by 30% = 0.375 tons according to theory, and taking the excess coefficient to be 5%, namely, the total sulfur content to be 0.375× (1+5%) = 0.394 tons;
For this purpose, about 0.6 ton of outsourced granular sulfur with the particle size of 2.8-6.0 mm and the sulfur content of more than or equal to 99 percent is sent into a granular sulfur storage bin 10, and the granular sulfur is conveyed into a granular sulfur melting heat preservation tank 17 through a granular sulfur conveying belt 12; the infrared heater 25 is opened to heat up and melt the granular sulfur, and the temperature of the liquid sulfur in the granular sulfur melting heat preservation tank 17 is controlled to be 130-150 ℃ for heat preservation; confirming that the liquid sulfur suction pump 16 is arranged at a position 1/3 high from the bottom of the tank body, and always keeping the 2/3 high capacity of the molten liquid sulfur in the granular sulfur melting heat preservation tank 17; maintaining the central pipeline nitrogen delivery valve 30 to be normally open, maintaining the nitrogen delivery pressure at 3Bar, and maintaining the check valve 29 to be closed;
After tin middlings in the fuming furnace are completely melted, namely when the melt temperature is 1150 ℃, keeping nitrogen delivery of a liquid sulfur injection burner 31 smooth, opening a liquid sulfur delivery pipeline check valve 29, starting a liquid sulfur suction pump 16 to inject liquid sulfur into the fuming furnace, starting a feeding head for 10min, starting according to 0t/h, increasing 0.1t/h every 1min, namely after 10min, the feeding speed of the liquid sulfur suction pump 16 reaches 1.0t/h, keeping fine adjustment of the feeding speed within 1.0+/-0.2 t/h, and when the feeding amount (weight) of the liquid sulfur reaches 90% of the calculated amount, namely, the liquid sulfur flowmeter 23 displays that the delivered sulfur is about 0.36 ton, taking a slag sample of the melt in the fuming furnace body 45 through a sampling rod, delivering assay analysis, and carrying out slag water quenching operation after the tin content of slag is less than or equal to 0.2%; if the tin content in the slag is higher than 0.2%, taking a melt slag sample every 1min, then carrying out assay analysis, stopping feeding and spraying of the liquid sulfur suction pump 16 after the tin content in the slag is less than or equal to 0.2%, and immediately opening a slag port 54 for slag discharging water quenching operation;
The pulverized coal in the pulverized coal furnace 36 is uniformly fed into the fuming furnace body 45 by controlling the pulverized coal conveying and blowing system while continuously spraying the liquid sulfur into the fuming furnace through the sulfur spraying burner 31, the pulverized coal feeding speed is kept at 1.3t/h, the conveying air pressure is stabilized at 3Bar, the sulfuration-reduction atmosphere in the fuming furnace is ensured, meanwhile, the monitoring condition of a flue gas monitor 52 at the outlet of a bag dust collector 51 is observed, the flue gas content SO 2 in the sulfur spraying and pulverized coal feeding process is ensured, the concentration of CO is respectively 0.9-1.5%, 7000-10000 ppm, and is lower than or higher than the interval value, the sulfur and the pulverized coal feeding amount are respectively increased and decreased to be fine-adjusted within +/-0.2 t/h, and the concentration of CO can be controlled within the interval value by adjusting the opening of a secondary air valve 48 of an ascending flue of the fuming furnace;
Stopping liquid sulfur feed injection after tin content in melt slag in a fuming furnace body 45 is less than or equal to 0.2%, namely stopping a liquid sulfur suction pump 16, simultaneously starting the power of an infrared heater of a liquid sulfur conveying pipeline to 80%, heating residual sulfur in a melting pipeline, closing a liquid sulfur conveying pipeline check valve 29 after 5min, continuously keeping a normal open state of a central pipeline nitrogen valve 35, respectively increasing or reducing a coal feeding speed of 0.1-0.3 t/h when the temperature in a sulfur conveying pipeline 21 rises to 130-150 ℃ and is constant, opening a purging nitrogen valve 28, keeping the purging nitrogen pressure to be more than or equal to 3Bar, continuously purging for 3-5 min, after residual sulfur in the pipeline is melted and automatically flowing back into a particle sulfur melting insulation tank 17, stopping the infrared heater of the liquid sulfur conveying pipeline, closing the purging nitrogen valve 28, keeping pulverized coal feed conveying into the fuming furnace, adjusting the pulverized coal feeding speed to be 0.5-1.0 t/h, observing the condition of a temperature monitor 46, ensuring that the rising flue temperature of the fuming furnace is 1100-1150 ℃ and is lower than or higher than the temperature range, respectively increasing or reducing the coal feeding speed of 0.1-0.3 t/h until the slag in the fuming furnace stops being completely discharged and the pulverized coal conveying valve is kept to be in a normal open state after the pulverized coal is completely discharged and the pulverized coal is not blown to 37;
After the condition in the fuming furnace body 45 is observed through the observation hole 47 and the complete discharge of slag in the furnace is confirmed, the central pipeline nitrogen valve 35 can be closed, the coal feeding and conveying air valve 37 can be closed, the sulfur injection burner 31 and the pulverized coal injection burner 40 are disassembled for blockage detection and cleaning, the burners are installed back to the original position again, the normal open state of the central pipeline nitrogen valve 35 and the pulverized coal conveying and air valve 37 is maintained again, the conveying air pressure is kept to be more than 3Bar, and the fuming furnace production operation can be started to enter the next period;
The sulfur injection burner 31 and the pulverized coal injection burner 40 are respectively arranged at two sides of the fuming furnace body 45, wherein the pulverized coal injection burner 40 is arranged at a position 100mm away from the bottom of the fuming furnace body 45, and the sulfur injection burner 31 is arranged at a position 100mm away from the upper part of the pulverized coal injection burner 40.
Example 3
Taking an 8m 2 fuming furnace as an object, processing 50 tons of tin-containing materials with the tin content of 5%wt in a single furnace within 6 hours, calculating the sulfur content of the vulcanizing agent to be vulcanized to be 50 tons multiplied by 5%wt multiplied by 30% = 0.75 tons according to theory, and taking the excess coefficient to be 10%, namely, the total sulfur content to be 0.75× (1+10%) = 0.825 tons;
For this purpose, about 1.24 tons of outsourced granular sulfur with the grain diameter of 2.8-6.0 mm and the sulfur content of more than or equal to 99 percent is sent into a granular sulfur storage bin 10, and the granular sulfur is conveyed into a granular sulfur melting heat preservation tank 17 through a granular sulfur conveying belt 12; the infrared heater 25 is opened to heat up and melt the granular sulfur, and the temperature of the liquid sulfur in the granular sulfur melting heat preservation tank 17 is controlled to be 130-150 ℃ for heat preservation; confirming that the liquid sulfur suction pump 16 is arranged at a position 1/3 high from the bottom of the tank body, and always keeping the 2/3 high capacity of the molten liquid sulfur in the granular sulfur melting heat preservation tank 17; maintaining the central pipeline nitrogen delivery valve 30 to be normally open, maintaining the nitrogen delivery pressure at 3Bar, and maintaining the check valve 29 to be closed;
After tin middlings in the fuming furnace are completely melted, namely when the melt temperature is 1150 ℃, keeping nitrogen delivery of a liquid sulfur injection burner 31 smooth, opening a liquid sulfur delivery pipeline check valve 29, starting a liquid sulfur suction pump 16 to inject liquid sulfur into the fuming furnace, starting a feeding head for 10min, starting according to 0t/h, increasing 0.1t/h every 1min, namely after 10min, the feeding speed of the liquid sulfur suction pump 16 reaches 1.0t/h, keeping fine adjustment of the feeding speed within 1.0+/-0.2 t/h, and when the feeding amount (weight) of the liquid sulfur reaches 90% of the calculated amount, namely, the liquid sulfur flowmeter 23 displays that the delivered sulfur is about 0.36 ton, taking a slag sample of the melt in the fuming furnace body 45 through a sampling rod, delivering assay analysis, and carrying out slag water quenching operation after the tin content of slag is less than or equal to 0.2%; if the tin content in the slag is higher than 0.2%, taking a melt slag sample every 1min, then carrying out assay analysis, stopping feeding and spraying of the liquid sulfur suction pump 16 after the tin content in the slag is less than or equal to 0.2%, and immediately opening a slag port 54 for slag discharging water quenching operation;
The pulverized coal in the pulverized coal furnace 36 is uniformly fed into the fuming furnace body 45 by controlling the pulverized coal conveying and blowing system while continuously spraying the liquid sulfur into the fuming furnace through the sulfur spraying burner 31, the pulverized coal feeding speed is kept at 1.3t/h, the conveying air pressure is stabilized at 3Bar, the sulfuration-reduction atmosphere in the fuming furnace is ensured, meanwhile, the monitoring condition of a flue gas monitor 52 at the outlet of a bag dust collector 51 is observed, the flue gas content SO 2 in the sulfur spraying and pulverized coal feeding process is ensured, the concentration of CO is respectively 0.9-1.5%, 7000-10000 ppm, and is lower than or higher than the interval value, the sulfur and the pulverized coal feeding amount are respectively increased and decreased to be fine-adjusted within +/-0.2 t/h, and the concentration of CO can be controlled within the interval value by adjusting the opening of a secondary air valve 48 of an ascending flue of the fuming furnace;
Stopping liquid sulfur feed injection after tin content in melt slag in a fuming furnace body 45 is less than or equal to 0.2%, namely stopping a liquid sulfur suction pump 16, simultaneously starting the power of an infrared heater of a liquid sulfur conveying pipeline to 80%, heating residual sulfur in a melting pipeline, closing a liquid sulfur conveying pipeline check valve 29 after 5min, continuously keeping a normal open state of a central pipeline nitrogen valve 35, respectively increasing or reducing a coal feeding speed of 0.1-0.3 t/h when the temperature in a sulfur conveying pipeline 21 rises to 130-150 ℃ and is constant, opening a purging nitrogen valve 28, keeping the purging nitrogen pressure to be more than or equal to 3Bar, continuously purging for 3-5 min, after residual sulfur in the pipeline is melted and automatically flowing back into a particle sulfur melting insulation tank 17, stopping the infrared heater of the liquid sulfur conveying pipeline, closing the purging nitrogen valve 28, keeping pulverized coal feed conveying into the fuming furnace, adjusting the pulverized coal feeding speed to be 0.5-1.0 t/h, observing the condition of a temperature monitor 46, ensuring that the rising flue temperature of the fuming furnace is 1100-1150 ℃ and is lower than or higher than the temperature range, respectively increasing or reducing the coal feeding speed of 0.1-0.3 t/h until the slag in the fuming furnace stops being completely discharged and the pulverized coal conveying valve is kept to be in a normal open state after the pulverized coal is completely discharged and the pulverized coal is not blown to 37;
After the condition in the fuming furnace body 45 is observed through the observation hole 47 and the complete discharge of slag in the furnace is confirmed, the central pipeline nitrogen valve 35 can be closed, the coal feeding and conveying air valve 37 can be closed, the sulfur injection burner 31 and the pulverized coal injection burner 40 are disassembled for blockage detection and cleaning, the burners are installed back to the original position again, the normal open state of the central pipeline nitrogen valve 35 and the pulverized coal conveying and air valve 37 is maintained again, the conveying air pressure is kept to be more than 3Bar, and the fuming furnace production operation can be started to enter the next period;
The sulfur injection burner 31 and the pulverized coal injection burner 40 are respectively arranged at two sides of the fuming furnace body 45, wherein the pulverized coal injection burner 40 is arranged at a position 100mm away from the bottom of the fuming furnace body 45, and the sulfur injection burner 31 is arranged at a position 100mm away from the upper part of the pulverized coal injection burner 40.
Example 4
Taking a 16m 2 fuming furnace as an object, processing tin-containing materials with the tin content of 11%wt into 100 tons in 6 hours in a single furnace, calculating the sulfur content of the vulcanizing agent to be vulcanized into 100 tons multiplied by 11%wt multiplied by 30% = 3.3 tons according to theory, and taking the excess coefficient as 10%, namely, the total sulfur content is 3.3× (1+10%) = 3.63 tons;
For this purpose, about 5.44 tons of outsourced granular sulfur with the grain diameter of 2.8-6.0 mm and the sulfur content of more than or equal to 99 percent is sent into a granular sulfur storage bin 10, and the granular sulfur is conveyed into a granular sulfur melting heat preservation tank 17 through a granular sulfur conveying belt 12; the infrared heater 25 is opened to heat up and melt the granular sulfur, and the temperature of the liquid sulfur in the granular sulfur melting heat preservation tank 17 is controlled to be 130-150 ℃ for heat preservation; confirming that the liquid sulfur suction pump 16 is arranged at a position 1/3 high from the bottom of the tank body, and always keeping the 2/3 high capacity of the molten liquid sulfur in the granular sulfur melting heat preservation tank 17; maintaining the central pipeline nitrogen delivery valve 30 to be normally open, maintaining the nitrogen delivery pressure at 3Bar, and maintaining the check valve 29 to be closed;
After tin middlings in the fuming furnace are completely melted, namely when the melt temperature is 1150 ℃, keeping nitrogen delivery of a liquid sulfur injection burner 31 smooth, opening a liquid sulfur delivery pipeline check valve 29, starting a liquid sulfur suction pump 16 to inject liquid sulfur into the fuming furnace, starting a feeding head for 10min, starting according to 0t/h, increasing 0.1t/h every 1min, namely after 10min, the feeding speed of the liquid sulfur suction pump 16 reaches 1.0t/h, keeping fine adjustment of the feeding speed within 1.0+/-0.2 t/h, and when the feeding amount (weight) of the liquid sulfur reaches 90% of the calculated amount, namely, the liquid sulfur flowmeter 23 displays that the delivered sulfur is about 0.36 ton, taking a slag sample of the melt in the fuming furnace body 45 through a sampling rod, delivering assay analysis, and carrying out slag water quenching operation after the tin content of slag is less than or equal to 0.2%; if the tin content in the slag is higher than 0.2%, taking a melt slag sample every 1min, then carrying out assay analysis, stopping feeding and spraying of the liquid sulfur suction pump 16 after the tin content in the slag is less than or equal to 0.2%, and immediately opening a slag port 54 for slag discharging water quenching operation;
The pulverized coal in the pulverized coal furnace 36 is uniformly fed into the fuming furnace body 45 by controlling the pulverized coal conveying and blowing system while continuously spraying the liquid sulfur into the fuming furnace through the sulfur spraying burner 31, the pulverized coal feeding speed is kept at 1.3t/h, the conveying air pressure is stabilized at 3Bar, the sulfuration-reduction atmosphere in the fuming furnace is ensured, meanwhile, the monitoring condition of a flue gas monitor 52 at the outlet of a bag dust collector 51 is observed, the flue gas content SO 2 in the sulfur spraying and pulverized coal feeding process is ensured, the concentration of CO is respectively 0.9-1.5%, 7000-10000 ppm, and is lower than or higher than the interval value, the sulfur and the pulverized coal feeding amount are respectively increased and decreased to be fine-adjusted within +/-0.2 t/h, and the concentration of CO can be controlled within the interval value by adjusting the opening of a secondary air valve 48 of an ascending flue of the fuming furnace;
Stopping liquid sulfur feed injection after tin content in melt slag in a fuming furnace body 45 is less than or equal to 0.2%, namely stopping a liquid sulfur suction pump 16, simultaneously starting the power of an infrared heater of a liquid sulfur conveying pipeline to 80%, heating residual sulfur in a melting pipeline, closing a liquid sulfur conveying pipeline check valve 29 after 5min, continuously keeping a normal open state of a central pipeline nitrogen valve 35, respectively increasing or reducing a coal feeding speed of 0.1-0.3 t/h when the temperature in a sulfur conveying pipeline 21 rises to 130-150 ℃ and is constant, opening a purging nitrogen valve 28, keeping the purging nitrogen pressure to be more than or equal to 3Bar, continuously purging for 3-5 min, after residual sulfur in the pipeline is melted and automatically flowing back into a particle sulfur melting insulation tank 17, stopping the infrared heater of the liquid sulfur conveying pipeline, closing the purging nitrogen valve 28, keeping pulverized coal feed conveying into the fuming furnace, adjusting the pulverized coal feeding speed to be 0.5-1.0 t/h, observing the condition of a temperature monitor 46, ensuring that the rising flue temperature of the fuming furnace is 1100-1150 ℃ and is lower than or higher than the temperature range, respectively increasing or reducing the coal feeding speed of 0.1-0.3 t/h until the slag in the fuming furnace stops being completely discharged and the pulverized coal conveying valve is kept to be in a normal open state after the pulverized coal is completely discharged and the pulverized coal is not blown to 37;
After the condition in the fuming furnace body 45 is observed through the observation hole 47 and the complete discharge of slag in the furnace is confirmed, the central pipeline nitrogen valve 35 can be closed, the coal feeding and conveying air valve 37 can be closed, the sulfur injection burner 31 and the pulverized coal injection burner 40 are disassembled for blockage detection and cleaning, the burners are installed back to the original position again, the normal open state of the central pipeline nitrogen valve 35 and the pulverized coal conveying and air valve 37 is maintained again, the conveying air pressure is kept to be more than 3Bar, and the fuming furnace production operation can be started to enter the next period;
The sulfur injection burner 31 and the pulverized coal injection burner 40 are respectively arranged at two sides of the fuming furnace body 45, wherein the pulverized coal injection burner 40 is arranged at a position 100mm away from the bottom of the fuming furnace body 45, and the sulfur injection burner 31 is arranged at a position 100mm away from the upper part of the pulverized coal injection burner 40.
Comparative example 1
Taking a fuming furnace of 4m 2 as an object, other condition factors are unchanged, namely taking pyrite with the sulfur content of about 35 percent as an example, wherein the pyrite also contains 50 percent of iron, the water content reaches 10 percent, and the surplus coefficient is 5 percent, namely the total sulfur content is 0.394 ton, so that the amount of pyrite is required to be 0.394/35 percent=1.13 ton;
The pyrite is conveyed into a melting pool of the fuming furnace through a furnace top belt to participate in vulcanization-reduction reaction, after 1.13 tons of pyrite is completely put into the furnace, the fuming volatilization operation of the fuming furnace is continuously kept for 10 minutes, sampling is carried out for analysis, the tin content of slag reaches 0.5 percent by weight, the fuming effect is poor, 0.07 tons of pyrite is continuously put into the fuming furnace for fuming volatilization, the tin content of the slag can be ensured to be less than 0.2 percent, the slag is discharged from a slag opening for water quenching, the smell of 'stinky eggs' can be smelled in water vapor after water quenching, obviously, the use amount of pyrite exceeds a theoretical value, the reaction is insufficient, and more waste is caused. In addition, in the vulcanization-reduction process, about 0.3 ton of 96% grade quartz sand is supplemented according to the slag-forming reaction (3), so that the operation load and the cost of the fuming furnace are increased.
Comparative example 2
Taking an 8m 2 fuming furnace as an object, other condition factors are unchanged, namely taking pyrite with the sulfur content of about 35 percent as an example, wherein the pyrite also contains 50 percent of iron, the water content reaches 10 percent, and the surplus coefficient is 10 percent, namely the total sulfur content is 0.825 ton, so that the amount of pyrite is required to be 0.825/35 percent=2.36 tons;
The pyrite is conveyed into a melting pool of the fuming furnace through a furnace top belt to participate in vulcanization-reduction reaction, after 2.36 tons of pyrite is completely put into the furnace, the fuming volatilization operation of the fuming furnace is continuously kept for 10 minutes, sampling is carried out for analysis, the tin content of slag reaches 0.48 percent by weight, the fuming effect is poor, 0.15 ton of pyrite is continuously put into the fuming furnace for fuming volatilization, the tin content of the slag can be ensured to be less than 0.2 percent, the slag is discharged from a slag opening for water quenching, the smell of 'stinky eggs' can be smelled in water vapor after water quenching, obviously, the use amount of pyrite exceeds a theoretical value, the reaction is insufficient, and more waste is caused. In addition, in the vulcanization-reduction process, about 0.6 ton of 96% grade quartz sand is supplemented according to the slag-forming reaction (3), so that the operation load and the cost of the fuming furnace are increased.
Comparative example 3
Taking a 16m 2 fuming furnace as an object, other condition factors are unchanged, namely taking pyrite with the sulfur content of about 35 percent as an example, wherein the pyrite also contains 50 percent of iron, the water content reaches 10 percent, and the surplus coefficient is 10 percent, namely the total sulfur content is 3.63 tons, so that the amount of pyrite is required to be 3.63/35 percent=10.4 tons;
The pyrite is conveyed into a melting pool of the fuming furnace through a furnace top belt to participate in vulcanization-reduction reaction, after 10.4 tons of pyrite is completely put into the furnace, the fuming volatilization operation of the fuming furnace is continuously kept for 10 minutes, sampling is carried out for analysis, the tin content of slag reaches 0.7% wt, the fuming effect is poor, 0.47 tons of pyrite is continuously put into the fuming furnace for fuming volatilization, the tin content of the slag can be ensured to be less than 0.2%, a slag opening is used for discharging the slag for water quenching, the smell of 'stinky eggs' can be smelled in water vapor after water quenching, and obviously, the use amount of pyrite exceeds a theoretical value, the reaction is insufficient, and more waste is caused. In addition, in the vulcanization-reduction process, about 2.89 tons of 96 percent grade quartz sand is supplemented according to the slag-forming reaction (3), so that the operation load and the cost of the fuming furnace are increased.
In the present specification, each embodiment is described in a progressive manner, and each embodiment is mainly described in a different point from other embodiments, and identical and similar parts between the embodiments are all enough to refer to each other. For the device disclosed in the embodiment, since it corresponds to the method disclosed in the embodiment, the description is relatively simple, and the relevant points refer to the description of the method section.
The previous description of the disclosed embodiments is provided to enable any person skilled in the art to make or use the present utility model. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the utility model. Thus, the present utility model is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (8)
1. The utility model provides a device that liquid sulphur directly sprays into fuming furnace and vulcanizes volatilize which characterized in that includes:
The device comprises a granular sulfur screening and belt conveying system, a granular sulfur melting heat preservation tank, a liquid sulfur suction pump, a liquid sulfur conveying pipeline, a pulverized coal conveying and blowing system, a fuming furnace, a slag water quenching system, a waste heat boiler, a surface cooler, a bag dust collector and a fuming furnace flue gas pipeline;
The granular sulfur screening and belt conveying system is arranged on one side above the granular sulfur melting heat preservation tank;
The liquid sulfur suction pump is connected with the granular sulfur melting heat preservation tank and vertically penetrates into the granular sulfur melting heat preservation tank;
The liquid sulfur suction pump, the liquid sulfur conveying pipeline, the fuming furnace, the waste heat boiler, the surface cooler, the bag dust collector and the fuming furnace flue gas pipeline are connected in sequence;
The pulverized coal conveying and blowing system and the slag water quenching system are respectively connected with the fuming furnace.
2. The device for direct injection of liquid sulfur into a fuming furnace for sulfidization volatilization as recited in claim 1, wherein said particulate sulfur screening and belt conveyor system comprises:
The device comprises a particle sulfur conical hopper, a conical hopper vibrator, a primary screen, a secondary screen, a conical hopper blanking valve, an intermediate bin vibrator, an intermediate bin blanking valve, a differential weighing device, a particle sulfur storage bin, a storage bin blanking valve and a particle sulfur conveying belt;
The primary screen, the granular sulfur conical hopper, the secondary screen, the conical hopper blanking valve, the middle bin blanking valve, the differential weighing device, the granular sulfur storage bin and the storage bin blanking valve are sequentially connected from top to bottom;
The conical hopper vibrator is arranged on the side wall of the particle sulfur conical hopper; the intermediate bin vibrator is arranged on the side wall of the intermediate bin;
the feeding end of the granular sulfur conveying belt is arranged at the lower side of the discharging valve of the storage bin, and the discharging end of the granular sulfur conveying belt is arranged at one side above the granular sulfur melting heat preservation tank.
3. The device for directly injecting liquid sulfur into fuming furnace for vulcanization volatilization according to claim 2, wherein the granular sulfur melting heat preservation tank is provided with a heat preservation tank thermometer, a liquid level meter, an infrared heating melter and a discharging hopper;
Wherein, the heat preservation tank thermometer and the liquid level meter are arranged above the granular sulfur melting heat preservation tank and penetrate into the granular sulfur melting heat preservation tank; the infrared heating melter is arranged in the wall body around the particle sulfur melting heat-preserving tank; the discharging hopper is arranged on one side above the granular sulfur melting heat preservation tank; the discharge end of the granular sulfur conveying belt is arranged above the discharging hopper;
the bottom of the liquid sulfur suction pump is provided with a suction pump filter screen.
4. The device for directly injecting liquid sulfur into a fuming furnace for vulcanization volatilization according to claim 3, wherein the outlet end of the liquid sulfur delivery pipeline is of an inverted V-shaped structure; the liquid sulfur conveying pipeline is provided with a liquid sulfur flowmeter, a conveying pipeline pressure gauge, an infrared heater, a nitrogen purging pipe, a check valve and a thermometer;
the infrared heater is arranged in the pipe wall of the liquid sulfur conveying pipeline;
the thermometer and the liquid sulfur flowmeter are arranged on the side wall of one side of the inlet end of the liquid sulfur conveying pipeline;
the conveying pipeline manometer is arranged in a pipeline at one side of the inlet end of the liquid sulfur conveying pipeline;
The nitrogen purging pipe is arranged at the top of the inverted V-shaped structure at the outlet end of the liquid sulfur conveying pipeline; a nitrogen purging pressure gauge and a nitrogen purging valve are arranged in the nitrogen purging pipe;
The check valve is arranged on one side of the outlet end of the liquid sulfur conveying pipeline.
5. The device for directly injecting liquid sulfur into fuming furnace for sulfuration volatilization according to claim 4, wherein said pulverized coal conveying and injecting system comprises a pulverized coal tank and a pulverized coal conveying pipeline;
The pulverized coal tank is connected with the fuming furnace through a pulverized coal conveying pipeline;
the inlet end of the pulverized coal conveying pipeline is provided with a coal feeding conveying air valve, and one side of the inlet end is provided with a pulverized coal conveying flowmeter.
6. The apparatus for direct injection of liquid sulfur into a fuming furnace for sulfiding volatilization as recited in claim 5, wherein said fuming furnace comprises: the device comprises a liquid sulfur injection burner, a pulverized coal injection burner, a furnace side liquid slag feeding chute, a furnace top feeding port, a fuming furnace body, a temperature monitor, an observation hole and a slag discharging port;
The liquid sulfur injection burner and the pulverized coal injection burner are respectively arranged at two sides of the bottom of the fuming furnace body; the pulverized coal injection burner is arranged at a position 100mm high from the bottom of the fuming furnace body, and the liquid sulfur injection burner is arranged at a position 100-150 mm high parallel to the upper part of the pulverized coal injection burner; the pulverized coal injection burner is connected with the pulverized coal conveying pipeline; the liquid sulfur injection burner is connected with the liquid sulfur conveying pipeline;
The slag discharge port is arranged at one side of the bottom of the fuming furnace body and is connected with the slag water quenching system;
The furnace side liquid slag feeding chute, the temperature monitor and the observation hole are respectively arranged on the side wall of the upper part of the fuming furnace body;
The furnace top feed inlet is arranged at one side of the top of the fuming furnace body; a furnace top belt feeding system matched with the furnace top feeding hole is arranged above the furnace top feeding hole;
The fuming furnace body is connected with the waste heat boiler, the surface cooler and the bag dust collector in sequence.
7. The device for directly injecting liquid sulfur into a fuming furnace for vulcanization volatilization as recited in claim 6, wherein a central pipeline nitrogen pipe is arranged at the inlet end of the liquid sulfur injection burner; the central pipeline nitrogen pipe is communicated with the liquid sulfur injection burner;
The inlet end of the central pipeline nitrogen pipe is respectively provided with a central pipeline nitrogen pressure gauge, a central pipeline nitrogen flowmeter and a central pipeline nitrogen valve.
8. The apparatus for direct injection of liquid sulfur into a fuming furnace for sulfidization vaporization of sulfur of claim 7, further comprising: a flue gas monitor, a secondary air valve and a dust remover;
the smoke monitor is arranged in the smoke pipeline of the fuming furnace;
the secondary air valve is arranged on the side wall of the bottom of the waste heat boiler;
The dust remover is arranged at the bottom between the waste heat boiler and the surface cooler and is connected with the waste heat boiler and the surface cooler.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322824487.2U CN220959673U (en) | 2023-10-20 | 2023-10-20 | Device for directly spraying liquid sulfur into fuming furnace for vulcanization and volatilization |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202322824487.2U CN220959673U (en) | 2023-10-20 | 2023-10-20 | Device for directly spraying liquid sulfur into fuming furnace for vulcanization and volatilization |
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| CN220959673U true CN220959673U (en) | 2024-05-14 |
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| CN202322824487.2U Active CN220959673U (en) | 2023-10-20 | 2023-10-20 | Device for directly spraying liquid sulfur into fuming furnace for vulcanization and volatilization |
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2023
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