CN105349772A - Device and method for reducing magnesium oxide content for concentrate desulfurization - Google Patents
Device and method for reducing magnesium oxide content for concentrate desulfurization Download PDFInfo
- Publication number
- CN105349772A CN105349772A CN201510816762.3A CN201510816762A CN105349772A CN 105349772 A CN105349772 A CN 105349772A CN 201510816762 A CN201510816762 A CN 201510816762A CN 105349772 A CN105349772 A CN 105349772A
- Authority
- CN
- China
- Prior art keywords
- caustic soda
- concentrate
- liquid caustic
- sulfur dioxide
- sloptank
- Prior art date
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- Granted
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- 239000012141 concentrate Substances 0.000 title claims abstract description 104
- CPLXHLVBOLITMK-UHFFFAOYSA-N magnesium oxide Inorganic materials [Mg]=O CPLXHLVBOLITMK-UHFFFAOYSA-N 0.000 title claims abstract description 63
- 239000000395 magnesium oxide Substances 0.000 title claims abstract description 34
- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 25
- 230000023556 desulfurization Effects 0.000 title claims abstract description 22
- 238000000034 method Methods 0.000 title claims abstract description 20
- AXZKOIWUVFPNLO-UHFFFAOYSA-N magnesium;oxygen(2-) Chemical compound [O-2].[Mg+2] AXZKOIWUVFPNLO-UHFFFAOYSA-N 0.000 title abstract description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 261
- 239000007788 liquid Substances 0.000 claims abstract description 112
- RAHZWNYVWXNFOC-UHFFFAOYSA-N Sulphur dioxide Chemical compound O=S=O RAHZWNYVWXNFOC-UHFFFAOYSA-N 0.000 claims abstract description 96
- 238000010521 absorption reaction Methods 0.000 claims abstract description 56
- 239000002562 thickening agent Substances 0.000 claims abstract description 34
- 238000003723 Smelting Methods 0.000 claims abstract description 29
- 239000006228 supernatant Substances 0.000 claims abstract description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000009826 distribution Methods 0.000 claims abstract description 16
- 235000011121 sodium hydroxide Nutrition 0.000 claims description 84
- 239000002002 slurry Substances 0.000 claims description 70
- 239000003546 flue gas Substances 0.000 claims description 46
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 44
- 239000007921 spray Substances 0.000 claims description 22
- 239000007789 gas Substances 0.000 claims description 13
- 238000013022 venting Methods 0.000 claims description 12
- 238000005272 metallurgy Methods 0.000 claims description 10
- 239000002994 raw material Substances 0.000 claims description 9
- 230000008676 import Effects 0.000 claims description 6
- 230000002411 adverse Effects 0.000 claims description 3
- 230000002950 deficient Effects 0.000 claims description 3
- FYYHWMGAXLPEAU-UHFFFAOYSA-N Magnesium Chemical compound [Mg] FYYHWMGAXLPEAU-UHFFFAOYSA-N 0.000 abstract description 2
- 239000003513 alkali Substances 0.000 abstract description 2
- 239000011777 magnesium Substances 0.000 abstract description 2
- 229910052749 magnesium Inorganic materials 0.000 abstract description 2
- 239000000779 smoke Substances 0.000 abstract 2
- 239000003795 chemical substances by application Substances 0.000 abstract 1
- 230000003009 desulfurizing effect Effects 0.000 abstract 1
- 230000001502 supplementing effect Effects 0.000 abstract 1
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 8
- 229910052759 nickel Inorganic materials 0.000 description 4
- 239000002893 slag Substances 0.000 description 4
- 241001062472 Stokellia anisodon Species 0.000 description 2
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 2
- 235000003599 food sweetener Nutrition 0.000 description 2
- 238000005065 mining Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002910 solid waste Substances 0.000 description 2
- 239000003765 sweetening agent Substances 0.000 description 2
- 235000008733 Citrus aurantifolia Nutrition 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 235000011941 Tilia x europaea Nutrition 0.000 description 1
- 238000006701 autoxidation reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000002608 ionic liquid Substances 0.000 description 1
- 239000004571 lime Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
- C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
- C22B1/00—Preliminary treatment of ores or scrap
- C22B1/11—Removing sulfur, phosphorus or arsenic other than by roasting
Landscapes
- Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Manufacturing & Machinery (AREA)
- Geochemistry & Mineralogy (AREA)
- Geology (AREA)
- General Life Sciences & Earth Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Materials Engineering (AREA)
- Mechanical Engineering (AREA)
- Metallurgy (AREA)
- Organic Chemistry (AREA)
- Treating Waste Gases (AREA)
- Gas Separation By Absorption (AREA)
Abstract
The invention discloses a device and method for reducing the magnesium oxide content for concentrate desulfuration. The device mainly comprises a concentrate pulp underground groove, an post-absorption concentrate pulp underground groove, a desulfurization tower, a sodium hydroxide security absorbing tower, an alkali distribution tank, a thickener, a thick pulp underground groove and a clean liquid pH adjusting groove. Concentrate pulp selected through beneficiation serves as a desulfurizing agent for absorbing sulfur dioxide in smoke; the content of the sulfur dioxide is detected after absorbing; the sulfur dioxide is exhausted after being detected to be qualified; if the sulfur dioxide is detected not to be qualified, the concentrate pulp absorbs sulfur dioxide continuously through sodium hydroxide in the sodium hydroxide security absorbing tower, and then the sulfur dioxide is exhausted; and meanwhile the pulp absorbing low-concentration sulfur dioxide is thickened to be supernatant liquid and thick pulp through the thickener, the thick pulp is discharged into the thick pulp underground groove, the pH value of the supernatant liquid is adjusted, and the supernatant liquid is conveyed to a beneficiation system after meeting the requirement for beneficiation and water distribution to serve as distributed water to be reused. According to the device and method for reducing the magnesium oxide content for concentrate desulfuration, sulfur dioxide in smelting smoke in low-concentration sulfur dioxide can be effectively removed, the content of oxide magnesium of concentrate is reduced, and the water supplementing content of the beneficiation system is reduced.
Description
Technical field
The invention belongs to smelting, chemical field, be specifically related to the device and method that a kind of concentrate desulfurization reduces content of magnesia.
Background technology
In the smelting process of sulphide ores, smelt the height of the content of magnesia in nickel ore concentrate, pyrometallurgical smelting slag making is had a significant impact, content of magnesia is high, and slag melting point can be caused to increase, and energy consumption increases, and be unfavorable for that slag nickel is separated, cause the nickeliferous rising of slag, therefore adopt effective ways to reduce Magnesia Content of Nickel Concentrate, the index request to Magnesia Content of Nickel Concentrate can be relaxed.
In the smelting process of sulphide ores, usually can produce a large amount of containing SO
2flue gas during smelting, serious pollution is caused to surrounding enviroment, low concentration SO
2flue gas during smelting has large-minded, SO
2concentration is low, and the feature such as fluctuate larger, the environmental protection gas collection mainly in smelt production, and current traditional treatment method is relatively more extensive, comprises lime method, ionic liquid method, activated coke method, alkali absorb method etc., technical maturity.But because flue gas during smelting amount is large, desired raw material amount is large, and processing cost is higher, and produce new solid waste in treating processes, liquid gives up.
Summary of the invention
The object of the invention is to solve the technical problem existed in prior art, provide a kind of energy scrubbing CO_2 and can reduce content of magnesia in concentrate, the concentrate desulfurization that desulfuration efficiency is high, cost is low reduces the device of content of magnesia.
Another object of the present invention is a kind of method in order to provide concentrate desulfurization to reduce content of magnesia.
In order to achieve the above object, the present invention is by the following technical solutions: a kind of concentrate desulfurization reduces the device of content of magnesia, comprise concentrate slurry sloptank, concentrate slurry sloptank after absorbing, thionizer, liquid caustic soda security personnel absorption tower, alkali-prepared tank, thickener, underflow sloptank and clear liquid pH regulator groove, described concentrate slurry sloptank is connected with the concentrate slurry entrance being positioned at thionizer bottom, the bottom of described thionizer is also connected with the top spray equipment in thionizer by recycle pump, the concentrate slurry outlet of described thionizer is connected with concentrate slurry sloptank after absorption, after described absorption, concentrate slurry sloptank is also connected with thickener, the bottom of described thickener is connected with underflow sloptank, the top of described thickener is connected with clear liquid pH regulator groove, the middle part of described thionizer is provided with the import of low-concentration sulfur dioxide flue gas during smelting, the lower entrances on the top of described thionizer is provided with venting port and venting port is ensured public security with exhaust emission pipeline and liquid caustic soda respectively absorption tower is connected, the lower entrances on described liquid caustic soda security personnel absorption tower and exhaust emission pipeline are respectively equipped with chain trip valve, described chain trip valve is connected with the outlet sulfur dioxide concentration detector being arranged on exhaust ports, the bottom on described liquid caustic soda security personnel absorption tower is also connected with the top liquid caustic soda spray equipment that liquid caustic soda is ensured public security in absorption tower by liquid caustic soda recycle pump, described liquid caustic soda security personnel absorption tower is connected with alkali-prepared tank, the top on described liquid caustic soda security personnel absorption tower is connected with exhaust emission pipeline, described exhaust emission pipeline is connected with blower fan.
Further, described low-concentration sulfur dioxide flue gas during smelting ingress is provided with entrance sulfur dioxide concentration detector.
Further, whipping appts is provided with in described clear liquid pH regulator groove.
Further, the pipeline that the bottom of described thickener is connected with underflow sloptank is provided with underflow valve.
Further, described alkali-prepared tank be provided with concentration be 30% liquid caustic soda add entrance and water distribution adds entrance.
Further, described clear liquid pH regulator groove is provided with concentration is that the liquid caustic soda of 9-11% adds entrance.
Further, described underflow sloptank is connected with raw materials for metallurgy storehouse by slush pump.
Further, after described absorption, concentrate slurry sloptank is connected with thickener by pump.
Further, described recycle pump and liquid caustic soda recycle pump are respectively two groups.
Concentrate desulfurization reduces a method for content of magnesia, and the method comprises the following steps:
After A, concentrate slurry ore dressing selected are delivered to concentrate slurry sloptank, concentrate slurry is delivered to thionizer by concentrate slurry entrance;
B, ON cycle pump, top spray equipment concentrate slurry is delivered in thionizer by recycle pump spray and under, sulfurous gas in flue gas absorbs with low-concentration sulfur dioxide flue gas during smelting counter current contact from bottom to top from thionizer, the basic activated component in concentrate slurry by concentrate slurry;
C, be delivered to when the concentrate slurry pH value after absorbing reaches 6.0-7.0 absorb after concentrate slurry sloptank, and through pump delivery in thickener, after thickener is dense, open underflow valve, underflow enters underflow sloptank, and is delivered in raw materials for metallurgy storehouse through slush pump;
Supernatant liquor after D, thickener are dense flows in clear liquid pH regulator groove, by adding the pH value that concentration is the liquid caustic soda adjustment supernatant liquor of 9-11% in clear liquid pH regulator groove, stirred by whipping appts, the pH value of supernatant liquor reaches ore dressing water distribution and requires rear as ore-sorting system water distribution reuse;
E, by outlet sulfur dioxide concentration detector, the sulfur dioxide concentration in the low-concentration sulfur dioxide flue gas during smelting of exhaust ports after concentrate slurry absorbs to be detected, detect qualified after, chain trip valve opens to the pipeline of exhaust emission pipeline, and flue gas is directly discharged from exhaust emission pipeline;
F, liquid caustic soda in prior alkali-prepared tank enters in liquid caustic soda security personnel absorption tower, when detecting defective, chain trip valve is cut to the pipeline of exhaust emission pipeline, open to the pipeline of liquid caustic soda security personnel absorption tower lower entrances, flue gas enters in liquid caustic soda security personnel absorption tower by the lower entrances on liquid caustic soda security personnel absorption tower, liquid caustic soda simultaneously in alkali-prepared tank enters in liquid caustic soda security personnel absorption tower, open liquid caustic soda recycle pump, liquid caustic soda from liquid caustic soda spray equipment spray and, with ensure public security absorption tower from liquid caustic soda in flue gas adverse current from bottom to top contact and continue to absorb the sulfurous gas in flue gas, flue gas after absorbing by liquid caustic soda is discharged from exhaust emission pipeline through the top on liquid caustic soda security personnel absorption tower.
Hinge structure of the present invention has following beneficial effect: concentrate desulfurization of the present invention reduces the device of content of magnesia, comprise concentrate slurry sloptank, absorb rear concentrate slurry sloptank, thionizer, liquid caustic soda ensure public security absorption tower, alkali-prepared tank, thickener, underflow sloptank and clear liquid pH regulator groove, its concentrate slurry ore dressing selected is delivered to as sweetening agent in thionizer, and concentrate slurry contains a certain amount of MgO, CaO, Al
2o
3, Fe
2o
3in basic oxide (being mainly MgO), instead of traditional sweetening agent, the basic oxide in concentrate slurry (being mainly MgO) are utilized to absorb sour gas sulfurous gas in low-concentration sulfur dioxide flue gas during smelting, after absorption, the content of sulfur dioxide in flue gas is detected, detect qualified rear discharge, if detect defective, discharge again after continuing to absorb the sulfurous gas in flue gas by the liquid caustic soda in liquid caustic soda security personnel absorption tower, simultaneously, the dense one-tenth supernatant liquor of ore pulp and underflow two portions of low-concentration sulfur dioxide will be absorbed by thickener, be delivered in raw materials for metallurgy storehouse through slush pump after underflow enters underflow sloptank, supernatant liquor regulates the pH value of supernatant liquor by adding liquid caustic soda, after meeting ore dressing water distribution requirement, supernatant liquor is delivered to ore-sorting system as water distribution reuse.The present invention can effectively by the sulfur dioxide removal in low-concentration sulfur dioxide flue gas during smelting, and reduce the content of concentrate autoxidation magnesium, achieve the comprehensive utilization of waste water, decrease ore-sorting system rate of water make-up, sweetening effectiveness is obvious, while guaranteeing flue gas qualified discharge, can significantly reduce traditional doctor solution consumption, reduce system operation cost, avoid the discharge that solid waste new in sweetening process, liquid are useless, finally achieve lower concentration flue gas during smelting sulfur dioxide treatment and the object reducing concentrate content of magnesia.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention.
Reference numeral implication of the present invention is as follows: 1, concentrate slurry sloptank; 2, concentrate slurry sloptank after absorbing; 3, recycle pump; 4, thionizer; 5, liquid caustic soda recycle pump; 6, blower fan; 7, alkali-prepared tank; 8, liquid caustic soda security personnel absorption tower; 9, chain trip valve; 10, sulfur dioxide concentration detector is exported; 11, entrance sulfur dioxide concentration detector; 12, underflow sloptank; 13, clear liquid pH regulator groove; 14, thickener; 15, top spray equipment; 16, low-concentration sulfur dioxide flue gas during smelting import; 17, venting port; 18, exhaust emission pipeline; 19, top liquid caustic soda spray equipment; 20, whipping appts; 21, underflow valve; 22, concentration be 30% liquid caustic soda add entrance; 23, water distribution adds entrance; 24, concentration is that the liquid caustic soda of 9-11% adds entrance.
Embodiment
Below in conjunction with the drawings and specific embodiments, the invention will be further described.
Embodiment 1
As shown in Figure 1, a kind of concentrate desulfurization reduces the device of content of magnesia, comprise concentrate slurry sloptank 1, concentrate slurry sloptank 2 after absorbing, thionizer 4, liquid caustic soda security personnel absorption tower 8, alkali-prepared tank 7, thickener 14, underflow sloptank 12 and clear liquid pH regulator groove 13, concentrate slurry sloptank 1 is connected with the concentrate slurry entrance being positioned at thionizer 4 bottom, the bottom of thionizer 4 is also connected with the top spray equipment 15 in thionizer 4 by two groups of recycle pumps 3, the concentrate slurry outlet of thionizer 4 is connected with concentrate slurry sloptank 2 after absorption, after absorbing, concentrate slurry sloptank 2 is also connected with thickener 14 by pump, the bottom of thickener 14 is connected with underflow sloptank 12, underflow sloptank 12 is connected with raw materials for metallurgy storehouse by slush pump, the pipeline that the bottom of thickener 14 is connected with underflow sloptank 12 is provided with underflow valve 21, the top of thickener 14 is connected with clear liquid pH regulator groove 13, it is that the liquid caustic soda of 9-11% adds entrance 24 that clear liquid pH regulator groove 13 is provided with concentration, whipping appts 20 is provided with in clear liquid pH regulator groove 13, the middle part of thionizer 4 is provided with low-concentration sulfur dioxide flue gas during smelting import 16, low-concentration sulfur dioxide flue gas during smelting import 16 place is provided with entrance sulfur dioxide concentration detector 11, the lower entrances on the top of thionizer 4 is provided with venting port 17 and venting port 17 is ensured public security with exhaust emission pipeline 18 and liquid caustic soda respectively absorption tower 8 is connected, the lower entrances on liquid caustic soda security personnel absorption tower 8 and exhaust emission pipeline 18 are respectively equipped with chain trip valve 9, chain trip valve 9 is connected with the outlet sulfur dioxide concentration detector 10 being arranged on venting port 17 place, the top liquid caustic soda spray equipment 19 also ensured public security in absorption tower 8 by two groups of liquid caustic soda recycle pumps 5 and liquid caustic soda in the bottom on liquid caustic soda security personnel absorption tower 8 is connected, liquid caustic soda security personnel absorption tower 8 is connected with alkali-prepared tank 7, alkali-prepared tank 7 be provided with concentration be 30% liquid caustic soda add entrance 22 and water distribution adds entrance 23, the top on liquid caustic soda security personnel absorption tower 8 is connected with exhaust emission pipeline 18, exhaust emission pipeline 18 is connected with blower fan 6.
The device above-mentioned concentrate desulfurization being reduced content of magnesia is used in certain mining and metallurgy refining unit normal productive process, specifically comprise the following steps: after the concentrate slurry (solid content is 20%, and pH value is 9.5) ore dressing selected is delivered to concentrate slurry sloptank 1, concentrate slurry is delivered to thionizer 4 by concentrate slurry entrance; ON cycle pump 3, by recycle pump 3 by concentrate slurry the top spray equipment 15 be delivered in thionizer 4 spray and under, concentrate slurry and low-concentration sulfur dioxide flue gas during smelting (sulfur dioxide concentration: 266mg/Nm from bottom to top from thionizer 4
3-2076mg/Nm
3, mean concns is 1314mg/Nm
3, exhaust gas volumn: 61423Nm
3/ h-91156Nm
3/ h, average tolerance is 70000Nm
3/ h) counter current contact, the sulfurous gas in flue gas absorbs by the basic activated component in concentrate slurry; (pH value is 6.4 to concentrate slurry after absorption, magnesium oxide mass percentage is less than 6.5%, meet pyrometallurgical smelting requirement) be delivered to the rear concentrate slurry sloptank 2 of absorption, and through pump delivery in thickener 14, after thickener 14 is dense, open underflow valve 21, underflow enters underflow sloptank 12, and is delivered in raw materials for metallurgy storehouse through slush pump; Supernatant liquor after thickener 14 is dense flows in clear liquid pH regulator groove 13, by adding the pH value that concentration is the liquid caustic soda adjustment supernatant liquor of 10.5% in clear liquid pH regulator groove 13, stirred by whipping appts 20, the pH value of supernatant liquor reaches ore dressing water distribution and requires rear as ore-sorting system water distribution reuse; Detected by the sulfur dioxide concentration exported in the low-concentration sulfur dioxide flue gas during smelting of sulfur dioxide concentration detector 10 pairs of venting port 17 places after concentrate slurry absorbs, detected result is SO
2concentration remains on 100mg/Nm substantially
3below, meet qualified discharge standard, chain trip valve 9 opens to the pipeline of exhaust emission pipeline 18, and flue gas is directly discharged from exhaust emission pipeline 18.
Embodiment 2
The concentrate desulfurization of the present embodiment reduces the device of content of magnesia with embodiment 1, use it for that the fluctuation of certain mining and metallurgy refining unit flue gas during smelting is comparatively large, sulfurous gas exceeds in the situation of concentration for the treatment of, specifically comprise the following steps: after the concentrate slurry (solid content is 20%, and pH value is 9.64) ore dressing selected is delivered to concentrate slurry sloptank 1, concentrate slurry is delivered to thionizer 4 by concentrate slurry entrance, ON cycle pump 3, by recycle pump 3 by concentrate slurry the top spray equipment 15 be delivered in thionizer 4 spray and under, concentrate slurry and low-concentration sulfur dioxide flue gas during smelting (sulfur dioxide concentration: 1682mg/Nm from bottom to top from thionizer 4
3-7859mg/Nm
3, mean concns: 3803mg/Nm
3, exhaust gas volumn: 51834Nm
3/ h-85692Nm
3/ h, average tolerance: 69523Nm
3/ h) counter current contact, the sulfurous gas in flue gas absorbs by the basic activated component in concentrate slurry, (pH value is 6.0 to concentrate slurry after absorption, magnesium oxide mass percentage is less than 6.5%, meet pyrometallurgical smelting requirement) be delivered to the rear concentrate slurry sloptank 2 of absorption, and through pump delivery in thickener 14, after thickener 14 is dense, open underflow valve 21, underflow enters underflow sloptank 12, and is delivered in raw materials for metallurgy storehouse through slush pump, supernatant liquor after thickener 14 is dense flows in clear liquid pH regulator groove 13, by adding the pH value that concentration is the liquid caustic soda adjustment supernatant liquor of 10.5% in clear liquid pH regulator groove 13, stirred by whipping appts 20, the pH value of supernatant liquor reaches ore dressing water distribution and requires rear as ore-sorting system water distribution reuse, by exporting the low-concentration sulfur dioxide flue gas during smelting of sulfur dioxide concentration detector 10 pairs of venting port 17 places after concentrate slurry absorbs, (flue gas concentration is more than 3500mg/Nm
3) in sulfur dioxide concentration detect, detected result is SO
2concentration is more than 400mg/Nm
3below, do not meet qualified discharge standard, chain trip valve 9 is cut to the pipeline of exhaust emission pipeline 18, open to the pipeline of liquid caustic soda security personnel absorption tower 8 lower entrances, it (is that the liquid caustic soda pump delivery of 32% is to alkali-prepared tank 7 by concentration in advance that flue gas enters in liquid caustic soda security personnel absorption tower 8 by the lower entrances on liquid caustic soda security personnel absorption tower 8, adding water and being mixed with concentration is enter into after the liquid caustic soda of 10.6% in liquid caustic soda security personnel absorption tower 8), open liquid caustic soda recycle pump 5, liquid caustic soda from top liquid caustic soda spray equipment 19 spray and, with ensure public security absorption tower 8 from liquid caustic soda in flue gas adverse current from bottom to top contact and continue to absorb the sulfurous gas in flue gas, (flue gas concentration remains on 60mg/Nm to flue gas after absorbing by liquid caustic soda
3below, qualified discharge requirement is met) discharge from exhaust emission pipeline 18 through the top on liquid caustic soda security personnel absorption tower 8.
Claims (10)
1. the device of a concentrate desulfurization reduction content of magnesia, it is characterized in that: comprise concentrate slurry sloptank (1), concentrate slurry sloptank (2) after absorbing, thionizer (4), liquid caustic soda security personnel absorption tower (8), alkali-prepared tank (7), thickener (14), underflow sloptank (12) and clear liquid pH regulator groove (13), described concentrate slurry sloptank (1) is connected with the concentrate slurry entrance being positioned at thionizer (4) bottom, the bottom of described thionizer (4) is also connected with the top spray equipment (15) in thionizer (4) by recycle pump (3), the concentrate slurry outlet of described thionizer (4) is connected with concentrate slurry sloptank (2) after absorption, after described absorption, concentrate slurry sloptank (2) is also connected with thickener (14), the bottom of described thickener (14) is connected with underflow sloptank (12), the top of described thickener (14) is connected with clear liquid pH regulator groove (13), the middle part of described thionizer (4) is provided with low-concentration sulfur dioxide flue gas during smelting import (16), the lower entrances on the top of described thionizer (4) is provided with venting port (17) and venting port (17) is ensured public security with exhaust emission pipeline (18) and liquid caustic soda respectively absorption tower (8) is connected, the lower entrances of described liquid caustic soda security personnel absorption tower (8) and exhaust emission pipeline (18) are respectively equipped with chain trip valve (9), described chain trip valve (9) is connected with the outlet sulfur dioxide concentration detector (10) being arranged on venting port (17) place, the bottom of described liquid caustic soda security personnel absorption tower (8) is also connected with top liquid caustic soda spray equipment (19) that liquid caustic soda is ensured public security in absorption tower (8) by liquid caustic soda recycle pump (5), described liquid caustic soda security personnel absorption tower (8) is connected with alkali-prepared tank (7), the top of described liquid caustic soda security personnel absorption tower (8) is connected with exhaust emission pipeline (18), described exhaust emission pipeline (18) is connected with blower fan (6).
2. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: described low-concentration sulfur dioxide flue gas during smelting import (16) place is provided with entrance sulfur dioxide concentration detector (11).
3. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: be provided with whipping appts (20) in described clear liquid pH regulator groove (13).
4. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: the pipeline that the bottom of described thickener (14) is connected with underflow sloptank (12) is provided with underflow valve (21).
5. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: described alkali-prepared tank (7) be provided with concentration be 30% liquid caustic soda add entrance (22) and water distribution adds entrance (23).
6. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: it is that the liquid caustic soda of 9-11% adds entrance (24) that described clear liquid pH regulator groove (13) is provided with concentration.
7. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: described underflow sloptank (12) is connected with raw materials for metallurgy storehouse by slush pump.
8. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: after described absorption, concentrate slurry sloptank (2) is connected with thickener (14) by pump.
9. a kind of concentrate desulfurization according to claim 1 reduces the device of content of magnesia, it is characterized in that: described recycle pump (3) and liquid caustic soda recycle pump (5) are respectively two groups.
10. concentrate desulfurization reduces a method for content of magnesia, it is characterized in that the method comprises the following steps:
After A, concentrate slurry ore dressing selected are delivered to concentrate slurry sloptank (1), concentrate slurry is delivered to thionizer (4) by concentrate slurry entrance;
B, ON cycle pump (3), the top spray equipment (15) concentrate slurry is delivered in thionizer (4) by recycle pump (3) spray and under, sulfurous gas in flue gas absorbs with low-concentration sulfur dioxide flue gas during smelting counter current contact from bottom to top from thionizer (4), the basic activated component in concentrate slurry by concentrate slurry;
C, when absorb after concentrate slurry pH value reach 6.0-7.0 time be delivered to absorb after concentrate slurry sloptank (2), and through pump delivery in thickener (14), after thickener (14) is dense, open underflow valve (21), underflow enters underflow sloptank (12), and is delivered in raw materials for metallurgy storehouse through slush pump;
Supernatant liquor after D, thickener (14) are dense flows in clear liquid pH regulator groove (13), by adding the pH value that concentration is the liquid caustic soda adjustment supernatant liquor of 9-11% in clear liquid pH regulator groove (13), stirred by whipping appts (20), the pH value of supernatant liquor reaches ore dressing water distribution and requires rear as ore-sorting system water distribution reuse;
E, by outlet sulfur dioxide concentration detector (10) to venting port (17) place through concentrate slurry absorb after low-concentration sulfur dioxide flue gas during smelting in sulfur dioxide concentration detect, detect qualified after, chain trip valve (9) opens to the pipeline of exhaust emission pipeline (18), and flue gas is directly discharged from exhaust emission pipeline (18);
F, liquid caustic soda in prior alkali-prepared tank (7) enters in liquid caustic soda security personnel absorption tower (8), when detecting defective, chain trip valve (9) is cut to the pipeline of exhaust emission pipeline (18), open to the pipeline of liquid caustic soda security personnel absorption tower (8) lower entrances, flue gas enters in liquid caustic soda security personnel absorption tower (8) by the ensure public security lower entrances on absorption tower (8) of liquid caustic soda, open liquid caustic soda recycle pump (5), liquid caustic soda from top liquid caustic soda spray equipment (19) spray and, contact with flue gas adverse current from bottom to top in absorption tower (8) of ensuring public security from liquid caustic soda and continue to absorb the sulfurous gas in flue gas, flue gas after absorbing by liquid caustic soda is discharged from exhaust emission pipeline (18) through the ensure public security top on absorption tower (8) of liquid caustic soda.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
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| CN106669374A (en) * | 2017-03-15 | 2017-05-17 | 云南驰宏锌锗股份有限公司 | Treatment equipment for temperature-rise flue gas containing dust, oil and sulfur dioxide for zinc smelting and roasting furnace |
| CN107185385A (en) * | 2017-07-07 | 2017-09-22 | 金川集团股份有限公司 | A kind of spuious flue gas during smelting wet dedusting of atm number, sulfur method |
| CN107952589A (en) * | 2017-11-17 | 2018-04-24 | 金川集团股份有限公司 | A kind of beneficiation method for reducing content of magnesia in Nelson's gravity treatment noble metal concentrate |
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| CN107185385A (en) * | 2017-07-07 | 2017-09-22 | 金川集团股份有限公司 | A kind of spuious flue gas during smelting wet dedusting of atm number, sulfur method |
| CN107952589A (en) * | 2017-11-17 | 2018-04-24 | 金川集团股份有限公司 | A kind of beneficiation method for reducing content of magnesia in Nelson's gravity treatment noble metal concentrate |
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| CN105349772B (en) | 2018-04-10 |
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Effective date of registration: 20240205 Address after: 737100 No. 2 Lanzhou Road, Beijing Road Street, Jinchuan District, Jinchang City, Gansu Province Patentee after: Jinchuan Group Nickel Cobalt Co.,Ltd. Country or region after: China Address before: 737103 No. 98, Jinchuan Road, Jinchang, Gansu Patentee before: JINCHUAN GROUP Co.,Ltd. Country or region before: China |