CA1268564A - Process to recover lead compounds - Google Patents
Process to recover lead compoundsInfo
- Publication number
- CA1268564A CA1268564A CA000553054A CA553054A CA1268564A CA 1268564 A CA1268564 A CA 1268564A CA 000553054 A CA000553054 A CA 000553054A CA 553054 A CA553054 A CA 553054A CA 1268564 A CA1268564 A CA 1268564A
- Authority
- CA
- Canada
- Prior art keywords
- lead compounds
- flotation
- lead
- anglesite
- base metals
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/004—Organic compounds
- B03D1/01—Organic compounds containing nitrogen
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D1/00—Flotation
- B03D1/001—Flotation agents
- B03D1/002—Inorganic compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2201/00—Specified effects produced by the flotation agents
- B03D2201/02—Collectors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
- B03D2203/00—Specified materials treated by the flotation agents; specified applications
- B03D2203/02—Ores
- B03D2203/04—Non-sulfide ores
Landscapes
- Chemical & Material Sciences (AREA)
- Inorganic Chemistry (AREA)
- Manufacture And Refinement Of Metals (AREA)
Abstract
ABSTRACT
The enrichment and recovery of lead compounds from wastes and intermediate products from hydrometallurgical production and processing of base metals as well as from complex oxidic ores is either difficult to achieve or connected with intense energy consumption. In this invention, direct flotation of lead compounds is applied for the abovementioned purpose, which is carried out by using amine based collecting and foaming reagents in a pH range of < or = 3 in the presence of inorganic acids and higher amounts of dissolved heavy metals from leaching processes.
The enrichment and recovery of lead compounds from wastes and intermediate products from hydrometallurgical production and processing of base metals as well as from complex oxidic ores is either difficult to achieve or connected with intense energy consumption. In this invention, direct flotation of lead compounds is applied for the abovementioned purpose, which is carried out by using amine based collecting and foaming reagents in a pH range of < or = 3 in the presence of inorganic acids and higher amounts of dissolved heavy metals from leaching processes.
Description
- 2 -This inventi~n relates to a process for enriehrnent and r~covery of lead compounds from wastes and intermediate products from hydrometallurgical production and processing of base mcl;alv; as well as from complex oxidic ores by flotation from pulps, which are acidic and of higher conce~trations of dissolved base metals.
Acid leaching of complex base metal bearing raw materials such as polymetallic ores and related roas-t products in the presence of sulfate ions leads to PbSO~ containing residues (MARTIN,M. T.
a. JANKOLA,W.A.; CIM-Bulletin (April 1985) p.77~, which comprise minor amounts of plumbojarosite and plumboferrite as well as other sulphates and oxides. Commonly the recovery of lead frorn such residues is achieved by pyrometallurgical processing as for instance the Waelz Process. For economic reasons, hydrometallurgical approaches are not used to recQver lead (WEIR,D.R.; Can. Met.Quart. 23 (1984) p.358). An alternative is given by indirect enrichment by magnetic separation, which however does not remove nonmagnetic impurities like SiO2 and alkaline earth sulphates (ROWLANDS,N.; J.Met. (June 1985) p.l8).
Residues containing PbS04 may also be derived from hydrometallurgical recovery of zinc and copper from flue dusts (REDDY,~.G.; J.Met. (April 1986) p.50 - 51), bottom ashes and scrap. If lead contents are sufficiently high, lead is recovered from these residues by means of pyrometallurgical treatment.
A usual method for the beneficiation of complex oxidic ores, which often contain anglesite, is the lead flotation with sulphydryl collectors after addition of Na2Sx9H20 at a pH
ranging between 6 and 11. Anglesite from the LP~ Process (leaching-precipitation-flotation) can be floated in the same manner (SCHUBERT,H.: Beneficiation of solid minera] raw materials II; (1986) p.408 - 409). Due to fine in-tergrowths, very small particle diameters and co-floating rninerals the recovery and the selectivity of the anglesite flotation are often low. A recent approach to solve this problem was the study ~X; '
Acid leaching of complex base metal bearing raw materials such as polymetallic ores and related roas-t products in the presence of sulfate ions leads to PbSO~ containing residues (MARTIN,M. T.
a. JANKOLA,W.A.; CIM-Bulletin (April 1985) p.77~, which comprise minor amounts of plumbojarosite and plumboferrite as well as other sulphates and oxides. Commonly the recovery of lead frorn such residues is achieved by pyrometallurgical processing as for instance the Waelz Process. For economic reasons, hydrometallurgical approaches are not used to recQver lead (WEIR,D.R.; Can. Met.Quart. 23 (1984) p.358). An alternative is given by indirect enrichment by magnetic separation, which however does not remove nonmagnetic impurities like SiO2 and alkaline earth sulphates (ROWLANDS,N.; J.Met. (June 1985) p.l8).
Residues containing PbS04 may also be derived from hydrometallurgical recovery of zinc and copper from flue dusts (REDDY,~.G.; J.Met. (April 1986) p.50 - 51), bottom ashes and scrap. If lead contents are sufficiently high, lead is recovered from these residues by means of pyrometallurgical treatment.
A usual method for the beneficiation of complex oxidic ores, which often contain anglesite, is the lead flotation with sulphydryl collectors after addition of Na2Sx9H20 at a pH
ranging between 6 and 11. Anglesite from the LP~ Process (leaching-precipitation-flotation) can be floated in the same manner (SCHUBERT,H.: Beneficiation of solid minera] raw materials II; (1986) p.408 - 409). Due to fine in-tergrowths, very small particle diameters and co-floating rninerals the recovery and the selectivity of the anglesite flotation are often low. A recent approach to solve this problem was the study ~X; '
- 3 ~ 6~
of electroflota-tion of anglesite in the pH-range from 3 to 11 using xanthate and alkylsulphate collectors (RAO,G.W., SCHNEIDER,F-U. u. HOBER~,H.; Erzmetall 40 (1987) p.183 - 188).
The Disadvantages of electroflota-tion are rapid pH-changes in the system and sensitivity to varying electrolyte concentrations making it difficul-t to controll the process. Sulphydryl collectors are of only limited use in the presence of sulphide impurities and dissolved base metal ions and they decompose at low pH values. The selectivity of anglesite flotation with alkylsulphates is hampered by co-floating mineral phases such as quartz, ironoxides and alkaline earth sulphates.
Our invention overcomes the aboveementioned problems in the following way (claims 1 to 10): By flotation at pH -~ 3 and by using amines or their watersoluble derivatives (preferably primary amines with hydrocarbon chain lengths of 10 to 16) as collecting and foaming reagents lead concentrates are produced from suspensions of fine grained (if necessary comminuted) wastes or byproducts from base metal production or processing as well as complex oxidic ores. The process is independent of the type of the flotation machine. Disturbing defoaming and flocculating reagents and Fe-III- ions respectively can be removed by thermal or wet chemical treatment. Since there is no significant negative influence by the presence of Zn-, Cu- and Fe~ ions on this lead flotation process, the parallel leaching of these metals is posslble, Advantages of the invention are as follows:
- Independence from type of flotation machine - no sensitivity towards high acidity of the flota-tion pulp - no adverse effects by dissolved Zn-, Cu- and Fe-II- ions - selectivity of flotation against Fe203, FeOOH, SiO2 and earth-alkaline sulphates - collective flotation of oxidic, sulphatic and sulphidic lead compounds - leaching o-f base metals such as Zn and Cu parallel to lead flotation.
_ 4 - ~ 6~
Lead flotation from acidic pulps with amines or -their derivatives according to the invention relies on the precipitation and formation of lead amine complexes on the surface of solid lead compounds and enhanced collector adsorption due to the negative charge of the anions present at the surfaces of the lead minerals. The solubility of the complexes and collectors is determined by the hydrocarbon chain lengths and character (primary to quaternary) of the amine used as well as by the pH value and rises with decreasing pH values and shorter chain lengths. Requirements for using amine collectors in lead flotation are a sufficient solubility and reactivity along with a most specific surface adsorption as well as the avoidance of insoluble complexes with metals other than lead. Cu, Zn and Fe are known for the formation of amine complexes at high pH levels. Another disturbing effect might arise from nonspecific reactions with anions like so2~ on mineral surfaces. The studies of the authors showed that due to low pH values neither Zn-, Cu- and Fe-II-cations nor So2 - or Cl -anions significantly impair the amine lead flotation process~ Another obstruction of the flotation process can be expected when trivalent Fe-ions are present which might inactivate the amine collector when in solution or decrease the flotation selectivity when present in insoluble compounds such as hematite (Fe203). Using amine collectors with shorter or longer hydrocarbon chain leng-ths (C10 or C16) reestablishes the flotation selectivity against iron oxide (Fe203) as well as against calcium sulphate (gypsum/CaSO~x2H20) which o-therwise would also cause unwanted collector adsorption via sulphate ions on its surface. The effectiveness of amines as lead collectors decreases from primary via secondary and tertiary to quaternary amines. Despite a sufficient recovery of lead sulfate and high selectivity against calcium sulphate which were found for dioctylammoniumchloride (chloride salt of secondary amine with chain lengths C~) its selectivity towards Fe203 proved to be unsatisfactory.
_ 5 ~ 6~3L
In the following three examples of application of the invention are described to illustrate its optimal use:
Example 1 _ _ _ _ _ _ _ _ _ Pure anglesite (PbS04) with a mean grain size d50 = 6.1 -~m and a specific surface of 0.4 m2/g as well as a pure sample of plattnerite (PbO2) with a mean grain size d50 = 4.4 ~m and a specific surface of 0.23 m2/g were used in separate flotation test series. The tests were carried out batchwise in a mechanical flotation cell of 5 1 in volume. Constant parameters were:
content of solids in pulp = 400 g/l dispersion time = 3 min pH regulation time = 5 min collector addition = 500 g/t dodecylammoniumchloride flotation time = 10 min stirrer velocity = 1500 min~
air throughput = 13 l/min The tests were conducted with flotation pulps of various salt contents, pH values, pH regulating reagents and temperatures.
The results are shown in table 1.
Table 1 __________________~_____._______________________________________ material varied parameter yield (%) ,_____________ __________________________________________________ PbS04 pH a 1 ~ 5 (H2S04) 99 ~ 8 saltcontent= 0 temperature= 20 C
PbS04 pH = 1,5 (H2S04) 97,3 ZnS04x7H20 = 350 g/l temperature= 20~ C
_________________________________________________________________ t~hle 1 / part b see next page - 6 - ~%
table 1 / part b material varied parameters yield ~%) _________.. ______________________________________ ._____________ PbS04 pH = 1,5 (H~S04) 99,2 CuS04x5H20 = 140 g/l temperature= 20 C
PbS04 pH = 0,5 (H2S04) 97,3 ZnS04x7H20 = 5 g/l CuS04x5H2.0 = 5 g/l temperature= 20 C
PbO2 pH = 3,0 (H2S04) 95,0 sa.ltcontent= 0 temperatu~ = 20 C
PbO2 pH = 3,0 (HC1) 97,3 saltcontent= 0 temperature= 20 C
PbO2 pH = 3,0 (H~S04) 80,4 ZnS04x7H20 = 50 g/l CuS04x5H20 = 50 g/1 temperature= 20C
PbO2 pH = 3,0 (H2S04) 92,1 ZnS04x7H~0 = 50 g/l CuS04x5~1zO = 50 g/1 temperature= 100C
______._________________________________________________________ ~685~i~
Example 2 Artificial mixtures of anglesite (PbS0~), plattnerite (PbO2) and galenite (PbS) with quartz (SiO2), hematite (Fe203) and gypsum (CaS04x2H20) were investigated in flotation studies with several amine collectors to examine the selectivity of the flotation process, Constant parameters were:
content of solids in pulp = 100 g/l dispersion time = 3 min pH regulation time = 5 min flotation time = 10 min collector addition = 500 g/t stirrer velocity = 1500 min 1 air throughput = 13 l/min temperature of pulp = 20 C
The tests were conducted with differen-t mineral mixtures, collecting reagents and pH values. The results are shown in table 2.
Table 2 ________________________________________________________________ lead added pH - collector Pb-mineral Pb-mineral mine- compound value l)RNH3Cl content in yield ral 2)R2NH2Cl concentra-te R = *) (%) (%) ____________________~___________________________________________ PbS04 50 % SiO2 1,5 1) C12H25 97,6 92,0 PbS04 30 % Fe,~03 1) C1oH2~ 75.3 86,2 30 % CaS04x2HzO 1,5 PbS04 30 % Fe203 1,5 1) C12~l25 69~9 93,8 30 % CaSO4x2H20 ______________________________~__________________________________ table 2 / p~r-t b see next page - 8 - ~ 4 tahle 2 ¦ par't b ________._______________________________________________________ lead added pH - collector Pb-mineral Pb-mineral mine- compound value l)RNH3Cl content in yield ral 2)R2NH2Cl concentrate R = *) (%) (%) ________________________________________________________________ PbS04 30 % Fe203 1,5 1) C~6 ~3 81,8 99,6 30 % caS04X2H22 PbS04 30 % Fe20~ 1,5 2) C8H17 76,1 84,0 30 % CaSO~x2H20 PbO2 50 % SiO2 3,0 1) ClZH2~ 96,2 60,0 PbS 50 /0 S102 3,0 1) C12H25 83,2 81,0 ________________________________________________________________ *) R = alkylgroup, 1) = primary alkylammoniumchloride, 2) = secon-dary alkylammoniumchloride Example 3 The combination of lead flotation and base metal leaching withsulphuric acid was tested with zinc leaching residues from a former lithopone producing plant. The investigated sample showed the following chemical composition:
ZnO 21,4 %
Fe20320,0 %
PbO8,5 %
M~027,1 %
CaO0,4 %
CuO0,2 %
SiO217,2 %
S021~, 9 %
Al23 ~8~;6~L
g Proven mineral composites were: Anglesite (PbS04), plumbojarosite (PbFe6(S04)4x(0H)12), plumboferrite (PbFe407), esperite ((Ca,Pb)ZnSiO4), franklinite and other spinel phases ((Zn,X)Fe204), illite (KA12((0H)2Si3010)) and quartz (SiO2).
Prior to leaching and flotation the material had been ground to a mean grain size d50 = 7 ~m. Constant parameters were:
content of solids in feed pulp = 100 g/l H2S04 addition = 200 kg/t temperature of pulp = 20 C
leaching time without flotation = 15 min The lead flotation was carried out with stepwise collector addition (collecting reagent hexadecylammoniumchlorid) and a total collector consumption of 2000 g/t. Flotation time was 30 min. The achieved yield of lead in concentrate was 81 % and the lead content 24 %. The yield of zinc in solution was analysed with 83 %. Fig. 1 shows X-ray diffraction spectra in the range of 2e = 10 to 40 (wavelengths CuKa) for the feed and the lead concentrate. Comparison of the peak intensities shows, that preferential anglesite and to a lesser degree plumbojarosite and plumboferrite had been floated.
of electroflota-tion of anglesite in the pH-range from 3 to 11 using xanthate and alkylsulphate collectors (RAO,G.W., SCHNEIDER,F-U. u. HOBER~,H.; Erzmetall 40 (1987) p.183 - 188).
The Disadvantages of electroflota-tion are rapid pH-changes in the system and sensitivity to varying electrolyte concentrations making it difficul-t to controll the process. Sulphydryl collectors are of only limited use in the presence of sulphide impurities and dissolved base metal ions and they decompose at low pH values. The selectivity of anglesite flotation with alkylsulphates is hampered by co-floating mineral phases such as quartz, ironoxides and alkaline earth sulphates.
Our invention overcomes the aboveementioned problems in the following way (claims 1 to 10): By flotation at pH -~ 3 and by using amines or their watersoluble derivatives (preferably primary amines with hydrocarbon chain lengths of 10 to 16) as collecting and foaming reagents lead concentrates are produced from suspensions of fine grained (if necessary comminuted) wastes or byproducts from base metal production or processing as well as complex oxidic ores. The process is independent of the type of the flotation machine. Disturbing defoaming and flocculating reagents and Fe-III- ions respectively can be removed by thermal or wet chemical treatment. Since there is no significant negative influence by the presence of Zn-, Cu- and Fe~ ions on this lead flotation process, the parallel leaching of these metals is posslble, Advantages of the invention are as follows:
- Independence from type of flotation machine - no sensitivity towards high acidity of the flota-tion pulp - no adverse effects by dissolved Zn-, Cu- and Fe-II- ions - selectivity of flotation against Fe203, FeOOH, SiO2 and earth-alkaline sulphates - collective flotation of oxidic, sulphatic and sulphidic lead compounds - leaching o-f base metals such as Zn and Cu parallel to lead flotation.
_ 4 - ~ 6~
Lead flotation from acidic pulps with amines or -their derivatives according to the invention relies on the precipitation and formation of lead amine complexes on the surface of solid lead compounds and enhanced collector adsorption due to the negative charge of the anions present at the surfaces of the lead minerals. The solubility of the complexes and collectors is determined by the hydrocarbon chain lengths and character (primary to quaternary) of the amine used as well as by the pH value and rises with decreasing pH values and shorter chain lengths. Requirements for using amine collectors in lead flotation are a sufficient solubility and reactivity along with a most specific surface adsorption as well as the avoidance of insoluble complexes with metals other than lead. Cu, Zn and Fe are known for the formation of amine complexes at high pH levels. Another disturbing effect might arise from nonspecific reactions with anions like so2~ on mineral surfaces. The studies of the authors showed that due to low pH values neither Zn-, Cu- and Fe-II-cations nor So2 - or Cl -anions significantly impair the amine lead flotation process~ Another obstruction of the flotation process can be expected when trivalent Fe-ions are present which might inactivate the amine collector when in solution or decrease the flotation selectivity when present in insoluble compounds such as hematite (Fe203). Using amine collectors with shorter or longer hydrocarbon chain leng-ths (C10 or C16) reestablishes the flotation selectivity against iron oxide (Fe203) as well as against calcium sulphate (gypsum/CaSO~x2H20) which o-therwise would also cause unwanted collector adsorption via sulphate ions on its surface. The effectiveness of amines as lead collectors decreases from primary via secondary and tertiary to quaternary amines. Despite a sufficient recovery of lead sulfate and high selectivity against calcium sulphate which were found for dioctylammoniumchloride (chloride salt of secondary amine with chain lengths C~) its selectivity towards Fe203 proved to be unsatisfactory.
_ 5 ~ 6~3L
In the following three examples of application of the invention are described to illustrate its optimal use:
Example 1 _ _ _ _ _ _ _ _ _ Pure anglesite (PbS04) with a mean grain size d50 = 6.1 -~m and a specific surface of 0.4 m2/g as well as a pure sample of plattnerite (PbO2) with a mean grain size d50 = 4.4 ~m and a specific surface of 0.23 m2/g were used in separate flotation test series. The tests were carried out batchwise in a mechanical flotation cell of 5 1 in volume. Constant parameters were:
content of solids in pulp = 400 g/l dispersion time = 3 min pH regulation time = 5 min collector addition = 500 g/t dodecylammoniumchloride flotation time = 10 min stirrer velocity = 1500 min~
air throughput = 13 l/min The tests were conducted with flotation pulps of various salt contents, pH values, pH regulating reagents and temperatures.
The results are shown in table 1.
Table 1 __________________~_____._______________________________________ material varied parameter yield (%) ,_____________ __________________________________________________ PbS04 pH a 1 ~ 5 (H2S04) 99 ~ 8 saltcontent= 0 temperature= 20 C
PbS04 pH = 1,5 (H2S04) 97,3 ZnS04x7H20 = 350 g/l temperature= 20~ C
_________________________________________________________________ t~hle 1 / part b see next page - 6 - ~%
table 1 / part b material varied parameters yield ~%) _________.. ______________________________________ ._____________ PbS04 pH = 1,5 (H~S04) 99,2 CuS04x5H20 = 140 g/l temperature= 20 C
PbS04 pH = 0,5 (H2S04) 97,3 ZnS04x7H20 = 5 g/l CuS04x5H2.0 = 5 g/l temperature= 20 C
PbO2 pH = 3,0 (H2S04) 95,0 sa.ltcontent= 0 temperatu~ = 20 C
PbO2 pH = 3,0 (HC1) 97,3 saltcontent= 0 temperature= 20 C
PbO2 pH = 3,0 (H~S04) 80,4 ZnS04x7H20 = 50 g/l CuS04x5H20 = 50 g/1 temperature= 20C
PbO2 pH = 3,0 (H2S04) 92,1 ZnS04x7H~0 = 50 g/l CuS04x5~1zO = 50 g/1 temperature= 100C
______._________________________________________________________ ~685~i~
Example 2 Artificial mixtures of anglesite (PbS0~), plattnerite (PbO2) and galenite (PbS) with quartz (SiO2), hematite (Fe203) and gypsum (CaS04x2H20) were investigated in flotation studies with several amine collectors to examine the selectivity of the flotation process, Constant parameters were:
content of solids in pulp = 100 g/l dispersion time = 3 min pH regulation time = 5 min flotation time = 10 min collector addition = 500 g/t stirrer velocity = 1500 min 1 air throughput = 13 l/min temperature of pulp = 20 C
The tests were conducted with differen-t mineral mixtures, collecting reagents and pH values. The results are shown in table 2.
Table 2 ________________________________________________________________ lead added pH - collector Pb-mineral Pb-mineral mine- compound value l)RNH3Cl content in yield ral 2)R2NH2Cl concentra-te R = *) (%) (%) ____________________~___________________________________________ PbS04 50 % SiO2 1,5 1) C12H25 97,6 92,0 PbS04 30 % Fe,~03 1) C1oH2~ 75.3 86,2 30 % CaS04x2HzO 1,5 PbS04 30 % Fe203 1,5 1) C12~l25 69~9 93,8 30 % CaSO4x2H20 ______________________________~__________________________________ table 2 / p~r-t b see next page - 8 - ~ 4 tahle 2 ¦ par't b ________._______________________________________________________ lead added pH - collector Pb-mineral Pb-mineral mine- compound value l)RNH3Cl content in yield ral 2)R2NH2Cl concentrate R = *) (%) (%) ________________________________________________________________ PbS04 30 % Fe203 1,5 1) C~6 ~3 81,8 99,6 30 % caS04X2H22 PbS04 30 % Fe20~ 1,5 2) C8H17 76,1 84,0 30 % CaSO~x2H20 PbO2 50 % SiO2 3,0 1) ClZH2~ 96,2 60,0 PbS 50 /0 S102 3,0 1) C12H25 83,2 81,0 ________________________________________________________________ *) R = alkylgroup, 1) = primary alkylammoniumchloride, 2) = secon-dary alkylammoniumchloride Example 3 The combination of lead flotation and base metal leaching withsulphuric acid was tested with zinc leaching residues from a former lithopone producing plant. The investigated sample showed the following chemical composition:
ZnO 21,4 %
Fe20320,0 %
PbO8,5 %
M~027,1 %
CaO0,4 %
CuO0,2 %
SiO217,2 %
S021~, 9 %
Al23 ~8~;6~L
g Proven mineral composites were: Anglesite (PbS04), plumbojarosite (PbFe6(S04)4x(0H)12), plumboferrite (PbFe407), esperite ((Ca,Pb)ZnSiO4), franklinite and other spinel phases ((Zn,X)Fe204), illite (KA12((0H)2Si3010)) and quartz (SiO2).
Prior to leaching and flotation the material had been ground to a mean grain size d50 = 7 ~m. Constant parameters were:
content of solids in feed pulp = 100 g/l H2S04 addition = 200 kg/t temperature of pulp = 20 C
leaching time without flotation = 15 min The lead flotation was carried out with stepwise collector addition (collecting reagent hexadecylammoniumchlorid) and a total collector consumption of 2000 g/t. Flotation time was 30 min. The achieved yield of lead in concentrate was 81 % and the lead content 24 %. The yield of zinc in solution was analysed with 83 %. Fig. 1 shows X-ray diffraction spectra in the range of 2e = 10 to 40 (wavelengths CuKa) for the feed and the lead concentrate. Comparison of the peak intensities shows, that preferential anglesite and to a lesser degree plumbojarosite and plumboferrite had been floated.
Claims (10)
1. A process for selective flotation of lead compounds from slurries containing dissolved heavy metals (e.g. from wastes and intermediate products from hydrometallurgical production and processing of base metals as well as from complex oxidic ores), said process comprising:
a) carrying out froth flotation with said slurries in the presence of inorganic acids at a pH < 3 or = 3 and using aliphatic primary or secondary watersoluble aminosalts with minimal 8 C atoms as collecting and foaming reagents in an amount effective to concentrate the solid lead compounds in the froth; and b) recovering the lead compounds with the froth.
a) carrying out froth flotation with said slurries in the presence of inorganic acids at a pH < 3 or = 3 and using aliphatic primary or secondary watersoluble aminosalts with minimal 8 C atoms as collecting and foaming reagents in an amount effective to concentrate the solid lead compounds in the froth; and b) recovering the lead compounds with the froth.
2. A process as claimed in claim 1, in which the lead compounds are anglesite (PbSO4) and plumboferrite (PbFe4O7) and the pH is < or = 1.5.
3. A process as claimed in claim 1, in wich the lead compounds are plumbojarosite (PbFe6(SO4)4x(OH)12), plattnerite (PbO2) and galenite (PbS) and the pH is between 1.5 and 3Ø
4. A process as claimed in claim 1, in which the lead compounds are anglesite (PbSO4), plumboferrite (PbFe4O7), plumbojarosite (PbFe6(SO4)4x(OH)12), plattnerite (PbO2) and galenite (PbS).
5. A process as claimed in claim 1, in which the concentration of Zn-. Cu-and Fe-II- ions in solution in the flotation pulp varies between zero and the concentration of saturation.
6. A process as claimed in claim 1, in which the inorganic acid is sulphuric acid.
7. A process as claimed in claim 1, in which the inorganic acid is hydrochloric acid.
8. A process as claimed in claim 1, which is carried out during leaching of base metals.
9. A process as claimed in claim 1, which is carried out after leaching of base metals.
10.
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE19873716012 DE3716012A1 (en) | 1987-05-11 | 1987-05-11 | Process for concentrating lead compounds |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1268564A true CA1268564A (en) | 1990-05-01 |
Family
ID=6327467
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA000553054A Expired CA1268564A (en) | 1987-05-11 | 1987-12-30 | Process to recover lead compounds |
Country Status (2)
| Country | Link |
|---|---|
| CA (1) | CA1268564A (en) |
| DE (1) | DE3716012A1 (en) |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| ES411058A1 (en) * | 1973-01-27 | 1975-12-01 | Asturiana De Zinc Sa | Process for concentrating lead and silver by flotation in products which contain oxidized lead |
| US4351668A (en) * | 1981-03-09 | 1982-09-28 | Cominco Ltd. | Flotation of Cu and Pb sulfide concentrates containing carbonates |
| CN85107378A (en) * | 1984-09-13 | 1987-03-18 | 陶氏化学公司 | From raw coal, reclaim the foaming agent composition and the foam flotation method of useful coal |
-
1987
- 1987-05-11 DE DE19873716012 patent/DE3716012A1/en not_active Withdrawn
- 1987-12-30 CA CA000553054A patent/CA1268564A/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| DE3716012A1 (en) | 1988-11-24 |
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