CN1544666A - Method for recovering nickel and aluminum from waste aluminum based nickel-containing catalyst - Google Patents

Abstract

The invention is a method of recovering nickelic and aluminum from waste aluminum-based nickel catalyst, it has the characters of novel technique, reasonable flow, simple and convenient method and easy operation, and convenient scaled production, and benefits environmental protection. It includes the steps: sodium carbonate sintering and state-changing--boiling water dissolving sodium aluminate and separating aluminum--- making reducing-matte-making melting on nickel residues to obtain nickel matte Ni3S2-FeS-Ni-Fe alloy or copper-nickel matte Cu2S-Ni3S2-FeS alloy---blowing to obtain high-grade nickel matte Ni3S2 or high-grade copper-nickel matte Cu2S-Ni3S2-Cu-Ni alloy---desiliconizing crude NaAlO2 solution---making carbonated decomposition to obtain aluminum hydrate Al2O3.3H2O---calcining to obtain anhydrous aluminum oxide alpha-Al2O3. It is suitable to recover nickel and aluminum from the waste residue generated by extracting molybdenum and vanadium from waste aluminum-based nickelic catalysts and disabled catalysts containing nickel, aluminum, molybdenum and vanadium.

Description

Reclaim the method for nickel and aluminium from aluminium scrap base nickel-containing catalyst

Technical field:

The present invention relates to non-ferrous metal refinement technique field, exactly it is the method that reclaims nickel and aluminium from aluminium scrap base nickel-containing catalyst.

Background technology:

According to statistics, about 50～700,000 tons of the annual spent catalyst that produces in the whole world will consume a large amount of precious metals and non-ferrous metal and oxide compound thereof for making these catalyzer.From resource rational utilization and environmental angle, all need the spent catalyst recovery of regenerating is made it to be reused.

Aluminium base nickel molybdenum, nickel cobalt molybdenum and cobalt molybdenum class catalyzer are by matrix Al ₂O ₃And the active ingredient composition, be widely used in the chemical fertilizer industry.Only the output of the present all kinds of chemical fertilizer catalysts of China remains on annual about 30,000 tons.Catalyzer is behind life-time service, and metals such as its active constituent nickel, cobalt, molybdenum, vanadium are subjected to the pollution of various impurity and lose activity, and become spent catalyst.Spent catalyst is the important secondary resource of non-ferrous metal.The method that reclaims non-ferrous metal from aluminium base spent catalyst has carrier dissolution method, dry type volatilization method, melting trapped method, plasmamelt process etc.Aluminium scrap base nickel molybdenum, nickel cobalt molybdenum, cobalt molybdenum class catalyzer are strip, trifolium shape and the φ 16 * φ 6mm Raschig ring shape catalyzer of coccoid or φ 3 * 3～8mm of φ 2.5～φ 10mm, and appearance colour is grey blue, light orchid, dark grey, yellow etc.Its major ingredient is (%), Al ₂O ₃24～85, Ni1.1～14 (high-nickel catalyst Ni content can reach more than 20%), or Co1.1～11.8, MoO～15, K ₂O+Na ₂O0.1～0.25, Fe ₂O ₃Trace, CaO trace (the high calcium catalyst CaO of minority content can reach 15%), V ₂O ₅Trace, SiO ₂0.2～2.0.Nickeliferous, aluminium, molybdenum, vanadium spent catalyst extract after molybdenum, the vanadium, and the typical composition of waste residue is (%) Al ₂O ₃62～65, Ni3.89～4.64, Na ₂The O trace, V ₂O ₅1.5, MoO ₃0.20, Fe ₂O ₃Trace, SiO ₂1.5.Because this type of catalyzer in its former manufacturing processed, is all handled through high-temperature calcination after the moulding, therefore, in spent catalyst and aforementioned waste residue, nickel is the NiO form, and cobalt is CoO or Co ₂O ₃Form, aluminium mainly are insoluble α-Al ₂O ₃, small part is r-Al ₂O ₃Form exists, and belongs to difficult material.When this class catalyzer and waste residue thereof adopted acid, the processing of alkali direct leaching process, effect was all undesirable.The former Al ₂O ₃Leaching yield is not high, and can cause nickel to disperse in solution, does not reach the purpose of separating nickel and aluminium; Though latter's nickel does not enter basic solution, Al ₂O ₃Solubility rate equally less than 50%, and the SiO in the raw material ₂, easily form the very little aluminosilicate (Na of solubleness ₂OAl ₂O ₃2SiO ₂2H ₂O) fouling is in the inwall of equipment, and filtration difficulty.Because raw material contains the Al up to 60%～80% ₂O ₃, also be not suitable for directly handling with melting trapped method, adopt plasmamelt process, this class spent catalyst or waste residue of melting under high temperature more than 1500 ℃, though can obtain Rhometal, because the raw material grade is low, energy consumption of unit product height, matrix Al ₂O ₃Also be not used.

Summary of the invention:

The purpose of this invention is to provide a kind of from Al ₂O ₃Be the effective method of separating nickel and aluminium in the aluminium scrap base nickel-containing catalyst of any crystal formation and the aforementioned waste residue, it is easy to implement, is beneficial to environmental protection, again can comprehensive recovery nickel and aluminium.

Method provided by the invention comprises that soda ash sintering transition-boiling water dissolving sodium aluminate separates aluminium-nickel slag reducing-matting smelting and gets nickel matte (Ni ₃S ₂-FeS-Ni-Fe alloy) or copper nickel matte (Cu ₂S-Ni ₃S ₂-FeS alloy)-blow Bessemer matte (Ni ₃S ₂) or copper Bessemer matte Cu ₂S-Ni ₃S ₂-Cu-Ni alloy)-thick NaAlO ₂Solution desilicification-carbonating branch solves aluminium hydroxide (Al ₂O ₃3H ₂O)-calcination gets anhydrous alumina (α-Al ₂O ₃) several steps, specific practice is: the waste residue that the spent catalyst of aluminium scrap base nickel-containing catalyst after (1) will pulverize or nickeliferous, aluminium, molybdenum, vanadium extracts after molybdenum, the alum mixes with soda ash, soda ash is yellow soda ash, its consumption is spent catalyst (or aforementioned waste residue): yellow soda ash (weight ratio)=1: 0.7～1.3, best 1: 0.9～1.1,700 ℃-1250 ℃ of temperature, best 1000 ℃～1150 ℃, material is in the sintering oven of liner high alumina brick, interaction in the best rotary kiln, generation transition reaction, constant temperature time 1～6 hour, best 3～4 hours.(2) the flue gas water spray washing of sintering oven generation makes gas temperature drop to 30 ℃～40 ℃, and smoke content reduces to 0.02 gram/rice ³～0.05 gram/rice ³, best 0.02～0.03 gram/rice ³After, as NaAlO ₂The CO that solution carbonation decomposes ₂Source of the gas.(3) after sintered material is pulverized, separate aluminium with boiling water dissolving sodium aluminate, this boiling water is the washing water of countercurrent washing nickel slag or washing aluminum hydroxide crystals, its consumption is a sintered material weight in grams number and the ratio 1: 2～10 of boiling water volume milliliter number, best 1: 4～6, temperature is the water boiling temperature, best＞95 ℃, 0.5～2 hour time, best 1 hour.Same ratio hot water countercurrent washing 2～3 times of undissolved nickel slag.(4) the thick NaAlO that the sintered material dissolving is obtained ₂, being heated to 85 ℃～95 ℃, best＞90 ℃ add lime (CaO) powder 5～10 grams by every liter of liquor capacity, best 6～8 grams, or add the milk of lime desiliconization that equal amts is prepared, stirring reaction 1～3 hour, best 2～3 hours, filter the back white residue, use hot wash.White residue returns sintering circuit and handles again to reclaim Al wherein ₂O ₃(5) with Al after the desiliconization ₂O ₃Concentration is the NaAlO of 100 grams per liters～140 grams per liters ₂Solution is heated to 60 ℃～80 ℃, best 70 ℃～75 ℃, presses Al in the solution ₂O ₃Al in content and the crystal seed ₂O ₃The ratio of content is 1: 1～1.5 adding aluminium hydroxide crystal seeds, under 8～10 rev/mins agitation condition, feeds CO ₂Gas carries out carbonating decomposition reaction, CO ₂Gas concentration 8%～14%, best more than 13%, 10～20 hours resolving times, best 14～16 hours.Aluminum hydroxide crystals is with pure water (soft water) washing, in 80 ℃～160 ℃ temperature oven dry.Decomposition nut liquid contains Al ₂O ₃5～7 grams per liters concentrate the back with dense Na ₂CO ₃The solution form is returned the sintering circuit batching.With aluminium hydroxide (Al ₂O ₃3H ₂O) obtain anhydrous alumina product (α-Al in 1200 ℃ of calcinings ₂O ₃).(6) the rich nickel slag behind the separation aluminium is with pyrite (main composition FeS ₂), (main composition is CaSO to Gypsum Mine ₄NH ₂O, n=2 or 3), copper sulfide concentrate (main composition CuFeS ₂) or cupric sulfide nickel ore concentrate (main composition CuFeS ₂, NisFeS) in any mineral make vulcanizing agent, with the smelting slag (FeO-SiO of copper smelting plant or nickel smeltery ₂-CaO type) or blowing slag (2FeOSiO ₂Type) any waste is made flux in, so that any carries out reducing-matting smelting as reductive agent and gets nickel matte (Ni in charcoal, coal or the coke ₃S ₂-FeS-Ni-Fe alloy) or copper nickel matte (Cu ₂S-Ni ₃S ₂-FeS alloy).Ratio of components is: rich nickel slag: vulcanizing agent: flux: reductive agent (weight ratio)=1: 0.1～0.3: 1～3: 0.02～0.05, best 1: 0.1～0.15: 1.5～2: 0.03,1250 ℃～1400 ℃ of smelting temperatures, best 1300 ℃～1350 ℃, smelting time 1～2 hour.Nickel matte or copper nickel matte are pressed copper, the traditional converting process in nickel smeltery, with quartzite (SiO ₂) do flux blowing and obtain Bessemer matte (Ni ₃S ₂) or copper Bessemer matte Cu ₂S-Ni ₃S ₂-Cu-Ni alloy), blowing slag Returning smelting operation is made flux usefulness.

Principal reaction equation in the technological process of the present invention is as follows:

1, soda ash sintering transition:

The oxide compound of Al, Si, Fe, V and Na in the material ₂CO ₃Following reaction is arranged:

(or Na ₂OAl ₂O ₃+ CO ₂↑)

Ni in the material exists with the NiO form, at high temperature with Al ₂O ₃, SiO ₂, Fe ₂O ₃Formation is insoluble in the NiOAl of water ₂O ₃, NiSiO ₃, NiFe ₂O ₄Compound.

2, boiling water dissolving sodium aluminate separates aluminium:

3, thick NaAlO ₂Solution desilicification:

4, NaAlO ₂Solution carbonation decomposes:

When having silicon to exist:

5, rich nickel slag reducing-matting smelting

When (1) making vulcanizing agent with pyrite:

When silicic acid nickel is arranged in the material:

When (2) making vulcanizing agent with Gypsum Mine:

When (3) making vulcanizing agent with copper sulfide concentrate and cupric sulfide nickel ore concentrate:

SiO is arranged ₂The time, the Fe that following formula generates ₃O ₄Following reaction takes place with FeS

6, nickel matte or copper nickel matte blowing, wherein nickel matte converting only has the oxidative slagging reaction of Fe and FeS:

Advantage of the present invention is: 1, Technology novelty, reasonable flowsheet structure can realize that the effective of nickel and aluminium separates and comprehensive the recovery.Aluminium hydroxide (the Al of preparation ₂O ₃3H ₂O) and aluminum oxide (α-Al ₂O ₃) reach the specification of quality of three grades of aluminium hydroxides of GB and industry tertiary oxidation aluminium respectively.The nickeliferous grade 17.94%～32.15% of the nickel matte that nickel slag reducing-matting smelting obtains.Smelting recovery Ni 〉=85%, Al is with Al ₂O ₃Meter 〉=79%.2, method is simple, is convenient to mass-producing enforcement and production application.3, Na ₂CO ₃Solution regeneration is multiplexing and utilize the discarded slag of copper, nickel smeltery to make flux, helps reducing the production cost of aluminium hydroxide and nickel matte.4, strong to adaptability to raw material, market outlook and promotional value are preferably arranged.The waste residue that the spent catalyst that the present invention is not only applicable to low-grade aluminium scrap base nickel-containing catalyst and nickeliferous, aluminium, molybdenum, vanadium extracts after molybdenum, the vanadium reclaims nickel and aluminium, is applicable to also that high-grade aluminium scrap base is nickeliferous, cobalt class catalyst recovery nickel, cobalt and aluminium.5, the soda ash sintering polling of project does not have damage by fume, and the sintering oven flue gas is used as NaAlO after purifying ₂The CO that solution carbonation decomposes ₂Source of the gas; Wet processing part process water can be realized the closed cycle operation, not outwards discharging; The white residue of sodium aluminate solution purification output returns sintering circuit and handles again, to reclaim Al wherein ₂O ₃And the slag of nickel slag melting operation output to be a kind of long-term stacking can not change form and the solid metallurgical slag that changes; Therefore, implement the technology of the present invention and can not work the mischief and influence, help environmental protection environment.

Description of drawings:

Fig. 1 is a process flow sheet of the present invention.

Embodiment:

Adopt FXS-300 type winnowing type pulverizer to pulverize aluminium scrap base nickel-containing catalyst and extract molybdenum vanadium waste residue afterwards; The coal firing indirect heater is made sintering oven, interior block high alumina brick, size of burner hearth length * wide * height=1500 * 1300 * 500 (millimeters).80 kilograms～100 kilograms of each chargings; Pulverize agglomerate with 9FZ-23 type hock type pulverizer; 300 liters and 1 meter ³Irony steel basin and reactor dissolving sintered material, 600 * 600 * 250 (millimeter) vacuum filtration case filters, washing nickel slag, strumbox drives with SZB-8 type water-ring vacuum pump; Carry out desiliconization and carbonating decomposition with Φ 500 * 600 (millimeter) stainless steel steel basin; It is the rich nickel slag of smelting furnace melting of 1500 * 250 * 800 (millimeters) that length * wide * height has been built in design by laying bricks or stones; Checked and used the implementation result that technological process of the present invention is handled aluminium scrap base nickel-containing catalyst and extracted molybdenum, vanadium waste residue afterwards; The transition of soda ash sintering, the result of boiling water separated and dissolved aluminium; The average output capacity of sintered material is 81.10%, Al ₂O ₃Solubility rate 79.93%～83.79%, nickel 2.1～2.63 times of enrichments in rich nickel slag; The aluminium hydroxide or the aluminum oxide of preparation reach three grades of specification of quality of GB respectively, the nickel matte nickel grade 17.94%～32.15% that nickel slag reducing-matting smelting obtains; Smelting recovery: Ni 〉=85%, Al is with Al ₂O ₃Meter 〉=79%.

Embodiment 1:

6 millimeters dark grey salad west of Φ 16 * Φ ring-type spent catalyst is pulverized material 1000 grams, content α-Al ₂O ₃49.20%, Ni11.40% (NiO14.5%), SiO ₂2.0%, CaO14.80%; (1) 1100 ℃～1150 ℃ of temperature, spent catalyst: yellow soda ash (weight ratio)=1: 1 condition, at SX ₂Sintering reaction is 3 hours in the-12-10 chamber type electric resistance furnace, obtains sintered material 1787 grams, and output capacity is 85.10%; (2) dissolve sintered material with boiling water, sintered material weight in grams number is 1: 4 with the ratio of boiling water volume milliliter number, and temperature is the water boiling temperature, and 1 hour time, the nickel slag weighs 472 grams, grade Ni24.12%, Al with oven dry after the hot wash 2 times, nickel slag ₂O ₃20.92%; In nickel slag composition, Al ₂O ₃Solubility rate 79.93%, 2.1 times of nickel enrichments.

Embodiment 2:

Nickeliferous, aluminium, molybdenum, vanadium spent catalyst extract 200 kilograms in pale blue waste residue after molybdenum, the vanadium, content Al ₂O ₃64.96%, Ni4.64% (NiO5.89%), V ₂O ₅1.50%, MoO ₃0.20%, SiO ₂1.5%, Na ₂O and Fe ₂O ₃Trace; (1) waste residue is oven dry, powder after the pulverizing, in aforementioned coal-fired furnace, divide 5 batches and carry out sintering, feed intake 40 kilograms at every turn, 1000 ℃～1050 ℃ of temperature, waste residue: yellow soda ash (weight ratio)=1: 1～1.25, sintering reaction 4～6 hours, obtain 336.4 kilograms of sintered materials altogether, output capacity 82.05%; (2) after sintered material was pulverized, the washing water dissolving with being heated to ebullient washing nickel slag dropped into 40 kilograms of sintered material powders at every turn, it is 1: 4～6 that sintered material weight kilogram number and boiling water volume rise number, temperature is the water boiling temperature, 1 hour time, same ratio hot water countercurrent washing 2 times of nickel slag.Obtain 72.7 kilograms of nickel slag meters, its composition Al ₂O ₃28.96%, Ni average grade 11.44%, Al ₂O ₃Solubility rate 83.79%, the nickel enrichment is 2.63 times in the nickel slag.(3) the mixed dissolution liquid (thick solution) with sintered material moves into stainless steel steel basin, its composition: Al for 40 liters ₂O ₃124.4 grams per liter, Ni0.005 grams per liter, SiO ₂0.71 grams per liter, be heated to 95 ℃, under agitation condition, add the lime powder desiliconization, consumption adds 7 gram CaO by every liquor capacity, adds coal powder 280 grams altogether, and temperature keeps 95 ℃ ± 5 ℃, 2 hours time, white residue is dried after with hot wash, and washing lotion is incorporated desiliconization liquid into, and liquor capacity is adjusted to 40 liters of original volumes.White residue weighs 620 grams, composition: Al ₂O ₃31.94%, SiO ₂2.88%, CaO47.13%; Desiliconization liquid (smart NaAlO ₂Solution) composition: Al ₂O ₃120 grams per liters, SiO ₂0.32 grams per liter, solution silicon ratio 375.Silicon decreasing ratio 66.62%, Al ₂O ₃The rate of recovery 96%.(4) the smart NaAlO after the above-mentioned desiliconization ₂Be heated to 75 ℃ in the carbonizer that 40 liters of immigrations of solution are made with stainless steel, add aluminium hydroxide crystal seed, its amount is pressed Al in the solution ₂O ₃With Al in the crystal seed ₂O ₃Weight ratio is calculating in 1: 1, adds 7.5 kilograms in aluminium hydroxide, under 8～10 rev/mins agitation condition, feeds the steel cylinder dress CO of technical grade ₂Gas carries out the carbonating decomposition reaction, and process temperature is by CO ₂The reaction heat that discharges with NaOH generation neutralization reaction in the solution maintains 70 ℃～50 ℃ temperature (envrionment temperature is 30 ℃), 16 hours decomposition reaction time, aluminum hydroxide crystals is extremely neutral with the hot tap water washing, dry to constant weight in 150 ℃ ± 10 ℃ temperature, washing lotion and mother liquor merge, and be adjusted to 40 liters of original volumes, contain Al ₂O ₃5.32 grams per liter, Al ₂O ₃Meter rate of decomposition 95.5%.Obtain 14.54 kilograms in aluminium hydroxide, 7.5 kilograms of deduction crystal seeds, 7.04 kilograms of true weights, aluminium hydroxide contains Al ₂O ₃65.03%, quality reaches three grades of aluminium hydroxide requirements of GB GB4294-84, from spent catalyst to the aluminium hydroxide product, with Al ₂O ₃Meter casting yield 76.88% counts white residue is returned the Al that sintering is handled recovery again ₂O ₃, Al then ₂O ₃The rate of recovery be 79.92%; Get 1000 gram aluminium hydroxides and obtained anhydrous alumina 642 grams, grade Al in 2 hours in 1200 ℃ of temperature calcinings ₂O ₃99.22%, quality reaches the requirement of coloured industry standard YS/T274-1888 tertiary oxidation aluminium.(5) get rich nickel slag 1kg, contain Ni14.07%; Make vulcanizing agent with pyrite; Smeltery's smelting slag is made flux, its composition FeO18.96%, SiO ₂41.04%, CaO14.23%; Powdered carbon is made reductive agent; In aforementioned 500 * 250 * 800 millimeters smelting furnaces of building by laying bricks or stones, make fuel with coke, with 40 ^#The melting of graphite clay crucible.Ratio of components is: rich nickel slag: pyrite: certain factory's smelting slag: powdered carbon=1: 0.2: 2.2: 0.03,1300 ℃～1350 ℃ of temperature, 1.5 hours time, obtain 0.417 kilogram of nickel matte, grade: Ni32.15%, 2.8 kilograms in slag contains Ni0.14%, the nickel melting rate of recovery 95.28%, from spent catalyst to the nickel matte rate of recovery 85.37%.

Embodiment 3:

Get 1 kilogram of rich nickel slag, nickel grade 10.83%; Make vulcanizing agent with Gypsum Mine, contain CaSO ₄2H ₂O87.51%; Smeltery's blowing slag is made flux, its composition FeO66.23%, SiO ₂23.05%; Coal dust is made reductive agent; Ratio of components: rich nickel slag: Gypsum Mine: blowing slag: coal dust=1 kilogram: 0.3 kilogram: 2 kilograms: 0.03 kilogram, with above-mentioned melting and crucible in 1300 ℃～1350 ℃, melting 1.5 hours, get 0.367 kilogram of nickel matte, grade, Ni27.80%, 2.8 kilograms in slag, contain Ni0.18%, the nickel melting rate of recovery 94.21%.

Embodiment 4:

Get 1 kilogram of rich nickel slag, nickel grade 10.83%; Make vulcanizing agent with copper nickel sulfide mineral, contain Cu1.8%, Ni2.21%; Above-mentioned refining slag is made flux, contains the Cu1.81% powdered carbon and makes reductive agent; Ratio of components: rich nickel slag: copper nickel sulfide mineral: Wingdale: blowing slag: powdered carbon=1 kilogram: 0.2 kilogram: 2 kilograms: 0.03 kilogram, with above-mentioned smelting furnace and crucible in 1300 ℃～1350 ℃, melting 1.5 hours, 0.371 kilogram of copper nickel matte, grade, Cu9.4%, Ni28.10%, 3.2 kilograms in slag, contain Cu0.12%, Ni0.16%, melting rate of recovery Cu87.62%, Ni94.55%.

Claims (3)

1, reclaims the method for nickel and aluminium from aluminium scrap base nickel-containing catalyst, comprise that soda ash sintering transition-boiling water dissolving sodium aluminate separates aluminium-nickel slag reducing-matting smelting and gets nickel matte Ni ₃S ₂-FeS-Ni-Fe alloy or copper nickel matte Cu ₂S-Ni ₃S ₂-FeS alloy-blow Bessemer matte Ni ₃S ₂Or copper Bessemer matte Cu ₂S-Ni ₃S ₂-Cu-Ni alloy-thick NaAlO ₂Solution desilicification-carbonating branch solves aluminium hydroxide Al ₂O ₃3H ₂O-calcine anhydrous alumina α-Al ₂O ₃Several steps is characterized in that:

A, soda ash sintering transition condition are: the waste residue that the spent catalyst of spent catalyst after the pulverizing or nickeliferous, aluminium, molybdenum, vanadium extracts after molybdenum, the alum mixes with soda ash, soda ash is yellow soda ash, its consumption is spent catalyst or aforementioned waste residue: yellow soda ash weight ratio=1: 0.7～1.3,700 ℃～1250 ℃ of temperature, material is interaction in the sintering oven of liner high alumina brick, generation transition reaction, constant temperature time 1～6 hour;

The sintering oven flue gas water spray washing that b, a step produce makes gas temperature drop to 30 ℃～40 ℃, and smoke content reduces to 0.02 gram/rice 3 ^～0.05 gram/rice ³After, as NaAlO ₂The CO that solution carbonation decomposes ₂The gas source of the gas;

C, boiling water dissolving sodium aluminate separates aluminum strip spare and is: after the agglomerate that step a is obtained is pulverized, hot water dissolving's sodium aluminate with boiling state, this hot water is the washing water of countercurrent washing nickel slag or washing aluminum hydroxide crystals, its consumption is a sintered material weight in grams number and the ratio 1: 2～10 of hot water volume milliliter number, temperature is the water boiling temperature, 0.5～2 hour time, same ratio hot water countercurrent washing 2～3 times of insoluble nickel slag;

D, nickel slag reducing-matting smelting condition are: nickel 2～3 times of enrichments in the nickel slag that the c step obtains claim rich nickel slag, with main composition FeS ₂Pyrite, main composition be CaSO ₄NH ₂The Gypsum Mine of O, wherein n=2 or 3, main composition CuFeS ₂Copper sulfide concentrate or main composition CuFeS ₂, NiSFeS the cupric sulfide nickel ore concentrate in any contains sulfur mineral and makes vulcanizing agent, be FeO-SiO with the smelting slag of copper smelting plant or nickel smeltery ₂-CaO type, or blowing slag 2FeOSiO ₂Any waste is made flux in the type, and so that any carries out matte smelting as reductive agent in charcoal, coal or the coke, ratio of components is: rich nickel slag: vulcanizing agent; Flux: reductive agent weight ratio=1: 0.1～0.3: 1～3: 0.02～0.05,1250 ℃～1400 ℃ of smelting temperatures, smelting time 1～2 hour;

E, the nickel matte Ni that the d step is obtained ₃S ₂-FeS-Ni-Fe alloy or copper nickel matte Cu ₂S-Ni ₃S ₂-FeS alloy is pressed copper, the traditional converting process in nickel smeltery, with SiO ₂As solvent blow Bessemer matte Ni ₃S ₂Or copper Bessemer matte Cu ₂S-Ni ₃S ₂-Cu-Ni alloy, the blowing slag returns the d operation and makes flux usefulness;

F, thick NaAlO ₂Solution desilicification method is: under 85 ℃～95 ℃ temperature, in c step gained solution, add the lime powder desiliconization, the milk of lime that lime consumption adds CaO 5～10 grams or prepares in this ratio adding in every liter of solution, stirring reaction 1～3 hour filters back hot wash white residue;

G, f step gained white residue is returned a operation, calculate by following reaction formula, and excessive respectively 10%-30% allocates Wingdale CaCO into ₃With sodium carbonate sintering again, to reclaim the contained Al of white residue ₂O ₃: ；

H, NaAlO ₂The solution carbonation decomposition method is: the smart NaAlO that the f step is obtained ₂Solution A l ₂O ₃Concentration is adjusted to 100 grams per liters～140 grams per liters, is heated to 60 ℃～80 ℃ in the carbonating groove, and 8～10 rev/mins of control chain type agitator speeds add aluminium hydroxide crystal seed, and add-on is Al in the solution ₂O ₃Al in content and the crystal seed ₂O ₃Ratio=1 of content: 1～1.5, blow the CO that blower fan obtains the b step with centrifugal ₂Content is 8%～14% clean air, is pressed in the groove by the bubbling hole of carbonating trench bottom, makes CO ₂Gas has contacted carbonation reaction with bubble form with solution, and temperature is by CO ₂The reaction heat that discharges with the NaOH neutralization reaction maintains 70 ℃～50 ℃, and 10～20 hours resolving times, aluminum hydroxide crystals is neutral with soft water or tap water countercurrent washing to washing lotion, and in 80 ℃～160 ℃ temperature oven dry, decomposition nut liquid contains Al ₂O ₃5 grams per liters～7 grams per liters are after the evaporation concentration, with dense Na ₂CO ₃The solution form is returned a operation and is made sintered material usefulness;

I, the aluminium hydroxide (Al that the h step is obtained ₂O ₃3H ₂O) press the traditional calcination method of aluminum oxide industry, in 1200 ℃ of temperature calcine anhydrous alumina (α-Al ₂O ₃).

2, the method from aluminium scrap base nickel-containing catalyst recovery nickel and aluminium according to claim 1 is characterized in that:

(1) described soda ash sintering transition condition is: the waste residue that the spent catalyst of spent catalyst after the pulverizing or nickeliferous, aluminium, molybdenum, vanadium extracts after molybdenum, the vanadium mixes with soda ash, soda ash is yellow soda ash, its consumption is spent catalyst or aforementioned waste residue: yellow soda ash weight ratio=1: 0.7～1.3,700 ℃～1250 ℃ of temperature, material is interaction in the sintering oven of liner high alumina brick, generation transition reaction, constant temperature time 1～6 hour;

(2) described boiling water dissolving sodium aluminate separation aluminum strip spare is, after the agglomerate that step a is obtained is pulverized, with boiling situation hot water dissolving sodium aluminate, this hot water is the washing water of countercurrent washing nickel slag or washing aluminum hydroxide crystals, its consumption is a sintered material weight in grams number and the ratio of hot water volume milliliter number is 1: 2～10, temperature is the water boiling temperature, 0.5～2 hour time, same ratio hot water countercurrent washing 2～3 times of nickel slag;

(3) described thick NaAlO ₂Solution desilicification method is: under 85 ℃～95 ℃ temperature, in the solution that the c step obtains, add the lime powder desiliconization, the milk of lime that lime consumption adds CaO5～10 grams or prepares in this ratio in every liter of solution, stirring reaction 1～3 hour filters back hot wash white residue;

(4) described NaAlO ₂The solution carbonation decomposition method is: the smart NaAlO that the f step is obtained ₂Solution A l ₂O ₃Concentration is adjusted to 100 grams per liters～140 grams per liters, is heated to 60 ℃～80 ℃ in the carbonating groove, is under 8～10 rev/mins of conditions at the chain type agitator speed, adds aluminium hydroxide crystal seed, and add-on is Al in the solution ₂O ₃Al in content and the crystal seed ₂O ₃Ratio=1 of content: 1～1.5, with the centrifugal blower fan that blows the CO that obtains by the b step ₂Content is 8%～14% clean air, is pressed in the groove by the bubbling hole of carbonating trench bottom, makes CO ₂Gas has contacted carbonation reaction with bubble form with solution, and temperature is by CO ₂The reaction heat that discharges with the NaOH neutralization reaction maintains 70 ℃～50 ℃, and resolving time 10-20 hour, it was neutral that aluminum hydroxide crystals is washed to washing lotion with soft water or tap water, and in 80 ℃～160 ℃ temperature oven dry, decomposition nut liquid contains Al ₂O ₃5 grams per liters～7 grams per liters are after the evaporation concentration, with dense Na ₂CO ₃The solution form is returned a operation and is made sintered material usefulness.

3, the method from aluminium scrap base nickel-containing catalyst recovery nickel and aluminium according to claim 1 is characterized in that:

(1) described nickel slag reducing-matting smelting condition: nickel enrichment 2-3 in the nickel slag that the c step obtains doubly is called rich nickel slag, with main composition FeS ₂Pyrite, main composition be CaSO ₄NH ₂The Gypsum Mine of O, wherein n=2 or 3, main composition CuFeS ₂Copper sulfide concentrate or main composition CuFeS ₂, NiSFeS the cupric sulfide nickel ore concentrate in any contains sulfur mineral and makes vulcanizing agent, with the smelting slag FeO-SiO of copper smelting plant or nickel smeltery ₂-CaO type or blowing slag 2FeOSiO ₂Any waste is made flux in the type, so that any carries out matte smelting as reductive agent in charcoal, coal or the coke, ratio of components is: rich nickel slag: vulcanizing agent: flux: reductive agent weight ratio=1: 0.1～0.3: 1～3: 0.02～0.05,1250 ℃～1400 ℃ of smelting temperatures, smelting time 1～2 hour;

(2) described nickel matte or copper nickel matte converting method are: the nickel matte Ni that the d step is obtained ₃S ₂-FeS-Ni-Fe alloy or copper nickel matte Cu ₂S-Ni ₃S ₂-FeS alloy is pressed copper, the traditional converting process in nickel smeltery, with quartzite SiO ₂Blow as flux and to obtain Bessemer matte Ni ₃S ₂Or copper Bessemer matte Cu ₂S-Ni ₃S ₂-Cu-Ni alloy, blowing slag 2FeOSiO ₂Type returns the d operation and makes smelting fusing agent usefulness.

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