CN1030563A - Extract the method and apparatus of chromium sesquioxide - Google Patents
Extract the method and apparatus of chromium sesquioxide Download PDFInfo
- Publication number
- CN1030563A CN1030563A CN 88103462 CN88103462A CN1030563A CN 1030563 A CN1030563 A CN 1030563A CN 88103462 CN88103462 CN 88103462 CN 88103462 A CN88103462 A CN 88103462A CN 1030563 A CN1030563 A CN 1030563A
- Authority
- CN
- China
- Prior art keywords
- extraction
- raw material
- catalyst
- carbonate
- ferrochrome
- 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.)
- Pending
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G37/00—Compounds of chromium
- C01G37/02—Oxides or hydrates thereof
Abstract
The invention provides a kind of extraction Cr
2O
3Method and apparatus, be characterized in earlier raw material being mixed with K, Na carbonate, again through fusing, water logging filter cleaner neutralization, reduction obtain Cr (OH)
3, fuse again and make.Its equipment mainly includes revolution calcining kiln, absorption reducing tower and process furnace.The present invention has technology, equipment, simple, with low cost, the high characteristics of byproduct saltcake purity that make.Can realize turning waste into wealth, bringing bigger economic results in society.Be specially adapted to useless ferrochrome catalyst or chromite and extract Cr
2O
3
Description
The invention belongs to the method and apparatus of the oxide compound that extracts chromium, be specially adapted to the utilization of useless ferrochrome catalyst.
Ferrochrome catalyst (claiming again conversion catalyst) is one of main catalyst of using of big small nitrogenous fertilizer plant, and national every annual consumption is ten thousand tons of 2-3 at present, with useless catalyst, is all filled out ditch when sanitary landfill, these catalyst contain Cr
2O
3Amount namely will have the Cr of 1400-4200 ton at 7-14% every year
2O
3The chromic anhydride of 2100-6000 ton (or be equivalent to) by jettisoning, is worth tens million of units.From resource is a waste greatly.From the social environment aspect, in these useless ferrochrome catalyst, existing quite a few Cr
2O
3Be converted into chromate.According to test, contained ferrochrome salt in the useless ferrochrome catalyst per ton can make ground or underground water contaminated exceed standard of 2-3 more than ten thousand tons not drink.In case and underground water contaminated be what be difficult to administer, misfortune and descendants.
In the past with containing Cr
2O
3Raw material such as chromite extract Cr
2O
3Method be, earlier with the same Na of raw material
2CO
3, the mixing such as dolomite, lime stone, under oxidizing atmosphere, fusing more than 1000 ℃ then, water logging is filtered, and uses H
2So
4Neutralization, again with liquid evaporation, dense H
2So
4Acidifying obtains Na
2Cr
2O
72H
2O, again acidifying fuse Cr
2O
3, its pair product is saltcake and NaHSo
4But this kind method Processes and apparatus is complicated, the cost height, and working condition is relatively poor, more can not realize extracting Cr from the ferrochrome catalyst
2O
3, because expense is high.
The object of the present invention is to provide a kind of extraction Cr of advantages of simple
2O
3Method and apparatus, the present invention is with low cost, can improve working conditions, and especially can extract Cr from conversion catalyst
2O
3
The technical essential of extracting method of the present invention is: what will crush earlier contains Cr
2O
3Raw material (such as ferrochrome catalyst or chromite etc.) and K, Na carbonate (be preferably Na
2CO
3) mix, in oxidizing atmosphere, fuse, fusing sintering temperature is 750-1300 ℃ (being preferably 900-1100 ℃), water logging filter cleaner then, the most handy hot water, with acid (such as HCl, HNo
3, H
3Po
4Deng, the most handy H
2SO
4), with the solution neutralization, remove Al(OH)
3The precipitation, surplus solution through reducing agent (such as sodium sulfite, sulfurous acid, Na
2S etc., the most handy SO
2) reduction (or reduce earlier neutralize afterwards) obtains Cr(OH)
3, again through 550-1200 ℃, be preferably 750-1000 ℃), heating obtains Cr under the nonoxidizing atmosphere again
2O
3, the reduction surplus solution can make saltcake through evaporating, concentrating and crystallizing.
The device of using the inventive method use is characterised in that: mainly include pulverizer revolution calcining kiln, water logging groove, water extracter, neutralizing well, absorption reducing tower and process furnace.
The present invention has the technology advantages of simple, and is with low cost, and the high characteristics of byproduct saltcake purity that make can realize turning waste into wealth, and eliminates environmental pollution, brings than the large economy social benefit, and it is low that equipment of the present invention also has a simple cost, characteristics such as good manufacturability.Be particularly suitable for extracting Cr with useless conversion catalyst or chromite
2O
3
Below be embodiments of the invention:
Embodiment 1:
Weigh and contain Cr
2O
37% useless conversion catalyst 100 grams add Na after grinding
2Co
325 grams, abundant mixing, in muffle furnace under oxidizing atmosphere in 1000 ℃ of molten burnings 40 minutes.Leach then, remove by filter quarrel, leaching liquid except that behind the aluminium, is used SO
2After the reduction thoroughly, filter, obtain Cr(OH)
3, filtrate obtains Na through evaporative crystallization
2SO
410H
2The O70 gram.Cr(OH)
3The drying roasting obtains Cr
2O
36.5 gram.Residual Cr in the quarrel
2O
3＜1%.
Embodiment 2:
Accompanying drawing is this device embodiment flow chart.
Among the figure, 1 is raw material, and 2 is rotary conveyor, and 3,6 is feeding machine, and 4 is ball mill, and 5 is lift, and 7 is rotary kiln, and 8 are the leaching pond, and 9 is boiler, and 10,16 is water extracter, and 11 is SO
2Producer, 12 is neutralization tank, and 13,14 is pump, and 15 is foam column, and 17 is electric furnace, 18 is salt cake pan.
Claims (9)
1, a kind of extraction Cr
2O
3Method, it is characterized in that the Cr that contains that will crush
2O
3Raw material mix with K, Na carbonate, roasting in oxidizing atmosphere, fusing sintering temperature are 750-1300 ℃, water logging filter cleaner then with the solution neutralization, is removed Al (OH) with acid
3, surplus solution obtains Cr (OH) through the reducing agent reduction
3, or reduce earlier and neutralize afterwards, heating obtains Cr under drying and the 550-1200 ℃ nonoxidizing atmosphere again
2O
3
2, extraction Cr according to claim 1
2O
3Method, it is characterized in that said K, Na carbonate are Na
2CO
3
3, extraction Cr according to claim 1
2O
3Method, it is characterized in that described fusing sintering temperature is preferably 900-1100 ℃.
4, extraction Cr according to claim 1
2O
3Method, it is characterized in that said reducing agent is SO
2
5, extraction Cr according to claim 1
2O
3Method, it is characterized in that said heating-up temperature is preferably 750-1000 ℃.
6, extraction Cr according to claim 1
2O
3Method, it is characterized in that said acid H
2SO
4
7, according to claim 1,2,3,4,5 or 6 described extraction Cr
2O
3Method, it is characterized in that the said Cr of containing
2O
3Raw material be useless ferrochrome catalyst or chromite.
8, a kind of claim 1,2,3,4,5, the employed device of 6 or 7 described methods is characterized in that mainly including pulverizer, revolution calcining kiln, water logging groove, water extracter, neutralizing well absorption reducing tower and process furnace.
9, device according to claim 8 is characterized in that including conveyor, feeding machine, ball mill, lift, rotary kiln, leaching pond, boiler, water extracter, SO
2Producer, neutralization tank, pump, foam column, electric furnace, salt cake pan.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88103462 CN1010677B (en) | 1988-06-04 | 1988-06-04 | Extract the method for chromium sesquioxide |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 88103462 CN1010677B (en) | 1988-06-04 | 1988-06-04 | Extract the method for chromium sesquioxide |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1030563A true CN1030563A (en) | 1989-01-25 |
| CN1010677B CN1010677B (en) | 1990-12-05 |
Family
ID=4832621
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 88103462 Expired CN1010677B (en) | 1988-06-04 | 1988-06-04 | Extract the method for chromium sesquioxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1010677B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100345768C (en) * | 2006-03-10 | 2007-10-31 | 锦州铁合金股份有限公司 | Method for treating chromium hydroxide |
| CN105543506A (en) * | 2016-02-19 | 2016-05-04 | 马桂文 | Method for producing high-purity chromium metal |
| CN112429776A (en) * | 2020-12-07 | 2021-03-02 | 乔柏人 | Process for producing chromic anhydride and ferrous oxalate by taking ferrochrome as raw material |
-
1988
- 1988-06-04 CN CN 88103462 patent/CN1010677B/en not_active Expired
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100345768C (en) * | 2006-03-10 | 2007-10-31 | 锦州铁合金股份有限公司 | Method for treating chromium hydroxide |
| CN105543506A (en) * | 2016-02-19 | 2016-05-04 | 马桂文 | Method for producing high-purity chromium metal |
| CN105543506B (en) * | 2016-02-19 | 2017-06-16 | 马桂文 | A kind of method for producing high-purity metal chromium |
| CN112429776A (en) * | 2020-12-07 | 2021-03-02 | 乔柏人 | Process for producing chromic anhydride and ferrous oxalate by taking ferrochrome as raw material |
| CN112429776B (en) * | 2020-12-07 | 2023-07-14 | 乔柏人 | Process for producing chromic anhydride and ferrous oxalate by taking ferrochrome as raw material |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1010677B (en) | 1990-12-05 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101265524B (en) | Method for extracting V2O5 from stone coal | |
| CN100482814C (en) | Extraction of vanadium and molybdenum compound from refused materials containing vanadium and molybdenum etc. multiple elements | |
| CN101274778B (en) | Method for extracting vanadic anhydride from stone coal | |
| CN102424412B (en) | Method of producing alumina from fly ash | |
| CN101134596A (en) | Technique for producing fine barium sulfate by barite sulfuric acid process | |
| CN103663511B (en) | HCl treatment coal ash for manufacturing is for the method for aluminum oxide | |
| CN103663510A (en) | Method for preparing aluminum oxide by using hydrochloric acid treatment coal ash | |
| CN109943713A (en) | A kind of leaching method of lepidolite ore | |
| CN102260801B (en) | Clean conversion method of stone coal | |
| CN208594131U (en) | A kind of waste acid resource system | |
| CN103993178A (en) | Method for recycling germanium from optical fiber wastes containing germanium | |
| CN1676461A (en) | Method for extracting iodine from rejected material generated during production of phosphor product from iodine-containing phosphorus ore | |
| CN1030563A (en) | Extract the method and apparatus of chromium sesquioxide | |
| CN101705377A (en) | Method for extracting vanadium from stone coal by wet-process enrichment and pyrogenic-process conversion | |
| CN104803403A (en) | Acid-alkali combined process for extracting alumina from coal-based solid waste through pre-desilication | |
| CN1254023A (en) | Leaching-out method for extracting vanadium from vanadium-containg ore calcines and its application in stone-coal calcination-direct vanadium-extracting process | |
| CN101289225A (en) | Novel process for preparing vanadic anhydride from firing residue of vanadium-containing stone coal | |
| CN108516569B (en) | Method for preparing lithium sulfate solution by roasting lepidolite | |
| CN102092725A (en) | Method for producing hydrate crystal silicon sodium titanate from waste strontium-barium glass | |
| CN105349778A (en) | Clean production method for recycling yellow phosphorus, iron oxide red and precious metal from ferrophosphorus | |
| CN111876597B (en) | Extraction of radioactive cause from molybdenite187Methods for Os | |
| CN108939822A (en) | A kind of method of phosphate fertilizer waste residue desulfurization and resource utilization | |
| CN111876617B (en) | Extraction of molybdenum, rhenium and radioactive origin187Methods for Os | |
| CN1118333A (en) | Process for extracting soluble non-sulfur potassium salt from feldspar | |
| CN106854701A (en) | A kind of silicon Rock coal containing alum water vapour charing pretreatment high prepares V2O5Method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C13 | Decision | ||
| GR02 | Examined patent application |