CN104120486A - Composite wire separation process and equipment thereof - Google Patents
Composite wire separation process and equipment thereof Download PDFInfo
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- CN104120486A CN104120486A CN201410374513.9A CN201410374513A CN104120486A CN 104120486 A CN104120486 A CN 104120486A CN 201410374513 A CN201410374513 A CN 201410374513A CN 104120486 A CN104120486 A CN 104120486A
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Abstract
The invention relates to a composite wire separation process and equipment thereof, wherein the process comprises the following steps: separation: oxidizing and removing copper in the composite wire by using separation liquid containing ferric ions with the content of 40-50g/L to obtain metal fibers, wherein the temperature of the separation liquid is 80-90 ℃, and the content of hydrogen ions in the separation liquid is 0.5-1 g/L; (b) and (3) oxidation: oxidizing ferrous ions in the separated liquid after the step is finished into ferric ions by using an oxidizing agent; (c) and (3) extraction: extracting divalent copper ions in the separation liquid after the step (b) is finished into an organic phase and separating the organic phase from a water phase; (d) heating: the extracted water phase becomes separated liquid again after being heated. The equipment suitable for the above-mentioned line-closing separation process is formed from separation tank (1), oxidation tank (3), extraction box (4) and heating tank (2) which are successively unidirectionally connected, and formed into a circulation. The composite line separation process provided by the invention has continuous production and high separation speed; the separation effect is good, and the produced metal fiber is free from corrosion; no industrial pollution and environmental protection.
Description
Technical field
The present invention relates to a kind of complex line separating technology and equipment thereof.
Background technology
With boundling Hubbing method, produce steel fiber in recent years because Application Areas is constantly expanded, market demand increases year by year, and the widely used steel fiber in market is Stainless Steel Fibre and iron-chromium-aluminum.With boundling Hubbing method, producing in the technique of steel fiber, first after metal wire material, isolated material, coating material boundling through repeatedly producing complex line after tube reducing drawing and annealing, then will the isolated material in complex line and coating material remove after manufacture steel fiber.Complex line continuous separation technology is the conventional process of producing high-quality steel fiber, existing complex line continuous separation technology is all to adopt electrochemical electrolysis technique, copper in complex line is transferred to negative electrode by the method for electrolysis, thereby reach the object that the copper in complex line is removed, this technique is because needs are using complex line as anode, electric current need to pass through from complex line, complex line is contact conduction under mobile status, high electric current can burn out conductive contact and complex line, cause electrolytic current density low, so electrochemical electrolysis process yields is low.Complex line in electrolytic process because metal wire material scatters gradually, conduction between metal wire material is also inhomogeneous, and the pole span of anode and cathode is also inhomogeneous, the first electrolysis of metal wire material that pole span is near, so cause the inhomogeneous quality product that affects steel fiber of complex line electrolysis.The anode of electrochemical electrolysis technique is that complex line is linear, and the electrolytic copper on negative plate can form copper post or copper knurl, if cleaning can be hung up complex line not in time, needs often to shut down cleaning copper post and copper knurl, thereby reduces steel fiber output.The electrolytic copper outward appearance unfairness of the production on negative plate, has reduced the quality of electrolytic copper.Electrolytic copper is produced to need to shut down after a certain amount of and is taken out electrolytic copper, also can reduce the output of steel fiber.
Summary of the invention
The object of the invention is to solve the yielding poorly of steel fiber in above-mentioned complex line separating technology, the problem that of poor quality and continuous production is not high.
For achieving the above object, the present invention adopts a kind of complex line separating technology, comprise the following steps: (a) separation: use and to contain the copper that parting liquid oxidation that content is the ferric ion of 40-50 g/L removes in complex line and obtain steel fiber, the temperature of parting liquid is 80-90 ℃, and in parting liquid, hydrionic content is 0.5-1 g/L; (b) oxidation: use the oxidation of divalent iron ion in the parting liquid after oxygenant completes step (a) to become ferric ion; (c) extraction: in the parting liquid after step (b) is completed, bivalent cupric ion is extracted into organic phase also and aqueous phase separation; (d) heating: the water after extraction again becomes parting liquid after heating.
Further, the organic phase after described extraction obtains copper through back extraction, electrodeposition again.
Further, the balance anion preferably sulfuric acid radical ion in described parting liquid.
Further, in described parting liquid, ferrous ion content is that 1-10 g/L, bivalent cupric ion content are 1-15 g/L.
Further, the oxygenant in described step (b) is hydrogen peroxide, ozone, pure oxygen, air, preferably hydrogen peroxide.
The present invention also provides a kind of equipment that is applicable to above-mentioned complex line separating technology, separator tank, oxidation trough, extraction box and heating tank, consists of, and separator tank, oxidation trough, extraction box and heating tank be unidirectional connection formation circulation successively.
Further, connect back extraction case and Winning cell on the extraction box of aforesaid device, wherein back extraction case is two-way connection and all formation circulations with extraction box, Winning cell.
Ferric ion in described parting liquid makes the copper in complex line be oxidized to bivalent cupric ion, ferric ion is reduced into ferrous ion simultaneously, in oxidation trough, with hydrogen peroxide, oxidation of divalent iron ion is become to ferric ion, and isolate bivalent cupric ion in extraction box is used extraction agent, the solution process heating tank heating of ferric ion comes back to separator tank becomes parting liquid.
After extraction, bivalent cupric ion is present in the organic phase of extraction box; In back extraction case, run into the acid of high density, the regeneration of extraction agent and hydrogen recombine, reenters extraction box for extraction, and bivalent cupric ion reenters and in water, flows into Winning cell; At Winning cell electrolytic deposition copper, produce oxygen and hydrogen ion simultaneously, hydrogen ion enters back extraction case again for back extraction.
Described be separated into continuous separate from, in the oxidizing reaction in oxidation trough and extraction box, the extraction of bivalent cupric ion can not carried out thoroughly, thus in parting liquid also containing ferrous ion: 1-10 g/L, bivalent cupric ion: 1-15 g/L.
Isolated material, coating material in the technique of boundling Hubbing method production steel fiber are usually selected copper, for oxidation, remove copper, and in complex line, the resistance of oxidation of metal wire material need be stronger than copper, and conventional material is stainless steel and ferrum-chromium-aluminum.
Beneficial effect of the present invention is: complex line separating technology is produced continuously, and velocity of separation is fast; Good separating effect, the steel fiber of production is corrosion-free; Without industrial pollution, environmental protection.The production having solved in Electrochemical separation technique is discontinuous, and production yields poorly, and needs to shut down cleaning electrolytic copper, the problems such as part metals fiber electrolytic corrosion.
Accompanying drawing explanation
Fig. 1: the device schematic diagram of implementing technique of the present invention.
In figure: 1, separator tank, 2, heating tank, 3, oxidation trough, 4, extraction box, 5, back extraction case, 6, Winning cell, 7, complex line, 8, steel fiber.
Embodiment
Below in conjunction with accompanying drawing, comparative example and embodiment, feature of the present invention and technique effect are described, but the invention is not restricted to specific embodiment.Extraction agent described in embodiment is the peaceful copper extractant Lix984N of (Cognis) company of Dutch section; Only length is different for the size of embodiment and separator tank described in comparative example, and in separator tank, the number of complex line is 24.
comparative example:
Use electrochemical electrolysis separation to remove copper, separated flute length 120 m, hydrogen ion content 0.5 g/L in electrolytic solution, ferrous ion content 12 g/L bivalent cupric ion content 13 g/L, balance anion is sulfate ion; DC electrolysis voltage 2 V.Complex line enters separator tank by the speed of 0.65 m/min, on average produces steel fiber 60 kg daily.
embodiment 1:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 50 g/L, hydrogen ion content 1 g/L, 85 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 1.04 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 47 g/L, ferrous ion content 3 g/L, and content of copper ion 4 g/L, hydrogen ion content 1 g/L, 85 ℃ of parting liquid temperature, on average produce steel fiber 100 kg daily.
embodiment 2:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 42 g/L, hydrogen ion content 1 g/L, 80 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 1.15 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 40 g/L, ferrous ion content 10 g/L, and content of copper ion 10 g/L, hydrogen ion content 1 g/L, 80 ℃ of parting liquid temperature, on average produce steel fiber 80 kg daily.
embodiment 3:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 50 g/L, hydrogen ion content 1 g/L, 85 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 1.4 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 44 g/L, ferrous ion content 11 g/L, and content of copper ion 15 g/L, hydrogen ion content 1 g/L, 85 ℃ of parting liquid temperature, on average produce steel fiber 135 kg daily.
embodiment 4:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 45 g/L, hydrogen ion content 0.5 g/L, 80 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 1.3 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 42 g/L, ferrous ion content 5 g/L, and content of copper ion 6 g/L, hydrogen ion content 0.5 g/L, 80 ℃ of parting liquid temperature, on average produce steel fiber 125 kg daily.
embodiment 5:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 48 g/L, hydrogen ion content 0.5 g/L, 80 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 1.33 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 46 g/L, ferrous ion content 6 g/L, and content of copper ion 7 g/L, hydrogen ion content 0.5 g/L, 80 ℃ of parting liquid temperature, on average produce steel fiber 130 kg daily.
embodiment 6:
Long 55 m of separator tank 1, separator tank 1 starting soln is ferric sulfate and sulfuric acid, ferric ion content 50 g/L, hydrogen ion content 0.5 g/L, 90 ℃ of parting liquid temperature, complex line 7 enters separator tank 1 by the speed of 2.08 m/min, and the copper in complex line 7 reacts generation copper sulfate and ferrous sulfate with the ferric sulfate in parting liquid, and the whole removals of copper in complex line 7 just become steel fiber 8.The parting liquid of separator tank 1 enters oxidation trough 3, and solution composition is ferric sulfate, ferrous sulfate, copper sulfate, sulfuric acid, with hydrogen peroxide, ferrous sulfate is oxidized to ferric sulfate, and the solution after oxidation enters extraction box 4.Extraction agent in extraction box 4 is combined with bivalent cupric ion, the bivalent cupric ion of organic phase and aqueous phase separation; Water enters and again flows into separator tank 1 after heating tank 2 heating and become parting liquid, and the bivalent cupric ion in organic phase enters back extraction case 5.Sulfuric acid in back extraction case 5 enters water by bivalent cupric ion back extraction to be become copper-bath and enters Winning cell 6, and the extractant regeneration of organic phase reenters extraction box 4 simultaneously.Copper-bath enters Winning cell 6 electrolytic depositions and obtains copper, oxygen and sulfuric acid, and sulfuric acid comes back to back extraction case 5 for back extraction.Whole technique is moved continuously, and the parting liquid composition of stable rear separator tank 1 is ferric ion content 48 g/L, ferrous ion 5 g/L, and cupric ion 6 g/L, hydrogen ion content 0.8 g/L, 90 ℃ of parting liquid temperature, on average produce steel fiber 185 kg daily.
Claims (7)
1. a complex line separating technology, it is characterized in that comprising the following steps: (a) separation: use and to contain the copper that parting liquid oxidation that content is the ferric ion of 40-50 g/L removes in complex line and obtain steel fiber, the temperature of parting liquid is 80-90 ℃, and in parting liquid, hydrionic content is 0.5-1 g/L; (b) oxidation: use the oxidation of divalent iron ion in the parting liquid after oxygenant completes step (a) to become ferric ion; (c) extraction: in the parting liquid after step (b) is completed, bivalent cupric ion is extracted into organic phase also and aqueous phase separation; (d) heating: the water after extraction again becomes parting liquid after heating.
2. complex line separating technology as claimed in claim 1, is characterized in that the organic phase after described extraction obtains copper through back extraction, electrodeposition again.
3. complex line separating technology as claimed in claim 1 or 2, is characterized in that the balance anion preferably sulfuric acid radical ion in described parting liquid.
4. complex line separating technology as claimed in claim 1 or 2, is characterized in that in described parting liquid, ferrous ion content is that 1-10 g/L, bivalent cupric ion content are 1-15 g/L.
5. complex line separating technology as claimed in claim 1 or 2, is characterized in that the oxygenant in described step (b) is hydrogen peroxide, ozone, pure oxygen, air, preferably hydrogen peroxide.
6. an equipment that is applicable to complex line separating technology described in claim 1, it is characterized in that being comprised of separator tank (1), oxidation trough (3), extraction box (4) and heating tank (2), separator tank (1), oxidation trough (3), extraction box (4), heating tank (2) be unidirectional connection formation circulation successively.
7. the equipment of complex line separating technology as claimed in claim 6, characterized by further comprising back extraction case (5) and Winning cell (6), and back extraction case (5) is two-way connection and all formation circulations with extraction box (4), Winning cell (6).
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107513792A (en) * | 2017-07-07 | 2017-12-26 | 湖南汇博金属材料有限责任公司 | A kind of metal fiber cloth and its preparation method and application |
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| US5993635A (en) * | 1995-03-22 | 1999-11-30 | M.I.M. Holdings Limited | Atmospheric mineral leaching process |
| CN1900345A (en) * | 2006-07-21 | 2007-01-24 | 周建华 | Metal fiber wire and its producing process |
| CN101220449A (en) * | 2008-01-25 | 2008-07-16 | 湖南惠同新材料股份有限公司 | Fire resistant iron chromium aluminum filament and production technique |
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| CN104120486B (en) | 2017-06-16 |
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