CN101543685A - Steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution - Google Patents
Steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution Download PDFInfo
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- CN101543685A CN101543685A CN200910301225A CN200910301225A CN101543685A CN 101543685 A CN101543685 A CN 101543685A CN 200910301225 A CN200910301225 A CN 200910301225A CN 200910301225 A CN200910301225 A CN 200910301225A CN 101543685 A CN101543685 A CN 101543685A
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- cobalt chloride
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Abstract
The invention relates to a steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution. A first heat exchanger, a second heat exchanger, a set of triple heat exchanger composed of three heat exchangers and a vacuum cooling system are added in the prior process. The steam is utilized at maximum extent, the enterprise production cost is saved and the outfall steam pollution is decreased.
Description
Technical field
The present invention relates to a kind of process for preparing steam utilization in the crystallization cobalt chloride process with cobalt chloride solution.
Background technology
As a kind of method that generally adopts, but the high purity water that produces in its process all do not obtain utilizing and directly effluxing, and caused the waste of the energy, has problem of environment pollution caused simultaneously yet in nickel cobalt hydrometallurgy cobalt chloride is produced in evaporation.
Summary of the invention
The purpose of this invention is to provide and a kind ofly prepare the process of steam utilization in the crystallization cobalt chloride process with cobalt chloride solution, this method can energy savings, reduces environmental pollution.
The technical solution used in the present invention is:
The process for preparing steam utilization in the crystallization cobalt chloride process with cobalt chloride solution, it is characterized in that at first cobalt chloride solution being pumped into the preceding liquid head tank of evaporation from evaporating preceding liquid storage tank, with the steam in first heat exchanger cobalt chloride solution in the liquid head tank before evaporating is preheated to 50-70 ℃, then the cobalt chloride solution after the preheating is put into evaporating kettle, feeding steam heats to the cobalt chloride solution in the evaporating kettle, evaporating kettle vacuum is-0.06-0MPa, temperature is 80-90 ℃, after evaporation finishes the cobalt chloride solution of remainder is put into to crystallization kettle and carries out the crystallization flow process; The steam condensate (SC) that the cobalt chloride solution of heating is used then enters into the second heat exchanger condensation, and condensed water enters the pure water storage tank, and heated cooling water enters sour molten workshop huge profit and uses; The steam that produces during the cobalt chloride solution evaporation enters into and carries out the heat exchange processing in first heat exchanger, condensed water enters into gas-liquid separator with remaining steam and carries out gas-liquid separation then, condensed water enters into the pure water storage tank, remaining steam then enters into three heat exchangers of being made up of three heat exchangers that are interconnected and carries out the steam condensation, condensed water enters the condensed water storage tank, is entering the distilled water storage tank then; The cooling water that is used for cooling steam enters sour molten workshop huge profit and uses after heating; Also not fully the steam residual air of condensation then enter vacuum system and cool off again, condensed water enters the pure water storage tank, the cooling water that is used to cool off enters sour molten workshop huge profit and uses after heating.
The present invention has increased by first heat exchanger, second heat exchanger, and three heat exchangers formed by three heat exchangers of cover, also increased a vacuum cooled system, original no steam is turned waste into wealth, saved the production cost of enterprise greatly, and the more important thing is to have reduced and efflux the pollution of steam environment.
The present invention is through after the above-mentioned process modification, liquid is increased to 60 ℃ by original room temperature (25 ℃) before the evaporation, 4.2kJ/kg ℃ of water specific heat capacity, average daily evaporation capacity 22m3, liquor capacity is evaporated to 8m3 by 22m3, and 90 ℃ of evaporating temperatures daily supply the 70 ℃ of hot water 100t in sour molten workshop, the heat of vaporization of water is 2260kJ/kg, can get and save evaporation steam every day:
Annual by 330 days, amount to the annual evaporation steam of saving
1.43×330＝471.9t
Reclaim evaporation water: 228=14t every day
Every day the recovered steam condensed water:
Every day, total high purity water 37.23t that reclaims was annual according to 330 days meters, amounted to and reclaimed pure water
37.23×330＝12285.9t。
The actual production Central Plains used pure water of extraction process makes by the pure water workshop.Pure water per ton need consume the 1.33t running water, and consumed power 3.76 kilowatt hours are discharged dense water (handling the higher water of back calcium ions and magnesium ions content) 0.096t.
Transform annual total the in back and save running water:
1.33×12285.9＝16340.2t
Annual saves energy:
3.76 * 12285.9=46194.984 kilowatt hour
The annual dense water of discharging that reduces:
0.096×12285.9＝1179.45t
Provide 70 ℃ of hot water of sour molten operation annual energy efficient:
4.2×103×100×330×(70-25)＝6.237×10
9kJ
The promptly annual steam of saving:
6.237×10
9÷(2260×103)＝2760t
Transform the total steam 3231.9t that saves in back, saves energy 46194.984 kilowatt hours are saved running water 16340.2t, reduce the dense water 1179.45t of discharging.
300,000 yuan of project implementation gross investments of the present invention, through actual trial run, 46194.984 kilowatt hours of can economizing on electricity in year are as calculated saved steam 3231.9t, save running water 16340.2t, reduce and discharge dense water 1179.45t.Production cost is reduced, and the consumption of power steam equal energy source descends obviously, and toxic emission reduces significantly, makes production environment obtain bigger improvement.
Description of drawings
Fig. 1 is a process chart of the present invention.
The specific embodiment
As shown in Figure 1, the process for preparing steam utilization in the crystallization cobalt chloride process with cobalt chloride solution of the present invention, at first cobalt chloride solution is pumped into the preceding liquid head tank of evaporation from evaporating preceding liquid storage tank, with the steam in first heat exchanger cobalt chloride solution in the liquid head tank before evaporating is preheated to 60 ℃, then the cobalt chloride solution after the preheating is put into evaporating kettle, feeding steam heats to the cobalt chloride solution in the evaporating kettle, evaporating kettle vacuum is-0.07MPa, temperature is 85 ℃, after evaporation finishes the cobalt chloride solution of remainder is put into to crystallization kettle and carries out the crystallization flow process; The steam condensate (SC) that the cobalt chloride solution of heating is used then enters into the second heat exchanger condensation, and condensed water enters the pure water storage tank, and heated cooling water enters sour molten workshop huge profit and uses; The steam that produces during the cobalt chloride solution evaporation enters into and carries out the heat exchange processing in first heat exchanger, condensed water enters into gas-liquid separator with remaining steam and carries out gas-liquid separation then, condensed water enters into the pure water storage tank, remaining steam then enters into three heat exchangers of being made up of three heat exchangers that are interconnected and carries out the steam condensation, condensed water enters the condensed water storage tank, is entering the distilled water storage tank then; The cooling water that is used for cooling steam enters sour molten workshop huge profit and uses after heating; Also not fully the steam residual air of condensation then enter vacuum system and cool off again, condensed water enters the pure water storage tank, the cooling water that is used to cool off enters sour molten workshop huge profit and uses after heating.
Claims (1)
- [claim 1] prepares the process of steam utilization in the crystallization cobalt chloride process with cobalt chloride solution, it is characterized in that at first cobalt chloride solution being pumped into the preceding liquid head tank of evaporation from evaporating preceding liquid storage tank, with the steam in first heat exchanger cobalt chloride solution in the liquid head tank before evaporating is preheated to 50-70 ℃, then the cobalt chloride solution after the preheating is put into evaporating kettle, feeding steam heats to the cobalt chloride solution in the evaporating kettle, evaporating kettle vacuum is-0.06-0MPa, temperature is 80-90 ℃, after evaporation finishes the cobalt chloride solution of remainder is put into to crystallization kettle and carries out the crystallization flow process; The steam condensate (SC) that the cobalt chloride solution of heating is used then enters into the second heat exchanger condensation, and condensed water enters the pure water storage tank, and heated cooling water enters sour molten workshop huge profit and uses; The steam that produces during the cobalt chloride solution evaporation enters into and carries out the heat exchange processing in first heat exchanger, condensed water enters into gas-liquid separator with remaining steam and carries out gas-liquid separation then, condensed water enters into the pure water storage tank, remaining steam then enters into three heat exchangers of being made up of three heat exchangers that are interconnected and carries out the steam condensation, condensed water enters the condensed water storage tank, is entering the distilled water storage tank then; The cooling water that is used for cooling steam enters sour molten workshop huge profit and uses after heating; Also not fully the steam residual air of condensation then enter vacuum system and cool off again, condensed water enters the pure water storage tank, the cooling water that is used to cool off enters sour molten workshop huge profit and uses after heating.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910301225XA CN101543685B (en) | 2009-03-30 | 2009-03-30 | Steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910301225XA CN101543685B (en) | 2009-03-30 | 2009-03-30 | Steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution |
Publications (2)
| Publication Number | Publication Date |
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| CN101543685A true CN101543685A (en) | 2009-09-30 |
| CN101543685B CN101543685B (en) | 2011-03-23 |
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| CN200910301225XA Expired - Fee Related CN101543685B (en) | 2009-03-30 | 2009-03-30 | Steam application technological process in the process for preparing the crystal cobalt chloride by cobalt chloride solution |
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103537114A (en) * | 2013-10-16 | 2014-01-29 | 科迈化工股份有限公司 | Crystal kettle device and method for controlling cooling speed of MBT (2- mercaptobenzothiazole) during production |
| CN106219573A (en) * | 2016-08-26 | 2016-12-14 | 海洲环保集团有限公司 | A kind of except scar salt production system |
| CN108675358A (en) * | 2018-07-17 | 2018-10-19 | 金川集团股份有限公司 | A kind of method for crystallising of cobalt chloride solution |
| CN108939601A (en) * | 2018-08-14 | 2018-12-07 | 徐晨 | A method of cobalt chloride is prepared by cobalt chloride solution evaporative crystallization |
Family Cites Families (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101041473A (en) * | 2006-03-16 | 2007-09-26 | 谷亮 | Method for preparation of waterless cobaltous chloride |
| JP2007298240A (en) * | 2006-05-01 | 2007-11-15 | Japan Steel Works Ltd:The | Triple effect absorption cold generation/output device |
| CN201010528Y (en) * | 2007-03-06 | 2008-01-23 | 天津市聚鑫源水处理技术开发有限公司 | Processing system for recycling ferrous chloride crystal and hydrochloric acid from hydrochloric acid waste liquid |
| CN100556811C (en) * | 2007-08-30 | 2009-11-04 | 内蒙古博源工程有限责任公司 | A kind of production method of low-salt dense soda ash and the system that produces low-salt dense soda ash thereof |
| CN100586866C (en) * | 2008-04-29 | 2010-02-03 | 江苏联海生物科技有限公司 | Method for extracting ferrous chloride, ferric trichloride, poly-ferric trichloride in waste acid of steel washing and plating |
-
2009
- 2009-03-30 CN CN200910301225XA patent/CN101543685B/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103537114A (en) * | 2013-10-16 | 2014-01-29 | 科迈化工股份有限公司 | Crystal kettle device and method for controlling cooling speed of MBT (2- mercaptobenzothiazole) during production |
| CN103537114B (en) * | 2013-10-16 | 2015-12-02 | 科迈化工股份有限公司 | Control the crystallization kettle device and method of lowering the temperature during accelerant MBT is produced |
| CN106219573A (en) * | 2016-08-26 | 2016-12-14 | 海洲环保集团有限公司 | A kind of except scar salt production system |
| CN108675358A (en) * | 2018-07-17 | 2018-10-19 | 金川集团股份有限公司 | A kind of method for crystallising of cobalt chloride solution |
| CN108939601A (en) * | 2018-08-14 | 2018-12-07 | 徐晨 | A method of cobalt chloride is prepared by cobalt chloride solution evaporative crystallization |
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| Publication number | Publication date |
|---|---|
| CN101543685B (en) | 2011-03-23 |
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