CN104930886A - Zinc hyperbaric oxygen leaching waste electrolyte heating method - Google Patents
Zinc hyperbaric oxygen leaching waste electrolyte heating method Download PDFInfo
- Publication number
- CN104930886A CN104930886A CN201510343574.3A CN201510343574A CN104930886A CN 104930886 A CN104930886 A CN 104930886A CN 201510343574 A CN201510343574 A CN 201510343574A CN 104930886 A CN104930886 A CN 104930886A
- Authority
- CN
- China
- Prior art keywords
- waste electrolyte
- pressure
- zinc
- heat exchanger
- steam
- 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
Abstract
The invention relates to a zinc hyperbaric oxygen leaching waste electrolyte heating method. The zinc hyperbaric oxygen leaching waste electrolyte heating method is characterized in that a spiral-plate heat exchanger is adopted for heating, a hot fluid is steam, a cold fluid is waste electrolyte, the pressure of waste electrolyte is higher than the working pressure of a zinc hyperbaric oxygen leaching reaction kettle, the steam pressure is higher than the pressure of the waste electrolyte, and the waste electrolyte is heated to be at the temperature higher than 70 DEG C. By the adoption of the method, the waste electrolyte is not leaked out, the maintenance amount of the heat exchanger on a station is reduced, the service life of the heat exchanger is quite prolonged, and the volume expansion of a system solution is not caused.
Description
Technical field
The invention belongs to field of hydrometallurgy, be specifically related to a kind of heating means of zinc pressure leaching waste electrolyte.
Background technology
In zinc pressure leaching process, adopt waste electrolyte directly to leach zinc sulfide concentrates, waste electrolyte has high temperature height corrodible property, and (temperature 35 ~ 40 DEG C, containing H
2sO
4150 ~ 200g/l), carry a part of solid anodes mud simultaneously secretly, due to the requirement of smelting process, waste electrolyte need be heated to more than 70 DEG C and enter reactor, because reactor general work pressure is 900 ~ 1200kpa, require that waste electrolyte is pressurized and be greater than reactor operating pressure.
Therefore, this waste electrolyte has HTHP height corrosion heat exchange characteristic, and the heat transmission equipment being generally used for waste electrolyte heating has plate type heat exchanger, tubular heat exchanger and spiral heat exchanger.The requirement of heat exchanger mainly contains three aspects: one is that requirement heat exchange efficiency is high, and two is the easy repair and maintenances of requirement, and three is requirement material corrosion resistances.It is simple that plate type heat exchanger has equipment, the features such as quick detachable cleaning, but the feature such as high voltage performance is poor, and tubular heat exchanger has structure and reliably not easily blocks, high pressure resistant, but equipment is huge.Spiral heat exchanger has the features such as heat exchange efficiency is high, high pressure resistant, therefore, generally mostly adopts spiral heat exchanger aborning.
The spiral heat exchanger adopted, structure is separated from each other helical duct, and cold fluid and hot fluid is with spiral template face for alternate flowing of conducting heat, and cold fluid and hot fluid passage can exchange use, to ensure that spiral plate hot and cold two sides thermal expansion and corrosion resistance are even, spiral plate service life can be extended.The material that current spiral heat exchanger adopts is 904L, SAF2507, titanium material, and after general spiral-plate heat exchanger is arranged on spent acid high-pressure pump, high pressure heat exchange, high-pressure pump can not corrode.But when waste electrolyte is heated to more than 70 DEG C, spiral plate material can produce hot spot, causes waste electrolyte to leak.Because do not allow waste electrolyte to leak in producing, therefore there is the spiral plate of hot spot to spiral heat exchanger frequent repair welding on station, once hot spot occurs in spiral plate deep, cannot repair welding on station, need integral replacing spiral plate, maintenance workload is large.
For the deficiency of spiral heat exchanger, graphite heat exchanger has been attempted in production, graphite heat exchanger mainly contains two aspect problems, although one is graphite material good corrosion resistance, but resistance to pressure is poor, before graphite heat exchanger can only be arranged on rotten sour high-pressure pump, low pressure heat exchange, waste electrolyte is heated to more than 70 DEG C, reactor is squeezed into again by high-pressure pump, high-pressure pump seriously corroded, the corrosion of spiral plate is equivalent to transfer to high-pressure pump, two is that graphite block has multiple hole runner, but aperture is less, the earth of positive pole easily blocks hole, cause graphite heat exchanger repair and maintenance workload large, the spiral plate corrosion that current production occurs, graphite block blocking and corresponding high-pressure pump etching problem have had a strong impact on the production run of zinc pressure leaching.
Summary of the invention
The present invention is by using the performance study of material 904L, SAF2507 and titanium material to spiral plate, discussion sulfuric acid concentration and temperature are to material corrosion impact, for 904L material, in sulfuric acid etc. corrosion rate curve display, the corrosion rate of 904L in variable concentrations sulfuric acid depends primarily on sulfuric acid temperature, namely contains H at waste electrolyte
2sO
4150 ~ 200g/l, waste electrolyte temperature is heated to more than 40 DEG C, 904L material corrosion aggravation, and to the waste electrolyte temperature do not heated 35 ~ 40 DEG C, 904L corrosion rate, within the scope of 0.1mm/a, is obviously corrosion resistant.Theoretical research and production reality all prove, adopt spiral plate material (904L, SAF2507, titanium material) as long as waste electrolyte temperature is heated to more than 40 DEG C, material corrosion aggravation, corrosion is inevitable, and corrosion occur in waste electrolyte side, with hot flow path steam pressure and temperature relation little.
Since corrosion is inevitable, so can only adopt new mode that waste electrolyte is not leaked, solve heat exchanger in producing simultaneously and need the problem often safeguarded, namely the present invention is conceived to this.
In current production, spiral heat exchanger uses hot fluid steam pressure to be low pressure 300 ~ 600kpa.Because steam pressure is lower than waste electrolyte pressure, waste electrolyte is easily caused to leak.And if traditional concept thinks that steam pressure is higher, a large amount of steam enters heat exchanger inside with high flow velocities, and in side, steam inlet, high velocity vapor can the strong erosion effect of output, the commissure intensity of spiral plate lower than material itself, easily by erosion.Opposite side waste electrolyte temperature can be very high, and sulfuric acid butt welded seam place also can produce strong corrosion.Therefore, think in the industry and adopt high pressure can make corrosion aggravation on the contrary, prior art adopts hot fluid steam pressure to be low pressure as far as possible, requirement is less than 600kpa, temperature is lower than 150 DEG C, to reduce the corrosion of waste electrolyte to spiral plate, abroad also have and adopt the normal pressure exhaust steam of flash process discharge as hot fluid to heat waste electrolyte.Its idea is all thought, low temperature and low pressure steam could reduce the corrosion of waste electrolyte to material as hot fluid, and this is also the reason always adopting in the industry low pressure.
But the present invention proves with test through theoretical, and above-mentioned traditional concept is also incorrect.In fact, adopt hot fluid steam pressure to be high pressure, make it higher than waste electrolyte pressure, be greater than the operating pressure 900 ~ 1200kpa of reactor, although also can corrosion be produced, greatly reduce the maintenance of heat exchanger on station.Concrete reason is as follows:
1) because steam pressure is higher than waste electrolyte pressure, once spiral plate has hot spot to produce, the waste electrolyte of leakage can be blown back by high steam, and import waste electrolyte fluid, finally enter reactor, waste electrolyte can not leak; But what is more important:
2) because high steam finally can bring the waste electrolyte of leakage into reactor, be equivalent to the centralized maintenance maintenance of a leak point being become multiple leak point, reduce the maintenance of heat exchanger on station, quite extend heat exchanger service life;
3) in addition, partial high pressure steam can enter in reactor with waste electrolyte in hot spot place, due to the characteristic of pressure vessel solution equilibria, high steam enters the moisture content of solution in reactor with waste electrolyte, pass through flash process, part can flash to again moisture content and take solution out of, can not cause System Solution volumetric expansion.
Accompanying drawing explanation
Fig. 1 and Fig. 2 is two kinds of heat exchange modes of the present invention.
Detailed description of the invention
The heating means of zinc pressure leaching waste electrolyte of the present invention, adopt spiral heat exchanger heating, hot fluid is steam, and cold fluid is waste electrolyte.Steam pressure higher than waste electrolyte pressure, the high 50 ~ 100kpa of preferred vapour pressure ratio waste electrolyte pressure.Heated by waste electrolyte to more than 70 DEG C, waste electrolyte pressure is greater than the operating pressure of zinc pressure leaching reactor.Waste electrolyte, before entering spiral heat exchanger, is first pressurized to through force (forcing) pump the operating pressure being greater than zinc pressure leaching reactor.
The present invention has two kinds of heat exchange mode: Fig. 1 to be that cold and hot fluid passage can exchange use, and high steam enters in the middle part of heat exchanger, is convenient to the maintenance of spiral plate on station; Fig. 2 cold and hot fluid passage cannot exchange use, and high steam enters from heat exchanger outside, is convenient to spiral plate and shifts out station maintenance.Operating procedure is as follows:
1) spiral heat exchanger waste electrolyte inlet valve 3 and outlet valve 4 is opened;
2) start spent acid high-pressure pump, pump into waste electrolyte and enter spiral heat exchanger;
3) open condensate drain outlet valve 2, open steam inlet valve 1, pass into steam;
4) open reactor waste electrolyte imported valve 5, entered reactor by heating waste electrolyte.
Claims (6)
1. the heating means of a zinc pressure leaching waste electrolyte, it is characterized in that adopting spiral heat exchanger heating, hot fluid is steam, cold fluid is waste electrolyte, waste electrolyte pressure is greater than the operating pressure of zinc pressure leaching reactor, waste electrolyte, higher than waste electrolyte pressure, is heated to more than 70 DEG C by steam pressure.
2. the heating means of zinc pressure leaching waste electrolyte according to claim 1, is characterized in that the high 50 ~ 100kpa of vapour pressure ratio waste electrolyte pressure.
3. the heating means of zinc pressure leaching waste electrolyte according to claim 1, is characterized in that waste electrolyte pressure is 1100 ~ 1400 kpa.
4. the heating means of zinc pressure leaching waste electrolyte according to claim 1, is characterized in that reactor operating pressure is 900 ~ 1200kpa.
5. the heating means of zinc pressure leaching waste electrolyte according to claim 1, is characterized in that waste electrolyte is before entering spiral heat exchanger, are first pressurized to through force (forcing) pump the operating pressure being greater than zinc pressure leaching reactor.
6. the heating means of zinc pressure leaching waste electrolyte according to claim 1, is characterized in that steam enters in the middle part of spiral heat exchanger, and cold and hot fluid passage capable of being exchanges and uses; Or steam enters from spiral heat exchanger outside, cold and hot fluid passage can not exchange use.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510343574.3A CN104930886A (en) | 2015-06-19 | 2015-06-19 | Zinc hyperbaric oxygen leaching waste electrolyte heating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510343574.3A CN104930886A (en) | 2015-06-19 | 2015-06-19 | Zinc hyperbaric oxygen leaching waste electrolyte heating method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN104930886A true CN104930886A (en) | 2015-09-23 |
Family
ID=54118165
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201510343574.3A Pending CN104930886A (en) | 2015-06-19 | 2015-06-19 | Zinc hyperbaric oxygen leaching waste electrolyte heating method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN104930886A (en) |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1119772A (en) * | 1964-12-07 | 1968-07-10 | Boliden Ab | Improvements in and relating to heat exchangers |
| CN2357306Y (en) * | 1999-03-23 | 2000-01-05 | 于明忠 | Boost efficient heat-exchanger |
| CN2773587Y (en) * | 2005-01-28 | 2006-04-19 | 杨有良 | Steam water mixed heater without noise |
| CN2775582Y (en) * | 2004-12-13 | 2006-04-26 | 北京普瑞林科贸发展有限公司 | Shock wave type super charged heat exchanger |
| CN202902907U (en) * | 2012-11-21 | 2013-04-24 | 长沙有色冶金设计研究院有限公司 | High-acid high-temperature high-pressure heat exchange system for waste electrolyte |
| JP2013170704A (en) * | 2012-02-17 | 2013-09-02 | Tlv Co Ltd | Heat exchanger |
-
2015
- 2015-06-19 CN CN201510343574.3A patent/CN104930886A/en active Pending
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1119772A (en) * | 1964-12-07 | 1968-07-10 | Boliden Ab | Improvements in and relating to heat exchangers |
| CN2357306Y (en) * | 1999-03-23 | 2000-01-05 | 于明忠 | Boost efficient heat-exchanger |
| CN2775582Y (en) * | 2004-12-13 | 2006-04-26 | 北京普瑞林科贸发展有限公司 | Shock wave type super charged heat exchanger |
| CN2773587Y (en) * | 2005-01-28 | 2006-04-19 | 杨有良 | Steam water mixed heater without noise |
| JP2013170704A (en) * | 2012-02-17 | 2013-09-02 | Tlv Co Ltd | Heat exchanger |
| CN202902907U (en) * | 2012-11-21 | 2013-04-24 | 长沙有色冶金设计研究院有限公司 | High-acid high-temperature high-pressure heat exchange system for waste electrolyte |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN105600855B (en) | A kind of seawater desalination system that vacuum chamber is formed using chemical reaction | |
| CN204202456U (en) | Asymmetric phase-change heat-exchanger | |
| CN104930886A (en) | Zinc hyperbaric oxygen leaching waste electrolyte heating method | |
| CN116815214A (en) | Electrolytic tank device and method | |
| CN204867784U (en) | Radiator welding equipment refrigeration cycle water system for transformer | |
| CN202254491U (en) | High temperature heat pump device for recovering waste heat of printing and dyeing wastewater | |
| CN207507218U (en) | NMP recovery pipe optimization systems in a kind of lithium battery production | |
| CN204342913U (en) | A kind of electroplating effluent cyclic utilization system | |
| CN212048878U (en) | Novel aboveground liquid sulfur storage facility | |
| CN214426469U (en) | Ionic membrane steam condensate recovery system | |
| CN210068419U (en) | Cooling water circulation vacuum unit | |
| CN202902907U (en) | High-acid high-temperature high-pressure heat exchange system for waste electrolyte | |
| CN104833243A (en) | Plastic heat exchanger for recovering waste heat of low-temperature smoke | |
| CN220767189U (en) | Electrolytic tank device | |
| CN205037794U (en) | Exempt from to wash plate heat exchanger | |
| CN207699696U (en) | Heat-exchange system in a kind of the PE electrolytic cells and slot of included exhaust system | |
| CN205747682U (en) | A kind of energy-saving steam heater system for air separation unit | |
| CN219792568U (en) | Semi-coke wastewater treatment device | |
| CN202304497U (en) | Sulfuric acid analyzing acid cooler | |
| CN208736214U (en) | A kind of distilled water return water reuse means | |
| CN219366382U (en) | Machine seal cooling water recycling system of liquid pump of ammonium polyphosphate device | |
| CN203518712U (en) | Heavy oil/heat transfer oil heat exchanger | |
| CN215522428U (en) | Sticky fluid treatment system | |
| CN213020485U (en) | Cooling system under special temperature control condition | |
| CN107638777A (en) | NMP recovery pipes optimization system in a kind of lithium battery production |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| RJ01 | Rejection of invention patent application after publication |
Application publication date: 20150923 |