CN202902907U - High-acid high-temperature high-pressure heat exchange system for waste electrolyte - Google Patents
High-acid high-temperature high-pressure heat exchange system for waste electrolyte Download PDFInfo
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- CN202902907U CN202902907U CN 201220618885 CN201220618885U CN202902907U CN 202902907 U CN202902907 U CN 202902907U CN 201220618885 CN201220618885 CN 201220618885 CN 201220618885 U CN201220618885 U CN 201220618885U CN 202902907 U CN202902907 U CN 202902907U
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- heat exchanger
- waste electrolyte
- spiral
- heat exchange
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Abstract
The utility model discloses a high-acid high-temperature high-pressure heat exchange system for waste electrolyte. The system comprises a spiral-plate-type heat exchanger made of 904L stainless steel plates or titanium materials, wherein the thickness of each plate is 4-5mm, an inlet at one end of the spiral-plate-type heat exchanger is communicated with a waste electrolyte storage tank through a pressing pump, and an inlet at the other end of the spiral-plate-type heat exchanger is communicated with a steam supply device. By means of the system, high-temperature and high-pressure heat exchange of the high-acid waste electrolyte is achieved.
Description
Technical field
The utility model relates to field of heat exchange equipment, and having provides a kind of waste electrolyte peracid HTHP heat-exchange system, can satisfy the service life of manufacturing technique requirent and prolongation heat exchanger.
Background technology
In the zinc concentrate direct leaching process, require waste electrolyte to be heated to entering reactor more than 70 ℃, to satisfy manufacturing technique requirent, waste electrolyte has the high etching characteristic of high temperature and (about 35～40 ℃ of temperature, contains H
2SO
4150～200g/l), carry simultaneously a part of solid anodes mud secretly, because reactor General Requirements operating pressure is 900～1200kPa, therefore, need solve two difficult problems to the waste electrolyte that adds reactor, the one, the waste electrolyte requirement temperature of being heated is high approximately 70 ℃, about 35 ℃ of the temperature difference, the 2nd, waste electrolyte requirement pressurized (approximately 1500kPa) just can enter reactor greater than the reactor operating pressure, this operating mode is different from traditional low-temp low-pressure waste electrolyte heat exchange mode (approximately 50 ℃ of temperature of heating, have a narrow range of temperature approximately 20 ℃, pressure low 300～600kPa), belong to the HTHP heat exchange, the problem that exists aborning is: (1) heat transfer effect is poor, and temperature does not reach and is heated requirement more than the waste electrolyte to 70 ℃; (2) earth of positive pole carried secretly of waste electrolyte is easily clogged heat transmission equipment, and the cleaning work amount is large; (3) the perishable leakage of heat transmission equipment material, maintenance workload is large.
The utility model content
For the deficiencies in the prior art, the utility model aims to provide a kind of waste electrolyte peracid HTHP heat-exchange system, can realize that by this system the waste electrolyte of overbased acidic carries out the HTHP heat exchange, and heat exchange efficiency is high.
For achieving the above object, the technical solution of the utility model is:
Waste electrolyte peracid HTHP heat-exchange system comprises spiral heat exchanger, and described spiral heat exchanger is the spiral heat exchanger that 904L stainless steel materials or titanium material are prepared from, and sheet metal thickness is 4mm-5mm; One end entrance of spiral heat exchanger is communicated with the waste electrolyte accumulator tank by force (forcing) pump, and other end entrance is communicated with steam providing apparatus.
The condensation-water drain caliber of described spiral heat exchanger is preferably 100mm-150mm.
The heat transmission equipment that is generally used for waste electrolyte heating has plate type heat exchanger, tubular heat exchanger and spiral heat exchanger, and it is simple that plate type heat exchanger has a device structure, quick detachable cleaning, and the heat exchange efficiency high, but board-like structure high voltage performance is poor; Tubular heat exchanger has the characteristics such as reliable in structure is difficult for clogging, high pressure resistant, but the tubular structure heat exchanger area is large, and equipment is huge; It is high that spiral heat exchanger has a heat exchange efficiency, and the characteristics such as high pressure resistant are selected spiral heat exchanger in the utility model.
The below makes further explanation the utility model:
1, adopt spiral heat exchanger, mainly rolled by a thin plate and form, consists of spaced-apart helical duct, cold fluid and hot fluid is alternate mobile as conducting heat take the spiral-shaped plate face, and the cold and hot fluid passage can Alternate.
2, design spiral sheet metal thickness is reasonable, is high pressure resistant 1500kPa, generally selects 4～5mm sheet material, and the welding material of paying special attention to the welding position can not be partially thin, prevents the possibility that the weakest welding portion leaks.
3, require equipment in the spiral heat exchanger production within certain service time, the cold and hot fluid passage is wanted Alternate, and is even to guarantee spiral plate hot and cold two sides thermal expansion and corrosion resistance, prolongs spiral plate service life.
4, according to waste electrolyte peracid HTHP heat transfer characteristic, prevent from or reduce waste electrolyte spiral sheet material is corroded, the spiral plate material is selected 904L stainless steel or titanium material.
5, design heat exchanger condensed water discharge pipe footpath is 100～150mm rationally, and condensed water discharge pipe is less than normal, condensed water is discharged not smooth, will reduce the heat exchange efficiency of heat exchanger.
6, in waste electrolyte, add FeSO
4Solution take the oxidation-reduction potential of control waste electrolyte rationally as 550～650mv, prevents or reduces waste electrolyte to the corrosiveness of spiral plate.
7, hot fluid steam pressure design load rationally is 300～600kPa, steam pressure is too high, a large amount of steam enters heat exchanger inside with high flow velocities, in the steam inlet side, the strong erosion effect of high velocity vapor meeting output, the commissure intensity of heat exchanger is lower than material itself, easily by erosion, opposite side waste electrolyte temperature may be very high, and sulfuric acid butt welded seam place also can produce strong row corrosion.Steam pressure is too low, and it is inadequate that hot fluid is brought heat into, can not satisfy the temperature requirement of heats cold fluid.
8, control advance the waste electrolyte temperature of heat exchanger can not too low (approximately 30 ℃), temperature is low will to keep the heat exchanger heat, the steam side flow that then adds increases, high-speed and high-temperature steam increases the erosion of equipment.
Compared with prior art, the utlity model has following advantage:
1, traditional waste electrolyte heat exchange is the low-temp low-pressure mode, and native system is the HTHP heat exchange, satisfies manufacturing technique requirent.
2, native system adopts special spiral plate special substance, controls simultaneously the measures such as waste electrolyte oxidation-reduction potential and steam inlet pressure, has greatly reduced the corrosion of spiral plate, has prolonged the service life of spiral plate type heat exchange.
Description of drawings:
Fig. 1 is waste electrolyte peracid HTHP heat-exchange system structural representation among the utility model embodiment;
Wherein, the 1st, steam inlet valve, the 2nd, condensate drain outlet valve, the 3rd, accumulator tank waste electrolyte outlet valve, the 4th, high-pressure pump imported valve, the 5th, high-pressure pump outlet valve, the 6th, the spiral heat exchanger inlet valve, the 7th, spiral heat exchanger outlet valve, the 8th, reactor waste electrolyte imported valve, the 9th, waste electrolyte accumulator tank, the 10th, spiral heat exchanger, the 11st, reactor, the 12nd, steam providing apparatus, the 13rd, force (forcing) pump.
The specific embodiment
Below in conjunction with drawings and Examples the utility model is described further.
Embodiment 1
Waste electrolyte peracid HTHP heat-exchange system comprises spiral heat exchanger 10, and described spiral heat exchanger 10 is the spiral heat exchanger that 904L stainless steel materials or titanium material are prepared from, and sheet metal thickness is 4mm-5mm; One end entrance of spiral heat exchanger 10 is communicated with waste electrolyte accumulator tank 9 by force (forcing) pump 13, and other end entrance is communicated with steam providing apparatus 12.The condensation-water drain caliber of described spiral heat exchanger is 100mm-150mm.
Working method:
1, opens condensate drain outlet valve 2, open steam inlet valve 1, pass into steam, control steam pressure 300～600kPa;
2, open spiral heat exchanger inlet valve 6 and spiral heat exchanger outlet valve 7;
3, in waste electrolyte, add FeSO
4Solution, take control waste electrolyte oxidation-reduction potential as 550～650mv; Open accumulator tank waste electrolyte outlet valve 3, opening high pressure pump discharge valve 5 and high-pressure pump imported valve 4 start high-pressure pump 13, waste electrolyte from waste electrolyte accumulator tank 9 by pumping in the spiral heat exchanger 10 after force (forcing) pump 13 pressurizations, be heated to 70 ℃, and be pressurized to 1500 kPa;
4, open reactor waste electrolyte imported valve 8, the waste electrolyte that is heated pressurization pumps into reactor 11.
Claims (2)
1. waste electrolyte peracid HTHP heat-exchange system comprises spiral heat exchanger, it is characterized in that, described spiral heat exchanger is the spiral heat exchanger that 904L stainless steel materials or titanium material are prepared from, and sheet metal thickness is 4mm-5mm; One end entrance of spiral heat exchanger is communicated with the waste electrolyte accumulator tank by force (forcing) pump, and other end entrance is communicated with steam providing apparatus.
2. described waste electrolyte peracid HTHP heat-exchange system according to claim 1 is characterized in that, the condensation-water drain caliber of described spiral heat exchanger is 100mm-150mm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220618885 CN202902907U (en) | 2012-11-21 | 2012-11-21 | High-acid high-temperature high-pressure heat exchange system for waste electrolyte |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201220618885 CN202902907U (en) | 2012-11-21 | 2012-11-21 | High-acid high-temperature high-pressure heat exchange system for waste electrolyte |
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| Publication Number | Publication Date |
|---|---|
| CN202902907U true CN202902907U (en) | 2013-04-24 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 201220618885 Expired - Fee Related CN202902907U (en) | 2012-11-21 | 2012-11-21 | High-acid high-temperature high-pressure heat exchange system for waste electrolyte |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104930886A (en) * | 2015-06-19 | 2015-09-23 | 长沙有色冶金设计研究院有限公司 | Zinc hyperbaric oxygen leaching waste electrolyte heating method |
-
2012
- 2012-11-21 CN CN 201220618885 patent/CN202902907U/en not_active Expired - Fee Related
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104930886A (en) * | 2015-06-19 | 2015-09-23 | 长沙有色冶金设计研究院有限公司 | Zinc hyperbaric oxygen leaching waste electrolyte heating method |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20130424 Termination date: 20191121 |
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| CF01 | Termination of patent right due to non-payment of annual fee |