CN219709553U - Jet-cavitation gold concentrate powder cyanide leaching gold extraction production device - Google Patents
Jet-cavitation gold concentrate powder cyanide leaching gold extraction production device Download PDFInfo
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- CN219709553U CN219709553U CN202321277694.4U CN202321277694U CN219709553U CN 219709553 U CN219709553 U CN 219709553U CN 202321277694 U CN202321277694 U CN 202321277694U CN 219709553 U CN219709553 U CN 219709553U
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- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 title claims abstract description 183
- 239000010931 gold Substances 0.000 title claims abstract description 101
- PCHJSUWPFVWCPO-UHFFFAOYSA-N gold Chemical compound [Au] PCHJSUWPFVWCPO-UHFFFAOYSA-N 0.000 title claims abstract description 98
- 229910052737 gold Inorganic materials 0.000 title claims abstract description 98
- 239000012141 concentrate Substances 0.000 title claims abstract description 78
- 239000000843 powder Substances 0.000 title claims abstract description 77
- 238000002386 leaching Methods 0.000 title claims abstract description 73
- 238000000605 extraction Methods 0.000 title claims abstract description 37
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 26
- 239000007788 liquid Substances 0.000 claims abstract description 484
- 238000005406 washing Methods 0.000 claims abstract description 268
- 238000002156 mixing Methods 0.000 claims abstract description 165
- 230000007246 mechanism Effects 0.000 claims abstract description 142
- 238000006243 chemical reaction Methods 0.000 claims abstract description 113
- HCHKCACWOHOZIP-UHFFFAOYSA-N Zinc Chemical compound [Zn] HCHKCACWOHOZIP-UHFFFAOYSA-N 0.000 claims abstract description 95
- 230000032683 aging Effects 0.000 claims abstract description 65
- 239000002002 slurry Substances 0.000 claims description 184
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 134
- 239000001301 oxygen Substances 0.000 claims description 134
- 229910052760 oxygen Inorganic materials 0.000 claims description 134
- 239000002893 slag Substances 0.000 claims description 120
- 239000012530 fluid Substances 0.000 claims description 68
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 63
- 239000000706 filtrate Substances 0.000 claims description 57
- 239000000243 solution Substances 0.000 claims description 53
- 239000007789 gas Substances 0.000 claims description 52
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 38
- 238000007599 discharging Methods 0.000 claims description 36
- KXZJHVJKXJLBKO-UHFFFAOYSA-N chembl1408157 Chemical compound N=1C2=CC=CC=C2C(C(=O)O)=CC=1C1=CC=C(O)C=C1 KXZJHVJKXJLBKO-UHFFFAOYSA-N 0.000 claims description 31
- 238000001914 filtration Methods 0.000 claims description 26
- 238000003756 stirring Methods 0.000 claims description 25
- 238000006073 displacement reaction Methods 0.000 claims description 20
- 230000000295 complement effect Effects 0.000 claims description 19
- 239000007921 spray Substances 0.000 claims description 19
- 239000011259 mixed solution Substances 0.000 claims description 15
- 238000011084 recovery Methods 0.000 claims description 15
- 230000000153 supplemental effect Effects 0.000 claims description 14
- 229940046892 lead acetate Drugs 0.000 claims description 12
- 239000002562 thickening agent Substances 0.000 claims description 9
- 239000002994 raw material Substances 0.000 claims description 6
- 239000000945 filler Substances 0.000 claims description 4
- 239000002912 waste gas Substances 0.000 claims description 3
- 238000012546 transfer Methods 0.000 abstract description 20
- 239000007787 solid Substances 0.000 abstract description 11
- 230000035484 reaction time Effects 0.000 abstract description 4
- 238000009854 hydrometallurgy Methods 0.000 abstract description 2
- 239000000463 material Substances 0.000 description 38
- 230000014759 maintenance of location Effects 0.000 description 25
- 238000000034 method Methods 0.000 description 15
- 239000012065 filter cake Substances 0.000 description 11
- 230000005484 gravity Effects 0.000 description 10
- 238000007333 cyanation reaction Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 230000009471 action Effects 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- MXZVHYUSLJAVOE-UHFFFAOYSA-N gold(3+);tricyanide Chemical compound [Au+3].N#[C-].N#[C-].N#[C-] MXZVHYUSLJAVOE-UHFFFAOYSA-N 0.000 description 5
- 239000002184 metal Substances 0.000 description 4
- 229910052751 metal Inorganic materials 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 3
- 238000002791 soaking Methods 0.000 description 3
- 238000009792 diffusion process Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000005507 spraying Methods 0.000 description 2
- 238000005728 strengthening Methods 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000002925 chemical effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 239000006194 liquid suspension Substances 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 150000002978 peroxides Chemical class 0.000 description 1
- 238000005381 potential energy Methods 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000035939 shock Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052725 zinc Inorganic materials 0.000 description 1
- 239000011701 zinc Substances 0.000 description 1
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Abstract
Jet-cavitation concentrate powder cyanide leaching gold extraction production device, which belongs to the technical field of gold extraction in hydrometallurgy; comprises a size mixing tank mechanism, a jet flow cyanidation tubular reactor mechanism, a jet flow cyanidation reaction tower mechanism, a jet flow cyanidation supplementary reactor mechanism, a three-layer washing and concentrating mechanism I, a cavitation cyanidation mechanism, an airflow cavitation cyanidation tubular reactor mechanism, an ageing tank mechanism, a three-layer washing and concentrating mechanism II, a noble liquid tank mechanism, a deoxidizing tower mechanism and a zinc powder mixing and replacing tank mechanism; the cavitation reactor and the jet reactor can form a sufficient gas-liquid (solid) mixing zone, so that heat transfer, mass transfer and momentum transfer are effectively promoted, the reaction is further enhanced, and the reaction rate and the product yield are improved; the utility model has advanced equipment, continuous operation and high automation degree, shortens the cyanidation reaction time and improves the production efficiency.
Description
Technical Field
The utility model belongs to the technical field of gold extraction in hydrometallurgy, and particularly relates to a jet-cavitation gold concentrate powder cyanide leaching gold extraction production device.
Background
The cyanide gold extraction method is the most important gold extraction method at present due to the characteristics of mature process, high cyanide leaching rate, low cost and the like; while the cyanidation leaching technique has advantages, there is still room for improvement, such as: the cyanide leaching time is shortened, the cyanide consumption is reduced, and the like; therefore, people develop extensive researches on the aspects of strengthening the cyanide gold leaching technology and the like so as to improve the leaching rate of the cyanide gold extraction. Several significant new advances have been made in this regard. Such as using pure oxygen instead of compressed air, peroxide assisted leaching, etc.; the methods all improve the concentration of dissolved oxygen in ore pulp and the utilization rate of active oxygen to different degrees, quicken the leaching speed of gold, improve the selectivity of leaching reaction, and consequently reduce cyanide consumption, thereby improving the leaching rate of gold, saving investment and reducing production cost. Most of cyanide leaching equipment is an open reaction kettle and the like, and the quantity of the cyanide equipment is large, the occupied area is large, the material consumption and the energy consumption are high, the heat transfer and mass transfer efficiency is low, the operation units are large, the reaction period is long, and the labor cost is high; the increase of the energy consumption and the material consumption in the cyanide gold extraction process leads to the rise of cost, which is unfavorable for industrial production.
The field is eagerly searching for a low-energy-consumption and environment-friendly cyanide gold extraction process and equipment, which can overcome the technical problems.
Disclosure of Invention
The utility model aims to provide a jet-cavitation gold concentrate powder cyanide leaching gold extraction production device. The jet reactor is used for the cyanation reaction, and the cavitation reactor is used for the cyanation reaction, so that the cavitation reactor and the jet reactor can form a sufficient gas-liquid (solid) mixing zone, thereby effectively promoting heat transfer, mass transfer and momentum transfer, further strengthening the reaction and improving the reaction rate and the product yield; the utility model has mature process, advanced equipment, continuous operation and high automation degree, shortens the cyanidation reaction time and improves the production efficiency.
In order to achieve the above purpose, the present utility model adopts the following technical scheme:
the jet-cavitation refined gold mineral powder cyanide leaching gold extraction production device comprises a size mixing tank mechanism, a jet cyanidation tubular reactor mechanism, a jet cyanidation reaction tower mechanism, a jet cyanidation supplementary reactor mechanism, a three-layer washing and concentration mechanism I, a cavitation cyanidation mechanism, an airflow cavitation cyanidation tubular reactor mechanism, an aging tank mechanism, a three-layer washing and concentration mechanism II, a noble liquid tank mechanism, a deoxidization tower mechanism and a zinc powder mixing and replacing tank mechanism; the slurry mixing tank mechanism is sequentially connected with the jet flow cyanidation tubular reactor mechanism, the jet flow cyanidation reaction tower mechanism, the jet flow cyanidation supplementary reactor mechanism and the three-layer washing and concentrating mechanism I, the three-layer washing and concentrating mechanism I is respectively connected with the noble liquid tank mechanism and the cavitation cyanidation mechanism, the noble liquid tank mechanism is sequentially connected with the deoxidizing tower mechanism and the zinc powder mixing and replacing tank, the cavitation cyanidation mechanism is sequentially connected with the aging tank mechanism and the three-layer washing and concentrating mechanism II, and the three-layer washing and concentrating mechanism II is connected with the three-layer washing and concentrating mechanism I.
The slurry mixing tank mechanism comprises a slurry mixing tank, wherein a raw material inlet of the slurry mixing tank is connected with a raw material outlet of a spiral feeder of the slurry mixing tank, gold concentrate powder is fed into the slurry mixing tank through the spiral feeder of the slurry mixing tank, a mechanical stirrer of the slurry mixing tank is arranged in the slurry mixing tank, and a liquid inlet is arranged at the top of the slurry mixing tank and used for introducing sodium cyanide solution, sodium hydroxide solution and treated lean liquid; the size mixing tank is used for mixing the gold concentrate powder, the sodium cyanide solution, the sodium hydroxide solution and the treated lean solution into slurry under the stirring of a mechanical stirrer of the size mixing tank.
The jet flow cyanide tube reactor mechanism comprises a jet flow cyanide tube reactor power fluid pump box and an oxygen buffer tank, wherein a slurry inlet of the jet flow cyanide tube reactor power fluid pump box is connected with a slurry outlet of a slurry mixing tank body, a slurry outlet of the jet flow cyanide tube reactor power fluid pump box is connected with a slurry inlet of the jet flow cyanide tube reactor power fluid pump, a slurry outlet of the jet flow cyanide tube reactor power fluid pump is connected with a slurry inlet of a jet flow cyanide tube reactor coupler, a slurry outlet of the jet flow cyanide tube reactor coupler is connected with a slurry inlet of a jet flow cyanide tube reactor, a slurry outlet of the jet flow cyanide tube reactor is connected with a slurry inlet of the jet flow cyanide tube reactor, a jet flow cyanide tube reactor turbulence element is arranged in the jet flow cyanide tube reactor, an oxygen buffer tank top is provided with an oxygen recovery inlet and a fresh oxygen inlet, an oxygen outlet of the oxygen buffer tank is respectively connected with a jet flow cyanide reactor coupler, a jet flow cyanide tube reactor coupler and a gas inlet of a cavitation machine high-pressure oxygen compressor of a cavitation machine, and the jet flow cyanide tube reactor is used for extracting gold concentrate, sodium hydroxide, sodium cyanide and gold leaching solution.
The jet flow cyanidation reaction tower mechanism comprises a jet flow cyanidation reaction tower, a mixed liquid inlet at the bottom of the jet flow cyanidation reaction tower is connected with a mixed liquid outlet of the jet flow cyanidation tubular reactor, so that cyanidation mixed liquid coming out of the jet flow cyanidation tubular reactor enters the jet flow cyanidation reaction tower, a mixed liquid outlet at the bottom of the jet flow cyanidation reaction tower is connected with a mixed liquid inlet of a jet flow cyanidation reaction tower power fluid pump box, the jet flow cyanidation reaction tower power fluid pump box is respectively connected with a jet flow cyanidation reaction tower coupler and a jet flow cyanidation reaction tower spray header mixed liquid inlet through a jet flow cyanidation reaction tower power fluid pump and a pipeline, jet flow cyanidation reaction tower ejectors are arranged around the jet flow cyanidation reaction tower coupler, and a jet flow cyanidation reaction tower demister is arranged in the jet flow cyanidation reaction tower at the top of the jet flow cyanidation reaction tower spray header, and the jet flow cyanidation reaction tower is used for carrying out cyanidation leaching and extracting gold continuously.
The jet flow cyanidation supplementary reactor mechanism comprises a jet flow cyanidation supplementary reactor, an oxygen outlet at the top of the jet flow cyanidation supplementary reactor is connected with an oxygen recovery system, an overflow outlet at the top of the jet flow cyanidation reaction tower is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor coupler through a pipeline, an oxygen escape outlet at the top of the jet flow cyanidation supplementary reactor is connected with an oxygen inlet of a jet flow cyanidation supplementary reactor coupler, a mixed liquor outlet at the bottom of the jet flow cyanidation supplementary reactor is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor power fluid pump box, a mixed liquor outlet of the jet flow cyanidation supplementary reactor power fluid pump box is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor coupler through a jet flow cyanidation supplementary reactor discharging pump and a pipeline, and the jet flow cyanidation supplementary reactor coupler is positioned in the jet flow cyanidation supplementary reactor, and the jet flow cyanidation supplementary reactor discharging pump box mixed liquor outlet is connected with a mixed liquor inlet of a three-layer washing thickener I through a jet flow cyanidation supplementary reactor discharging pump and a pipeline; the jet cyanidation supplemental reactor is used for cyanidation of the mixed solution and the escaped oxygen to continuously carry out supplemental cyanidation leaching to extract gold.
The three-layer washing and concentrating mechanism I comprises a three-layer washing and concentrating machine I, a noble liquid inlet and a washing water inlet are formed in the outer wall of the three-layer washing and concentrating machine I, a noble liquid outlet of the three-layer washing and concentrating machine I is connected with a noble liquid inlet of a noble liquid tank, a mixed liquid inlet of the three-layer washing and concentrating machine I is connected with a mixed liquid outlet of a jet cyanidation supplementary reactor discharge pump, a three-layer washing and concentrating machine I stirring rake is arranged in the three-layer washing and concentrating machine I, a lean liquid slag slurry outlet at the bottom of the three-layer washing and concentrating machine I is connected with a lean liquid slag slurry inlet of a pump box of a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I, and a lean liquid slag slurry outlet of the three-layer washing and concentrating machine I is connected with a lean liquid slag slurry inlet of a cavitation cyanidation mechanism through a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I; the three-layer washing and concentrating machine I is used for washing cyanide mixed liquor and separating noble liquor and lean liquor slag slurry.
The cavitation cyanidation mechanism comprises a cavitation cyanidation machine, wherein a lean liquid slag slurry inlet of the cavitation cyanidation machine is connected with a lean liquid slag slurry outlet of a lean liquid slag slurry discharge pump of the three-layer washing concentration machine I, a cavitation inner stirrer and a cavitation outer stirrer which are matched with each other are arranged in the cavitation cyanidation machine, an air flow cavitation nozzle of the cavitation cyanidation machine is arranged on the outer wall of the cavitation cyanidation machine, an oxygen inlet of the air flow cavitation nozzle of the cavitation cyanidation machine is connected with an oxygen outlet of a high-pressure oxygen compressor of the cavitation cyanidation machine, sodium cyanide and sodium hydroxide liquid inlets are arranged at the top of the cavitation cyanidation machine, and the cavitation cyanidation machine is used for carrying out secondary cyanidation leaching gold extraction on lean liquid slag slurry, sodium cyanide solution, sodium hydroxide solution and oxygen.
The device comprises a gas flow cavitation cyanidation tubular reactor mechanism, wherein the gas flow cavitation cyanidation tubular reactor mechanism comprises a gas flow cavitation cyanidation tubular reactor, a gas flow cavitation cyanidation tubular reactor turbulent flow element is arranged in the gas flow cavitation cyanidation tubular reactor, a gas flow cavitation tubular reactor gas flow cavitation nozzle is arranged on the outer wall of the gas flow cavitation cyanidation tubular reactor, an oxygen inlet of the gas flow cavitation cyanidation tubular reactor gas flow cavitation nozzle is connected with an oxygen outlet of a high-pressure oxygen compressor of the cavitation cyanidation machine, a mixed liquid inlet of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid outlet of a feed pump box of the gas flow cavitation cyanidation tubular reactor through a feed pump of the gas flow cavitation cyanidation tubular reactor, a mixed liquid inlet of the feed pump box of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid outlet of a bottom end of the cavitation cyanidation machine, and the mixed liquid outlet of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid inlet of an aging tank.
The aging tank mechanism comprises an aging tank, an aging tank mechanical stirrer is arranged in the aging tank, an oxygen outlet at the top of the aging tank is connected with an oxygen recovery system, a mixed liquor overflow port of the aging tank is connected with a mixed liquor inlet of a pump box of a discharging pump of the aging tank, a mixed liquor outlet of the pump box of the discharging pump of the aging tank is connected with a mixed liquor inlet of a three-layer washing concentration mechanism II through a discharging pump of the aging tank, and the aging tank is used for continuously cyaniding, leaching and gold extraction of the mixed liquor.
The three-layer washing and concentrating mechanism II comprises a three-layer washing and concentrating machine II, wherein a mixed liquid inlet of the three-layer washing and concentrating machine II is connected with a mixed liquid outlet of an aging tank discharge pump, a three-layer washing and concentrating machine II stirring rake is arranged in the three-layer washing and concentrating machine II, a treated lean liquid inlet is arranged on the outer side of the three-layer washing and concentrating machine II, a noble liquid overflow port of the three-layer washing and concentrating machine II is connected with a noble liquid inlet of a three-layer washing and concentrating machine II noble liquid discharge pump box, a noble liquid outlet of the three-layer washing and concentrating machine II is connected with a noble liquid inlet of the three-layer washing and concentrating machine I through a three-layer washing and concentrating machine II noble liquid discharge pump, a lean liquid slag slurry outlet at the bottom of the three-layer washing and concentrating machine II is connected with a lean liquid slag slurry inlet of the three-layer washing and concentrating machine II, and a lean liquid slag slurry outlet of the three-layer washing and concentrating machine II is connected with a filter press of a leaching slag treatment system; the liquid outlet of the lean liquid slag slurry filter press of the three-layer washing and concentrating machine II is connected with the liquid inlet of the lean liquid slag slurry filter tank of the three-layer washing and concentrating machine II, the liquid outlet of the lean liquid slag slurry filter tank of the three-layer washing and concentrating machine II is connected with the lean liquid tank through the lean liquid slag slurry filter discharging pump of the three-layer washing and concentrating machine II, and the three-layer washing and concentrating machine II is used for washing cyanide mixed liquid and separating noble liquid and lean liquid slag slurry.
The noble liquid tank mechanism comprises a noble liquid tank, a noble liquid inlet of the noble liquid tank is connected with a noble liquid outlet of the three-layer washing and concentrating machine I, a noble liquid outlet at the bottom of the noble liquid tank is connected with a noble liquid inlet of a noble liquid compressor through a noble liquid tank discharge pump, a slag soaking outlet of the noble liquid compressor is connected with a slag soaking treatment system, a liquid outlet of the noble liquid tank compressor is connected with a liquid inlet of a noble liquid filtering liquid tank, a liquid outlet of the noble liquid filtering liquid tank is connected with a liquid inlet of a noble liquid precise filter through a noble liquid filtering liquid pump, a filter residue outlet of the noble liquid precise filter is connected with a slag soaking treatment system, a filtrate outlet of the noble liquid precise filter is connected with a filtrate inlet of the deoxidizing tower mechanism, and the noble liquid tank is used for separating noble liquid suspended matters and precisely filtering noble liquid filtering liquid.
The deoxidizing tower mechanism comprises a deoxidizing tower, a deoxidizing tower spray header and deoxidizing tower packing are respectively arranged at the inner top and the middle part of the deoxidizing tower, a deoxidizing tower spray header filtrate inlet is connected with a filtrate outlet of a noble liquid precision filter, a deoxidizing tower top waste gas outlet is connected with a deoxidizing tower vacuum pump, a deoxidizing filtrate outlet at the bottom of the deoxidizing tower is connected with a deoxidizing filtrate inlet of a zinc powder mixing replacement tank mechanism through a deoxidizing tower discharging pump, and the deoxidizing tower is used for vacuum stripping of dissolved oxygen from the noble liquid precision filtrate.
The zinc powder mixing and replacing tank mechanism comprises a zinc powder mixing and replacing tank, wherein a deoxidized filtrate inlet of the zinc powder mixing and replacing tank is connected with a deoxidized filtrate outlet of a deoxidizing tower discharging pump, a zinc powder mixing and replacing tank mechanical stirrer is arranged in the zinc powder mixing and replacing tank, a zinc powder inlet at the top of the zinc powder mixing and replacing tank is connected with a zinc powder outlet of a zinc powder spiral feeder, a lead acetate solution inlet is arranged on the outer wall of the zinc powder mixing and replacing tank, a replacement liquid outlet of the zinc powder mixing and replacing tank is connected with a zinc powder mixing and replacing tank pump tank replacement liquid inlet, a zinc powder mixing and replacing tank discharge pump is connected with a replacement liquid inlet of a replacing filter press through a zinc powder mixing and replacing tank discharge pump, a gold mud outlet of a replacing compressor is connected with a gold mud treatment system, a liquid outlet of the replacing compressor is connected with a liquid inlet of a barren liquid tank, a barren liquid outlet of the barren liquid tank is connected with a barren liquid treatment system through a barren liquid pump, and a barren liquid inlet of the barren liquid tank is connected with a barren liquid slag-liquid outlet of a three-layer washing thickener II, and the zinc powder mixing and replacing tank is used for precisely replacing the deoxidized liquid and gold mud.
A jet-cavitation gold concentrate powder cyanide leaching gold extraction production method comprises the following steps:
Step 1, concentrate ore powder enters sodium cyanide solution, sodium hydroxide solution and treated lean solution in a size mixing tank through a spiral feeder of the size mixing tank, and is mixed into slurry under the stirring of a mechanical stirrer of the size mixing tank; the slurry enters a power fluid pump box of the jet cyaniding tubular reactor through gravity;
step 2, the slurry in the slurry mixing tank enters a jet cyaniding tubular reactor power fluid pump box through gravity, the jet cyaniding tubular reactor power fluid pump pumps the slurry from the jet cyaniding tubular reactor power fluid pump box, the slurry pumped out of the jet cyaniding tubular reactor power fluid pump enters a jet cyaniding tubular reactor coupler, and meanwhile, the oxygen from the oxygen buffer tank is sucked; the mixed material from the jet flow cyanidation tubular reactor coupler enters a jet flow cyanidation tubular reactor ejector and then enters a jet flow cyanidation tubular reactor, and gold concentrate powder, sodium cyanide solution, sodium hydroxide solution and oxygen are subjected to cyanidation leaching to extract gold under the disturbance of a turbulent flow element of the jet flow cyanidation tubular reactor; the cyanide mixed solution from the jet cyanide tubular reactor enters a jet cyanide reaction tower;
step 3, introducing cyanide mixed liquor from the jet flow cyanide tubular reactor into the bottom of a jet flow cyanide reaction tower, introducing cyanide mixed liquor from the bottom of the jet flow cyanide reaction tower into a jet flow cyanide reaction tower power fluid pump box through gravity, pumping cyanide mixed liquor from the jet flow cyanide reaction tower power fluid pump box by a jet flow cyanide reaction tower power fluid pump, introducing part of cyanide mixed liquor from the jet flow cyanide reaction tower power fluid pump into a cyanide reaction tower spray header below a jet flow cyanide reaction tower demister, spraying for demisting, introducing part of cyanide mixed liquor into a jet flow cyanide reaction tower coupler, and simultaneously sucking oxygen from an oxygen buffer tank; the mixed material from the jet cyanation reaction tower coupler enters a jet cyanation reaction tower ejector and then enters a jet cyanation reaction tower; introducing cyanide mixed liquor overflowed from the upper part of the jet cyanidation reaction tower into a jet cyanidation supplementary reactor;
Step 4, introducing cyanide mixed liquor overflowed from the upper part of the jet flow cyanide reaction tower into a jet flow cyanide complementary reactor, introducing cyanide mixed liquor at the bottom of the jet flow cyanide complementary reactor into a jet flow cyanide complementary reactor power fluid pump box through gravity, introducing cyanide mixed liquor from the jet flow cyanide complementary reactor power fluid pump box into the jet flow cyanide complementary reactor power fluid pump, introducing cyanide mixed liquor from the jet flow cyanide complementary reactor power fluid pump into a jet flow cyanide complementary reactor coupler, and simultaneously sucking oxygen escaping from the jet flow cyanide reaction tower; the cyanide mixed solution from the coupler of the jet cyanidation supplementary reactor enters the jet cyanidation supplementary reactor ejector and then enters the jet cyanidation supplementary reactor; the oxygen escaping from the top of the jet flow cyanidation supplemental reactor is removed to an oxygen recovery system, cyanidation mixed liquid overflowing from the upper part of the jet flow cyanidation supplemental reactor enters a pump box of a discharge pump of the jet flow cyanidation supplemental reactor, and then enters a three-layer washing concentrator I through a discharge pump of the jet flow cyanidation supplemental reactor;
step 5, the noble liquid from the noble liquid discharge pump of the three-layer washing and concentrating machine II and the cyanide mixed liquid from the discharge pump of the jet cyanide complementary reactor enter the three-layer washing and concentrating machine I, and are washed by three layers of washing water under the stirring of a stirring rake of the three-layer washing and concentrating machine I; the noble liquid overflows from the upper part of the three-layer washing and concentrating machine I to enter a noble liquid tank, lean liquid slag slurry is separated from the lower part of the three-layer washing and concentrating machine I, and enters a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I through a lean liquid slag slurry discharge pump box of the three-layer washing and concentrating machine I, and then enters a cavitation cyanidation machine;
Step 6, a high-pressure oxygen compressor of the cavitation cyanider supplies high-pressure gas to a gas flow cavitation nozzle of the cavitation cyanider to generate gas flow cavitation; mechanical cavitation can be generated between the cavitation outer stirrer and the cavitation inner stirrer which are counter-rotated; the lean liquid slag slurry enters sodium cyanide solution, sodium hydroxide solution and oxygen in a cavitation cyanider through a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I, and cyanided leaching is accelerated under the action of airflow cavitation and mechanical cavitation; a gas phase oxygen removal recovery system at the top of the cavitation cyanider; the cyanide mixed solution in the cavitation cyanidation machine enters a cavitation cyanidation tubular reactor feed pump through a gas flow cavitation cyanidation tubular reactor feed pump box and then enters a gas flow cavitation cyanidation tubular reactor;
step 7, a high-pressure oxygen compressor of the cavitation cyanidation machine provides high-pressure gas for an airflow cavitation nozzle of the airflow cavitation cyanidation tubular reactor to generate airflow cavitation; the cyanide mixed solution in the cavitation cyanidation machine enters a feed pump of the cavitation cyanidation tubular reactor through a pump box of the feed pump of the cavitation cyanidation tubular reactor, and then enters the cavitation cyanidation tubular reactor, so that cyanidation leaching is accelerated under the disturbance of a turbulent flow element of the jet flow cyanidation tubular reactor and under the action of airflow cavitation; the cyanide mixed solution in the airflow cavitation cyanide tubular reactor is conveyed into the bottom of the aging tank through pressure;
Step 8, conveying the cyanide mixed liquor in the airflow cavitation cyanide tubular reactor to the bottom of the ageing tank through pressure, and continuously carrying out cyanide leaching to extract gold under the stirring of a mechanical stirrer; the gas phase at the top of the aging tank enters an oxygen recovery system, the cyanidation mixed liquor at the upper part of the aging tank overflows into a pump box of a discharge pump of the aging tank, and the cyanidation mixed liquor enters a three-layer washing concentrator II through the discharge pump of the aging tank;
step 9, introducing the cyanide mixed solution from the ageing tank discharge pump into a three-layer washing and concentrating machine II, and washing the treated lean solution under the stirring of a stirring rake of the three-layer washing and concentrating machine II; separating lean liquid slag slurry from the lower part of the three-layer washing and concentrating machine II, wherein the lean liquid slag slurry enters a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine II through a lean liquid slag slurry discharge pump box of the three-layer washing and concentrating machine II, and then enters a lean liquid slag slurry filter press of the three-layer washing and concentrating machine II; solid-liquid separation is carried out on the lean liquid slag slurry through a lean liquid slag slurry filter press of a three-layer washing and concentrating machine II, and leaching residues after washing with washing water are removed from a leaching residue treatment system; the filtrate and the washing water enter a lean liquid slag slurry filtrate tank of a three-layer washing and concentrating machine II, and the filtrate and the washing water enter the lean liquid tank through a lean liquid slag slurry filtrate discharge pump of the three-layer washing and concentrating machine II; the noble liquid overflows from the upper part of the three-layer washing and concentrating machine II to enter a noble liquid discharge pump box of the three-layer washing and concentrating machine II, and the noble liquid enters the upper part of the three-layer washing and concentrating machine I through a noble liquid discharge pump of the three-layer washing and concentrating machine II; the noble liquid of the three-layer washing and concentrating machine I and the noble liquid of the three-layer washing and concentrating machine II overflow together and enter a noble liquid tank;
Step 10, the noble liquid of the three-layer washing and concentrating machine I and the noble liquid of the three-layer washing and concentrating machine II overflow together and enter a noble liquid tank, the noble liquid enters a noble hydraulic filter through a noble liquid tank discharge pump, the noble liquid is subjected to solid-liquid separation through the noble hydraulic filter, and the leached slag after washing by the washing water is removed from a leached slag treatment system; the precious liquid filtering clear liquid and the washing water enter a precious liquid filtering liquid tank, the precious liquid filtering liquid pump pumps the precious liquid filtering liquid into a precious liquid precision filter, the precious liquid filtering liquid is filtered by a precision filter element, the precious liquid precision filtrate overflows into a deoxidizing tower, and waste residues filtered by the precious liquid precision filter are washed by washing water and enter a leaching residue treatment system;
step 11, a vacuum pump of the deoxidizing tower provides vacuum for the deoxidizing tower; overflowing the precious liquid precise filtrate into a deoxidizing tower, spraying the precious liquid precise filtrate onto a deoxidizing tower filler through a deoxidizing tower spray header, removing oxygen dissolved in the precious liquid precise filtrate by vacuum provided for the deoxidizing tower by means of a deoxidizing tower vacuum pump, and feeding the deoxidized precious liquid precise filtrate into a zinc powder mixing displacement tank through a deoxidizing tower discharge pump;
step 12, the deoxidized precious liquid precise filtrate enters a zinc powder mixing and replacing tank through a deoxidizing tower discharge pump, zinc powder enters the zinc powder mixing and replacing tank through a zinc powder spiral feeder, and lead acetate solution enters the zinc powder mixing and replacing tank, and the precious liquid precise filtrate, the zinc powder and the lead acetate solution are uniformly mixed under the stirring of a zinc powder mixing and replacing tank mechanical stirrer; the displacement liquid enters a pump box of a discharging pump of a zinc powder mixing displacement tank by means of gravity, the discharging pump of the zinc powder mixing displacement tank pumps the displacement liquid into a displacement filter press, and the displacement liquid is subjected to solid-liquid separation by the displacement filter press; the filtered barren liquor and washing water enter a barren liquor tank, and the barren liquor is pumped to a barren liquor treatment system by a barren liquor pump; and (5) feeding the gold mud washed by the washing water into a Jin Niliao bin, and removing the gold mud from the gold mud bin.
The grain diameter of the concentrate powder in the step 1 is less than 0.045mm at 95% and the grade of Au is 62g/t; the temperature in the size mixing tank is normal temperature, the pressure is normal pressure, and the mass concentration of the concentrate powder of the size is 40%; sodium cyanide: the mass ratio of the concentrate powder is 1:500, pH is 9.5-10; the retention time of the materials is 0.75 to 1 hour;
the temperature in the jet cyaniding tubular reactor in the step 2 is normal temperature, and the pressure is 1 MPa-1.05 MPa; jet cyanidation tubular reactor coupler feeds oxygen: concentrate powder 1Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank;
the temperature in the jet flow cyanidation reaction tower in the step 3 is normal temperature, and the pressure is 0.6MPa to 0.65MPa; the jet cyanidation reaction column coupler feeds oxygen: concentrate powder of 2Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank; the retention time of the materials is 9-10 h;
the temperature in the jet cyanidation supplementary reactor in the step 4 is normal temperature, and the pressure is 0.55MPa to 0.6MPa; the retention time of the materials is 4-5 h;
the temperature in the three-layer washing and concentrating machine I in the step 5 is normal temperature, and the pressure is normal pressure; washing water: the mass ratio of the concentrate powder is 2.5:1, both are calculated according to the mass added initially by a size mixing tank; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine I is 40%; the retention time of the materials is 4-5 h;
The temperature in the cavitation cyanider in the step 6 is normal temperature and pressureThe force is 0.6MPa to 0.65MPa; sodium cyanide: the mass ratio of the concentrate powder is 1:500, wherein the pH is 9.5-10 according to the mass of the initial addition of the size mixing tank; cavitation cyanide air flow cavitation nozzle feed oxygen: concentrate powder of 2Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank; the pressure of the oxygen outlet of the high-pressure oxygen compressor of the cavitation cyanider is 10MPa; the retention time of the materials is 5-6 h;
the temperature in the airflow cavitation cyanidation tubular reactor in the step 7 is normal temperature, and the pressure is 1.0 MPa-1.05 MPa; the airflow cavitation nozzle of the airflow cavitation cyanide tubular reactor is used for feeding oxygen: concentrate powder 1Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank; the pressure of the oxygen outlet of the high-pressure oxygen compressor of the cavitation cyanider is 10MPa;
the temperature in the aging tank in the step 8 is normal temperature, and the pressure is 0.55MPa to 0.6MPa; the retention time of the materials is 5-6 h;
the temperature in the three-layer washing and concentrating machine II in the step 9 is normal temperature, and the pressure is normal pressure; the lean solution after treatment: the mass ratio of the concentrate powder is 2:1, both are calculated according to the mass added initially by a size mixing tank; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine II is 40%; the feeding pressure of the lean liquid slag slurry filter press is 0.8Mpa, and the lean liquid slag slurry filter press washes: the mass ratio of the concentrate powder is 2:1, the wet content of a filter cake is 10% according to the mass of the initial addition of a size mixing tank; the retention time of the material II of the three-layer washing and concentrating machine is 4-5 h;
The temperature in the noble liquid tank in the step 10 is normal temperature, and the pressure is normal pressure; the feeding pressure of the noble hydraulic filter is 0.8Mpa, and the noble hydraulic filter washes: the mass ratio of the concentrate powder is 1:50, the wet content of the filter cake is 20% based on the mass initially added in the size mixing tank; the temperature of the noble liquid precise filter is normal temperature, the inlet pressure is 0.2MPa, and the outlet pressure of the noble liquid precise filtrate is normal pressure; the retention time of the materials in the noble liquid tank is 2-3 h;
the temperature in the deoxidizing tower in the step 11 is normal temperature, and the pressure is 0.02MPa; the residence time of the deoxidizing tower material is 1 h-1.5 h;
the temperature in the zinc powder mixing and replacing tank in the step 12 is normal temperature, and the pressure is normal pressure; zinc powder: the mass ratio of the lead acetate is 10:1, and the zinc powder is as follows: the mass ratio of the concentrate powder is 3:10000, both of which are calculated according to the mass of the initial addition of the size mixing tank; the feeding pressure of the displacement filter press is 0.8Mpa, and the washing water of the displacement filter press is: the mass ratio of the concentrate powder is 1:100, both of which are calculated according to the mass of the initial addition of the size mixing tank; jin Nizhi, the grade of which is 20 percent, and the moisture content of a gold mud filter cake is 20 percent; the residence time of the zinc powder mixed replacement tank material is 1 h-1.5 h.
Compared with the prior art, the utility model has the beneficial effects that:
1. The escaped oxygen is recycled, waste is changed into valuable, and resources are effectively utilized.
2. The jet reactor and the cavitation reactor can form a sufficient gas-liquid (solid) mixing zone, so that heat transfer, mass transfer and momentum transfer are effectively promoted, the reaction is further enhanced, and the reaction rate and the product yield are improved.
3. The utility model has the advantages of mature process, advanced equipment, continuous operation, high automation degree, shortened cyanidation reaction time, energy conservation, improved production efficiency and environmental friendliness.
Drawings
FIG. 1 is a schematic diagram of a jet-cavitation gold concentrate powder cyanide leaching gold extraction production device;
reference numerals: 1. 1-1 parts of a size mixing tank, 1-2 parts of a size mixing tank spiral feeder and 1-2 parts of a size mixing tank mechanical stirrer;
2. 2-1 parts of jet flow cyanidation tubular reactor, 2-2 parts of jet flow cyanidation tubular reactor power fluid pump box, 2-3 parts of jet flow cyanidation tubular reactor power fluid pump, 2-4 parts of jet flow cyanidation tubular reactor coupler, 2-5 parts of jet flow cyanidation tubular reactor ejector, 2-6 parts of jet flow cyanidation tubular reactor turbulence element and oxygen buffer tank;
3. 3-1 parts of jet flow cyanidation reaction tower, 3-2 parts of jet flow cyanidation reaction tower power fluid pump box, 3-2 parts of jet flow cyanidation reaction tower power fluid pump, 3-3 parts of jet flow cyanidation reaction tower coupler, 3-4 parts of jet flow cyanidation reaction tower sprayer, 3-5 parts of jet flow cyanidation reaction tower spray header, 3-6 parts of jet flow cyanidation reaction tower demister;
4. Jet flow cyanidation supplementary reactor, 4-1, jet flow cyanidation supplementary reactor power fluid pump box, 4-2, jet flow cyanidation supplementary reactor power fluid pump, 4-3, jet flow cyanidation supplementary reactor coupler, 4-4, jet flow cyanidation supplementary reactor ejector, 4-5, jet flow cyanidation supplementary reactor discharge pump box, 4-6, jet flow cyanidation supplementary reactor discharge pump
5. Three layers of washing and concentrating machines I, 5-1 and three layers of washing and concentrating machines I are provided with stirring rakes, 5-2 parts of a pump box of a lean liquid slag slurry discharging pump of the three-layer washing and concentrating machine I, and 5-3 parts of a lean liquid slag slurry discharging pump of the three-layer washing and concentrating machine I;
6. the device comprises a cavitation cyanider, a high-pressure oxygen compressor of the cavitation cyanider, a gas flow cavitation nozzle of the cavitation cyanider, a cavitation outer stirrer, a cavitation inner stirrer and a cavitation inner stirrer, wherein the cavitation cyanider comprises a cavitation inlet pipe, a cavitation outlet pipe, a cavitation inlet pipe and a cavitation outlet pipe;
7. the device comprises an airflow cavitation cyanidation tubular reactor, a 7-1 airflow cavitation cyanidation tubular reactor feeding pump box, a 7-2 airflow cavitation cyanidation tubular reactor feeding pump, a 7-3 airflow cavitation nozzle of the airflow cavitation cyanidation tubular reactor, a 7-4 airflow cavitation cyanidation tubular reactor turbulence element;
8. 8-1 parts of an ageing tank, 8-2 parts of an ageing tank mechanical stirrer, 8-3 parts of an ageing tank discharge pump box and 8-3 parts of an ageing tank discharge pump;
9. The three-layer washing and concentrating machine II, 9-1, the three-layer washing and concentrating machine II stirring rake, 9-2, the three-layer washing and concentrating machine II noble liquid discharge pump box, 9-3, the three-layer washing and concentrating machine II noble liquid discharge pump, 9-4, the three-layer washing and concentrating machine II lean liquid slag slurry discharge pump box, 9-5, the three-layer washing and concentrating machine II lean liquid slag slurry discharge pump, 9-6, the three-layer washing and concentrating machine II lean liquid slag slurry filter press, 9-7, the three-layer washing and concentrating machine II lean liquid slag slurry filtrate tank, 9-8, the three-layer washing and concentrating machine II lean liquid slag slurry filtrate discharge pump;
10. 10-1 parts of a noble liquid tank, 10-2 parts of a noble liquid tank discharge pump, 10-3 parts of a noble liquid hydraulic filter, 10-3 parts of a noble liquid filtering liquid tank, 10-4 parts of a liquid-collecting liquid pump, 10-5 parts of a liquid-collecting precision filter, 10-6 parts of a precision filter core;
11. the device comprises a deoxidizing tower, 11-1, a deoxidizing tower vacuum pump, 11-2, a deoxidizing tower spray header, 11-3, deoxidizing tower filler and 11-4 deoxidizing tower discharge pumps;
12. 12-1 parts of zinc powder mixing and replacing tank, 12-2 parts of zinc powder spiral feeder, 12-3 parts of zinc powder mixing and replacing tank mechanical stirrer, 12-4 parts of zinc powder mixing and replacing tank discharge pump box, 12-5 parts of zinc powder mixing and replacing tank discharge pump, 12-6 parts of replacing filter press, a lean solution tank, 12-7 parts of lean solution pump, 12-8 parts of gold mud bin.
Detailed Description
The utility model is described in further detail below with reference to the drawings and examples.
As shown in figure 1, the jet-cavitation gold concentrate powder cyanide leaching gold extraction production device comprises a size mixing tank mechanism, a jet cyanide tubular reactor mechanism, a jet cyanide reaction tower mechanism, a jet cyanide supplementary reactor mechanism, a three-layer washing and concentrating mechanism I, a cavitation and cyanidation mechanism, an airflow cavitation and cyanidation tubular reactor mechanism, an aging tank mechanism, a three-layer washing and concentrating mechanism II, a noble liquid tank mechanism, a deoxidizing tower mechanism and a zinc powder mixing and replacing tank mechanism; the slurry mixing tank mechanism is sequentially connected with the jet flow cyanidation tubular reactor mechanism, the jet flow cyanidation reaction tower mechanism, the jet flow cyanidation supplementary reactor mechanism and the three-layer washing and concentrating mechanism I, the three-layer washing and concentrating mechanism I is respectively connected with the noble liquid tank mechanism and the cavitation cyanidation mechanism, the noble liquid tank mechanism is sequentially connected with the deoxidizing tower mechanism and the zinc powder mixing and replacing tank, the cavitation cyanidation mechanism is sequentially connected with the aging tank mechanism and the three-layer washing and concentrating mechanism II, and the three-layer washing and concentrating mechanism II is connected with the three-layer washing and concentrating mechanism I.
The slurry mixing tank mechanism comprises a slurry mixing tank 1, wherein a raw material inlet of the slurry mixing tank 1 is connected with a raw material outlet of a slurry mixing tank spiral feeder 1-1, gold concentrate powder is conveyed into the slurry mixing tank 1 through the slurry mixing tank spiral feeder 1-1, a slurry mixing tank mechanical stirrer 1-2 is arranged in the slurry mixing tank 1, and a liquid inlet is formed in the top of the slurry mixing tank 1 and used for introducing sodium cyanide solution, sodium hydroxide solution and treated lean liquid; the size mixing tank 1 is used for mixing the gold concentrate powder, the sodium cyanide solution, the sodium hydroxide solution and the treated lean solution into slurry under the stirring of the mechanical stirrer 1-2 of the size mixing tank.
The jet flow cyanide tube reactor mechanism comprises a jet flow cyanide tube reactor power fluid pump box 2-1 and an oxygen buffer tank 2-6, wherein a slurry inlet of the jet flow cyanide tube reactor power fluid pump box 2-1 is connected with a slurry inlet of a tank body of the slurry mixing tank 1, a slurry outlet of the jet flow cyanide tube reactor power fluid pump box 2-1 is connected with a slurry inlet of the jet flow cyanide tube reactor power fluid pump 2-2, a slurry outlet of the jet flow cyanide tube reactor power fluid pump 2-2 is connected with a slurry inlet of a jet flow cyanide tube reactor coupler 2-3, a slurry outlet of the jet flow cyanide tube reactor coupler 2-3 is connected with a slurry inlet of a jet flow cyanide tube reactor ejector 2-4, a slurry outlet of the jet flow cyanide tube reactor ejector 2-4 is connected with a slurry inlet of the jet flow cyanide tube reactor 1, a jet flow disturbing element 2-5 is arranged in the jet flow cyanide tube reactor 1, a recovery oxygen and fresh oxygen inlet are arranged at the top of the oxygen buffer tank 2-6, an oxygen outlet of the oxygen buffer tank 2-6 is respectively connected with the jet flow cyanide tube reactor 3-3, the jet flow cyanide tube reactor 2-3, the oxygen buffer tank 2-6 is used for carrying out high-pressure cavitation of the gold-metal cyanide tube reactor, and the gold-metal cyanide tube reactor is used for carrying out high-pressure cavitation leaching of the gold-metal cyanide gas, and the gold-metal cyanide tube reactor is used for carrying out high pressure leaching.
The jet flow cyanidation reaction tower mechanism comprises a jet flow cyanidation reaction tower 3, a mixed liquid inlet at the bottom of the jet flow cyanidation reaction tower 3-1 is connected with a mixed liquid outlet of a jet flow cyanidation tubular reactor 2, so that cyanidation mixed liquid coming out of the jet flow cyanidation tubular reactor 2 enters the jet flow cyanidation reaction tower 3, a mixed liquid outlet at the bottom end of the jet flow cyanidation reaction tower 3 is connected with a mixed liquid inlet of a jet flow cyanidation reaction tower power fluid pump box 3-1, the jet flow cyanidation reaction tower power fluid pump box 3-1 is connected with a jet flow cyanidation reaction tower coupler 3-3 and a mixed liquid inlet of a jet flow cyanidation reaction tower spray header 3-5 through a jet flow cyanidation reaction tower power fluid pump 3-2 and a pipeline, jet flow cyanidation reaction tower ejectors 3-4 are arranged around the jet flow cyanidation reaction tower coupler 3-3, jet flow cyanidation reaction tower demisters 3-6 are arranged in the jet flow cyanidation reaction tower spray header 3-5, and the jet flow cyanidation reaction tower 3 is used for carrying out cyanidation and leaching continuously.
The jet flow cyanidation supplementary reactor mechanism comprises a jet flow cyanidation supplementary reactor 4, an oxygen outlet at the top of the jet flow cyanidation supplementary reactor 4 is connected with an oxygen recovery system, an overflow outlet at the top of a jet flow cyanidation reaction tower 3 is connected with a mixed liquor inlet of the jet flow cyanidation supplementary reactor 4, an oxygen escape outlet at the top of the jet flow cyanidation supplementary reactor 3 is connected with an oxygen inlet of a jet flow cyanidation supplementary reactor coupler 4-3 through a pipeline, a mixed liquor outlet at the bottom of the jet flow cyanidation supplementary reactor 4 is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor power fluid pump box 4-1, a mixed liquor outlet of the jet flow cyanidation supplementary reactor power fluid pump box 4-1 is connected with a mixed liquor inlet of the jet flow cyanidation supplementary reactor power fluid pump box 4-2 through a jet cyanidation supplementary reactor power fluid pump 4-2, the jet flow cyanidation supplementary reactor coupler 4-3 is positioned in the jet flow cyanidation supplementary reactor 4, and the mixed liquor outlet of the jet flow cyanidation supplementary reactor 4-1 is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor I through a pipeline; the jet cyanidation supplemental reactor 4 is used for carrying out supplemental cyanidation leaching gold extraction on cyanidation mixed liquor and escaped oxygen.
The three-layer washing and concentrating mechanism I comprises a three-layer washing and concentrating machine I5, a noble liquid inlet and a washing water inlet are formed in the outer wall of the three-layer washing and concentrating machine I5, a noble liquid outlet of the three-layer washing and concentrating machine I5 is connected with a noble liquid inlet of a noble liquid tank 10, a mixed liquid inlet of the three-layer washing and concentrating machine I5 is connected with a mixed liquid outlet of a jet cyanidation supplementary reactor discharge pump 4-6, a three-layer washing and concentrating machine I stirring rake 5-1 is arranged in the three-layer washing and concentrating machine I5, a lean liquid and slag slurry outlet at the bottom of the three-layer washing and concentrating machine I is connected with a lean liquid and slag slurry inlet of a three-layer washing and concentrating machine I lean liquid and slag slurry discharge pump box 5-2, and a lean liquid and slag slurry outlet of the three-layer washing and concentrating machine I lean liquid and slag slurry discharge pump 5-3 is connected with a lean liquid and slag slurry inlet of a cyanidation mechanism 6; the three-layer washing and concentrating machine I5 is used for washing cyanide mixed liquor and separating noble liquor and lean liquor slag slurry.
The cavitation cyanidation mechanism comprises a cavitation cyanidation machine 6, wherein a lean liquid slag slurry inlet of the cavitation cyanidation machine 6 is connected with a lean liquid slag slurry outlet of a lean liquid slag slurry discharge pump 5-3 of the three-layer washing concentration machine I, a cavitation inner stirrer 6-3 and a cavitation outer stirrer 6-4 which are matched with each other are arranged in the cavitation cyanidation machine 6, a cavitation cyanidation machine airflow cavitation nozzle 6-2 is arranged on the outer wall of the cavitation cyanidation machine 6, an oxygen inlet of the cavitation cyanidation machine airflow cavitation nozzle 6-2 is connected with an oxygen outlet of a cavitation cyanidation machine high-pressure oxygen compressor 6-1, sodium cyanide and sodium hydroxide liquid inlets are arranged at the top of the cavitation cyanidation machine 6, and the cavitation cyanidation machine 6 is used for carrying out secondary cyanidation leaching gold extraction on the lean liquid slag slurry, sodium cyanide solution, sodium hydroxide solution and oxygen.
The air flow cavitation cyanidation tubular reactor mechanism comprises an air flow cavitation cyanidation tubular reactor 7, an air flow cavitation cyanidation tubular reactor turbulence element 7-4 is arranged in the air flow cavitation cyanidation tubular reactor 7, an air flow cavitation nozzle 7-3 of the air flow cavitation cyanidation tubular reactor is arranged on the outer wall of the air flow cavitation cyanidation tubular reactor 7, an oxygen inlet of the air flow cavitation cyanidation tubular reactor air flow cavitation nozzle 7-3 is connected with an oxygen outlet of a high-pressure oxygen compressor 6-1 of the cavitation cyanidation machine, a mixed liquid inlet of the air flow cavitation cyanidation tubular reactor 7 is connected with a mixed liquid outlet of a feeding pump box 7-1 of the air flow cavitation cyanidation tubular reactor through an air flow cavitation cyanidation tubular reactor feeding pump 7-2, a mixed liquid inlet of the feeding pump box 7-1 of the air flow cavitation cyanidation tubular reactor is connected with a mixed liquid outlet at the bottom end of the cavitation cyanidation machine 6, and the mixed liquid outlet of the air flow cavitation cyanidation tubular reactor 7 is connected with a mixed liquid inlet of an aging tank.
The aging tank mechanism comprises an aging tank 8, an aging tank mechanical stirrer 8-1 is arranged in the aging tank 8, an oxygen outlet at the top of the aging tank 8 is connected with an oxygen recovery system, a mixed liquor overflow port of the aging tank 8 is connected with a mixed liquor inlet of an aging tank discharging pump box 8-2, a mixed liquor outlet of the aging tank discharging pump box 8-2 is connected with a mixed liquor inlet of a three-layer washing concentration mechanism II 9 through an aging tank discharging pump 8-3, and the aging tank 8 is used for continuously cyaniding, leaching and gold extraction of the cyanide mixed liquor.
The three-layer washing and concentrating mechanism II comprises a three-layer washing and concentrating machine II 9, wherein a mixed liquid inlet of the three-layer washing and concentrating machine II 9 is connected with a mixed liquid outlet of an aging tank discharge pump 8-3, a three-layer washing and concentrating machine II stirring rake 9-1 is arranged in the three-layer washing and concentrating machine II 9, a treated lean liquid inlet is arranged on the outer side of the three-layer washing and concentrating machine II, a noble liquid overflow port of the three-layer washing and concentrating machine II 9 is connected with a three-layer washing and concentrating machine II noble liquid outlet pump box 9-2 noble liquid inlet, a three-layer washing and concentrating machine II noble liquid outlet pump box 9-2 noble liquid outlet is connected with a three-layer washing and concentrating machine I5 noble liquid inlet through a three-layer washing and concentrating machine II noble liquid outlet pump 9-3, a lean liquid slag slurry outlet at the bottom of the three-layer washing and concentrating machine II is connected with a three-layer washing and concentrating machine II liquid slag slurry outlet pump box 9-4, and a three-layer washing and concentrating machine II lean liquid inlet is connected with a three-layer washing and concentrating machine filter press 9-6, and a three-layer washing and concentrating system filter press is arranged on the three-layer washing and concentrating machine II; the liquid outlet of the lean liquid slag slurry filter press 9-6 of the three-layer washing and concentrating machine II is connected with the liquid inlet of the lean liquid slag slurry filtrate tank 9-7 of the three-layer washing and concentrating machine II, the liquid outlet of the lean liquid slag slurry filtrate tank 9-7 of the three-layer washing and concentrating machine II is connected with the lean liquid tank 12-6 through the lean liquid slag slurry filtrate discharging pump 9-3 of the three-layer washing and concentrating machine II, and the three-layer washing and concentrating machine II 9 is used for washing cyanide mixed liquid and separating noble liquid and lean liquid slag slurry.
The noble liquid tank mechanism comprises a noble liquid tank 10, a noble liquid inlet of the noble liquid tank 10 is connected with a noble liquid outlet of a three-layer washing concentration machine I5, a noble liquid outlet at the bottom of the noble liquid tank 10 is connected with a noble liquid inlet of a noble liquid compressor 10-2 through a noble liquid tank discharge pump 10-1, a washing water inlet is arranged on the noble liquid compressor 10-2, a slag leaching outlet of the noble liquid compressor 10-2 is connected with a slag leaching treatment system, a liquid outlet of the noble liquid compressor 10-2 is connected with a liquid inlet of a noble liquid filtering liquid tank 10-3, a liquid outlet of the noble liquid filtering liquid tank 10-3 is connected with a liquid inlet of a noble liquid precise filter 10-5 through a noble liquid filtering liquid pump 10-4, a flushing water inlet is arranged at the top of the noble liquid precise filter 10-5, a precise filter element 10-6 is arranged in the noble liquid precise filter 10-5, a filter residue outlet of the noble liquid precise filter 10-5 is connected with the slag leaching treatment system, a filtrate outlet of the noble liquid precise filter 10-5 is connected with a filtrate inlet of the noble liquid filtering liquid mechanism, and the noble liquid tank 10-is used for separating and precise filtering noble liquid suspension.
The deoxidizing tower mechanism comprises a deoxidizing tower 11, a deoxidizing tower spray header 11-2 and a deoxidizing tower packing 11-3 are respectively arranged at the top and the middle part in the deoxidizing tower 11, a filtrate inlet of the deoxidizing tower spray header 11-2 is connected with a filtrate outlet of a precious liquid precise filter 10-5, a waste gas outlet at the top of the deoxidizing tower 11 is connected with a deoxidizing tower vacuum pump 11-1, a deoxidizing filtrate outlet at the bottom of the deoxidizing tower 11 is connected with a deoxidizing filtrate inlet of the zinc powder mixing replacement tank mechanism through a deoxidizing tower discharging pump 11-4, and the deoxidizing tower 11 is used for vacuum stripping dissolved oxygen from the precious liquid precise filtrate.
The zinc powder mixing and replacing tank mechanism comprises a zinc powder mixing and replacing tank 12, wherein a deoxidized filtrate inlet of the zinc powder mixing and replacing tank 12 is connected with a deoxidized filtrate outlet of a deoxidizing tower discharging pump 11-4, a zinc powder mixing and replacing tank mechanical stirrer 12-2 is arranged in the zinc powder mixing and replacing tank 12, a zinc powder inlet at the top of the zinc powder mixing and replacing tank 12 is connected with a zinc powder outlet of a zinc powder screw conveyer 12-1, a lead acetate solution inlet is arranged on the outer wall of the zinc powder mixing and replacing tank 12, a replacement liquid outlet of the zinc powder mixing and replacing tank 12 is connected with a replacement liquid inlet of a zinc powder mixing and replacing pump box 12-3, a replacement liquid outlet of the zinc powder mixing and replacing pump box 12-3 is connected with a replacement liquid inlet of a replacing filter press 12-5 through a zinc powder mixing and replacing tank discharging pump 12-4, a gold mud outlet of a replacing compressor 12-5 is connected with a gold mud treatment system, a liquid outlet of the replacing compressor 12-5 is connected with a liquid inlet of a lean liquid tank 12-6, a lean liquid outlet of the lean liquid tank 12-6 is connected with a lean liquid pump 12-7 through a lean liquid pump 12-7, and a lean liquid inlet of a lean liquid tank 12-6 is connected with a lean filtrate outlet of a lean liquid pump 12-8 of a slag washing thickener, and the zinc powder is used for precise replacement of the zinc mud is used for replacing the waste slurry.
A jet-cavitation gold concentrate powder cyanide leaching gold extraction production method comprises the following steps:
step 1, the grain size of the concentrate powder is less than 0.045mm, the grade Au is 62g/t, the feeding flow is 1238kg/h, the concentrate powder enters into sodium cyanide solution, sodium hydroxide solution and treated lean solution in a size mixing tank 1 through a size mixing tank spiral feeder 1-1, and the concentrate powder is mixed into slurry under the stirring of a mechanical stirrer 1-1 of the size mixing tank; the slurry enters a jet cyaniding tubular reactor power fluid pump box 2-1 through gravity; the temperature in the size mixing tank 1 is normal temperature, the pressure is normal pressure, and the mass concentration of the concentrate powder of the size is 40%; the feed rate of the lean liquid after treatment is 1857kg/h; sodium cyanide: the mass ratio of the concentrate powder is 1:500, sodium cyanide feed rate 2.476kg/h, pH 9.5; the retention time of the material is 0.75h;
step 2, the slurry in the slurry mixing tank 1 enters a jet flow cyanidation tubular reactor power fluid pump box 2-1 through gravity, the jet flow cyanidation tubular reactor power fluid pump 2-2 sucks the slurry from the jet flow cyanidation tubular reactor power fluid pump box 2-1, the slurry from the jet flow cyanidation tubular reactor power fluid pump 2-2 enters a jet flow cyanidation tubular reactor coupler 2-3, and meanwhile, oxygen from an oxygen buffer tank is sucked; the mixed material coming out of the jet flow cyanidation tubular reactor coupler 2-3 enters the jet flow cyanidation tubular reactor ejector 2-4 and then enters the jet flow cyanidation tubular reactor 2, and gold concentrate powder, sodium cyanide solution, sodium hydroxide solution and oxygen are subjected to cyanidation leaching under the disturbance of the jet flow cyanidation tubular reactor turbulence element 2-5 to extract gold; the cyanide mixed solution from the jet cyanide tubular reactor 2 enters a jet cyanide reaction tower 3; the temperature in the jet cyaniding tubular reactor 2 is normal temperature and the pressure is 1MPa; jet cyanidation tubular reactor coupler 2-3 feeds oxygen: concentrate powder 1Nm 3 :1000kg, oxygen feed rate 1.238Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the Wherein, the jet flow cyanidation tubular reactor coupler 2-3 is used for feeding oxygen and concentrate powder according to the mass of the initial addition of the size mixing tank;
step 3, introducing the cyanide mixed solution from the jet cyanation tubular reactor 2 into the jet cyanation reactionThe cyanide mixed liquid at the bottom of the tower 3 enters a jet flow cyanide reaction tower power fluid pump box 3-1 through gravity, the jet flow cyanide reaction tower power fluid pump 3-2 sucks the cyanide mixed liquid from the jet flow cyanide reaction tower power fluid pump box 3-1, and part of the cyanide mixed liquid from the jet flow cyanide reaction tower power fluid pump 3-2 enters a jet flow cyanide reaction tower spray header 3-5 below a jet flow cyanide reaction tower demister 3-6 for spray demisting; the other part of the mixed material enters a jet flow cyanidation reaction tower coupler 3-3, oxygen from an oxygen buffer tank 2-6 is sucked at the same time, and the mixed material coming out of the jet flow cyanidation reaction tower coupler 3-3 enters a jet flow cyanidation reaction tower ejector 3-4 and then is ejected into the jet flow cyanidation reaction tower 3; the cyanide mixed solution overflowed from the upper part of the jet cyanidation reaction tower 3 enters a jet cyanidation supplementary reactor 2; the temperature in the jet flow cyanidation reaction tower 3 is normal temperature, and the pressure is 0.6MPa; jet cyanidation tower coupler 3-3 feeds oxygen: concentrate powder of 2Nm 3 :1000kg, oxygen and concentrate powder are fed into the jet cyanidation reaction tower coupler 3-3 according to the mass of the initial addition of the size mixing tank, and the oxygen feeding flow is 2.476Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the The retention time of the materials is 10h;
step 4, introducing cyanide mixed liquor overflowed from the upper part of the jet flow cyanide reaction tower 3 into a jet flow cyanide complementary reactor 4, introducing cyanide mixed liquor at the bottom of the jet flow cyanide complementary reactor 4 into a jet flow cyanide complementary reactor power fluid pump box 4-1 through gravity, introducing cyanide mixed liquor from the jet flow cyanide complementary reactor power fluid pump box 4-1 into the jet flow cyanide complementary reactor power fluid pump 4-2, introducing cyanide mixed liquor from the jet flow cyanide complementary reactor power fluid pump 4-2 into a jet flow cyanide reactor coupler 4-3, introducing oxygen escaping from the jet flow cyanide reaction tower 3, introducing cyanide mixed liquor from the jet flow cyanide complementary reactor coupler 4-3 into the jet flow cyanide complementary reactor ejector 4-4, and introducing the cyanide mixed liquor into the jet flow cyanide complementary reactor 4; the oxygen escaping from the top of the jet flow cyanidation supplemental reactor 4 is removed from the oxygen recovery system, cyanidation mixed liquor overflowing from the upper part of the jet flow cyanidation supplemental reactor 4 enters a jet flow cyanidation supplemental reactor discharge pump box 4-5, and then enters a three-layer washing concentrator I5 through a jet flow cyanidation supplemental reactor discharge pump 4-6; the temperature in the jet cyanidation supplementary reactor 4 is normal temperature, and the pressure is 0.55MPa; the retention time of the material is 5h;
Step 5, the noble liquid from the three-layer washing thickener II 9 of the three-layer washing thickener II noble liquid discharge pump 9-3 and the cyanide mixed liquid from the jet cyanide complementary reactor discharge pump 4-6 enter the three-layer washing thickener I5, and are washed by three-layer washing water under the stirring of the stirring rake 5-1 of the three-layer washing thickener I; the noble liquid overflows from the upper part of the three-layer washing and concentrating machine I1 to enter a noble liquid tank 10, lean liquid slag slurry is separated from the lower part of the three-layer washing and concentrating machine I5, and enters a lean liquid slag slurry discharging pump 5-3 of the three-layer washing and concentrating machine I through a lean liquid slag slurry discharging pump box 5-2 of the three-layer washing and concentrating machine I and then enters a cavitation cyanider 6; the temperature in the three-layer washing concentrator I5 is normal temperature, and the pressure is normal pressure; washing water: the mass ratio of the concentrate powder is 2.5:1, according to the mass of the initial addition of the size mixing tank, the feeding flow of washing water is 3095kg/h; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine I5 is 40%; the retention time of the material is 5h;
step 6, a high-pressure oxygen compressor 6-1 of the cavitation cyanider provides high-pressure gas for a gas flow cavitation nozzle 6-2 of the cavitation cyanider to generate gas flow cavitation; mechanical cavitation can be generated between the cavitation outer stirrer 6-3 and the cavitation inner stirrer 6-4 which are counter-rotated; the lean liquid slag slurry enters sodium cyanide solution, sodium hydroxide solution and oxygen in a cavitation cyanider 6 through a lean liquid slag slurry discharge pump 5-3 of a three-layer washing and concentrating machine I, and cyanidation leaching is accelerated under the action of airflow cavitation and mechanical cavitation; a gas phase oxygen removal recovery system at the top of the cavitation cyanider 6; the cyanide mixed solution in the cavitation cyanidation machine 6 enters a feed pump 7-2 of the cavitation cyanidation tubular reactor through a feed pump box 7-1 of the cavitation cyanidation tubular reactor, and then enters the cavitation cyanidation tubular reactor 7; the temperature in the cavitation cyanider 6 is normal temperature, and the pressure is 0.6MPa; sodium cyanide: the mass ratio of the concentrate powder is 1:500, wherein the pH value is 9.5 and the feeding flow rate of sodium cyanide is 2.476kg/h according to the mass initially added by a size mixing tank; cavitation cyanide machine airflow cavitation nozzle 6-2 feeding Oxygen: concentrate powder of 2Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank; oxygen feed flow 2.476Nm 3 The method comprises the steps of carrying out a first treatment on the surface of the The pressure of the oxygen outlet of the high-pressure oxygen compressor 6-1 of the cavitation cyanider is 10MPa; the retention time of the material is 6 hours;
step 7, a high-pressure oxygen compressor 6-1 of the cavitation cyanidation machine provides high-pressure gas for an airflow cavitation nozzle 7-3 of the airflow cavitation cyanidation tubular reactor to generate airflow cavitation; the cyanide mixed solution in the cavitation cyanidation machine 6 enters the feed pump 7-2 of the cavitation cyanidation tubular reactor through the feed pump box 7-1 of the cavitation cyanidation tubular reactor, and then enters the cavitation cyanidation tubular reactor 7, and the cyanidation leaching is accelerated under the disturbance of the turbulent flow element 7-4 of the cavitation cyanidation tubular reactor and the action of the cavitation of the airflow; the cyanide mixed solution in the airflow cavitation cyanide tubular reactor 7 is conveyed into the bottom of the aging tank 8 by pressure; the temperature in the airflow cavitation cyanidation tubular reactor 7 is normal temperature, and the pressure is 1.0MPa; the airflow cavitation nozzle of the airflow cavitation cyanide tubular reactor 7 is used for feeding oxygen: concentrate powder 1Nm 3 :1000kg, both of which are calculated according to the mass of the initial addition of the size mixing tank; oxygen feed flow 1.238Nm 3 The pressure of the oxygen outlet of the high-pressure oxygen compressor 6-1 of the cavitation cyanider is 10MPa;
step 8, conveying the cyanide mixed liquor in the airflow cavitation cyanide tubular reactor 7 into the bottom of the aging tank 8 through pressure, and continuously carrying out cyanide leaching to extract gold under the stirring of the mechanical stirrer 8-1 of the aging tank; the gas phase at the top in the aging tank 8 enters an oxygen recovery system, the cyanidation mixed liquor at the upper part in the aging tank 8 overflows into a pump box 8-2 of a discharge pump of the aging tank, and the cyanidation mixed liquor enters a three-layer washing concentrator II 9 through a discharge pump 8-3 of the aging tank; the temperature in the aging tank 8 is normal temperature, and the pressure is 0.55MPa; the retention time of the material is 6 hours;
step 9, introducing the cyanide mixed solution from the ageing tank discharge pump 8-3 into a three-layer washing and concentrating machine II 9, and washing the lean solution after being treated under the stirring of a stirring rake 9-1 of the three-layer washing and concentrating machine II; lean liquid slag slurry is separated from the lower part of the three-layer washing and concentrating machine II, enters the lean liquid slag slurry discharging pump 9-5 of the three-layer washing and concentrating machine II through the lean liquid slag slurry discharging pump box 9-4 of the three-layer washing and concentrating machine II, and then enters the lean liquid slag slurry filter press 9-6 of the three-layer washing and concentrating machine II; the lean liquid slag slurry is subjected to solid-liquid separation by a three-layer washing and concentrating machine II lean liquid slag slurry filter press 9-6, and the leached slag after washing by washing water is removed from the leached slag treatment system; the filtrate and the washing water enter a lean liquid slag slurry filtrate tank 9-7 of a three-layer washing concentrator II, and the filtrate and the washing water enter the lean liquid tank through a lean liquid slag slurry filtrate discharge pump 9-8 of the three-layer washing concentrator II; the noble liquid overflows from the upper part of the three-layer washing and concentrating machine II to enter a noble liquid discharging pump box 9-2 of the three-layer washing and concentrating machine II, and the noble liquid enters the upper part of the three-layer washing and concentrating machine I5 through a noble liquid discharging pump 9-3 of the three-layer washing and concentrating machine II; the noble liquid of the three-layer washing and concentrating machine I5 and the noble liquid of the three-layer washing and concentrating machine II 9 overflow together and enter a noble liquid tank 10; the temperature in the three-layer washing and concentrating machine II 9 is normal temperature, and the pressure is normal pressure; the lean solution after treatment: the mass ratio of the concentrate powder is 2:1, both of which are based on the mass of the initial addition of the size mixing tank 1, the feeding flow of the lean liquid after treatment is 2476kg/h; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine II 9 is 40%; 9-6 of a lean liquid slag slurry filter press of the three-layer washing and concentrating machine II has the feeding pressure of 0.8Mpa, and 9-6 of washing water of the lean liquid slag slurry filter press of the three-layer washing and concentrating machine II: the mass ratio of the concentrate powder is 2:1, according to the mass of the initial addition of the size mixing tank, the feeding flow of washing water is 2476kg/h, and the moisture content of a filter cake is 10%; the retention time of the II 9 material of the three-layer washing and concentrating machine is 5 hours;
Step 10, precious liquid in the three-layer washing and concentrating machine I5 and precious liquid in the three-layer washing and concentrating machine II 9 overflow into a precious liquid tank 10 together, the precious liquid enters a precious hydraulic filter 10-2 through a precious liquid tank discharge pump 10-1, the precious liquid is subjected to solid-liquid separation through the precious hydraulic filter 10-2, and leaching residues after washing with washing water are removed from a leaching residue treatment system; the precious liquid filtering clear liquid and washing water enter a precious liquid filtering liquid tank 10-3, a precious liquid filtering liquid pump 10-4 pumps the precious liquid filtering liquid into a precious liquid precision filter 10-5, the precious liquid filtering clear liquid is filtered by a precision filter element 10-6, precious liquid precision filtrate overflows and enters a deoxidizing tower 11, and waste residues filtered by the precious liquid precision filter 10-5 are washed by washing water and enter a residue leaching treatment system; the temperature in the noble liquid tank 10 is normal temperature, and the pressure is normal pressure; the feeding pressure of the noble hydraulic filter 10-2 is 0.8Mpa, and the noble hydraulic filter 10-2 washes: the mass ratio of the concentrate powder is 1:50, both of which are based on the mass of the initial addition of the size mixing tank, wherein the feeding flow of washing water is 24.76kg/h, and the moisture content of a filter cake is 20%; the temperature of the noble liquid precise filter 10-5 is normal temperature, the inlet pressure is 0.2MPa, and the outlet pressure of the noble liquid precise filtrate is normal pressure; the retention time of the materials in the noble liquid tank 10 is 3 hours;
step 11, a deoxidizing tower vacuum pump 11-1 provides vacuum for the deoxidizing tower; the precious liquid precise filtrate overflows into a deoxidizing tower 11, is sprayed on a deoxidizing tower filler 11-3 through a deoxidizing tower spray header 11-2, and removes oxygen dissolved in the precious liquid precise filtrate by means of vacuum provided by a deoxidizing tower vacuum pump 11-1 for the deoxidizing tower, and the deoxidized precious liquid precise filtrate enters a zinc powder mixing and replacing tank 12 through a deoxidizing tower discharge pump 11-1; the temperature in the deoxidizing tower 11 is normal temperature and the pressure is 0.02MPa; the residence time of the material in the deoxidizing tower 11 is 1.5h;
Step 12, the deoxidized precious liquid precise filtrate enters a zinc powder mixing and replacing tank 12 through a deoxidizing tower discharge pump 11-4, zinc powder enters the zinc powder mixing and replacing tank 12 through a zinc powder spiral feeder 12-1, lead acetate solution enters the zinc powder mixing and replacing tank 12, and the precious liquid precise filtrate, the zinc powder and the lead acetate solution are uniformly mixed under the stirring of a zinc powder mixing and replacing tank mechanical stirrer 12-2; the displacement liquid enters a pump box 12-3 of a discharging pump of a zinc powder mixing displacement tank by means of gravity, the discharging pump 12-4 of the zinc powder mixing displacement tank pumps the displacement liquid into a displacement filter press 12-5, and the displacement liquid is subjected to solid-liquid separation by the displacement filter press 12-5; the filtered barren liquor and washing water enter a barren liquor tank 12-6, and the barren liquor is pumped to a barren liquor treatment system by a barren liquor pump; the gold mud after washing by the washing water enters a Jin Niliao bin 12-8, and the gold mud of the gold mud bin 12-8 is treated by gold mud removing treatment system, wherein the temperature in the zinc powder mixing and replacing tank 12 is normal temperature and the pressure is normal pressure; zinc powder: the mass ratio of the lead acetate is 10:1, and the zinc powder is as follows: the mass ratio of the concentrate powder is 3:10000, wherein the zinc powder feeding flow rate is 0.124kg/h and the lead acetate feeding flow rate is 0.0124kg/h according to the mass of the initial addition of the size mixing tank; the feeding pressure of the replacement filter press 12-5 is 0.8Mpa, and the washing water of the replacement filter press 12-5 is: the mass ratio of the concentrate powder is 1:100, wherein the feeding flow rate of the washing water is 12.38kg/h according to the mass of the initial addition of the size mixing tank; the grade of the gold mud is 20% (mass), the moisture content of a gold mud filter cake is 20%, the discharge flow of the gold mud filter cake is 1.520kg/h, and the retention time of the zinc powder mixing and replacing tank material is 1 h-1.5 h.
Example 2
Example 2 a jet-cavitation gold concentrate powder cyanide leaching gold extraction production method is different from example 1 in that:
the grain diameter of the concentrate powder in the step 1 is 95 percent less than 0.045mm, the grade Au is 62g/t, the feeding amount is 1238kg/h, the temperature in the size mixing tank 1 is normal temperature, the pressure is normal pressure, the mass concentration of the concentrate powder in the slurry is 40 percent, and the feeding flow of the barren liquor is 1857kg/h; sodium cyanide: the mass ratio of the concentrate powder is 1:500, sodium cyanide feed rate 2.476kg/h; the pH was 9.5; the retention time of the materials is 1h;
the temperature in the jet cyaniding tubular reactor in the step 2 is normal temperature, and the pressure is 1.05MPa; jet cyanidation tubular reactor coupler 2-3 feeds oxygen: concentrate powder 1Nm 3 :1000kg, both based on the initial mass of the surge tank, of 1.238Nm of oxygen feed flow 3 ；
The temperature in the jet flow cyanidation reaction tower in the step 3 is normal temperature, and the pressure is 0.65MPa; the coupler feeds oxygen: concentrate powder of 2Nm 3 :1000kg, both based on the initial mass of the surge tank, of 2.476Nm of oxygen feed flow 3 The method comprises the steps of carrying out a first treatment on the surface of the The retention time of the materials is 9h;
the temperature in the jet cyanidation supplementary reactor in the step 4 is normal temperature, and the pressure is 0.55MPa; the retention time of the material is 5h;
The temperature in the three-layer washing and concentrating machine I in the step 5 is normal temperature, and the pressure is normal pressure; washing water: the mass ratio of the concentrate powder is 2.5:1, according to the mass of the initial addition of the size mixing tank, the feeding flow of washing water is 3095kg/h; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine I is 40%; the retention time of the material is 4 hours;
the temperature in the cavitation cyanider in the step 6 is normal temperature, and the pressure is 0.65MPa; sodium cyanide: the mass ratio of the concentrate powder is 1:500, wherein the feeding flow rate of sodium cyanide is 2.476kg/h according to the mass initially added by a size mixing tank; pH is at10; cavitation cyanide air flow cavitation nozzle feed oxygen: concentrate powder of 2Nm 3 :1000kg, both based on the initial mass of the surge tank, of 2.476Nm of oxygen feed flow 3 The method comprises the steps of carrying out a first treatment on the surface of the The pressure of the oxygen outlet of the high-pressure oxygen compressor of the cavitation cyanider is 10MPa; the retention time of the material is 5h;
the temperature in the airflow cavitation cyanidation tubular reactor in the step 7 is normal temperature, and the pressure is 1.05MPa; the airflow cavitation nozzle of the airflow cavitation cyanide tubular reactor 7 is used for feeding oxygen: concentrate powder 1Nm 3 :1000kg, both based on the initial mass of the surge tank, of 1.238Nm of oxygen feed flow 3 The method comprises the steps of carrying out a first treatment on the surface of the The pressure of the oxygen outlet of the high-pressure oxygen compressor of the cavitation cyanider is 10MPa;
The temperature in the aging tank in the step 8 is normal temperature, and the pressure is 0.6MPa; the retention time of the material is 5h;
the temperature in the three-layer washing and concentrating machine II in the step 9 is normal temperature, and the pressure is normal pressure; the lean solution after treatment: the mass ratio of the concentrate powder is 2:1, the mass of the two materials is calculated according to the mass of the initial addition of a size mixing tank, and the feeding flow of the lean liquid after treatment is 2476kg/h; the solid content of the discharged lean liquid slag slurry of the three-layer washing and concentrating machine II is 40%; the feeding pressure of the lean liquid slag slurry filter press is 0.8Mpa, and the lean liquid slag slurry filter press washes: the mass ratio of the concentrate powder is 2:1, according to the mass of the initial addition of the size mixing tank, the feeding flow of washing water is 2476kg/h, and the moisture content of a filter cake is 10%; the retention time of the material II of the three-layer washing and concentrating machine is 4 hours;
the temperature in the noble liquid tank in the step 10 is normal temperature, and the pressure is normal pressure; the feeding pressure of the noble hydraulic filter is 0.8Mpa, and the noble hydraulic filter washes: the mass ratio of the concentrate powder is 1:50, both of which are based on the mass of the initial addition of the size mixing tank, wherein the feeding flow of washing water is 24.76kg/h, and the moisture content of a filter cake is 20%; the temperature of the noble liquid precise filter is normal temperature, the inlet pressure is 0.2MPa, and the outlet pressure of the noble liquid precise filtrate is normal pressure; the retention time of the materials in the noble liquid tank is 2 hours;
The temperature in the deoxidizing tower in the step 11 is normal temperature, and the pressure is 0.02MPa; the residence time of the deoxidizing tower material is 1h;
the temperature in the zinc powder mixing and replacing tank in the step 12 is normal temperature, and the pressure is normal pressure; zinc powder: the mass ratio of the lead acetate is 10:1, and the zinc powder is as follows: the mass ratio of the concentrate powder is 3:10000, wherein the zinc powder feeding flow rate is 0.124kg/h and the lead acetate feeding flow rate is 0.0124kg/h according to the mass of the initial addition of the size mixing tank; the feeding pressure of the displacement filter press is 0.8Mpa, and the washing water of the displacement filter press is: the mass ratio of the concentrate powder is 1:100, wherein the feeding flow rate of the washing water is 12.38kg/h according to the mass of the initial addition of the size mixing tank; the grade of the gold mud is 20 percent (mass), the moisture content of a gold mud filter cake is 20 percent, and the discharge flow of the gold mud filter cake is 1.523kg/h; the residence time of the zinc powder mixed replacement tank material is 1h.
According to the jet flow-cavitation gold concentrate powder cyanide leaching gold extraction production device and method, gold concentrate powder (grade Au62 g/t) is used for cyanide leaching gold extraction, gold mud grade is 20% (mass), and cyanide leaching yield is greater than 98% (mass).
In view of the engineering problems and market demands described above, the present utility model provides a jet reactor for cyanidation reactions and a cavitation reactor for cyanidation reactions; in the jet reactor, because the power fluid is sprayed out at high speed through the sprayer, a negative pressure area is generated at the gas or liquid suction inlet of the coupler, so that the gas or liquid is sucked, rapidly expands in the negative pressure area and is beaten into tiny bubbles or liquid drops by the power fluid, and enters the mixing cavity; at the moment, the gas and the liquid are fully mixed in the mixing cavity, and are accelerated and discharged due to energy exchange, the speed can be close to the sonic speed, and the potential energy of the mixed liquid is increased to the maximum through the diffusion cavity of the ejector, so that the effects of mass transfer and heat transfer are stronger, and the heat transfer, the mass transfer and the momentum transfer in the process are greatly enhanced; the strong microcosmic mixing characteristic can lead the chemical reaction to be carried out rapidly, and the mixing scale is reduced rapidly due to the turbulence state, the vortexes with different scales and mutually folded collisions enhance the turbulence intensity, enhance the energy diffusion, promote the molecules to reach more effective high-level collisions when the chemical reaction occurs, effectively improve the mixing and mass transfer effects in the reactor, and improve the reaction rate; in the cavitation reactor, as the cavitation process of forming, developing and collapsing vapor or gas cavities in the liquid or on the liquid-solid interface when the local pressure in the liquid is reduced, the cavitation can generate strong shock waves and microjet in a very small range, and hot spots are generated, the temperature can reach 10000K, the pressure is about 100MPa, and the corresponding cavitation effects such as hot spot effect, mechanical effect, chemical effect and the like are generated, so that the chemical reaction is facilitated; the cavitation cyanider high-pressure fluid pump provides high-pressure fluid for the cavitation cyanider hydrodynamic cavitation nozzle to generate hydrodynamic cavitation; mechanical cavitation can be generated between the cavitation outer stirrer and the cavitation inner stirrer which are counter-rotated; the lean liquid slag slurry enters sodium cyanide solution, sodium hydroxide solution and oxygen in a cavitation cyanider through a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I, and cyanided leaching is accelerated under the action of airflow cavitation and mechanical cavitation;
The jet flow reactor and the cavitation reactor provided by the utility model can form a sufficient gas-liquid-solid mixing zone, so that heat transfer, mass transfer and momentum transfer are effectively promoted, the reaction is further enhanced, and the cyanidation reaction rate and cyanidation leaching extraction Jin Shoulv are improved; the utility model has the advantages of mature process, advanced equipment, continuous operation, high automation degree, shortened cyanidation reaction time, energy conservation, improved production efficiency and environmental friendliness.
The technical scheme of the utility model is explained in the technical scheme, the protection scope of the utility model cannot be limited by the technical scheme, and any changes and modifications to the technical scheme according to the technical substance of the utility model belong to the protection scope of the technical scheme of the utility model.
Claims (9)
1. The jet-cavitation concentrate powder cyanide leaching gold extraction production device is characterized by comprising a size mixing tank mechanism, a jet cyanide tubular reactor mechanism, a jet cyanide reaction tower mechanism, a jet cyanide complementary reactor mechanism, a three-layer washing and concentrating mechanism I, a cavitation cyanidation mechanism, an airflow cavitation cyanidation tubular reactor mechanism, an ageing tank mechanism, a three-layer washing and concentrating mechanism II, a noble liquid tank mechanism, a deoxidizing tower mechanism and a zinc powder mixing and replacing tank mechanism; the slurry mixing tank mechanism is sequentially connected with the jet flow cyanidation tubular reactor mechanism, the jet flow cyanidation reaction tower mechanism, the jet flow cyanidation supplementary reactor mechanism and the three-layer washing and concentrating mechanism I, the three-layer washing and concentrating mechanism I is respectively connected with the noble liquid tank mechanism and the cavitation cyanidation mechanism, the noble liquid tank mechanism is sequentially connected with the deoxidizing tower mechanism and the zinc powder mixing and replacing tank, the cavitation cyanidation mechanism is sequentially connected with the aging tank mechanism and the three-layer washing and concentrating mechanism II, and the three-layer washing and concentrating mechanism II is connected with the three-layer washing and concentrating mechanism I.
2. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the slurry mixing tank mechanism comprises a slurry mixing tank, wherein a raw material inlet of the slurry mixing tank is connected with a raw material outlet of a spiral feeder of the slurry mixing tank, gold concentrate powder is fed into the slurry mixing tank through the spiral feeder of the slurry mixing tank, a mechanical stirrer of the slurry mixing tank is arranged in the slurry mixing tank, and a liquid inlet is arranged at the top of the slurry mixing tank and used for introducing sodium cyanide solution, sodium hydroxide solution and treated lean liquid; the size mixing tank is used for mixing the gold concentrate powder, the sodium cyanide solution, the sodium hydroxide solution and the treated lean solution into slurry under the stirring of a mechanical stirrer of the size mixing tank.
3. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the jet flow cyanide tube reactor mechanism comprises a jet flow cyanide tube reactor power fluid pump box and an oxygen buffer tank, wherein a slurry inlet of the jet flow cyanide tube reactor power fluid pump box is connected with a slurry outlet of a slurry mixing tank body, a slurry outlet of the jet flow cyanide tube reactor power fluid pump box is connected with a slurry inlet of the jet flow cyanide tube reactor power fluid pump, a slurry outlet of the jet flow cyanide tube reactor power fluid pump is connected with a slurry inlet of a jet flow cyanide tube reactor coupler, a slurry outlet of the jet flow cyanide tube reactor coupler is connected with a slurry inlet of a jet flow cyanide tube reactor, a slurry outlet of the jet flow cyanide tube reactor is connected with a slurry inlet of the jet flow cyanide tube reactor, a jet flow cyanide tube reactor turbulent flow element is arranged in the jet flow cyanide tube reactor, an oxygen buffer tank top is provided with an oxygen recovery inlet and a fresh oxygen buffer tank, an oxygen outlet of the oxygen buffer tank is respectively connected with a jet flow cyanide reactor coupler, a jet flow cyanide tube reactor coupler and a gas inlet of a cavitation machine high-pressure oxygen compressor of a cavitation machine of the cavitation machine, and the jet flow cyanide tube reactor is used for extracting gold concentrate, sodium hydroxide, sodium cyanide and gold leaching solution;
The jet flow cyanidation reaction tower mechanism comprises a jet flow cyanidation reaction tower, a mixed liquid inlet at the bottom of the jet flow cyanidation reaction tower is connected with a mixed liquid outlet of a jet flow cyanidation tubular reactor, so that cyanidation mixed liquid coming out of the jet flow cyanidation tubular reactor enters the jet flow cyanidation reaction tower, a mixed liquid outlet at the bottom of the jet flow cyanidation reaction tower is connected with a mixed liquid inlet of a jet flow cyanidation reaction tower power fluid pump box, the jet flow cyanidation reaction tower power fluid pump box is respectively connected with a jet flow cyanidation reaction tower coupler and a jet flow cyanidation reaction tower spray head mixed liquid inlet through a jet flow cyanidation reaction tower power fluid pump and a pipeline, jet flow cyanidation reaction tower ejectors are arranged around the jet flow cyanidation reaction tower coupler, and a jet flow cyanidation reaction tower demister is arranged in the jet flow cyanidation reaction tower at the top of the jet flow cyanidation reaction tower spray head, and the jet flow cyanidation reaction tower is used for carrying out cyanidation leaching and extracting gold continuously;
the jet flow cyanidation supplementary reactor mechanism comprises a jet flow cyanidation supplementary reactor, an oxygen outlet at the top of the jet flow cyanidation supplementary reactor is connected with an oxygen recovery system, an overflow outlet at the top of the jet flow cyanidation reaction tower is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor coupler through a pipeline, an oxygen escape outlet at the top of the jet flow cyanidation supplementary reactor is connected with an oxygen inlet of a jet flow cyanidation supplementary reactor coupler, a mixed liquor outlet at the bottom of the jet flow cyanidation supplementary reactor is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor power fluid pump box, a mixed liquor outlet of the jet flow cyanidation supplementary reactor power fluid pump box is connected with a mixed liquor inlet of a jet flow cyanidation supplementary reactor coupler through a jet flow cyanidation supplementary reactor discharging pump and a pipeline, and the jet flow cyanidation supplementary reactor coupler is positioned in the jet flow cyanidation supplementary reactor, and the jet flow cyanidation supplementary reactor discharging pump box mixed liquor outlet is connected with a mixed liquor inlet of a three-layer washing thickener I through a jet flow cyanidation supplementary reactor discharging pump and a pipeline; the jet cyanidation supplemental reactor is used for cyanidation of the mixed solution and the escaped oxygen to continuously carry out supplemental cyanidation leaching to extract gold.
4. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the three-layer washing and concentrating mechanism I comprises a three-layer washing and concentrating machine I, a noble liquid inlet and a washing water inlet are formed in the outer wall of the three-layer washing and concentrating machine I, a noble liquid outlet of the three-layer washing and concentrating machine I is connected with a noble liquid inlet of a noble liquid tank, a mixed liquid inlet of the three-layer washing and concentrating machine I is connected with a mixed liquid outlet of a jet cyanidation supplementary reactor discharge pump, a three-layer washing and concentrating machine I stirring rake is arranged in the three-layer washing and concentrating machine I, a lean liquid slag slurry outlet at the bottom of the three-layer washing and concentrating machine I is connected with a lean liquid slag slurry inlet of a pump box of a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I, and a lean liquid slag slurry outlet of the three-layer washing and concentrating machine I is connected with a lean liquid slag slurry inlet of a cavitation cyanidation mechanism through a lean liquid slag slurry discharge pump of the three-layer washing and concentrating machine I; the three-layer washing and concentrating machine I is used for washing cyanide mixed liquor and separating noble liquor and lean liquor slag slurry.
5. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the cavitation cyanidation mechanism comprises a cavitation cyanidation machine, wherein a lean liquid slag slurry inlet of the cavitation cyanidation machine is connected with a lean liquid slag slurry outlet of a lean liquid slag slurry discharge pump of the three-layer washing concentration machine I, a cavitation inner stirrer and a cavitation outer stirrer which are matched with each other are arranged in the cavitation cyanidation machine, an air flow cavitation nozzle of the cavitation cyanidation machine is arranged on the outer wall of the cavitation cyanidation machine, an oxygen inlet of the air flow cavitation nozzle of the cavitation cyanidation machine is connected with an oxygen outlet of a high-pressure oxygen compressor of the cavitation cyanidation machine, sodium cyanide and sodium hydroxide liquid inlets are arranged at the top of the cavitation cyanidation machine, and the cavitation cyanidation machine is used for carrying out secondary cyanidation leaching gold extraction on lean liquid slag slurry, sodium cyanide solution, sodium hydroxide solution and oxygen.
6. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the device comprises a gas flow cavitation cyanidation tubular reactor mechanism, wherein the gas flow cavitation cyanidation tubular reactor mechanism comprises a gas flow cavitation cyanidation tubular reactor, a gas flow cavitation cyanidation tubular reactor turbulent flow element is arranged in the gas flow cavitation cyanidation tubular reactor, a gas flow cavitation tubular reactor gas flow cavitation nozzle is arranged on the outer wall of the gas flow cavitation cyanidation tubular reactor, an oxygen inlet of the gas flow cavitation cyanidation tubular reactor gas flow cavitation nozzle is connected with an oxygen outlet of a high-pressure oxygen compressor of the cavitation cyanidation machine, a mixed liquid inlet of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid outlet of a feed pump box of the gas flow cavitation cyanidation tubular reactor through a feed pump of the gas flow cavitation cyanidation tubular reactor, a mixed liquid inlet of the feed pump box of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid outlet of a bottom end of the cavitation cyanidation machine, and the mixed liquid outlet of the gas flow cavitation cyanidation tubular reactor is connected with a mixed liquid inlet of an aging tank.
7. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the aging tank mechanism comprises an aging tank, an aging tank mechanical stirrer is arranged in the aging tank, an oxygen outlet at the top of the aging tank is connected with an oxygen recovery system, a mixed liquor overflow port of the aging tank is connected with a mixed liquor inlet of a pump box of a discharging pump of the aging tank, a mixed liquor outlet of the pump box of the discharging pump of the aging tank is connected with a mixed liquor inlet of a three-layer washing concentration mechanism II through a discharging pump of the aging tank, and the aging tank is used for continuously cyaniding, leaching and gold extraction of the mixed liquor.
8. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the three-layer washing and concentrating mechanism II comprises a three-layer washing and concentrating machine II, wherein a mixed liquid inlet of the three-layer washing and concentrating machine II is connected with a mixed liquid outlet of an aging tank discharge pump, a three-layer washing and concentrating machine II stirring rake is arranged in the three-layer washing and concentrating machine II, a treated lean liquid inlet is arranged on the outer side of the three-layer washing and concentrating machine II, a noble liquid overflow port of the three-layer washing and concentrating machine II is connected with a noble liquid inlet of a three-layer washing and concentrating machine II noble liquid discharge pump box, a noble liquid outlet of the three-layer washing and concentrating machine II is connected with a noble liquid inlet of the three-layer washing and concentrating machine I through a three-layer washing and concentrating machine II noble liquid discharge pump, a lean liquid slag slurry outlet at the bottom of the three-layer washing and concentrating machine II is connected with a lean liquid slag slurry inlet of the three-layer washing and concentrating machine II, and a lean liquid slag slurry outlet of the three-layer washing and concentrating machine II is connected with a filter press of a leaching slag treatment system; the liquid outlet of the lean liquid slag slurry filter press of the three-layer washing and concentrating machine II is connected with the liquid inlet of the lean liquid slag slurry filter tank of the three-layer washing and concentrating machine II, the liquid outlet of the lean liquid slag slurry filter tank of the three-layer washing and concentrating machine II is connected with the lean liquid tank through the lean liquid slag slurry filter discharging pump of the three-layer washing and concentrating machine II, and the three-layer washing and concentrating machine II is used for washing cyanide mixed liquid and separating noble liquid and lean liquid slag slurry.
9. The jet-cavitation gold concentrate powder cyanide leaching gold extraction production device according to claim 1, which is characterized in that: the noble liquid tank mechanism comprises a noble liquid tank, a noble liquid inlet of the noble liquid tank is connected with a noble liquid outlet of the three-layer washing and concentrating machine I, a noble liquid outlet at the bottom of the noble liquid tank is connected with a noble liquid inlet of a noble liquid compressor through a noble liquid tank discharge pump, a slag leaching outlet of the noble liquid compressor is connected with a slag leaching treatment system, a liquid outlet of the noble liquid tank compressor is connected with a liquid inlet of a noble liquid filtering liquid tank, a liquid outlet of the noble liquid filtering liquid tank is connected with a liquid inlet of a noble liquid precise filter through a noble liquid filtering liquid pump, a filter residue outlet of the noble liquid precise filter is connected with a slag leaching treatment system, a filtrate outlet of the noble liquid precise filter is connected with a filtrate inlet of the deoxidizing tower mechanism, and the noble liquid tank is used for separating noble liquid suspended matters and precisely filtering noble liquid filtering liquid;
the device comprises a deoxidizing tower, wherein a deoxidizing tower spray header and deoxidizing tower filler are respectively arranged at the inner top and the middle part of the deoxidizing tower, a deoxidizing tower spray header filtrate inlet is connected with a filtrate outlet of a noble liquid precision filter, a deoxidizing tower top waste gas outlet is connected with a deoxidizing tower vacuum pump, a deoxidizing filtrate outlet at the bottom of the deoxidizing tower is connected with a deoxidizing filtrate inlet of a zinc powder mixing displacement tank mechanism through a deoxidizing tower discharge pump, and the deoxidizing tower is used for vacuum removal of dissolved oxygen from the noble liquid precision filtrate;
The zinc powder mixing and replacing tank mechanism comprises a zinc powder mixing and replacing tank, wherein a deoxidized filtrate inlet of the zinc powder mixing and replacing tank is connected with a deoxidized filtrate outlet of a deoxidizing tower discharging pump, a zinc powder mixing and replacing tank mechanical stirrer is arranged in the zinc powder mixing and replacing tank, a zinc powder inlet at the top of the zinc powder mixing and replacing tank is connected with a zinc powder outlet of a zinc powder spiral feeder, a lead acetate solution inlet is arranged on the outer wall of the zinc powder mixing and replacing tank, a replacement liquid outlet of the zinc powder mixing and replacing tank is connected with a zinc powder mixing and replacing tank pump tank replacement liquid inlet, a zinc powder mixing and replacing tank discharge pump is connected with a replacement liquid inlet of a replacing filter press through a zinc powder mixing and replacing tank discharge pump, a gold mud outlet of a replacing compressor is connected with a gold mud treatment system, a liquid outlet of the replacing compressor is connected with a liquid inlet of a barren liquid tank, a barren liquid outlet of the barren liquid tank is connected with a barren liquid treatment system through a barren liquid pump, and a barren liquid inlet of the barren liquid tank is connected with a barren liquid slag-liquid outlet of a three-layer washing thickener II, and the zinc powder mixing and replacing tank is used for precisely replacing the deoxidized liquid and gold mud.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321277694.4U CN219709553U (en) | 2023-05-24 | 2023-05-24 | Jet-cavitation gold concentrate powder cyanide leaching gold extraction production device |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321277694.4U CN219709553U (en) | 2023-05-24 | 2023-05-24 | Jet-cavitation gold concentrate powder cyanide leaching gold extraction production device |
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| CN219709553U true CN219709553U (en) | 2023-09-19 |
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| CN202321277694.4U Active CN219709553U (en) | 2023-05-24 | 2023-05-24 | Jet-cavitation gold concentrate powder cyanide leaching gold extraction production device |
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| CN (1) | CN219709553U (en) |
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