CN108504854A - A kind of method of phase transformation ore dressing - Google Patents
A kind of method of phase transformation ore dressing Download PDFInfo
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Abstract
The invention discloses a kind of methods of phase transformation ore dressing, include the following steps：Feedstock processing；Combustion air heats；600~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, fuel enters from the fuel port of fluidized calcination room, full combustion of fuel makes the temperature of fluidized calcination room reach in raw material mainly by more than phase change material boiling point, 600~900 DEG C of raw materials enter from the feed inlet of fluidized calcination room, become solid, liquid, gas three-phase material after being calcined 3~5 seconds to be discharged from the top of fluidized calcination room, into high-temperature gas-solid separator；High-temperature gas-solid separation, the processing of gaseous substance.Resource consumption of the present invention is few, energy saving, safe and environment-friendly.
Description
Technical field
The present invention relates to beneficiation methods, relate in particular to a kind of method of phase transformation ore dressing.
Background technology
Phase transformation --- refer to the process of substance from a kind of phase transition be another phase.Physics, chemical property in material system
It is identical, with other parts there are the uniform parts of apparent interface to be known as phase.Corresponding with solid, liquid, gas tri-state, substance has solid
Phase, liquid phase, gas phase.
Existing beneficiation method is according to the physicochemical properties of different minerals in ore, using gravity separation method, floatation, magnetic separation
Method, chemical method etc., valuable mineral and gangue mineral are separated, and the valuable mineral of various symbiosis (association) is made mutually to divide as far as possible
From, remove or reduce objectionable impurities, with smelted or other industry needed for raw material process.
The deficiency that existing beneficiation method is primarily present:
1, gravity separation method：There is sewage discharge waste water resource using a large amount of water, pollutes environment.
2, floatation：There is dressing agent addition to have mineral dressing additive pollution to concentrate selection and tailing, to use a large amount of washings
Tailing waste water resource, and have sewage discharge.
3, magnetic method：By the effect of magnetic influence of mineral, to not having magnetic mineral not work.
4, chemical method：Chemicals resource is consumed, tailing is polluted with chemicals, and there are chemicals transport, storages
And operational hazards.Use a large amount of washings, waste water resource.
Existed using above method：There is sewage discharge polluted source, there is tailings discharging to occupy large amount of land resources, resource wave
Fei great, environmental pollution is big, endangers people's life.
Invention content
A kind of few, energy saving, the safe and environment-friendly phase of resource consumption for being provided it is an object of the invention to overcome disadvantages mentioned above
Become the method for ore dressing.
A kind of method of phase transformation ore dressing of the present invention, includes the following steps：
(1) feedstock processing：Raw material is crushed to 15~35mm, drying is 5~8%, grinds to 150~300 μ to attachment water content
After m, into fourth stage flue gas direct heat exchanger, after level Four flue gas direct heat exchanger is heated to 600~900 DEG C, from the first order
The bottom of flue gas direct heat exchanger goes out to make a return journey fluidized calcination room；
(2) combustion air heats：Combustion air enters fourth stage direct heat exchanger, 600 are heated to through level Four direct heat exchanger~
After 900 DEG C, go out to make a return journey fluidized calcination room at the top of first order direct heat exchanger；
(3) fluidized calcination：600~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, combustion of the fuel from fluidized calcination room
Material mouth enters, and full combustion of fuel makes the temperature of fluidized calcination room reach in raw material mainly by more than phase change material boiling point, 600~
900 DEG C of raw materials enter from the feed inlet of fluidized calcination room, become solid, liquid, gas three-phase material from boiling after being calcined 3~5 seconds
The top of calcining compartment is discharged, into high-temperature gas-solid separator；
(4) high-temperature gas-solid detaches：After the separation of high-temperature gas-solid separator, gaseous substance is arranged from the top of high-temperature gas-solid separator
Go out, into first order indirect type heat exchanger；Solid, liquid phase substance becomes clinker and is discharged from the bottom of high-temperature gas-solid separator, enters
After clinker indirect type cooler is cooled to 60~80 DEG C, concentrate is obtained；
(5) processing of gaseous substance：Into after the gaseous substance heat exchange of first order indirect type heat exchanger, temperature is reduced to mainly
By more than the fusing point of phase change material, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into first order height
Liquid phase substance and gaseous substance are carried out gas-liquid separation by wet liquid/gas separator, and liquid phase substance is from first order high temperature gas-liquid separator
Bottom is discharged, and cools to 250~300 DEG C through level Four direct heat exchanger and combustion air heat exchange, is cooled down into first order indirect type
Device is cooled to 60~80 DEG C, obtains product one；Gaseous substance is discharged from the top of first order high temperature gas-liquid separator, into second
Grade indirect type heat exchanger exchanges heat more than the fusing point by phase change material set to this grade, below boiling point so that gaseous substance transformation
For gas-liquid phase mixture, gas-liquid separation is carried out subsequently into second level high temperature gas-liquid separator, liquid phase substance is from second level high temperature
The bottom of gas-liquid separator is discharged, and is cooled to 60~80 DEG C into second level indirect type cooler, obtains product two；Gaseous substance
From the top of second level high temperature gas-liquid separator be discharged, into third level indirect type heat exchanger exchange heat to this grade set by phase transformation
More than the fusing point of substance, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into third level high temperature gas-liquid
Separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of third level high temperature gas-liquid separator, obtains product three；Gas gas-phase objects
Matter from the top of third level high temperature gas-liquid separator be discharged, into fourth stage indirect type heat exchanger exchange heat to this grade set by phase
Become the fusing point of substance or more, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into fourth stage High Temperature Gas
Liquid/gas separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of fourth stage high temperature gas-liquid separator, indirect into the fourth stage
Formula cooler is cooled to 60~80 DEG C, obtains product four；Gaseous substance is discharged from the top of fourth stage high temperature gas-liquid separator, into
Enter level V indirect type heat exchanger to exchange heat more than the fusing point by phase change material set to this grade, below boiling point so that gas gas-phase objects
Qualitative change is gas-liquid phase mixture, carries out gas-liquid separation subsequently into level V high temperature gas-liquid separator, liquid phase substance is from the 5th
The bottom discharge of grade high temperature gas-liquid separator, is cooled to 60~80 DEG C into level V indirect type cooler, obtains product five, gas
Phase substance is discharged as flue gas from the top of level V high temperature gas-liquid separator, into first order flue gas direct heat exchanger and raw material
It exchanges heat.
A kind of method of above-mentioned phase transformation ore dressing, wherein：Flue gas in (5) step is through level Four flue gas direct heat exchanger and original
Material exchanges heat to after 250~300 DEG C, and into low temperature gas-solid separator, flue gas is discharged from the top of low temperature gas-solid separator, into receipts
Dirt device, the flue gas after gathering dust out enter drying from dust-precipitator, are used for drying material；From dust-precipitator bottom discharge solids with it is low
The bottom discharge solids of wet solid separator enters first order flue gas direct heat exchanger and enters fluidized calcination room together with raw material.
A kind of method of above-mentioned phase transformation ore dressing, wherein：Raw material is bauxite, Bayer process aluminium oxide tailing and asbestos mine etc..
A kind of method of above-mentioned phase transformation ore dressing, wherein：Fuel is natural gas, oil liquefied gas or coal gas.
Compared with prior art, the present invention having a significant effect, it was found from technical solution：Master is being continuously improved in the present invention
The refractory material that superhigh temperature can be continuously available under the premise of phase change material temperature is wanted, so as to obtain the metal of ultra-high temperature
Oxide, phase change oxide purity is high, good product quality.At high temperature since slag amount is very little, cannot function as heating combustion-supporting sky
The heat medium of gas will do heat transferring medium using phase change material.Without using any chemicals, chemicals resource is saved.
Dry method is run, and saves water resource.Kind of a poly-metal deoxide product can be obtained by handling a kind of ore, and clinker is concentrate (rare gold
Belong to mine) it is used for refining rare metal and does high grade refractory；Resource utilization is high.Using flue gas and raw material heat exchange, liquid phase object
Matter exchanges heat with combustion air.Tailing is pollution-free, not deslagging.System is run under negative pressure, fluidized calcination low noise, no molten bath row
Material, dump temperature is low, and no high temperature safe hidden danger, security risk is small, energy saving.There is no flame phenomenon, no fire hazard.
Description of the drawings
Fig. 1 is the process flow chart of the present invention.
Specific implementation mode
Embodiment 1：
A kind of phase transformation beneficiation method (method of processing bauxite, with Fe2O3For main phase change material), include the following steps：
(1) feedstock processing：Raw material is crushed to 15~35mm, drying is 5~8%, grinds to 150~300 μ to attachment water content
After m, into fourth stage flue gas direct heat exchanger, after level Four flue gas direct heat exchanger is heated to 600~900 DEG C, from the first order
The bottom of flue gas direct heat exchanger goes out to make a return journey fluidized calcination room；
(2) combustion air heats：Combustion air enters fourth stage direct heat exchanger, 600 are heated to through level Four direct heat exchanger~
After 900 DEG C, go out to make a return journey fluidized calcination room at the top of first order direct heat exchanger；
(3) fluidized calcination：600~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, combustion of the fuel from fluidized calcination room
Material mouth enters, and full combustion of fuel makes the temperature of fluidized calcination room reach Fe2O3Boiling point more than 3450~3600 DEG C, 600~
900 DEG C of raw materials enter from the feed inlet of fluidized calcination room, become solid, liquid, gas three-phase material from boiling after being calcined 3~5 seconds
The top of calcining compartment is discharged, into high-temperature gas-solid separator；
(4) high-temperature gas-solid detaches：After the separation of high-temperature gas-solid separator, gaseous substance is arranged from the top of high-temperature gas-solid separator
Go out, into first order indirect type heat exchanger；Solid, liquid phase substance becomes clinker and is discharged from the bottom of high-temperature gas-solid separator, enters
After clinker indirect type cooler is cooled to 60~80 DEG C, concentrate is obtained；
(5) processing of gaseous substance：Into after the gaseous substance heat exchange of first order indirect type heat exchanger, temperature is reduced to
Fe2O3Fusing point more than, 3200~3380 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into
Liquid phase substance and gaseous substance are carried out gas-liquid separation by first order high temperature gas-liquid separator, and liquid phase substance is from first order high temperature gas-liquid
The bottom of separator is discharged, and 250~300 DEG C is cooled to through level Four direct heat exchanger and combustion air heat exchange, between the first order
After the formula cooler of connecing is cooled to 60~80 DEG C, product one is obtained；Gaseous substance is arranged from the top of first order high temperature gas-liquid separator
Go out, into second level indirect type heat exchanger, temperature is reduced to Al2O3Fusing point more than, 2300~2900 DEG C below of boiling point,
So that gaseous substance is changed into gas-liquid phase mixture, gas-liquid separation, liquid phase are carried out subsequently into second level high temperature gas-liquid separator
Substance is discharged from the bottom of second level high temperature gas-liquid separator, after being cooled to 60~80 DEG C into second level indirect type cooler,
Obtain product two；Gaseous substance is discharged from the top of second level high temperature gas-liquid separator, will into third level indirect type heat exchanger
Temperature is reduced to SiO2Fusing point more than, 2000~2200 DEG C below of boiling point so that gaseous substance is changed into gas-liquid and mixes
Object carries out gas-liquid separation subsequently into third level high temperature gas-liquid separator, and liquid phase substance is from third level high temperature gas-liquid separator
Bottom is discharged, and obtains product three；Gaseous substance is discharged from the top of third level high temperature gas-liquid separator, into fourth stage indirect type
Temperature is reduced to Na by heat exchanger2It is more than the fusing point of O, 1600~1900 DEG C below of boiling point so that gaseous substance is changed into gas
Liquid phase mixture carries out gas-liquid separation subsequently into fourth stage high temperature gas-liquid separator, and liquid phase substance is from fourth stage high temperature gas-liquid
The bottom of separator is discharged, and after being cooled to 60~80 DEG C into fourth stage indirect type cooler, obtains product four；Gaseous substance from
The top of fourth stage high temperature gas-liquid separator is discharged, and into level V indirect type heat exchanger, temperature is reduced to K2The fusing point of O with
Upper, 1200~1400 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into level V High Temperature Gas
Liquid/gas separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of level V high temperature gas-liquid separator, indirect into level V
After formula cooler is cooled to 60~80 DEG C, product five is obtained, gaseous substance is as flue gas from level V high temperature gas-liquid separator
Top is discharged, and exchanges heat into first order flue gas direct heat exchanger with raw material.Flue gas is through level Four flue gas direct heat exchanger and original
Material exchanges heat to after 250~300 DEG C, and into low temperature gas-solid separator, flue gas is discharged from the top of low temperature gas-solid separator, into receipts
Dirt device, the flue gas after gathering dust out enter drying from dust-precipitator, are used for drying material；From dust-precipitator bottom discharge solids with it is low
The bottom discharge solids of wet solid separator enters first order flue gas direct heat exchanger and enters fluidized calcination room together with raw material.
With phase transformation Fe2O3Handle the material variation such as table 1 of bauxite
Phase transformation Fe2O3One ton of bauxite of processing obtains；Fe2O3Measure 337.4kg, TiO2Measure 37.5kg, Al2O3Measure 352.8kg, CaO
Measure 15.9kg, SiO2Measure 155.3kg, Na2O amounts 9.10kg, K2O amount 11.3kg and 78.4kg concentrate.
Embodiment 2：
A kind of phase transformation beneficiation method (processing Bayer process aluminium oxide tailing, with Fe2O3For main phase change material), including following step
Suddenly：
(1) feedstock processing：Raw material stoving is 5~8%, ground to after 150~300 μm to attachment water content, into the fourth stage
Flue gas direct heat exchanger directly changes after the direct flue gas direct heat exchanger of level Four is heated to 650~900 DEG C from first order flue gas
The bottom of hot device goes out to make a return journey fluidized calcination room；
(2) combustion air heats：Combustion air enters fourth stage direct heat exchanger, 650 are heated to through level Four direct heat exchanger~
After 900 DEG C, go out to make a return journey fluidized calcination room at the top of first order direct heat exchanger；
(3) fluidized calcination：650~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, combustion of the fuel from fluidized calcination room
Material mouth enters, and full combustion of fuel makes the temperature of fluidized calcination room reach Fe2O3More than boiling point 3450~3600 DEG C, 650~
900 DEG C of raw materials enter from the feed inlet of fluidized calcination room, become solid, liquid, gas three-phase material from boiling after being calcined 3~5 seconds
The top of calcining compartment is discharged, into high-temperature gas-solid separator；
(4) high-temperature gas-solid detaches：After the separation of high-temperature gas-solid separator, gaseous substance is arranged from the top of high-temperature gas-solid separator
Go out, into first order indirect type heat exchanger；Solid, liquid phase substance becomes clinker and is discharged from the bottom of high-temperature gas-solid separator, enters
After clinker indirect type cooler is cooled to 60~80 DEG C, concentrate is obtained；
(5) processing of gaseous substance：Into after the gaseous substance heat exchange of first order indirect type heat exchanger, temperature is reduced to
Fe2O3Fusing point more than, 3150~3380 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into
Liquid phase substance and gaseous substance are carried out gas-liquid separation by first order high temperature gas-liquid separator, and liquid phase substance is from first order high temperature gas-liquid
The bottom of separator is discharged, and 250~300 DEG C is cooled to through level Four direct heat exchanger and combustion air heat exchange, between the first order
After the formula cooler of connecing is cooled to 60~80 DEG C, product one is obtained；Gaseous substance is arranged from the top of first order high temperature gas-liquid separator
Go out, into second level indirect type heat exchanger, temperature is reduced to Al2O3Fusing point more than, 2350~2900 DEG C below of boiling point,
So that gaseous substance is changed into gas-liquid phase mixture, gas-liquid separation, liquid phase are carried out subsequently into second level high temperature gas-liquid separator
Substance is discharged from the bottom of second level high temperature gas-liquid separator, after being cooled to 60~80 DEG C into second level indirect type cooler,
Obtain product two；Gaseous substance is discharged from the top of second level high temperature gas-liquid separator, will into third level indirect type heat exchanger
Temperature is reduced to SiO2Fusing point more than, 2000~2150 DEG C below of boiling point so that gaseous substance is changed into gas-liquid and mixes
Object carries out gas-liquid separation subsequently into third level high temperature gas-liquid separator, and liquid phase substance is from third level high temperature gas-liquid separator
Bottom is discharged, and obtains product three；Gaseous substance is discharged from the top of third level high temperature gas-liquid separator, into fourth stage indirect type
Temperature is reduced to Na by heat exchanger2It is more than the fusing point of O, 1650~1900 DEG C below of boiling point so that gaseous substance is changed into gas
Liquid phase mixture carries out gas-liquid separation subsequently into fourth stage high temperature gas-liquid separator, and liquid phase substance is from fourth stage high temperature gas-liquid
The bottom of separator is discharged, and after being cooled to 60~80 DEG C into fourth stage indirect type cooler, obtains product four；Gaseous substance from
The top of fourth stage high temperature gas-liquid separator is discharged, and into level V indirect type heat exchanger, temperature is reduced to K2The fusing point of O with
Upper, 1100~1400 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into level V High Temperature Gas
Liquid/gas separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of level V high temperature gas-liquid separator, indirect into level V
After formula cooler is cooled to 60~80 DEG C, product five is obtained, gaseous substance is as flue gas from level V high temperature gas-liquid separator
Top is discharged, and exchanges heat into first order flue gas direct heat exchanger with raw material.Flue gas is through level Four flue gas direct heat exchanger and original
Material exchanges heat to after 250~300 DEG C, and into low temperature gas-solid separator, flue gas is discharged from the top of low temperature gas-solid separator, into receipts
Dirt device, the flue gas after gathering dust out enter drying from dust-precipitator, are used for drying material；From dust-precipitator bottom discharge solids with it is low
The bottom discharge solids of wet solid separator enters first order flue gas direct heat exchanger and enters fluidized calcination room together with raw material.
With phase transformation Fe2O3Handle the material variation such as the following table 2 of Bayer process aluminium oxide tailing
Phase transformation Fe2O3One ton of Bayer process aluminium oxide tailing of processing obtains；Fe2O3210.2kg, MgO amount 10.3kg, TiO of measuring2Amount
15.0kg、Al2O3209.6kg, CaO amount 184.0kg, SiO of measuring2Measure 156.6kg, Na2O amounts 44.0kg, K2O amounts 0.9kg and
53.4kg concentrate.
Embodiment 3：
A kind of method of phase transformation ore dressing (processing asbestos mine, with MgO for main phase change material), includes the following steps：
(1) feedstock processing：To be crushed to 15~35mm, be dried to moisture weight content raw material be 5~8%, grind to 150~
After 300 μm, into fourth stage flue gas direct heat exchanger, after level Four flue gas direct heat exchanger is heated to 700~900 DEG C, from
The bottom of level-one flue gas direct heat exchanger goes out to make a return journey fluidized calcination room；
(2) combustion air heats：Combustion air enters fourth stage direct heat exchanger, 700 are heated to through level Four direct heat exchanger~
After 900 DEG C, go out to make a return journey fluidized calcination room at the top of first order direct heat exchanger；
(3) fluidized calcination：700~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, combustion of the fuel from fluidized calcination room
Material mouth enters, and full combustion of fuel makes the temperature of fluidized calcination room reach 3650~3800 DEG C of MgO boiling points or more, and 700~900
DEG C raw material enters from the feed inlet of fluidized calcination room, becomes solid, liquid, gas three-phase material from fluidized calcination after 3~5 seconds through calcination
The top of room is discharged, into high-temperature gas-solid separator；
(4) high-temperature gas-solid detaches：After the separation of high-temperature gas-solid separator, gaseous substance is arranged from the top of high-temperature gas-solid separator
Go out, into first order indirect type heat exchanger；Solid, liquid phase substance becomes clinker and is discharged from the bottom of high-temperature gas-solid separator, enters
After clinker indirect type cooler is cooled to 60~80 DEG C, concentrate is obtained；
(5) processing of gaseous substance：Into after the gaseous substance heat exchange of first order indirect type heat exchanger, temperature is reduced to MgO
Fusing point more than, 3450~3550 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into first
Liquid phase substance and gaseous substance are carried out gas-liquid separation by grade high temperature gas-liquid separator, and liquid phase substance is from first order high temperature gas-liquid separation
The bottom of device is discharged, and 250~300 DEG C is cooled to through level Four direct heat exchanger and combustion air heat exchange, into first order indirect type
After cooler is cooled to 60~80 DEG C, product one is obtained；Gaseous substance is discharged from the top of first order high temperature gas-liquid separator, into
Enter second level indirect type heat exchanger, temperature is reduced to Fe2O3Fusing point more than, 2500~3380 DEG C below of boiling point so that gas
Phase substance is changed into gas-liquid phase mixture, subsequently into second level high temperature gas-liquid separator carry out gas-liquid separation, liquid phase substance from
The bottom of second level high temperature gas-liquid separator is discharged, and after being cooled to 60~80 DEG C into second level indirect type cooler, is produced
Product two；Gaseous substance is discharged from the top of second level high temperature gas-liquid separator, and into third level indirect type heat exchanger, temperature is dropped
Down to SiO2Fusing point more than, 2000~2100 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, then
Gas-liquid separation is carried out into third level high temperature gas-liquid separator, liquid phase substance is arranged from the bottom of third level high temperature gas-liquid separator
Go out, obtains product three；Gaseous substance is discharged from the top of third level high temperature gas-liquid separator, exchanges heat into fourth stage indirect type
Temperature is reduced to Na by device2It is more than the fusing point of O, 1700~1900 DEG C below of boiling point so that gaseous substance is changed into liquid phase
Mixture carries out gas-liquid separation subsequently into fourth stage high temperature gas-liquid separator, and liquid phase substance is from fourth stage high temperature gas-liquid separation
The bottom of device is discharged, and after being cooled to 60~80 DEG C into fourth stage indirect type cooler, obtains product four；Gaseous substance is from the 4th
The top discharge of grade high temperature gas-liquid separator, into level V indirect type heat exchanger, K is reduced to by temperature2More than the fusing point of O,
1000~1400 DEG C below of boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into level V high temperature gas-liquid
Separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of level V high temperature gas-liquid separator, into level V indirect type
After cooler is cooled to 60~80 DEG C, product five is obtained；Gaseous substance is as flue gas from the top of level V high temperature gas-liquid separator
Portion is discharged, and exchanges heat into first order flue gas direct heat exchanger with raw material.Flue gas is through level Four flue gas direct heat exchanger and raw material
Heat exchange is to after 250~300 DEG C, and into low temperature gas-solid separator, flue gas is discharged from the top of low temperature gas-solid separator, into gathering dust
Device, the flue gas after gathering dust out enter drying from dust-precipitator, are used for drying material；Solids and low temperature is discharged from dust-precipitator bottom
The bottom discharge solids of gas-solid separator enters first order flue gas direct heat exchanger and enters fluidized calcination room together with raw material.
The material variation such as the following table 3 of asbestos mine are handled with phase transformation MgO
| Project | K2O | Na2O | M gO | SiO2 | Fe2O3 | Other | It is total | Au2O3g/t |
| Chemical composition % | 1.50 | 0.73 | 41.41 | 38.97 | 9.03 | 8.36 | 100.00 | 0.035 |
| Phase transformation ore dressing inventory | 1.50 | 0.73 | 41.41 | 38.97 | 9.03 | 0.00 | 91.64 | 0.035 |
| Residue doses | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 8.36 | 8.36 | |
| Remaining chemical constituent % | 0.00 | 0.00 | 0.00 | 0.00 | 0.00 | 100.00 | 100.00 |
Phase transformation MgO handles one ton of asbestos mine and obtains；MgO amounts 414.1kg, Fe2O3Measure 90.3kg, Au2O3Measure 0.035g, SiO2Amount
389.7kg、K2O amounts 15.0kg, Na2O amount 7.3kg and 83.6kg concentrate.
The above described is only a preferred embodiment of the present invention, being not intended to limit the present invention in any form, appoint
What is simply repaiied to any made by above example according to the technical essence of the invention without departing from technical solution of the present invention content
Change, equivalent variations and modification, in the range of still falling within technical solution of the present invention.
Claims (4)
1. a kind of method of phase transformation ore dressing, includes the following steps：
（1）Feedstock processing：Raw material is crushed to 15~35mm, drying to adhesive water content is 5~8%, is ground to 150~300
After μm, into fourth stage flue gas direct heat exchanger, after level Four flue gas direct heat exchanger is heated to 600~900 DEG C, from the first order
The bottom of flue gas direct heat exchanger goes out to make a return journey fluidized calcination room；
（2）Combustion air heats：Combustion air enters fourth stage direct heat exchanger, 600 are heated to through level Four direct heat exchanger~
After 900 DEG C, go out to make a return journey fluidized calcination room at the top of first order direct heat exchanger；
（3）Fluidized calcination：600~900 DEG C of combustion airs enter from the bottom of fluidized calcination room, combustion of the fuel from fluidized calcination room
Material mouth enters, and full combustion of fuel makes the temperature of fluidized calcination room reach in raw material mainly by more than phase change material boiling point, 600~
900 DEG C of raw materials enter from the feed inlet of fluidized calcination room, become solid, liquid, gas three-phase material from boiling after being calcined 3~5 seconds
The top of calcining compartment is discharged, into high-temperature gas-solid separator；
（4）High-temperature gas-solid detaches：After the separation of high-temperature gas-solid separator, gaseous substance is arranged from the top of high-temperature gas-solid separator
Go out, into first order indirect type heat exchanger；Solid, liquid phase substance becomes clinker and is discharged from the bottom of high-temperature gas-solid separator, enters
After clinker indirect type cooler is cooled to 60~80 DEG C, concentrate is obtained；
（5）The processing of gaseous substance：Into after the gaseous substance heat exchange of first order indirect type heat exchanger, temperature is reduced to mainly
By more than the fusing point of phase change material, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into first order height
Liquid phase substance and gaseous substance are carried out gas-liquid separation by wet liquid/gas separator, and liquid phase substance is from first order high temperature gas-liquid separator
Bottom is discharged, and cools to 250~300 DEG C through level Four direct heat exchanger and combustion air heat exchange, is cooled down into first order indirect type
After device is cooled to 60~80 DEG C, product one is obtained；Gaseous substance is discharged from the top of first order high temperature gas-liquid separator, into the
Two level indirect type heat exchanger exchanges heat more than the fusing point by phase change material set to this grade, below boiling point so that gaseous substance turns
Become gas-liquid phase mixture, carries out gas-liquid separation subsequently into second level high temperature gas-liquid separator, liquid phase substance is from second level height
The bottom of wet liquid/gas separator is discharged, and after being cooled to 60~80 DEG C into second level indirect type cooler, obtains product two；Gas phase
Substance is discharged from the top of second level high temperature gas-liquid separator, exchanges heat the quilt set to this grade into third level indirect type heat exchanger
More than the fusing point of phase change material, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into third level high temperature
Gas-liquid separator carries out gas-liquid separation and obtains product three after liquid phase substance is discharged from the bottom of third level high temperature gas-liquid separator；
Gaseous substance is discharged from the top of third level high temperature gas-liquid separator, exchanges heat to this grade and sets into fourth stage indirect type heat exchanger
The fusing point by phase change material more than, below boiling point so that gaseous substance is changed into gas-liquid phase mixture, subsequently into the fourth stage
High temperature gas-liquid separator carries out gas-liquid separation, and liquid phase substance is discharged from the bottom of fourth stage high temperature gas-liquid separator, into the 4th
After grade indirect type cooler is cooled to 60~80 DEG C, product four is obtained；Gaseous substance is from the top of fourth stage high temperature gas-liquid separator
Portion is discharged, into level V indirect type heat exchanger exchanges heat more than the fusing point by phase change material set to this grade, boiling point is hereinafter, make
It obtains gaseous substance and is changed into gas-liquid phase mixture, gas-liquid separation, liquid phase object are carried out subsequently into level V high temperature gas-liquid separator
Matter is discharged from the bottom of level V high temperature gas-liquid separator, after being cooled to 60~80 DEG C into level V indirect type cooler, obtains
To product five, gaseous substance is discharged as flue gas from the top of level V high temperature gas-liquid separator, direct into first order flue gas
Heat exchanger exchanges heat with raw material.
2. a kind of method of phase transformation ore dressing as described in claim 1, wherein：The（5）Flue gas in step is direct through level Four flue gas
After the heat exchange of heat exchanger and raw material is cooled to 250~300 DEG C, into low temperature gas solid separation, flue gas is from the top of low temperature gas-solid separator
Portion is discharged, and into dust-precipitator, the flue gas after gathering dust out enters drying from dust-precipitator, is used for drying material；From dust-precipitator bottom
Discharge solids enters first order flue gas direct heat exchanger together with raw material with the bottom of low temperature gas-solid separator discharge solids
Into fluidized calcination room.
3. a kind of method of phase transformation ore dressing as claimed in claim 1 or 2, wherein：Raw material is bauxite, Bayer process aluminium oxide tailing
With asbestos mine etc..
4. a kind of method of phase transformation ore dressing as claimed in claim 1 or 2, wherein：Fuel is natural gas, oil liquefied gas or coal
Gas.
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