CN105107435B - A kind of fluidized reactor and the method using the reactor for treatment ore - Google Patents
A kind of fluidized reactor and the method using the reactor for treatment ore Download PDFInfo
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- CN105107435B CN105107435B CN201510574108.6A CN201510574108A CN105107435B CN 105107435 B CN105107435 B CN 105107435B CN 201510574108 A CN201510574108 A CN 201510574108A CN 105107435 B CN105107435 B CN 105107435B
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- 239000011572 manganese Substances 0.000 description 11
- 239000003638 chemical reducing agent Substances 0.000 description 10
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- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 8
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- 229910019142 PO4 Inorganic materials 0.000 description 2
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- UQMRAFJOBWOFNS-UHFFFAOYSA-N butyl 2-(2,4-dichlorophenoxy)acetate Chemical compound CCCCOC(=O)COC1=CC=C(Cl)C=C1Cl UQMRAFJOBWOFNS-UHFFFAOYSA-N 0.000 description 2
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Abstract
The present invention relates to a kind of fluidized reactor (1), the reactor (1) at least has combustion chamber (10) and the first reative cell (20), and the combustion chamber (10) and first reative cell (20) are separated from one another by being arranged on injection arch (11) at the top of the combustion chamber (10)；The high-temperature gas produced through burning in the combustion chamber (10) can spurt into first reative cell (20) by the flow path (111) being arranged on injection arch (11), and the high-temperature gas for spurting into the first reative cell (20) can be used to hold up the solid particle material of first reative cell (20) and carry out high-temperature heating reaction.The reactor that the present invention is provided is applied to middle-low grade ore, overcome the high energy consumption issues caused using the reactor of prior art, the reactiveness of reactor of the invention especially centering poor value is controlled, solve the problems, such as material occur melting, coking and cause slag-drip opening block.
Description
Technical field
A kind of reactor the present invention relates to chemical production technical field and the method using the reactor for treatment ore, especially
Its a kind of method for being related to fluidized reactor suitable for solid particle and ore being processed using the fluidized reactor.
Background technology
It is well known that mineral resources are the material bases of human survival and development.Root according to relevant statistics, work in the world
The raw material 70% of industry manufactured goods comes from mineral resources, and the energy has 90% from mineral resources.China is mineral resources in the world
Compare one of more complete a few countries of abundant, mineral.The mineral resources of China have the characteristics that：
First, distribution of mineral deposits is uneven, and some important pillar mineral products are generally not enough, it is necessary to long-term shortage or proved reserves
Dependence on import.Second, many rich ores of lean ore are few, and low-grade refractory ore proportion is big, and such as China's iron ore average grade is
33.5%, it is lower than world average level more than 10 percentage points；Manganese ore average grade is only 22%, with the industry of world's merchantable ore
The 48% of standard differs greatly；Copper mine average grade is only 0.87%；Phosphorus ore average grade only 16.95%；Bauxite is almost complete
It is diaspore, separation and Extraction difficulty is very big.3rd, Large-super Large mineral deposit is few, in-Small Ore Deposits are more, be with copper mine
Example, the copper mine place of production more than 900 that China finds so far is located, and wherein Large-super Large mineral deposit only accounts for 3%, and medium-sized mineral deposit accounts for 9%, small
Type mineral deposit up to 88%.4th, the mineral deposit of single mineral is few, and intergrowth deposit is more, and the common of China, accompanying mineral deposit are accounted for according to statistics
Verify the 80% of ore reserve.
At present, China in the utilization of ore resource exist comprehensive utilization consciousness it is thin, make a low multiple use；Technology is owed
Lack, the problem that technological level falls behind.Especially the comprehensive utilization technique of centering poor value is more short of, and it is mainly showed
：Traditional mineral products producing process complexity, long flow path, high cost；Mining technology technical merit falls behind, selects the automatic of smelting process
Controlled level is low, selecting-smelting process not science, abandons many associations, the loss of symbiosis component；Large Efficient low consumption selects smelting to process dress
Standby to lack, ore dressing plant equipment is not high；It is relative to lack the elder generation that comprehensive reutilization is carried out to solid waste such as mine tailing, waste residues
Enter equipment and technique.Therefore, in order to utilize middle-low grade ore, developing a kind of novel reactor and novel production process has turned into
Problem demanding prompt solution.
For fixed bed reactors, the fluidized-bed reactor using fluidization technology has heat transfer and mass-transfer efficiency
Height, bed temperature tends to uniform, can prevent hot-spot, operates the features such as relatively stablizing, at present as a basic technology,
It is widely used in the every field such as chemical industry, metallurgy, the energy, environmental protection.Chinese patent (Publication No. CN 102616759A) is disclosed
A kind of fluidized-bed reactor.Zoneofoxidation and reduction are distinguished and realize heat by the fluidized-bed reactor of the patent by heat-conducting plate
Coupling, by making ore materials Reduction on Fluidized Bed, reinforcing heat, matter transmission are greatly reduced its reduction temperature and reaction time, solve
The problems such as rotary kiln putty ring formation.But, there is following defect in implementation process in the patent：First, the gas of the patent point
Cloth device is in planar structure, if deposited more solid particle on gas distributor, plane gas distributor is difficult to hold
Fracture is easily caused by its gravity, and slag mouth is arranged on gas distributor top, the gas distributor of planar structure is not yet
Beneficial to the smooth discharge of slag.Secondly, the energy in combustion process by plane gas distributor is not enough, it is difficult to will reduce
The ore of reaction zone holds up and is dispersed in whole reducing zone so that the ore of entrance is deposited in reduction reaction area mostly
Bottom, reduction effect is undesirable, and the ore for entering easily results in blockage to gas distributor, and what influence was reacted continuously enters
OK.Again, zoneofoxidation and reduction are distinguished by heat-conducting plate, realizes that heat is coupled using heat-conducting plate, it is impossible to make full use of
Heat, easily causes the loss of heat, prevents zoneofoxidation from obtaining enough heats.In addition, the oxygen-enriched air of the patent and centre
Air inlet is flowed up product gas from below, because the flow velocity of the two is different, causes mixed effect undesirable so that oxidation
Reaction carries out insufficient.
Chinese patent (Publication No. CN 101413056A) discloses a kind of reactor for manganese ore.The patent
Reactor is three sections of reduction roasters of vertical structure of upper, middle and lower.Epimere is firing chamber, to multitubular firing chamber or irregular ball
Shape roasting device in manganese powder carry out isolation flame roasting, be conducive to manganese mineral powder reduce and will not airborne dust.But, the roasting of the patent
Room is multipipe structure, it is necessary to multiple burner could meet requirement of each pipe to heat, not only increases the cost of equipment, wastes combustion
Material；And, even the multiple burners of distribution, it is also difficult to ensure that the reduction temperature of each pipe is uniform so that reduction product quality is present
Difference.Air after recovery waste heat is passed through fuel gas inlet pipe by the patent again, although can be improved the utilization of heat energy, but be fired
Gas and air mixing are uneven, and fuel combustion forms flame long so that burning is insufficient, causes the waste of the energy.
In addition, in middle-low grade ore comprehensive utilization technique, also following two technical problems are easily by this area
What technical staff ignored：One is that at high temperature, the fractions in ore easily form molten state material, such as coke, silica, phosphorus ore
Stone etc.；When molten state material of the viscosity flow on furnace wall drops to discharging opening, the reduction of temperature easily causes molten state material coking,
And then discharging opening is resulted in blockage so that reaction can not be carried out continuously, and need frequent clean reactor.Two is existing reaction
The insulation material used in device mostly amorphous refractory, such as mullite pouring material, high alumina castable or corundum castable,
The thickness of refractory masses used is usually 1000~1400mm, although the refractory masses for using in the prior art can be effectively
The loss of furnace heat is controlled, but the thickness of refractory masses is thicker, greatly reduces the free space of reactor.
Therefore, being badly in need of a kind of advanced reactor of exploitation can substitute reaction equipment backward in the prior art, with solution
The Utilizing question of poor value.
The content of the invention
For the deficiency of prior art, the invention provides a kind of fluidized reactor, the reactor at least has burning
The injection of room and the first reative cell, the combustion chamber and first reative cell by being arranged on the top of combustion chamber is encircleed each other
Separate so that the high-temperature gas produced through burning in the combustion chamber can be led to by the jet flow being arranged on the injection arch
First reative cell is spurted into road upwards, and the high-temperature gas for spurting into the first reative cell can be used to anti-by described first
Answer the solid particle material of room to hold up and carry out high-temperature heating reaction.First reative cell can be referred to as reduction room.It is described
First reative cell can also be referred to as oxidizing chamber.First reative cell is also referred to as catalyst chamber.First reative cell
It is also referred to as replacing room.The injection arch can also be referred to as the gas distributor of arch.The injection arch can also be by
The referred to as shower nozzle of arch.The flow path can be referred to as spray orifice.The flow path can also be referred to as stomata.
According to a preferred embodiment, the injection arch is the domes being made up of refractory material；Described at least one
Individual flow path is arranged in the cambered surface near the axis of the injection arch, and the size of the flow path at least meets
Gas flow rate after the fuel in combustion chamber gas expansion.The domes can also be referred to as Curved structure.
According to a preferred embodiment, the reactor also has the second reative cell, and first reative cell is by adding
The intermediate product being thermally generated rises to second reative cell, and the intermediate product and the described second reaction with high temperature gas flow
The unstrpped gas that room enters proceeds pyroreaction；The high temperature gas flow and described flowed up by first reative cell
The airflow interface that the flow of feed gas that two reative cells enter forms stabilization divides with by first reative cell and second reative cell
Separate.Second reative cell can be referred to as reduction room.Second reative cell can also be referred to as oxidizing chamber.Described second
Reative cell is also referred to as catalyst chamber.
According to a preferred embodiment, there is collection viscosity flow to exist respectively for first reative cell and second reative cell
The component that dams of the molten state material on furnace wall, the component that dams is respectively arranged at first reative cell and described second anti-
The bottom of room is answered, and the component that dams dams fairlead, and at least one including at least one first cut-off grooves and first
Individual second cut-off groove and second dams fairlead；Wherein, first cut-off groove and second cut-off groove, radially-inwardly to dash forward
The mode for going out is embedded in the combination refractory masses, and the interface of first cut-off groove and second cut-off groove is upward
Incline to receive molten state material of the viscosity flow in furnace wall；Described first dams fairlead and the described second opening for damming fairlead
Be inclined upwardly and described first dam fairlead and described second dam fairlead with its lower edge that is open respectively with described first
The mode of the interface lower edge docking of cut-off groove and second cut-off groove is arranged at first cut-off groove and described second and dams
Derived outside stove with by the molten state material collected by it in groove.The component that dams can be referred to as collection assembly.It is described to dam
Groove can be referred to as collecting tank.The fairlead that dams can be referred to as delivery line.The fairlead that dams can also be referred to as
Drainage tube.
According to a preferred embodiment, the bottom of combustion chamber is provided with a fuel gas inlet pipe along axis direction,
The upper end of the fuel gas inlet pipe is provided with a combustion head；Wherein, the combustion head is made up of high-temperature refractory, and institute
The domed structure of combustion head is stated, has multiple a diameter of 6 by warp, weft direction arranged for interval in the cambered surface of the arch combustion head
The spray orifice of~12mm；The surrounding of the combustion head there also is provided at least two air hoses, and the air hose top is furnished with least one
Individual detection mouth, the detection mouthful is used to monitor the fired state of the combustion chamber.The combustion head can be referred to as burner.It is described
Combustion head may also be referred to as combustion gas head.The detection mouth can be referred to as temperature monitoring mouthful.The detection mouth can also be referred to as
Temperature control mouthful.The spray orifice can be referred to as through hole.The spray orifice can also be referred to as passage.
According to a preferred embodiment, the reactor also includes being combined by fire resisting molding mass and castable refractory
Combination refractory masses, the shell of the reactor, and the combination fire proofed wood are lining in the combination refractory masses
The thickness of the bed of material is 500~700mm.The combination refractory masses can be referred to as heat-insulation layer.
According to a preferred embodiment, first reative cell also includes at least one feed pipe and at least one deslagging
Pipe；Wherein, the feed pipe is located at dam component bottom and the feed pipe of second reative cell Open Side Down with it
Inclined mode is arranged at the top of first reative cell；The scum pipe dams under component positioned at first reative cell
Described in portion and the scum pipe are arranged in the way of its acclivitous opening lower edge dock with the cambered surface of the injection arch
The lower end of the first reative cell.The scum pipe can also be referred to as discharge nozzle.The opening lower edge of the scum pipe and the injection
The mode of the cambered surface docking of arch can also be referred to as the tangent side of cambered surface that the opening lower edge of the scum pipe is encircleed with the injection
Formula.
According to a preferred embodiment, the high temperature of the combustion chamber and first reative cell is 700~1350 DEG C, institute
The high temperature for stating the second reative cell is 700~1800 DEG C.
According to a preferred embodiment, second reative cell also includes at least one outlet and at least one air inlet
Pipe；Wherein, the outlet be arranged at second reative cell top be used to derive along the direction of axis product and/
Or exclude tail gas；The air inlet pipe is arranged at the bottom of second reative cell and higher than the group of damming of second reative cell
The position of part is used to the intermediate product for importing unstrpped gas and second reative cell being travelled up to first reative cell
Continue to participate in reaction.
Present invention also offers a kind of method that ore is processed using fluidized reactor of the invention, methods described is included such as
Lower step：Refining is made, will again carry out making refining after ore reduction, form solid particle as raw material；Heating, before reaction starts, combustion gas
Heated with the first reative cell and the second reative cell to the reactor with combustion adjuvant mixed combustion by combustion head；Instead
Should, the solid particle is held up and suspended by the gas that the flow path from injection arch sprays upwards after entering the first reative cell
There is first step reaction in first reative cell, and the combustion reaction and first step reaction are described by being arranged on
The injection arch of top of combustion chamber is separated from one another；And/or the intermediate product of the first reative cell generation is entered by ascending air
Enter the second reative cell and second step reaction occurs at high temperature with the unstrpped gas entered from air inlet pipe, and the first step is anti-
The unstrpped gas that should be entered with second reative cell by the upward air-flow of first reative cell with second step reaction
The airflow interface for forming stabilization is separated from one another；Collection of products and deslagging, gaseous product and/or tail gas after having reacted pass through
Mouth pipe is derived outside stove, and solid product and/or tailings after having reacted are discharged out of the furnace by scum pipe.It is described to make refining and be referred to as
The raw material preparatory stage.It is described to make refining and be referred to as granulating stage.First reaction can be referred to as reduction reaction.It is described
First reaction can also be referred to as oxidation reaction.First reaction is also referred to as catalytic reaction.First reaction is also
Displacement can be referred to as to react.Second reaction can be referred to as reduction reaction.Second reaction can also be referred to as oxygen
Change reaction.Second reaction is also referred to as catalytic reaction.
The method of the utilization reactor for treatment ore that the present invention is provided, also comprises the following steps：Fused mass is collected：The first step
The molten state material that reaction and/or second step reaction are produced is collected through the first cut-off groove and/or the second cut-off groove.Collect to damming
The molten state material of groove by first dam fairlead and/or second dam fairlead derive stove outside.
Fluidized reactor and use the method for the reactor for treatment ore at least with following advantage that the present invention is provided：
(1) present invention sets injection arch structure by the top of combustion chamber, will be burnt by the flow path for spraying arch
The high temperature air jet that room burning is produced enters the first reative cell, can make the ore particles of the first reative cell in fluidized state, fluidisation
The ore particles of state are easier to react；The high-temperature gas flow velocity for spraying into the first reative cell by flow path is larger, foot
To hold up the ore particles in the first reative cell；Even if high-temperature high-speed airflow cannot hold up the larger particle in part is suspended in the
One reative cell, it is also possible to bear its gravity by spraying arch, it is ensured that ore particles react in the first reative cell.
(2) reactor of the invention only has a combustion head, by the spray orifice being evenly arranged on combustion head, can make burning
Indoor combustion gas is well mixed with combustion adjuvant air, and burning forms short flame so that full combustion of fuel.
(3) present invention secondary intake pipes are arranged on the second reative cell, by air inlet pipe enter unstrpped gas can with it is same
The intermediate product that high temperature gas flow rises continues to react, and solves oxygen-enriched air pipe is arranged under reactor in the prior art
Side, it is difficult to and the problem that intermediate product fully reacts.
(4) present invention is respectively provided with cut-off groove and the fairlead that dams in the bottom of the first reative cell and the second reative cell, leads to
Cross cut-off groove by viscosity flow furnace wall molten state collecting material, then by dam fairlead will collect molten state material derive stove
Outward, it is to avoid molten state material results in blockage to scum pipe.
(5) refractory material that the present invention will be used in the prior art is changed to combine refractory masses, can not only improve guarantor
Temp effect, and can substantially reduce the thickness of adiabator layer, increase the free space of reactor.
(6) present invention provide fluidized reactor and using the reactor for treatment ore method be applied in, it is low-grade
The comprehensive utilization of ore, overcomes the problem that prior art consersion unit falls behind the high energy consumption and environmental pollution for causing；The present invention
Especially centering, the reactiveness of poor value and the reaction time is controlled, and solves material and melting, coking and blocking occurs
Problem, be capable of achieving continous way production.
Brief description of the drawings
Fig. 1 is the structural representation of fluidized reactor of the invention；
Fig. 2 is the cross-sectional view of injection arch of the invention；
Fig. 3 is the cross-sectional view of combustion head of the invention；With
Fig. 4 is the spray orifice location arrangements schematic diagram of combustion head of the invention.
Reference numerals list
1：Reactor 10：Combustion chamber 20：First reative cell
30：Second reative cell 40：Shell 50：Combination refractory masses
11：Injection arch 12：Detection mouth 13：Air hose
14：Combustion head 15：Fuel gas inlet pipe 21：Feed pipe
22：First cut-off groove 23：First dams fairlead 24：Scum pipe
31：Outlet 32：Air inlet pipe 33：Second cut-off groove
34：Second dams fairlead 111：Flow path 141：Spray orifice
Specific embodiment
It is described in detail below in conjunction with the accompanying drawings.
Fig. 1 shows a kind of fluidized reactor 1.As shown in figure 1, reactor 1 at least reacts with combustion chamber 10 and first
Room 20.The reative cell 20 of combustion chamber 10 and first is separated by spraying arch 11.Injection arch 11 is arranged on the top of combustion chamber 10.Combustion
It is anti-that the flow path 111 that the high-temperature gas produced through burning in burning room 10 can be encircleed on 11 by being arranged on injection spurt into first
Answer room 20.Spurting into the high-temperature gas of the first reative cell 20 can be used to hold up the solid particle material of the first reative cell 20 simultaneously
Carry out high-temperature heating reaction.The fluidized reactor 1 that the present invention is provided sets injection arch 11 by the top of combustion chamber 10, passes through
The high temperature air jet that burning in combustion chamber 10 is produced is entered the first reative cell 20 by the flow path 111 of injection arch 11, penetrating
Hot-gas temperature may be up to 1350 DEG C or so, it is sufficient to which the ore particles for making the first reative cell 20 are in fluidized state.Fluidized state
Ore particles be easier to reaction carrying out.In addition, compared with plane gas distributor, 11 are encircleed by the injection of arch
High-temperature gas flow velocity is larger, it is sufficient to hold up the ore particles in the first reative cell 20, it is ensured that ore particles are in the first reative cell 20
React.The energy solved in the prior art by gas distributor is not enough, it is difficult to hold up the ore in reduction reaction area
And it is dispersed in whole reducing zone so that the ore of entrance is deposited on the middle and lower part in reduction reaction area mostly, and reduction effect is not
Preferable problem.Even if the larger particle in part cannot all be held up and be suspended in the first reative cell 20 by high-temperature high-speed airflow, also may be used
Its gravity is born with by spraying arch 11.The injection arch 11 of arch can bear heavier solid particle compared with the distributor of plane,
With advantage not easy to break.
Fig. 2 shows the cross-sectional view of injection arch 11 of the invention.Injection arch 11 is made up of refractory material
Domes, as shown in Figure 2.11 advantages for being made arch are encircleed in injection：Injection arch 11 by the way of middle surrounding high is low,
The residue particles fallen after reaction is complete on injection arch 11 can be made to slide to the slag-drip opening of reactor and discharge out of the furnace, realize reaction
It is carried out continuously.The domes design of injection arch 11 solves residue particles in the prior art and piles up in the reactor, causes anti-
Answering efficiency gradually reduces, reacts the problem that can not be carried out continuously.According to a preferred embodiment, flow path 111 uniformly sets
Put in the cambered surface near 11 axis of injection arch.Flow path 111 is only arranged on the arc near the axis of injection arch 11
On face, the flow velocity for spraying gas can be increased.In addition, being not provided with flow path on away from the cambered surface of 11 axis of injection arch
111, also may be such that the residue particles for sliding to reactor slag-drip opening smoothly discharge out of the furnace, it is to avoid residue particles fall into flow path
111 and it is resulted in blockage.The size of flow path 111 at least meets the gas stream after the fuel gas expansion of combustion chamber 10
Speed.According to hydrodynamics method, its size at least meets the fuel gas expansion of combustion chamber 10 to the size of flow path 11
Gas flow rate afterwards, it is to avoid the high-temperature gas produced in combustion chamber 10 expands and causes security incident.The size of flow path 111
Also should be less than the size of ore particles in the first reative cell 20, it is to avoid ore particles result in blockage to it.
According to a preferred embodiment, reactor 1 also has the second reative cell 30, as shown in Figure 1.First reative cell 20
The intermediate product of heated generation can rise to the second reative cell 30 with high temperature gas flow.Intermediate product enters with the second reative cell 30
Unstrpped gas proceed second step pyroreaction.By the high temperature gas flow for controlling the first reative cell 20 to rise and the second reaction
Room 30 enter flow of feed gas with formed stabilization airflow interface.Airflow interface is by 30 points of the first reative cell 20 and the second reative cell
Separate.Reactor of the invention 1 is applicable not only to only need the i.e. achievable technique of single step reaction, be equally applicable to need two steps and
The technique that could be completed is reacted above.The raw material that the high temperature gas flow and the second reative cell 30 risen by the first reative cell 20 are entered
Air-flow can be separated the first reative cell 20 with the second reative cell 30 with forming stable airflow interface, distinguish two-step reaction
Carried out in two relatively independent spaces, solve and in the prior art distinguished zoneofoxidation and reduction using heat-conducting plate, caused
Thermal loss and zoneofoxidation can not obtain the problem of enough heats.
At a high temperature of 700~1800 DEG C, the fractions in ore easily form molten state material, such as coke, silica, phosphorus
Ore etc..The temperature of the first reative cell 20 and/or the second reative cell 30 is slightly less than due to the temperature of slag-drip opening, viscosity flow is on furnace wall
Molten state material when dropping to slag-drip opening, the reduction of temperature easily causes molten state material coking, and then slag-drip opening is caused
Block.Molten state material easily results in blockage to slag-drip opening so that reaction can not be carried out continuously, it is also desirable to frequent clean reactor
Technical problem is ignored by those skilled in the art, at present yet without preferable solution.Refer again to Fig. 1, the first reaction
The reative cell 30 of room 20 and second has the component that dams of the molten state material for collecting viscosity flow on furnace wall respectively.The component that dams is distinguished
It is arranged at the bottom of the first reative cell 20 and the second reative cell 30.The component that will dam is respectively arranged at the first reative cell 20 and second
The reason for 30 bottom of reative cell is：Because the first reative cell 20 in reactor 1 is different with the temperature of the second reative cell 30, along furnace wall
Dirty molten state material can change its state with the change of temperature.If only setting the component that dams, can not only increase and cut
The size of component is flowed, can also cause to derive the flows decrease of molten state material.Importantly, set the component that dams can not
Molten state material is collected in time.If for example, only the first reative cell 20 set the component that dams, in the second reative cell 30
Molten state material is likely to become solidification state rather than molten state after flowing to the first reative cell 20, it is impossible to is trapped collect components, solidifies
The material of state falls to being likely to result in the blocking of slag-drip opening.If conversely, only setting the component that dams, the in the second reative cell 30
The molten state material that one reative cell 20 is produced can not be trapped component and collect immediately so that the impurity in products of generation is more.Such as
Shown in Fig. 1, the component that dams includes that at least one first cut-off grooves 22 and first dam fairlead 23, and at least one second sections
Chute 33 and second dams fairlead 34.First cut-off groove 22 and the second cut-off groove 33 are embedded in the way of radially-inwardly protruding
Combination refractory masses 50.First cut-off groove 22 and the second cut-off groove 33 are arranged to a ring shape along furnace wall.First cut-off groove 22
Interface with the second cut-off groove 33 is inclined upwardly, and viscosity flow can be by the first cut-off groove 22 when the molten state material of furnace wall flows downward
Collected with the second cut-off groove 33.First dam fairlead 23 and second dam fairlead 34 opening upwards incline.First dams
Fairlead 23 and second dam fairlead 34 opening lower edge respectively with the interface of the first cut-off groove 22 and the second cut-off groove 33 under
Along docking, the molten state material collected in the first cut-off groove 22 and the second cut-off groove 33 can be made to be exported outside stove in time.Avoid
Pile up excessive molten state material and have impact on the reaction efficiency in reactor 1 in one cut-off groove 22 and the second cut-off groove 33.Always
It, first dams fairlead 23 and the second inclined design of fairlead 34 of damming is more beneficial for the molten state material in stove
Derive.
With continued reference to Fig. 1, the bottom of combustion chamber 10 is provided with a fuel gas inlet pipe 15 along axis direction.By fuel gas inlet
The combustion gas that pipe 15 enters can be the fuel such as coal gas, natural gas, liquefied gas.The upper end of fuel gas inlet pipe 15 is provided with a burning
First 14.Combustion head 14 is made up of high-temperature refractory.The domed structure of combustion head 14.Pressed in the cambered surface of arch combustion head 14
Through, weft direction arranged for interval.Preferably, spray orifice 141 parallel can be arranged equally spacedly.A diameter of 6~12mm of spray orifice 141.
According to a preferred embodiment, combustion head 14 is hemispherical dome structure, as shown in Figure 3.By warp, latitude on hemispherical combustion head 14
The parallel equidistant principle in line direction is disposed with the spray orifice 141 of multiple a diameter of 6~12mm, as shown in Figure 4.Combustion head 14 is set
Domes are calculated as, and arrange that multiple spray orifices 141 are in order that entering from fuel gas inlet pipe 15 in the cambered surface of combustion head 14
Combustion gas, through spray orifice 141 spray after, be well mixed with the combustion adjuvant air in combustion chamber 10 so that the burning of combustion gas is more abundant,
Solve the problems, such as that fuel combustion is insufficient in the prior art.In addition, the present invention only has a combustion head 14, and set
In the bottom of combustion chamber 10, it also avoid increasing the problem of equipment cost and waste of fuel.Air hose 13 is arranged on combustion head 14
Surrounding, also for making, the air of entrance is uniform with the combustion gas mixing that spray orifice 141 sprays so that the burning of combustion gas is more abundant.It is empty
The quantity at least two of tracheae 13, more preferably preferably 4,6.The top of air hose 13 is equipped with least one detection mouth
12, detection mouth 12 is used to monitor the fired state of combustion chamber 10.Detection mouth 12 can be temperature sensing mouthful, may also be micro amount of oxygen detection
Mouthful, its purpose is for monitoring the fired state of combustion gas in combustion chamber 10.
According to a preferred embodiment, reactor 1 also includes combination refractory masses 50.Combination refractory masses 50 by
Fire resisting molding mass and castable refractory are combined.The shell 40 of reactor 1 is lining in combination refractory masses 50.Combination fire resisting
The thickness of material layer 50 is 500~700mm.The refractory material for using in the prior art mostly amorphous refractory.For example, not
Come stone castable, high alumina castable or corundum castable.The outer of reactor 1 will be lining in refractory masses of the prior art
Shell 40, the thickness of required refractory masses is thicker, usually 1000~1400mm.When in-furnace temperature is 1350 DEG C or so, lead to
Cross refractory masses so that the temperature outside stove is 80 DEG C or so.Although the refractory masses for using in the prior art can be effectively
The loss of furnace heat is controlled, but the thickness of refractory masses is thicker, greatly reduces the free space of reactor.This hair
The bright combination refractory material for being changed to be combined by fire resisting molding mass and castable refractory by amorphous refractory, can be fully sharp
With fire resisting molding mass and the advantage of castable refractory.Not only can be decreased to for the thickness of refractory masses by combination refractory material
500~700mm, and when in-furnace temperature is 1350 DEG C or so, after combining refractory masses, the temperature outside stove can be reduced
To 50 DEG C or so.
With continued reference to Fig. 1, the first reative cell 20 also includes at least one feed pipe 21 and at least one scum pipe 24.Charging
Pipe 21 is located at the component bottom of damming of the second reative cell 20.Open Side Down that inclined mode is arranged at first is anti-with it for feed pipe 21
Answer the top of room 20.Feed pipe 21 is made up of a horizontal segment and a tilting section.The structure design mode of the feed pipe 21, is easy to solid
Body granule materials enter the first reative cell 20 at the appropriate speed.Solid particle material into the first reative cell 20 is injected arch
The high-temperature high-speed airflow that 11 flow path 111 sprays holds up, and is suspended in the first reative cell 20, carries out first step pyroreaction.
Scum pipe 24 is located at the component bottom of damming of the first reative cell 20.Scum pipe 24 is encircleed with its acclivitous opening lower edge with injection
The mode of 11 cambered surface docking is arranged at the lower end of the first reative cell 20.Scum pipe 24 uses inclined design, mainly
In order to the solid product of the tailings after allowing the first reative cell 20 to have reacted and/or reaction generation discharges out of the furnace in time.In addition, deslagging
The opening lower edge of pipe 24 is just docked with the cambered surface end of injection arch 11, can also make the tail slid to surrounding from the middle part of injection arch 11
Slag can discharge out of the furnace in time.The structure design so of scum pipe 24, can make tailings discharge reactor 1 in time, realize the company of reaction
It is continuous to carry out.
According to a preferred embodiment, the high temperature of the reative cell 20 of combustion chamber 10 and first is 700~1350 DEG C.Second is anti-
The high temperature for answering room 30 is 700~1800 DEG C.According to a preferred embodiment, the high temperature of the reative cell 20 of combustion chamber 10 and first is
900~1300 DEG C, the high temperature of the second reative cell 30 is 800~1700 DEG C.Preferred implementation method is, combustion chamber 10 and first
The high temperature of reative cell 20 is 1100~1200 DEG C, and the high temperature of the second reative cell 30 is 900~1600 DEG C.Reactor of the invention 1
It is applicable to the course of reaction by high-temperature process ore.The different ore for the treatment of, required high temperature is preferably with existing
Temperature in technology.
With continued reference to Fig. 1, the second reative cell 30 also includes at least one outlet 31 and at least one air inlet pipe 32.Outlet
Pipe 31 is arranged at the top of the second reative cell 30 and is used to derive the gaseous product of reaction along the direction of axis and/or excludes tail
Gas.Air inlet pipe 32 is arranged at the position of the bottom of the second reative cell 30 and the component that dams higher than the second reative cell 30.Air inlet
The intermediate product that pipe 32 is used to import unstrpped gas and rise to the second reative cell 30 with the first reative cell 20 continues to participate in reaction.
The second reative cell 30 is arranged at by by air inlet pipe 32, the first reative cell 20 can be made relatively independent with the reaction of the second reative cell 30
Carrying out, solve in the prior art by auxiliary air inlet tube be arranged in zoneofoxidation lower section so that oxygen-enriched air be difficult to and in
Between the well-mixed problem of product.
A kind of method that ore is processed using reactor 1 of the invention, the method is comprised the following steps：
Refining is made, 10~100 mesh will be screened to after ore reduction.After adding raw material needed for first step reaction and sieving
Ore mixing make refining.The solid particle of a diameter of 3~4mm is formed as raw material for standby.Material needed for first step reaction can
Be reducing agent, oxidant, catalyst, dispersant or other first steps reaction needed for material.Ore and reducing agent are made 3
The solid particle of~4mm is mainly the requirement according to reacting furnace.The step contributes to what feed particles were ejected in reactor
High-temperature gas holds up and fluidizes so that reaction is easier to make for.
Heating, before reaction starts, combustion gas is introduced from fuel gas inlet pipe 15.The combustion gas of introducing is by the spray orifice on combustion head 14
Enter combustion chamber 10 after 141 ejections.Meanwhile, introduce combustion adjuvant from air intlet pipe 13.Through spray orifice 141 spray after combustion gas with help
Combustion agent air is well mixed so that the burning of combustion gas is more abundant, solves the problems, such as that fuel combustion is insufficient in the prior art.
Reaction, solid particle enters the first reative cell 20 from feed pipe 21.Solid particle is by the jet flow from injection arch 11
The high-temperature gas that passage 111 sprays upwards holds up.Allow that solid particle is suspended in the generation of the first reative cell 20 first step anti-
Should.The high temperature of the first reative cell 20 is 700~1350 DEG C.Combustion reaction and first step reaction are by being arranged on the top of combustion chamber 10
Injection arch it is 11 separated from one another.The reactor is also applied for the reaction for needing two steps to complete.During first reative cell 20 is generated
Between product by ascending air enter the second reative cell 30.Intermediate product into the second reative cell 30 enters with from air inlet pipe 32
Unstrpped gas occur at high temperature second step reaction.The high temperature of the second reative cell 30 is 700~1800 DEG C.The first step react and
The air-flow that second step reaction is risen by the first reative cell 20 and the unstripped gas bodily form that the air inlet pipe 32 of the second reative cell 30 enters
Airflow interface into stabilization is separated from one another.
Collection of products and deslagging, gaseous product and/or tail gas after having reacted are derived outside stove by outlet 31.React
Solid product and/or tailings afterwards is discharged out of the furnace by scum pipe 24.
The method that the utilization reactor 1 that the present invention is provided processes ore, also comprises the following steps：
Fused mass is collected, the molten state material that first step reaction and/or second step reaction are produced through the first cut-off groove 22 and/
Or second cut-off groove 33 collect.Collect molten state material to cut-off groove and dammed by first and fairlead 23 and/or second dam and draw
Outlet pipe 34 is derived outside stove.Solve molten state material to result in blockage slag-drip opening so that the problem that reaction can not be carried out continuously.
In being applied to using the method for reactor for treatment ore of the invention, the comprehensive utilization of poor value, overcome
Prior art consersion unit falls behind the problem of the high energy consumption and environmental pollution for causing；The present invention especially centering, poor value
Reactiveness and reaction time are controlled, and solve the problems, such as that melting, coking and blocking occurs in material, are capable of achieving continous way life
Produce.
Embodiment 1
As a example by mid low grade phosphate rock being processed using reactor of the invention 1 and produces phosphorus pentoxide.
Producing phosphorus pentoxide by phosphorus ore needs by two-step reaction, as follows：
Ca3(PO4)2+A→P4↑+other chemical compositions △ H>0
P4+5O2=2P2O5 △H<0
Wherein A is the reducing agent that can reduce phosphorus, can be charcoal, silica, lime stone etc..
Raw material into reactor is needed by making refining.Make concretely comprising the following steps for refining：The mid low grade phosphate rock stone that will be gathered
(phosphorous 17~22%) are sieved after crushing, and the particle diameter of rock phosphate in powder is less than 20 mesh.Again by the phosphorus ore after reducing agent and sieving
It is put into together and makes furnace and make refining, the little particle of a diameter of 3~4mm is formed, as raw material for standby.Phosphorus ore and reducing agent are made small
Particle is mainly the requirement according to reacting furnace, and the step contributes to the fluidisation of reduction reaction process feed particles.
Reaction starts preceding, it is necessary to introduce combustion gas from fuel gas inlet pipe 15, introduce combustion adjuvant air from air hose 13.Combustion gas is passed through
After spray orifice 141 on combustion head 14 sprays, can be well mixed with combustion adjuvant air, combustion gas is fully burnt.Meanwhile, pass through
The fired state of combustion gas in the detection monitoring of mouth 12 combustion chamber 10 above air hose.When in-furnace temperature reaches 1200 DEG C or so,
Start to feed intake.Feed particles after making refining enter the first reative cell 20 of reactor, the raw material of entrance from feed pipe 21
Grain is held up by the high temperature and high speed gas that the flow path 111 from injection arch 11 sprays, and is suspended in the first reative cell 20, while
Reduction reaction is carried out at a high temperature of 1200 DEG C.Tailings after having reacted discharges stove by the scum pipe 24 of the lower section of the first reative cell 20
Outward.The intermediate product phosphorus simple substance for reacting generation enters the second reative cell 30 with the air-flow for flowing up, while being reacted with from second
There is oxidation reaction in the oxygen-enriched air that the air inlet pipe 32 of room 30 enters, generate phosphorus pentoxide at a high temperature of 1650 DEG C.Generation
Phosphorus pentoxide can be derived outside stove from the outlet 31 on the top of the second reative cell 30.The oxidation carried out in second reative cell 30 is anti-
Exothermic reaction is should be, therefore without setting the high temperature needed for combustion head can also make the temperature of the second reative cell 30 reach reaction again.
In addition, the molten state material for generating during the course of the reaction, can be by the component that dams on the first reative cell 20 and the second reative cell 30
Collect and derive outside stove.
Therefore, in the reactor for treatment for being provided using the present invention, low-grade phosphate ore stone produce phosphorus pentoxide, overcome existing
The hot method for having technology prepares the high energy consumption of phosphoric acid and the problem of pollution environment, and especially right using the reactor that the present invention is provided
In, the reactiveness of low-grade phosphate ore stone and reaction time be controlled, solve material and asking for melting, coking and blocking occur
Topic, is capable of achieving continous way production.
Embodiment 2
As a example by manganese ore being processed using reactor of the invention 1 and produces manganese oxide.
The cardinal principle for producing manganese oxide by manganese ore is pyrolusite (MnO2) in the presence of reducing agent, it is heated to 700~
1000 DEG C, high price manganese oxide changes into the low price manganese for being easy to Ore Leaching at a low price.Reaction is as follows：
2MnO2+ C=2MnO+CO2 △H>0
Charcoal reducing agent therein can also be substituted with reducing agents such as silica, lime stones.
Raw material into reactor is needed by making refining.Make concretely comprising the following steps for refining：The middle-low grade manganese ore that will be gathered
Sieved after broken, the particle diameter of manganese ore is less than 60 mesh.Reducing agent is put into together with the manganese ore after sieving again makes furnace
Refining is made, the little particle of a diameter of 3~4mm is formed, as raw material for standby.Manganese ore and reducing agent are made little particle and are mainly basis
The requirement of reacting furnace, the step contributes to the fluidisation of reduction reaction process feed particles.
Reaction starts preceding, it is necessary to introduce combustion gas from fuel gas inlet pipe 15, introduce combustion adjuvant air from air hose 13.Combustion gas is passed through
After spray orifice 141 on combustion head 14 sprays, can be well mixed with combustion adjuvant air, combustion gas is fully burnt.Meanwhile, pass through
The fired state of combustion gas in the detection monitoring of mouth 12 combustion chamber 10 above air hose.When in-furnace temperature reaches 800 DEG C or so, open
Beginning feeds intake.Feed particles after making refining enter the first reative cell 20 of reactor, the feed particles of entrance from feed pipe 21
The high temperature and high speed gas sprayed by the flow path 111 from injection arch 11 holds up, and is suspended in the first reative cell 20, while
Reduction reaction is carried out at a high temperature of 800 DEG C.MnO after having reacted discharges stove by the scum pipe 24 of the lower section of the first reative cell 20
Outward.The carbon dioxide tail gas for reacting generation can be derived outside stove from the outlet 31 on the top of reactor 1.In addition, during the course of the reaction
The molten state material of generation, collect components and can be derived outside stove by damming for the first reative cell 20.
Therefore, the reactor for treatment manganese ore for being provided using the present invention produces MnO, and the reactor for overcoming prior art is made
Into high energy consumption and pollution environment problem, and reactiveness of the reactor especially to manganese ore that is provided using the present invention and
Reaction time is controlled, and solves the problems, such as that melting, coking and blocking occurs in material.
It should be noted that above-mentioned specific embodiment is exemplary, those skilled in the art can disclose in the present invention
Various solutions are found out under the inspiration of content, and these solutions also belong to disclosure of the invention scope and fall into this hair
Within bright protection domain.It will be understood by those skilled in the art that description of the invention and its accompanying drawing be it is illustrative and not
Constitute limitations on claims.Protection scope of the present invention is limited by claim and its equivalent.
Claims (9)
1. a kind of fluidized reactor (1), the reactor (1) at least has a combustion chamber (10) and the first reative cell (20), its
It is characterised by, the combustion chamber (10) and first reative cell (20) are by the injection that is arranged at the top of the combustion chamber (10)
Arch (11) is separated from one another so that the high-temperature gas produced through burning in the combustion chamber (10) can be by being arranged on the spray
The flow path (111) penetrated on arch (11) spurts into first reative cell (20) upwards, described to spurt into the first reative cell
(20) high-temperature gas can be used to hold up the solid particle material of first reative cell (20) and to carry out high-temperature heating anti-
Should, injection arch (11) is the domes being made up of refractory material；At least one flow path (111) is arranged on institute
State in the cambered surface near injection arch (11) axis, and the size of the flow path (111) at least meets the combustion chamber
(10) gas flow rate after fuel gas expansion.
2. fluidized reactor (1) as claimed in claim 1, it is characterised in that the reactor (1) also has the second reative cell
(30), the intermediate product of the heated generation of first reative cell (20) rises to second reative cell with high temperature gas flow
, and the unstrpped gas that enters with second reative cell (30) of the intermediate product proceeds pyroreaction (30)；Pass through
The flow of feed gas that the high temperature gas flow that first reative cell (20) rises enters with second reative cell (30) forms stabilization
Airflow interface is separated with by first reative cell (20) with second reative cell (30).
3. fluidized reactor (1) as claimed in claim 2, it is characterised in that first reative cell (20) and described second
Reative cell (30) has the component that dams of the molten state material for collecting viscosity flow on furnace wall respectively, and the component that dams is respectively provided with
In first reative cell (20) and the bottom of second reative cell (30), and the component that dams includes at least one the
One cut-off groove (22) and first dams fairlead (23), and at least one second cut-off grooves (33) and second dam fairlead
(34)；Wherein,
First cut-off groove (22) and second cut-off groove (33) are embedded in combination fire resisting in the way of radially-inwardly protruding
Material layer (50), and the interface of first cut-off groove (22) and second cut-off groove (33) is inclined upwardly to receive viscosity flow
In the molten state material of furnace wall；
Described first dam fairlead (23) and described second dam fairlead (34) opening upwards incline and described first
Dam fairlead (23) and described second dam fairlead (34) with its be open lower edge respectively with first cut-off groove (22) and
The mode of the interface lower edge docking of second cut-off groove (33) is arranged at first cut-off groove (22) and described second and dams
Derived outside stove with by the molten state material collected by it in groove (33).
4. fluidized reactor (1) as claimed in claim 1 or 2, it is characterised in that combustion chamber (10) bottom is along axis
Direction is provided with a fuel gas inlet pipe (15), and the upper end of the fuel gas inlet pipe (15) is provided with a combustion head (14)；Its
In,
The combustion head (14) is made up of high-temperature refractory, and the combustion head (14) domed structure, in the arch
There is the spray orifice (141) of multiple a diameter of 6~12mm in the cambered surface of combustion head (14) by warp, weft direction arranged for interval；
The surrounding of the combustion head (14) there also is provided at least two air hoses (13), and air hose (13) top is equipped with least
One detection mouth (12), the mouth (12) that detects is for monitoring the fired state of the combustion chamber (10).
5. fluidized reactor (1) as claimed in claim 1 or 2, it is characterised in that the reactor (1) also includes by fire resisting
The combination refractory masses (50) that molding mass and castable refractory are combined, institute is lining in combination refractory masses (50)
The shell (40) of reactor (1) is stated, and the thickness of combination refractory masses (50) is 500~700mm.
6. fluidized reactor (1) as claimed in claim 2, it is characterised in that first reative cell (20) is also included at least
One feed pipe (21) and at least one scum pipe (24)；Wherein,
The feed pipe (21) positioned at second reative cell (20) dam component bottom and the feed pipe (21) with it
Inclined mode that Open Side Down is arranged at the top of first reative cell (20)；
The scum pipe (24) positioned at first reative cell (20) dam component bottom and the scum pipe (24) with it
The mode that acclivitous opening lower edge is docked with the cambered surface of injection arch (11) is arranged at first reative cell (20)
Lower end.
7. fluidized reactor (1) as claimed in claim 2, it is characterised in that the combustion chamber (10) and first reaction
The high temperature of room (20) is 700~1350 DEG C, and the high temperature of second reative cell (30) is 700~1800 DEG C.
8. fluidized reactor (1) as claimed in claim 2, it is characterised in that second reative cell (30) is also included at least
One outlet pipe (31) and at least one air inlet pipe (32)；Wherein,
The outlet (31) is arranged at the second reative cell (30) top and is used to derive reaction product along the direction of axis
Thing and/or exclusion tail gas；
The air inlet pipe (32) is arranged at the bottom of second reative cell (30) and higher than second reative cell (30)
The dam position of component is used to import unstrpped gas and rises to second reative cell (30) with first reative cell (20)
Intermediate product continue participate in reaction.
9. the method that a kind of fluidized reactor (1) of one of utilization preceding claims processes ore, it is characterised in that the side
Method comprises the following steps：
Refining is made, will again carry out making refining after ore reduction, form solid particle as raw material；
Heating, before reaction starts, combustion gas is by combustion head (14) with combustion adjuvant mixed combustion with first to the reactor (1)
Reative cell (20) and the second reative cell (30) are heated；
Reaction, the solid particle enters the flow path (111) encircleed from injection on (11) after the first reative cell (20) upwards
The gas of ejection holds up and is suspended in first reative cell (20) and first step reaction occurs, and the combustion reaction and described
By being arranged on injection at the top of the combustion chamber (10), to encircle (11) separated from one another for first step reaction；And/or it is described first anti-
Answer room (20) generate intermediate product by ascending air enter the second reative cell (30) and with the original entered from air inlet pipe (32)
There is second step reaction in material gas, and first step reaction and second step reaction are anti-by described first at high temperature
The airflow interface that the unstrpped gas that the air-flow for answering room (20) to rise enters with second reative cell (30) forms stabilization divides each other
Separate；
Collection of products and deslagging, gaseous product and/or tail gas after having reacted are derived outside stove by outlet (31), after having reacted
Solid product and/or tailings discharged out of the furnace by scum pipe (24).
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5060913A (en) * | 1989-08-30 | 1991-10-29 | Regents Of The University Of Minnesota | Integrated metallurgical reactor |
| CN101413056A (en) * | 2008-11-25 | 2009-04-22 | 朱军 | Manganese ore reduction calcination method and apparatus |
| CN102616759A (en) * | 2012-03-26 | 2012-08-01 | 武汉工程大学 | Technique and device for preparing phosphoric acid by fluidized bed reactor |
| CN204151392U (en) * | 2014-08-22 | 2015-02-11 | 东北大学 | Vertical containing TiO2 slag reduction calciner |
-
2015
- 2015-09-10 CN CN201510574108.6A patent/CN105107435B/en active Active
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5060913A (en) * | 1989-08-30 | 1991-10-29 | Regents Of The University Of Minnesota | Integrated metallurgical reactor |
| CN101413056A (en) * | 2008-11-25 | 2009-04-22 | 朱军 | Manganese ore reduction calcination method and apparatus |
| CN102616759A (en) * | 2012-03-26 | 2012-08-01 | 武汉工程大学 | Technique and device for preparing phosphoric acid by fluidized bed reactor |
| CN204151392U (en) * | 2014-08-22 | 2015-02-11 | 东北大学 | Vertical containing TiO2 slag reduction calciner |
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