CN110214049A - Heat-treating methods and device for contaminated solid - Google Patents
Heat-treating methods and device for contaminated solid Download PDFInfo
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- CN110214049A CN110214049A CN201780010201.1A CN201780010201A CN110214049A CN 110214049 A CN110214049 A CN 110214049A CN 201780010201 A CN201780010201 A CN 201780010201A CN 110214049 A CN110214049 A CN 110214049A
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- 239000007787 solid Substances 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000012535 impurity Substances 0.000 claims abstract description 26
- 238000012546 transfer Methods 0.000 claims abstract description 16
- 239000000446 fuel Substances 0.000 claims description 9
- 229910052793 cadmium Inorganic materials 0.000 claims description 8
- BDOSMKKIYDKNTQ-UHFFFAOYSA-N cadmium atom Chemical compound [Cd] BDOSMKKIYDKNTQ-UHFFFAOYSA-N 0.000 claims description 8
- 238000001816 cooling Methods 0.000 claims description 6
- 230000001590 oxidative effect Effects 0.000 claims description 6
- 238000012545 processing Methods 0.000 claims description 6
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- NBIIXXVUZAFLBC-UHFFFAOYSA-K phosphate Chemical compound [O-]P([O-])([O-])=O NBIIXXVUZAFLBC-UHFFFAOYSA-K 0.000 claims description 3
- 239000010452 phosphate Substances 0.000 claims description 3
- 230000003134 recirculating effect Effects 0.000 claims description 3
- 230000003068 static effect Effects 0.000 claims 1
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- 238000010438 heat treatment Methods 0.000 abstract description 15
- 238000002485 combustion reaction Methods 0.000 abstract description 3
- 230000005540 biological transmission Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 35
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 8
- 239000001301 oxygen Substances 0.000 description 8
- 229910052760 oxygen Inorganic materials 0.000 description 8
- 230000008901 benefit Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 238000009825 accumulation Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000002912 waste gas Substances 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000003337 fertilizer Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 229910052785 arsenic Inorganic materials 0.000 description 1
- RQNWIZPPADIBDY-UHFFFAOYSA-N arsenic atom Chemical compound [As] RQNWIZPPADIBDY-UHFFFAOYSA-N 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000001354 calcination Methods 0.000 description 1
- -1 carbonate compound Chemical class 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000005202 decontamination Methods 0.000 description 1
- 230000003588 decontaminative effect Effects 0.000 description 1
- 238000007872 degassing Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000013021 overheating Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000008188 pellet Substances 0.000 description 1
- 239000002006 petroleum coke Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007086 side reaction Methods 0.000 description 1
- 239000002689 soil Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
- B01J6/001—Calcining
- B01J6/004—Calcining using hot gas streams in which the material is moved
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/34—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with stationary packing material in the fluidised bed, e.g. bricks, wire rings, baffles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
- B01J8/36—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with fluidised bed through which there is an essentially horizontal flow of particles
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
- B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
- B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
- B09B3/40—Destroying solid waste or transforming solid waste into something useful or harmless involving thermal treatment, e.g. evaporation
-
- C—CHEMISTRY; METALLURGY
- C05—FERTILISERS; MANUFACTURE THEREOF
- C05B—PHOSPHATIC FERTILISERS
- C05B13/00—Fertilisers produced by pyrogenic processes from phosphatic materials
- C05B13/02—Fertilisers produced by pyrogenic processes from phosphatic materials from rock phosphates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00513—Controlling the temperature using inert heat absorbing solids in the bed
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
- B01J2208/023—Details
- B01J2208/024—Particulate material
- B01J2208/025—Two or more types of catalyst
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Processing Of Solid Wastes (AREA)
Abstract
Heat-treating methods and device for contaminated solid.The present invention relates to the heat treatments of contaminated solid.In first step (i), using heat transmission medium by counter-current flow, contaminated solid is preheated to 100-600 DEG C of temperature at least one preheating section.Then in second step (ii), contaminated solid is heated to 600-1300 DEG C of temperature in the first reactor, the impurity thus contained in solid is partly discharged in a gaseous form and obtains exhaust gas.Pass through third step (iii), in the second reactor 600-1300 DEG C at a temperature of solid is heat-treated, thus the impurity contained in solid is discharged in a gaseous form, and in four steps (iv), as a heat transfer medium and/or combustion air is recycled at least one preheating section by exhaust gas.
Description
The present invention relates to a kind of heat-treating methods and device for contaminated solid, include the following steps: step
(i), for the solid to be preheated to using heat transfer medium at least one preheating section 100-600 DEG C of temperature, step (ii),
For the solid to be heated to 600-1300 DEG C of temperature in the first reactor, the impurity thus contained in the solid is partly
Be expelled out of in a gaseous form, and obtain exhaust gas, step (iii) be directed toward in the second reactor 600-1300 DEG C at a temperature of should
The heat treatment of solid, the impurity thus contained in the solid is at least partly discharged in a gaseous form and step (iv), will give up
Gas is sent at least one preheating section as a heat transfer medium.
The heat treatment of known solid to be from a variety of methods to remove impurity, for example, the hot decontamination of polluted soil or coal and
The high-temperature degassing of petroleum coke.It consumes energy very much however, heating solid within the scope of 600-1300 DEG C of typical temperature.Therefore,
The optimum capacity recycling for the exhaust gas for including in these methods is essential for the economy of these methods.
However, the heat treatment that impurity is removed from solid has the shortcomings that add, i.e. impurity contained by least part
It is evaporated and is therefore transmitted in the exhaust gas of heat treatment.Such as from common heat treatment, such as known to calcining, by be preheated
Material is contacted with the direct counter-current flow of exhaust gas and directly, is most simply recycled the sensible heat of the exhaust gas of formation therefore is impossible
: since impurity is discharged at high temperature in exhaust gas and includes that in the offgas, can occur in this case for preheating
It is attached to again by physics and chemical process during the counter-current flow of purpose comprising impurity in the offgas still relatively cool
On solid.Therefore, because the re-absorption of the pollutant of release, was previously contaminated by the solid of thermal cleaning again.When it then
When being introduced into actual heat treatment, due to remaining impurity, be equally almost not suitable for generating necessary purity.Moreover, even
During continuous, the extreme accumulation of impurity occurs within the short time.
However, the heat exchange surface being restricted due to economic cause, the indirect thermal benefit of heat included in exhaust gas
With including the clearly worse thermal efficiency, and the energy economy of this method is therefore reduced.In addition, required device is being obtained and is being tieed up
The obvious expense of shield aspect is higher.
Therefore, the purpose as basis of the invention is to provide a kind of method, and this method passes through heat in energy-optimised mode
Processing removes impurity from solid.
The purpose is solved by the method for the feature with claim 1.
For this purpose, contaminated solid directly connects initially in processing step (i) at least one preheating section, with exhaust gas
100-600 DEG C of temperature is touched and be preheated to, however preferably reaches permission and is technically advantageously employed discharged combustion in large quantities
Burn the temperature of the sensible heat of gas.As a result, there is direct heat transmitting between heat transfer medium exhaust gas and solid to be heated, thus
The high thermal efficiency is especially realized in the heat exchange of multistage.Then, the solid preheated in this way is in first reactor
In be preheated to 600-1300 DEG C, preferably 600-1200 DEG C, even more preferably 750-1000 DEG C of temperature, and gas wherein included
State impurity is by part discharge to obtain exhaust gas.The first process section so run allows to recycle the big portion for including in burning waste gas
Divide sensible heat.
According to the present invention, exhaust gas is supplied to preheating section as a heat transfer medium, and in preheating section, exhaust gas passes through the adverse current with solid
It flows and is directly contacted with the solid.By means of the burning of gaseous state or liquid fuel, make the solid so preheated in the first reaction
Temperature is further increased in device.The solid preheated in the first reactor is discharged into second reactor, in the second reactor
Middle hot solids then-depend on the solid temperature-realized in the first processing step be maintained at the specific temperature or further by
The temperature of (in the second reactor) to 600-1300 DEG C is heated, the impurity thus still contained is discharged in a gaseous form.Due to
The waste gas stream of two reactors has relatively small amount, it is thus possible to which no longer by heat utilization, and pollutant wherein included is no longer
Again it is absorbed on the solid purified now.
This has the advantage that evicting from for impurity must only partially occur in the first reactor, and largely
On be transferred in second reactor.The accumulation of impurity to be eliminated is thus prevented, as the solid that can ensure final has
Enough purity is the same.Meanwhile the advantages of additionally providing in preheating section from the exhaust gas direct heat transfer from first reactor, this
It is exactly why this method can significantly more efficiently be run on energy.At this point, will not be led using second reactor
Cause heat demand be significantly increased again because in the first reactor contaminated material have reached evict impurity from needed for temperature
Degree, and covered the endothermic process that can be can be carried out herein on energy.Therefore, it is necessary to apply in the second reactor
Heat and the exhausted air quantity therefore generated are relatively small.
Advantageously, preheating contains at least two preheating section.It is guided in a counter-current configuration in the exhaust gas from first reactor
When to solid to be heated, this is particularly advantageous, because of that realizing high energy transmission with Low investment cost simultaneously.
In addition, ought in the first reactor-and if not under reducing atmosphere operation-in the second reactor, in 1-20
Volume %, preferably 1-15 volume %, when being heated under the oxygen content of particularly preferred 1-5 volume %, it was demonstrated that be advantageous.This tool
Have the advantage that the oxygen supply due to the reduction compared with air atmosphere, fuel economy is enhanced, and may less generation
Undesirable side reaction.However, in order to provide energy required in burner, at least existing if fuel burns in reactor
There must be enough oxygen in first reactor for the combustion process.
Product especially should be to generate the best atmosphere for removing impurity in the second reactor being wherein finally purified
Oxygen content operation.This can be oxidizing atmosphere or is also possible to reducing atmosphere.Since solid herein is with relatively high
Temperature enters, and preferably finally establishes the temperature in the second reactor, therefore introduced by direct or indirect burning herein
Heat is generally also much smaller, this is why this does not need excessively high oxygen and contains in the case where direct burning and oxidizing atmosphere
Amount.Preferably, step (ii) occurs in oxidizing atmosphere, and step (iii) is carried out with reducing atmosphere.
Furthermore, it was demonstrated that realize that heating is in first and/or second reactor by supplying preferred liquid or gaseous fuel
It is advantageous, because can ensure uniform heat distribution in reactor in this way.
However, simultaneously, through supply hot gas in first and/or second reactor, especially in the second reactor
Realize heating can also to be advantageous, because no longer needing burning of the oxygen for supplied fuel in reactor, non-
In the case where often low oxygen content or complete exclusion oxygen, control reaction is possible.
Another advantageous aspect of the invention provides material to be clean and is cooled after through second reactor, wherein
Using gas, preferably air etc. are for cooling down.The heat gas being subsequently cooled can be introduced into preheating section and/or first and/
Or second reactor, thus also utilize the energy.It is possible thereby to further increase the energy efficiency of this method.
Such as-but be not limited to-the method can be easily used for phosphatic solid, wherein impurity is typically logical
Overheating Treatment is discharged.The raw material phosphate especially precipitated is since (it can be with for carbonate compound and relatively high cadmium content
Removed by method described herein) both be further processed into fertilizer and as Fertilizer application in terms of damaged
Evil.Meanwhile this method is also applied for phosphatic secondary raw material, impurity can be reduced using the processing step or
It even is eliminated.
In addition, the method can be used for cadmium content in 1-500ppm, the preferably solid of 5-300ppm particularly well, because
By heat treatment cadmium (Cd) safely can be removed from the solid.Influence of this method to mineral is not limited only to cadmium, further includes
All substances that can be volatilized or decompose by the effect of high temperature and restriction atmosphere, such as arsenic (are only listed in many impurity
It is a kind of).
In detail, the first reactor and there is reduction that the phosphate-containing material with cadmium content needs to have oxidizing atmosphere
Second reactor (the most preferably O of atmosphere2=0 weight %) to remove contained cadmium.And it is therefore not desirable to which exhaust gas is recycled to elder generation
Preceding processing step, because it will lead to Cadmium accumulation.
In addition, when first and/or second reactor are used as with fixed or recirculating fluidized bed fluidized-bed reactor operation
When, it was demonstrated that it is advantageous, wherein herein it is envisioned that any combination.Fluidized-bed reactor provides particularly preferred quality and heat transmitting
The advantages of.Meanwhile according to the method for the present invention particularly suitable for fluidized bed, because due to fluidizing gas, it is ensured that gas phase and solid
The strong mixing of phase, the result is that highly uniform Temperature Distribution.
The sphere of preferred inertia and heat proof material is introduced into the reactor for be designed as fluidized-bed reactor and is also advantageous,
The sphere has the diameter of 5-50mm.Especially when reducing atmosphere to be generated, can thus it be largely fulfilled
At required partial oxidation.
In addition, the present invention also includes the device of the feature with claim 11.
This device includes at least one preheating section, for being preheated solid by counter-current flow preferably by heat transfer medium
To 100-600 DEG C of temperature.
In addition, it includes the first reactor for solid to be heated to 600-1300 DEG C of temperature, thus contain in solid
Some impurity is partly discharged in a gaseous form and obtains exhaust gas.In addition, the device includes returning from first reactor
Exhaust gas is introduced preheating section by the return duct by return pipe road and second reactor as a heat transfer medium, so as to 600 DEG C-
Further heat treatment for solid at a temperature of 1300 DEG C, to evict impurity from a gaseous form.
It is further envisioned that in one apparatus, first and/or second reactor be designed as rotary kiln.
In addition, advantageous aspect of the invention provides at least one preheating section being designed as cyclone separator.
Depending on desired use, in two reactors for solid retention needed for various chemical-physical processes occur
Time can most preferably be adjusted by selected geometry (construction) and the in operation variation of bed height or bed density.
Furthermore it is preferred that be used for different atmosphere two individual reactor designs, especially with oxidizing atmosphere first reactor and
The design of second reactor with reducing atmosphere.
First reactor typically transfers solid to second reactor, it is preferable to use used in second reactor operation
Temperature.Under normal circumstances, this causes the energy to be consumed minimum.Since the temperature in two reactors can be by corresponding
Fuel supplies unrestricted choice in a wide range, if therefore in two reactors can also be using different temperature-at other
In favorably.
The present invention will be further described with reference to Fig. 1.Itself or all features for being shown and being described with any combination form this
The theme of invention.
In the accompanying drawings:
Fig. 1 shows schematic diagram according to the method for the present invention.
By pipeline 1 and 2, solid is introduced into the first preheating section 10 in the form of particle or pellet.In pipeline 2,
Obtain the mixture of fresh solid Yu the hot waste gas from pipeline 23.In the first preheating section 10, from the fresh solid of pipeline 1
Then body is heated by the gas from pipeline 23, and exhaust gas is discharged by pipeline 11.
By pipeline 12, the solid of heating is supplied to the second preheating section 13.Into second preheating section 13, pipeline 22 is beaten
It opens and hot gas is introduced into the second preheating section 13 to preheat, wherein then by pipeline 23 by gas discharge and first
It is used as heat transfer medium again in preheating section 10 in slightly cooling form.
Further the solid of preheating is discharged and is supplied to third preheating section 15 by pipeline 14.Equally supplied from pipeline 21
Heat transfer medium is then discharged by pipeline 22 from cyclone separator 15 again.It is to pass through that this interconnection, which typically results in each preheating section,
Counter-current flow, i.e., solid is heated more and more by each preheating section, and exhaust gas is more and more cooling.This leads to maximum
Heat transmitting.Preferably, preheating section is designed as cyclone separator.
From third preheating section 15, solid is discharged to by pipeline 16 and is supplied to solid conveyer 18, solid is defeated from solid
Machine 18 is sent to enter first reactor 20 by pipeline 19.The first reactor is advantageously designed to fluidized-bed reactor, especially
It is preferably designed for recirculating fluidized bed.
By pipeline 24, fuel (preferably liquid or gaseous form, particularly preferable as containing methane or hydrogen-containing gas) is drawn
Enter first reactor 20.By pipeline 25, the solid of heating is discharged to and is supplied to another solid conveyer 26, it is defeated from solid
Send machine 26 that the solid of heating is supplied to second reactor 30 by pipeline 27,28.The second reactor can be fixed
Fluidisation type, or it is also preferred that it is designed as circulating fluid bed reactor.By pipeline 31, it can also supply fuel or hot gas.
Gas is discharged to by pipeline 32 and is supplied to cyclone separator 33 or another gas-solid separator.
From gas-solid separator 33, preferably cyclone separator, contaminated exhaust gas is discharged by pipeline 34, and passes through pipeline
Product is supplied to solid conveyer 36 by 35.Fraction solids are recycled into from solid conveyer 36 by pipeline 37 and pipeline 28
Enter reactor, further to improve product quality.
By pipeline 38, another part of product enters cooler 40.It is by air that product is cold in the cooler
But, which is introduced into cooler 40 and pipeline 43 by pipeline 41 and condenser 42.Cooling product passes through 47 quilt of pipeline
Discharge.
It can will be introduced into first reactor 20 due to the cooling air being heated by pipeline 44 and 45, and preferably
It is used as fluidizing gas there.It is equally conceivable, alternatively or is also proportionally drawn the air by pipeline 46
Enter in second reactor 30.
Appended drawing reference
1,2 pipelines
10 preheating sections
11,12 pipelines
13 preheating sections
14 pipelines
15 preheating sections
16 pipelines
17 solid conveyers
18 pipelines
20 first reactors
21-25 pipeline
26 gas-solid conveyers
27,28 pipelines
30 second reactors
31,32 pipelines
33 gas-solid separators
34,35 pipelines
36 solid conveyers
37,38 pipelines
40 coolers
41 pipelines
42 condensers
43-47 pipeline
Claims (12)
1. a kind of heat-treating methods for contaminated solid, comprising the following steps:
I) using heat transfer medium by through-flow, contaminated solid is preheated to 100-600 DEG C of temperature at least one preheating section,
Ii) contaminated solid is heated to 600-1300 DEG C of temperature, the impurity thus contained in solid in the first reactor
Exhaust gas is at least partly discharged and obtained in a gaseous form,
Iii) in the second reactor 600-1300 DEG C at a temperature of solid is heat-treated, what is thus contained in solid is miscellaneous
Matter is at least partly discharged in a gaseous form, and
Iv) exhaust gas is sent at least one described preheating section as a heat transfer medium.
2. the method according to claim 1, wherein upstream guiding solid and heat transfer medium described in extremely
A few preheating section.
3. method according to any of the preceding claims, which is characterized in that first and/or second reactor restoring
Or it is run in oxidizing atmosphere.
4. method according to any of the preceding claims, which is characterized in that input first and/or second reactor
Energy is generated by supplying the fuel to burn in first and/or second reactor.
5. method according to any of claims 1-4, which is characterized in that input first and/or second reactor
Energy is generated at least partially through supply hot gas.
6. method according to any of the preceding claims, which is characterized in that after processing step (iv), solid is extremely
Partially by gas cooling, and will thus heated gas be introduced into first and/or second reactor.
7. method according to any of the preceding claims, which is characterized in that solid includes the phosphate of 1-500ppm
And/or cadmium content.
8. method according to any of the preceding claims, which is characterized in that first and/or second reactor conduct tool
There is static or recirculating fluidized bed fluidized-bed reactor to run.
9. according to the method described in claim 8, it is characterized in that, there is diameter in a fluidized bed reactor is 0.05-50mm
Sphere.
10. a kind of heat-treating apparatus for contaminated solid, comprising:
At least one preheating section (10,13,15) is used to that the solid to be preheated to 100-600 DEG C using heat transfer medium and consolidates
Temperature,
First reactor (20) is used to for the solid being heated to 600-1300 DEG C of temperature, thus contains in the solid
Impurity at least partly gaseous form and obtain exhaust gas, and
Second reactor (30), be used for 600-1300 DEG C at a temperature of be heat-treated the solid, thus contain in the solid
Some impurity is at least partly discharged in a gaseous form,
It is characterized in that, at least one return duct (21,22,23) enters at least one preheating section from first reactor (20)
(10,13,15), by the return duct by the exhaust gas introduce as a heat transfer medium at least one preheating section (10,13,
15)。
11. device according to claim 10, which is characterized in that at least one preheating section (10,13,15) is designed as whirlwind
Separator.
12. device described in 0 or 11 according to claim 1, which is characterized in that first reactor (20) and/or second reactor
(30) it is designed as fixed or circulating fluidized bed reactor.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DE102016103349.9 | 2016-02-25 | ||
| DE102016103349.9A DE102016103349A1 (en) | 2016-02-25 | 2016-02-25 | Method and device for thermal treatment of a contaminated solid |
| PCT/EP2017/054183 WO2017144593A1 (en) | 2016-02-25 | 2017-02-23 | Process and apparatus for the thermal treatment of contaminated solids |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN110214049A true CN110214049A (en) | 2019-09-06 |
Family
ID=58314155
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201780010201.1A Pending CN110214049A (en) | 2016-02-25 | 2017-02-23 | Heat-treating methods and device for contaminated solid |
Country Status (5)
| Country | Link |
|---|---|
| EP (1) | EP3419747A1 (en) |
| CN (1) | CN110214049A (en) |
| DE (1) | DE102016103349A1 (en) |
| MA (1) | MA43718A (en) |
| WO (1) | WO2017144593A1 (en) |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN85102137A (en) * | 1984-03-09 | 1987-01-24 | F·L·史密斯公司 | From unpurified phosphoric acid salt, remove the method for cadmium |
| US6491738B1 (en) * | 1999-06-21 | 2002-12-10 | Pohang Iron & Steel Co., Ltd. | 2-stage fluidized bed type fine iron ore reducing apparatus, and reducing method using the apparatus |
| WO2005026397A2 (en) * | 2003-09-18 | 2005-03-24 | Outokumpu Technology Oy | Process and plant for the heat treatment of solids containing titanium |
| CN1756851A (en) * | 2002-12-23 | 2006-04-05 | 奥托昆普技术公司 | Method and plant for the heat treatment of solids containing iron oxide using a fluidized bed reactor |
| CN101142329A (en) * | 2005-03-16 | 2008-03-12 | 奥图泰有限公司 | Process and plant for the heat treatment of solids containing titanium |
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| US4017585A (en) * | 1974-10-29 | 1977-04-12 | Dorr-Oliver Incorporated | Fluid bed calcination process |
| GB1557248A (en) * | 1976-09-09 | 1979-12-05 | Macaskill D | Calcination of materials |
| DE3322159A1 (en) * | 1983-06-21 | 1985-01-03 | Metallgesellschaft Ag, 6000 Frankfurt | METHOD FOR SEPARATING POLLUTANTS FROM EXHAUST GAS |
| DD237762A3 (en) * | 1984-01-30 | 1986-07-30 | Schwermasch Liebknecht Veb K | METHOD AND APPARATUS FOR MULTI-STAGE TREATMENT OF ORGANIC SHOOTERS |
| US5560762A (en) * | 1994-03-24 | 1996-10-01 | Metallgesellschaft Ag | Process for the heat treatment of fine-grained iron ore and for the conversion of the heat treated iron ore to metallic iron |
| DE19945771C1 (en) * | 1999-09-24 | 2001-02-22 | Muehlen Gmbh & Co Kg Dr | Process for gasifying organic materials comprises cracking the materials by contacting with a hot heat carrier medium which is removed from a solid carbonaceous residue after leaving the pyrolysis reactor and conveyed to a heating zone |
| DE10260737B4 (en) * | 2002-12-23 | 2005-06-30 | Outokumpu Oyj | Process and plant for the heat treatment of titanium-containing solids |
| DE10336676C5 (en) * | 2003-08-09 | 2011-03-31 | Outokumpu Oyj | Process and plant for the reduction of iron oxide-containing solids |
| DE102007032683B4 (en) * | 2007-07-13 | 2014-09-11 | Outotec Oyj | Process and plant for refining oleaginous solids |
| US20090208402A1 (en) * | 2008-02-20 | 2009-08-20 | Rossi Robert A | Process and system for producing commercial quality carbon dioxide from fine particle limestone |
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| EP2992268B1 (en) * | 2013-05-03 | 2020-01-15 | Outotec (Finland) Oy | Process and plant for separating heavy metals from phosphorus-containing starting material |
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2016
- 2016-02-25 DE DE102016103349.9A patent/DE102016103349A1/en not_active Withdrawn
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2017
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- 2017-02-23 EP EP17710831.3A patent/EP3419747A1/en not_active Withdrawn
- 2017-02-23 WO PCT/EP2017/054183 patent/WO2017144593A1/en active Application Filing
- 2017-02-23 CN CN201780010201.1A patent/CN110214049A/en active Pending
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Also Published As
| Publication number | Publication date |
|---|---|
| DE102016103349A1 (en) | 2017-08-31 |
| MA43718A (en) | 2018-11-28 |
| WO2017144593A1 (en) | 2017-08-31 |
| EP3419747A1 (en) | 2019-01-02 |
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