CN112892147B - Method for treating mixed gas - Google Patents
Method for treating mixed gas Download PDFInfo
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- CN112892147B CN112892147B CN202110131255.1A CN202110131255A CN112892147B CN 112892147 B CN112892147 B CN 112892147B CN 202110131255 A CN202110131255 A CN 202110131255A CN 112892147 B CN112892147 B CN 112892147B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/54—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/54—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms
- B01D46/543—Particle separators, e.g. dust precipitators, using ultra-fine filter sheets or diaphragms using membranes
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/56—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours with multiple filtering elements, characterised by their mutual disposition
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
- B01D5/0033—Other features
- B01D5/0036—Multiple-effect condensation; Fractional condensation
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D7/00—Sublimation
- B01D7/02—Crystallisation directly from the vapour phase
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/08—Compounds containing halogen
- C01B33/107—Halogenated silanes
- C01B33/1071—Tetrachloride, trichlorosilane or silicochloroform, dichlorosilane, monochlorosilane or mixtures thereof
- C01B33/10715—Tetrachloride, trichlorosilane or silicochloroform, dichlorosilane, monochlorosilane or mixtures thereof prepared by reacting chlorine with silicon or a silicon-containing material
- C01B33/10721—Tetrachloride, trichlorosilane or silicochloroform, dichlorosilane, monochlorosilane or mixtures thereof prepared by reacting chlorine with silicon or a silicon-containing material with the preferential formation of tetrachloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B33/00—Silicon; Compounds thereof
- C01B33/08—Compounds containing halogen
- C01B33/107—Halogenated silanes
- C01B33/10778—Purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01F—COMPOUNDS OF THE METALS BERYLLIUM, MAGNESIUM, ALUMINIUM, CALCIUM, STRONTIUM, BARIUM, RADIUM, THORIUM, OR OF THE RARE-EARTH METALS
- C01F7/00—Compounds of aluminium
- C01F7/48—Halides, with or without other cations besides aluminium
- C01F7/56—Chlorides
- C01F7/62—Purification
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G23/00—Compounds of titanium
- C01G23/02—Halides of titanium
- C01G23/022—Titanium tetrachloride
- C01G23/024—Purification of tetrachloride
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01G—COMPOUNDS CONTAINING METALS NOT COVERED BY SUBCLASSES C01D OR C01F
- C01G49/00—Compounds of iron
- C01G49/10—Halides
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/80—Compositional purity
Abstract
The invention discloses a method for treating mixed gas. The mixed gas has at least two metal chloride gases, the temperatures of the at least two metal chloride gases for phase change into solid are different, and the treatment method comprises the following steps: s1, primary separation: cooling the temperature of the mixed gas to a first temperature, condensing the first metal chloride gas in the mixed gas to a first solid at the first temperature, and then collecting the first solid; s2, secondary separation: cooling the temperature of the mixed gas to a second temperature, condensing the second metal chloride gas in the mixed gas to a second solid at the second temperature, and then collecting the second solid; wherein the first temperature is greater than the second temperature and the second metal chloride gas is gaseous at the first temperature. Therefore, the treatment method of the mixed gas of the invention separates step by utilizing the difference of the phase transition temperature of the metal chloride gas in the mixed gas, thereby not only ensuring higher purity, but also fully utilizing the gradient change of the temperature.
Description
Technical Field
The invention relates to the technical field of treatment of mixed gas, in particular to a treatment method of mixed gas generated by chlorination of fly ash.
Background
The fly ash is fine ash formed by smoke generated after coal combustion, and is main solid waste discharged by a coal-fired power plant. The main oxide composition of the fly ash of the thermal power plant in China is SiO2、Al2O3、FeO、Fe2O3、CaO、TiO2And the like. A large amount of fly ash can form dust to pollute the atmosphere, and toxic chemical substances in the fly ash can cause serious harm to human bodies and organisms. Fly ash produced by thermal power plant in ChinaIt has reached hundreds of millions of tons every year and increased year by year. These fly ashes, on the one hand, cause serious environmental pollution, and, on the other hand, contain usable resources. Therefore, how to extract the useful resources from the fly ash to realize high-value comprehensive utilization has important practical significance.
At present, the main international research direction is the acid method aluminum extraction process, but the effect is not ideal; on the basis, a chlorination technical route is generated, for example, Chinese patent CN102502665A discloses a method for comprehensively recovering valuable elements in fly ash, the method realizes the recovery of various metals in the fly ash by utilizing multiple processes of two-stage chlorination, reduction, rectification and the like, but the method has complex process and is difficult to realize industrial treatment.
Disclosure of Invention
Aiming at mixed gas formed by a plurality of metal chloride gases, in particular to mixed gas generated by chlorination reaction of fly ash, the invention aims to provide a method for treating mixed gas, which has obviously better process and effect than the background art.
The technical scheme provided by the invention for realizing the aim is as follows:
a method for treating a mixed gas having at least two metal chloride gases that differ in temperature at which the at least two metal chloride gases phase-change to a solid, comprising the steps of: s1, primary separation: cooling the temperature of the mixed gas to a first temperature, condensing the first metal chloride gas in the mixed gas to a first solid at the first temperature, and then collecting the first solid; s2, secondary separation: cooling the temperature of the mixed gas to a second temperature, condensing the second metal chloride gas in the mixed gas to a second solid at the second temperature, and then collecting the second solid; wherein the first temperature is greater than the second temperature and the second metal chloride gas is gaseous at the first temperature.
Further, the mixed gas is generated by reacting metal oxides of at least two different metals with chlorine at 950-1350 ℃.
Further, the mixed gas is generated by the reaction of fly ash and surplus chlorine in chlor-alkali industry or PVC industry in a chlorination furnace; the first temperature is 250-280 ℃, and the first solid mainly comprises ferric chloride; the second temperature is 120-140 ℃, and the second solid mainly comprises aluminum chloride.
Further, the mixed gas also has solid particle impurities, and the treatment method further comprises the following steps: s0, primary separation: cooling the temperature of the mixed gas to a primary temperature, and then collecting solid particle impurities; the primary temperature is 450-550 ℃; and/or the mixed gas also has a third metal chloride gas, and the treatment method further comprises the following steps: s3, three-stage separation: cooling the temperature of the mixed gas to a third temperature, condensing a third metal chloride gas in the mixed gas to a liquid at the third temperature, and then collecting the liquid; the third temperature is 0-30 ℃, and the liquid mainly comprises silicon chloride and titanium chloride.
Further, the solid particle impurities separated and collected in the primary stage are re-fed into the chlorination furnace for reaction; and the tail gas output by the third-stage separation is input into the chlorination furnace again for reaction.
Further, the primary separation adopts a primary heat exchange structure to cool the mixed gas, and adopts a primary filtering structure to perform gas-solid separation; the primary separation adopts a primary heat exchange dust removal structure to cool the mixed gas and collect part of first solids, and adopts a primary filtering structure to collect the rest of the first solids; the secondary separation adopts a secondary heat exchange dust removal structure to cool the mixed gas and collect part of second solids, and adopts a secondary filtering structure to collect the rest of second solids; and the third-stage separation adopts a third-stage heat exchange structure to cool the mixed gas and collect liquid.
Further, the first-stage heat exchange dust removal structure and/or the second-stage heat exchange dust removal structure are/is provided with: a first passage in which the mixed gas flows and through which the mixed gas passes; a second channel in which the heat exchange medium flows and which passes through; the separating mechanism is used for separating the first channel from the second channel and exchanging heat between the mixed gas in the first channel and the heat exchange medium in the second channel; the flow direction of the mixed gas in the first channel is different from the flow direction of the heat exchange medium in the second channel; part of the solids in the mixed gas is discharged from below the first channel.
Furthermore, the primary separation is provided with at least two primary heat exchange dust removal structures which are arranged at intervals in the horizontal direction, and the flow directions of the mixed gas in two adjacent primary heat exchange dust removal structures are opposite; and/or the secondary separation is provided with at least two secondary heat exchange dust removal structures which are arranged at intervals in the horizontal direction, and the flow directions of the mixed gas in the two adjacent secondary heat exchange dust removal structures are opposite.
Furthermore, a first-stage heat exchange dust removal structure adjacent to the first-stage filter structure and the first-stage filter structure share an ash hopper; and/or the secondary heat exchange dust removal structure adjacent to the secondary filter structure and the secondary filter structure share one ash bucket.
Furthermore, at least the primary filtering structure and the primary filtering structure in the primary filtering structure, the primary filtering structure and the secondary filtering structure adopt filtering media made of metal materials; the filtering medium is preferably a metal fiber felt, a sintered metal porous membrane, a metal net, a ceramic membrane or ceramic fiber; the pore diameter of the filter medium is 1 to 100 μm, preferably 5 to 50 μm, and more preferably 10 to 30 μm.
Therefore, the treatment method of the mixed gas provided by the invention separates the metal chloride gas step by utilizing the difference of the phase transition temperature of the metal chloride gas in the mixed gas, so that the higher purity is ensured, the gradient change of the temperature is fully utilized, no extra energy input is needed in the separation process, and the energy is saved and the environment is protected while the resources are fully recovered. The method has the advantages that the step-by-step separation of the mixed gas is realized only by combining heat exchange and filtration, and the first solid, the second solid and the liquid have higher quality.
The invention is further described with reference to the following figures and detailed description. Additional aspects and advantages of the invention will be set forth in part in the description which follows and, in part, will be obvious from the description, or may be learned by practice of the invention.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to assist in understanding the invention, and are included to explain the invention and their equivalents and not limit it unduly. In the drawings:
fig. 1 is a schematic structural view of a first embodiment of a mixed gas processing system.
FIG. 2 is a schematic structural diagram of a first embodiment of a primary separation unit.
FIG. 3 is a schematic structural diagram of a second embodiment of the primary separation unit.
FIG. 4 is a schematic structural view of a third embodiment of the primary separation unit.
FIG. 5 is a schematic structural view of a third embodiment of the primary separation unit.
FIG. 6 is a schematic diagram of a second embodiment of a mixed gas processing system.
FIG. 7 is a schematic structural view of an embodiment of an ash discharge structure.
FIG. 8 is a schematic structural diagram of a third embodiment of a mixed gas processing system.
The relevant references in the above figures are:
100-chlorination furnace, 210-primary heat exchange structure, 220-tertiary heat exchange structure, 310-primary filter structure, 320-primary filter structure, 330-secondary filter structure, 401-primary heat exchange dust removal structure, 402-secondary heat exchange dust removal structure, 410-flow channel, 420-first baffle, 430-second baffle, 440-solid collection mechanism, 441-ash bucket, 450-ash collection tank, 460-water tank, 470-temperature detector, 481-first control valve, 482-second control valve, 491-first channel, 492-second channel, 493-division mechanism, 510-nitrogen storage tank, 520-nitrogen heater, 530-back blowing bag, 540-intermediate ash tank, 610-intermediate pipeline, 620-balance pipeline, 630-a first balance gas conveying pipeline, 641-a first rapper, 642-a second rapper, 651-a first valve, 652-a second valve, 653-a third valve, 654-a fourth valve, 655-a fifth valve, 656-a star-shaped ash discharging valve, 501-a primary ash discharging unit, 502-a primary ash discharging unit, 503-a secondary ash discharging unit, 710-a liquid chlorine storage tank, 720-a first conveying branch pipe, 730-a chlorine gas heater, 740-a pressure regulator, 750-a second balance gas conveying pipeline, 760-a fan, 770-a pressure detector and 780-a third control valve.
Detailed Description
The invention will be described more fully hereinafter with reference to the accompanying drawings. Those skilled in the art will be able to implement the invention based on these teachings. Before the present invention is described in detail with reference to the accompanying drawings, it is to be noted that:
the technical solutions and features provided in the present invention in the respective sections including the following description may be combined with each other without conflict.
Moreover, the embodiments of the present invention described in the following description are generally only some embodiments of the present invention, and not all embodiments. Therefore, all other embodiments obtained by a person of ordinary skill in the art based on the embodiments of the present invention without any creative effort shall fall within the protection scope of the present invention.
With respect to terms and units in the present invention. The terms "comprising," "having," and any variations thereof in the description and claims of this invention and the related sections are intended to cover non-exclusive inclusions.
The first embodiment of the method for treating the mixed gas is to treat the mixed gas generated by performing a chlorination reaction on fly ash and chlorine at 950-1350 ℃, wherein the chlorination reaction is performed in a chlorination furnace 100, and silica (the molecular formula is SiO) in the fly ash2) Aluminum oxide (molecular formula is Al)2O3) Ferrous oxide (FeO molecular formula), ferric oxide (Fe molecular formula)2O3) Calcium oxide (CaO in molecular formula) and titanium dioxide (TiO in molecular formula)2) After chlorination reaction of various metal oxides, mixed gas mainly comprising ferric chloride, aluminum chloride, silicon chloride, titanium chloride and dust is generated, and obviously, the mixed gas is high-temperature dust-containing gas.
The first embodiment of the mixed gas processing method includes the steps of:
s0, primary separation: cooling the temperature of the mixed gas to a primary temperature, and then collecting solid particle impurities; the primary temperature is less than or equal to 550 ℃;
s1, primary separation: cooling the temperature of the mixed gas to a first temperature, condensing the first metal chloride gas in the mixed gas to a first solid at the first temperature, and then collecting the first solid; the first temperature is less than or equal to 280 ℃, the first metal chloride gas is mainly ferric chloride gas, and the first solid is mainly ferric chloride (the molecular formula is FeCl)3) Solid formation;
s2, secondary separation: cooling the temperature of the mixed gas to a second temperature, condensing the second metal chloride gas in the mixed gas to a second solid at the second temperature, and then collecting the second solid; the second temperature is less than or equal to 140 ℃, the second metal chloride gas is mainly aluminum chloride gas, and the second solid is mainly aluminum chloride (the molecular formula is AlCl)3) Solid formation;
s3, three-stage separation: cooling the temperature of the mixed gas to a third temperature, condensing a third metal chloride gas in the mixed gas to a liquid at the third temperature, and then collecting the liquid; the third temperature is less than or equal to 30 ℃, and the liquid mainly comprises silicon chloride (the molecular formula is SiCl)4) And titanium chloride (molecular formula is TiCl)4) And (4) forming.
Therefore, the treatment method of the mixed gas provided by the invention separates the metal chloride gas step by utilizing the difference of the phase transition temperature of the metal chloride gas in the mixed gas, so that the higher purity is ensured, the gradient change of the temperature is fully utilized, no extra energy input is needed in the separation process, and the energy is saved and the environment is protected while the resources are fully recovered.
Wherein, in order to ensure that the ferric chloride is in a gaseous state at the primary temperature, the primary temperature is preferably 450-550 ℃;
in order to ensure that the aluminum chloride is gaseous at the first temperature, the first temperature is preferably 250-280 ℃;
in order to ensure that the silicon chloride and the titanium chloride are in a gaseous state at the second temperature, the second temperature is preferably 120-140 ℃;
in order to ensure high heat exchange efficiency and production efficiency, the third temperature is preferably 0 to 30 ℃.
In order to further fully save resources, the chlorine gas adopts surplus chlorine gas in the chlor-alkali industry or the PVC industry, namely, raw materials for generating the mixed gas are all generated from resources which are difficult to fully utilize for the second time in the prior art, so that the maximum utilization of the resources is realized.
The solid particle impurities collected in the primary separation may also contain metal oxides which cannot fully participate in the chlorination reaction, so that the solid particle impurities are re-input into the chlorination furnace 100 for deep chlorination reaction, and the full utilization of the fly ash resource can be realized.
After primary separation, secondary separation and tertiary separation, valuable metal chlorides in the mixed gas are effectively recovered, so that the tail gas output by the tertiary separation is mainly chlorine; the tail gas is re-input into the chlorination furnace 100 for chlorination reaction, so that the full utilization of resources can be further realized.
The liquid mainly comprising silicon chloride and titanium chloride obtained by the three-stage separation can be further separated by fractional rectification.
In view of the above technical concept, the second embodiment of the mixed gas processing method according to the present invention is a method for processing a mixed gas composed of at least two gases having different temperatures of phase change to solid, that is, a method for processing a mixed gas according to the present invention can process a mixed gas composed of gases having different temperatures of phase change to solid, such as nitride, oxide, sulfide, carbide, etc., in addition to a mixed gas composed of a metal chloride gas, and can also achieve the technical effects of stepwise separation.
The second embodiment of the mixed gas processing method includes the steps of:
s1, primary separation: cooling the temperature of the mixed gas to a first temperature, condensing the first gas in the mixed gas to a first solid at the first temperature, and then collecting the first solid;
s2, secondary separation: and cooling the temperature of the mixed gas to a second temperature, condensing the second gas in the mixed gas to a second solid at the second temperature, and collecting the second solid.
When the mixed gas further has a third gas which is gaseous at the second temperature and is condensed into liquid at the third temperature, the processing method further includes step S3, three-stage separation: and cooling the temperature of the mixed gas to a third temperature, condensing the third gas in the mixed gas into liquid at the third temperature, and then collecting the liquid.
When the mixed gas is generated by smelting the solid raw materials, the mixed gas may further have solid particle impurities which can not be converted into gas, and in this case, the processing method further comprises the step S0 of primary separation: the temperature of the mixed gas is cooled to a primary temperature and then the solid particulate impurities are collected. Therefore, the purity and the quality of the subsequent recovered product can be improved.
Depending on the composition of the gas mixture, the number of separation stages may be set correspondingly, or the separation order may be adjusted. For example, the mixed gas may be composed of three gases with different temperatures, which change into a solid. However, in order to sufficiently ensure that the first gas is in a gaseous state at the primary temperature, the second gas is in a gaseous state at the first temperature, and the third gas is in a gaseous state at the second temperature, the primary temperature, the first temperature, the second temperature, and the third temperature are sequentially decreased in a gradient of at least 50 ℃.
In order to realize the above-described method for treating a mixed gas and to ensure a satisfactory separation effect while occupying a minimum space, the present invention provides a mixed gas treatment system as follows.
Fig. 1 is a schematic structural view of a first embodiment of a mixed gas processing system.
As shown in fig. 1, the mixed gas processing system includes a primary separation unit, a secondary separation unit, and a tertiary separation unit, wherein,
the primary separation unit comprises a primary heat exchange structure 210 and a primary filtering structure 310 which are connected in sequence, wherein the primary heat exchange structure 210 is used for cooling the mixed gas discharged from the chlorination furnace 100 to a primary temperature, and the primary filtering structure 310 is used for collecting solid particle impurities in the mixed gas;
the primary separation unit comprises a primary heat exchange dust removal structure 401 and a primary filtering structure 320 which are sequentially connected, the primary heat exchange dust removal structure 401 is used for cooling the temperature of the mixed gas to a first temperature, so that the first gas in the mixed gas is condensed into a first solid at the first temperature and part of the first solid is collected, and the primary filtering structure 320 is used for collecting the rest of the first solid;
the secondary separation unit comprises a secondary heat exchange dust removal structure 402 and a secondary filtering structure 330 which are sequentially connected, the secondary heat exchange dust removal structure 402 is used for cooling the temperature of the mixed gas to a second temperature, so that the second gas in the mixed gas is condensed into a second solid at the second temperature and part of the second solid is collected, and the secondary filtering structure 330 is used for collecting the rest of the second solid;
the three-stage separation unit comprises a three-stage heat exchange structure 220, wherein the three-stage heat exchange structure 220 is used for cooling the temperature of the mixed gas to a third temperature, so that the third gas in the mixed gas is condensed into liquid at the third temperature and the liquid is collected.
Therefore, the mixed gas treatment system disclosed by the invention realizes the step-by-step separation of the mixed gas only by adopting the combination of the heat exchange structure and the filtering structure, and the first solid, the second solid and the liquid have higher quality, so that an unexpected technical effect is achieved.
The primary separation unit and the primary separation unit have high temperatures, so that the filter media of the primary filter structure 310 and the primary filter structure 320 need to withstand high temperatures, and the conventional filter bag is hard to withstand high temperatures, so that at least the primary filter structure 310 and the primary filter structure 320 of the primary filter structure 310, the primary filter structure 320 and the secondary filter structure 330 are made of metal filter media.
The filter medium made of a metal material is preferably a sintered metal porous film which is free from support or has support (which means that raw material powder is attached to a support and sintered together) disclosed in chinese patent application publications of CN104759630A, CN104759629A, CN104874798A, CN104959611A, CN104959612A and CN104874801A filed by the applicant of the present application. Of course, other sintered metal porous membranes, or metal fiber mats, metal meshes, ceramic membranes, or ceramic fibers may be used. The filtering media made of metal materials not only have obviously higher filtering precision and corrosion resistance than the filtering bags, but also can filter high-temperature dust-containing gas with the temperature of more than or equal to 280 ℃, and do not need to be additionally provided with heat exchange units with higher energy consumption.
The aperture of the metal porous film is within 1-100 mu m, especially within 5-50 mu m, so as to ensure better filtering precision. When the aperture is 10-30 μm, the filter has good air permeability besides good filtering precision. In specific embodiments, the pore size of the porous metal film may be 1 μm, 5 μm, 8 μm, 10 μm, 15 μm, 20 μm, 25 μm, 30 μm, 50 μm, 80 μm, 100 μm, or other values.
For the mixed gas generated by the reaction of the fly ash and the surplus chlorine in the chlor-alkali industry or the PVC industry in the chlorination furnace 100, the primary heat exchange structure 210 still has a high temperature during treatment, and therefore, the primary heat exchange structure 210 is preferably but not limited to a waste heat boiler to rapidly recover high-temperature heat.
Because tertiary the separation element locates processing system's end, the temperature difference of mist and heat transfer medium is less, and treats that recovery resource exists with the liquid form, consequently, in order to accelerate heat exchange efficiency, tertiary heat transfer structure 220 adopts the water-cooled heat exchanger commonly used can, the liquid after the condensation flows out from the below of heat exchanger.
The first-stage separation unit and the second-stage separation unit preferably adopt a heat exchange dust removal structure capable of collecting condensed solids during heat exchange, so that the energy consumption of a subsequent filtering structure can be obviously reduced, the integration of heat exchange and dust removal is realized, and the process is favorably shortened and the equipment volume is reduced.
The first-stage separation unit and the second-stage separation unit may adopt any one of the following four specific embodiments, and the first-stage separation unit is described as an example below.
FIG. 2 is a schematic structural diagram of a first embodiment of a primary separation unit.
As shown in fig. 2, a primary heat exchange dust removal structure 401 and a primary filter structure 320 in the primary separation unit are independent from each other, wherein the primary heat exchange dust removal structure 401 can collect a part of the first solids while cooling the mixed gas, and the primary filter structure 320 collects the rest of the first solids; specifically, the primary heat exchange dust removal structure 401 has a flow channel 410, a first baffle 420, a second baffle 430 and a solids collection mechanism 440; wherein flow channel 410 has an inlet end and an outlet end; the first baffle 420 is connected to the bottom and side of the flow channel 410, leaving a gap between the first baffle 420 and the top of the flow channel 410 for the mixed gas to flow; the second baffle 430 is connected to the top and side of the flow channel 410, leaving a gap between the second baffle 430 and the bottom of the flow channel 410 for the mixed gas to flow; the solid collecting mechanism 440 is arranged below the flow channel 410 and communicated with the flow channel 410, the solid collecting mechanism 440 is provided with ash buckets 441 which are arranged in sequence, and the upper end of each ash bucket 441 is connected with the flow channel 410 and the bottom of the first baffle 420; the first baffle 420 and the second baffle 430 are spaced apart between the inlet end and the outlet end. Therefore, the mixed gas entering the flow channel 410 from the gas inlet end is discharged from the gas outlet end after multiple baffling motions, the temperature of the mixed gas is naturally reduced in the multiple baffling motions, no heat exchange medium is additionally adopted, and part of first solids in the mixed gas fall into the ash bucket 441 to be collected. Wherein the first solids collected by the solids collecting mechanism 440 are first discharged into the ash collecting tank 450 and then discharged from the ash collecting tank 450, thereby simplifying the operation.
FIG. 3 is a schematic structural diagram of a second embodiment of the primary separation unit.
As shown in fig. 3, on the basis of the first embodiment, in order to more accurately control the outlet temperature of the primary heat exchange and dust removal structure 401, the primary heat exchange and dust removal structure 401 in the second embodiment further includes a water tank 460, a liquid inlet pipe, a liquid outlet pipe, a temperature detector 470, a first control valve 481, a hot gas delivery pipe, a second control valve 482 and a controller, the water tank 460 is disposed above the flow channel 410, the water tank 460 includes a liquid inlet and a liquid outlet, the liquid inlet pipe is communicated with the liquid inlet, the liquid outlet pipe is communicated with the liquid outlet, the temperature detector 470 is used for detecting the mixed gas temperature at the outlet end and/or the inlet end of the flow channel 410, the first control valve 481 is disposed on the liquid inlet pipe, the hot gas delivery pipe is used for delivering hot gas, the outlet end of the hot gas delivery pipe is communicated with the inlet end of the flow channel 410, the second control valve 482 is disposed on the hot gas delivery pipe, thus, the controller controls the opening and closing of the first and second control valves 481 and 482 according to the detection value of the temperature detector 470 to achieve accurate heat exchange temperature control. For example, when the temperature detector 470 detects that the temperature of the mixed gas at the outlet end and/or the inlet end of the flow channel 410 is too high, the controller controls the first control valve 481 to open, so that water is fed into the water tank 460 to lower the temperature of the mixed gas; when the temperature detector 470 detects that the temperature of the mixed gas at the outlet end and/or the inlet end of the flow channel 410 is too low, the controller controls the second control valve 482 to open, so that hot gas is input into the mixed gas to raise the temperature of the mixed gas, and finally the first solid is effectively recovered by the first-stage separation unit, thereby preventing the influence on the subsequent separation units.
Wherein, the flowing direction of the water in the water tank 460 is preferably opposite to the flowing direction of the mixed gas in the flow channel 410, so that the water and the mixed gas can exchange heat in a convection manner, and the heat exchange effect is better.
FIG. 4 is a schematic structural view of a third embodiment of the primary separation unit.
As shown in fig. 4, the primary heat-exchanging and dust-removing structure 401 and the primary filtering structure 320 are an integrated structure, wherein the primary heat-exchanging and dust-removing structure 401 may be the heat-exchanging and dust-removing structure shown in fig. 2 or fig. 3, the output ends of the primary filtering structure 320 and the primary heat-exchanging and dust-removing structure 401 share one ash bucket 441, and the mixed gas flows into the ash bucket 441 from top to bottom and then passes through the filtering medium of the primary filtering structure 320 from bottom to top.
It can be seen that the primary separation unit shown in fig. 4 will have a smaller equipment volume and reduce line ash deposition compared to the configurations shown in fig. 2-3.
In the above three embodiments of the primary separation unit, the height of the gap d1 is 2 to 15cm, the horizontal distance d3 between the first baffle 420 and the second baffle 430 is 0.3 to 1m, and the height d2 between the first baffle 420 and the second baffle 430 is greater than or equal to 1m, so as to ensure the best fluidity and baffling effect, in the embodiment, the height of the gap d1 is 2cm, 4cm, 6cm, 8cm, 11cm, 13cm, 15cm or other values, the horizontal distance d3 between the first baffle 420 and the second baffle 430 is 0.3m, 0.5m, 0.8m, 1m or other values, and the height d2 between the first baffle 420 and the second baffle 430 is 1m, 2m, 3m, 4m, 5m or other values.
The first baffle 420 and the second baffle 430 are vertically disposed so that the first solid is prevented from being deposited on the first baffle 420 and the second baffle 430. However, when the first and second baffles 420 and 430 are disposed in a non-vertical direction, the mixed gas is deflected more effectively, and a small amount of the first solid is deposited on the upper end of the first baffle 420 due to the thickness of the first baffle 420, and at this time, a rapping mechanism may be provided to remove the first solid deposited on the first and second baffles 420 and 430.
The primary separation unit of the above three specific embodiments may process the above mixed gas, and may also be used for cooling and dedusting high-temperature dusty gas, that is, the primary heat exchange and dedusting structure 401 may be used for pre-dedusting while cooling the high-temperature dusty gas, and the primary filter structure 320 further intercepts dust in the high-temperature dusty gas by using a filter medium. For example, the primary heat exchange dust removal structure 401 and the primary filter structure 320 can replace the heat exchange dust removal device in the chinese patent application with application number 2020116204714, and cool and remove dust from high-temperature dust-containing gas in the fields of fuming furnace gas, copper matte flue gas produced by pyrometallurgical copper smelting, and the like. In addition, the high-temperature dusty gas treatment method adopting the primary heat exchange dust removal structure 401 in the three specific embodiments has the advantages of simple process, convenience in operation and the like.
Similarly, the fourth embodiment of the primary separation unit can also be any one of the heat exchange dust removing devices shown in fig. 7-15 of the chinese patent application with application number 2020116204714, preferably the heat exchange dust removing device with small volume shown in fig. 14 or fig. 15. That is, as shown in fig. 5 (i.e., the heat exchange dust removal device shown in fig. 15 of the chinese patent application with application number 2020116204714), the fourth embodiment of the primary separation unit is a primary heat exchange dust removal structure 401 and a primary filter structure 320 that are integrally connected, where the primary heat exchange dust removal structure 401 is capable of collecting a part of the first solids while cooling the mixed gas, and the primary filter structure 320 collects the rest of the first solids; specifically, the primary heat exchange and dust removal structure 401 has a first channel 491, a second channel 492, and a dividing mechanism 493, the mixed gas flows in the first channel 491 and passes through the first channel 491, the heat exchange medium flows in the second channel 492 and passes through the second channel 492, the dividing mechanism is used for dividing the first channel 491 from the second channel 492 and exchanging heat between the mixed gas in the first channel 491 and the heat exchange medium in the second channel 492, and the flowing direction of the mixed gas in the first channel 491 is different from the flowing direction of the heat exchange medium in the second channel 492; the first solid in the mixed gas is discharged from below the first passage 491; the primary separation unit is provided with at least two primary heat exchange and dust removal structures 401 which are arranged at intervals in the horizontal direction, the flow directions of mixed gas in the two adjacent primary heat exchange and dust removal structures 401 are opposite, and the primary heat exchange and dust removal structure 401 adjacent to the primary filter structure 320 and the primary filter structure 320 share one ash bucket 441.
FIG. 6 is a schematic diagram of a second embodiment of a mixed gas processing system.
As shown in fig. 6, on the basis of the first embodiment, the mixed gas treatment system of the second embodiment further includes an ash removal unit and an ash discharge unit; the ash removal unit removes dust deposited on the filter media of the primary filter structure 310, the primary filter structure 320 and the secondary filter structure 330 by using a nitrogen back-blowing air bag 530, and the ash removal unit discharges solids collected by the primary separation unit, the primary separation unit and the secondary separation unit by using an ash removal structure.
The ash discharging unit includes a primary ash discharging unit 501 discharging solid particle impurities collected by the primary separating unit, a primary ash discharging unit 502 discharging first solids collected by the primary separating unit, and a secondary ash discharging unit 503 discharging second solids collected by the secondary separating unit. The first-stage ash discharge unit 502 is described below as an example.
FIG. 7 is a schematic structural view of an embodiment of an ash discharge structure.
As shown in fig. 7, the ash discharge structure has an intermediate duct 610, an intermediate ash tank 540, an ash discharge duct, a balance duct 620, and a first balance gas conveying duct 630; the intermediate pipeline 610 is connected with the ash bucket 441 of the primary filtering structure 320, and the intermediate pipeline 610 is provided with a first valve 651 and a second valve 652; the intermediate ash tank 540 is connected with the intermediate pipeline 610; the ash discharge pipeline is connected with the intermediate ash tank 540 and is provided with a third valve 653 and a star-shaped ash discharge valve 656; the balance pipeline 620 is connected with the intermediate ash tank 540 and the air inlet pipe of the primary filtering structure 320, and a fourth valve 654 is arranged on the balance pipeline 620; the first balance gas conveying pipeline 630 is connected with the intermediate ash tank 540, and a fifth valve 655 is arranged on the first balance gas conveying pipeline 630; the ash bucket 441 is provided with a first vibrator 641; the middle ash tank 540 is provided with a second rapping device 642; a first material level meter is arranged on the ash bucket 441; the middle ash tank 540 is provided with a second level indicator; the ash bucket 441 is provided with a first explosion venting valve; the intermediate ash tank 540 is provided with a second explosion venting valve.
The use method of the ash discharging structure comprises the following steps:
s1: opening the fourth valve 654 and the fifth valve 655 to replace the gas in the intermediate ash tank 540; closing the fifth valve 655 after the replacement is complete;
s2: opening the first valve 651 and the first rapper 641 to allow the first solids to drain into the intermediate conduit 610 but not to drain; the first valve 651 and the first rapper 641 are then closed;
s3: opening the second valve 652 to allow the first solids to drain into the intermediate ash tank 540; second valve 652 is then closed;
s4: opening the fifth valve 655, replacing the gas in the intermediate ash tank 540 again; closing the fifth valve 655 after the replacement is complete;
s5: closing the fourth valve 654;
s6: the fifth valve 655, the second rapper 642, the third valve 653 and the star-type ash discharge valve 656 are opened in sequence for ash discharge.
In the above-described mixed gas treatment system, the ash discharge structure is mainly used for discharging ash from the ash bucket 441 below the filter structure. When the primary heat exchange dust removing structure 401 and the primary filtering structure 320 are of an integrated structure, the first solid collected by the solid collecting mechanism 440, which is not connected with the primary filtering structure 320, in the primary heat exchange dust removing structure 401 is firstly discharged into the ash collecting tank 450, and then is discharged into the intermediate ash tank 540. When the primary heat exchange and dust removal structure 401 and the primary filtering structure 320 are of a split structure, the first solids collected by the solids collection mechanism 440 in the primary heat exchange and dust removal structure 401 are all discharged into the ash collection tank 450 at first, and then discharged into the intermediate ash tank 540.
Besides the mixed gas treatment system, the ash discharge unit can be used for discharging ash of other conventional dust removal devices, and particularly when combustible and explosive gases are contained in materials, the ash discharge unit can ensure high safety when used for discharging ash.
FIG. 8 is a schematic structural diagram of a third embodiment of a mixed gas processing system.
As shown in fig. 8, the mixed gas treatment system of the third embodiment further includes a first recovery unit, a second recovery unit, a chlorine gas generation unit, and a pressure control unit on the basis of the second embodiment; the chlorine generating unit is used for converting liquid chlorine into chlorine and inputting the chlorine into the chlorination furnace 100 for reaction; the first recovery unit is used for inputting the tail gas output by the third-stage separation unit into the chlorination furnace 100 again for reaction; the second recovery unit is used for inputting the solid particle impurities collected by the primary separation unit into the chlorination furnace 100 again for reaction; the pressure control unit is used to control the pressure of the chlorine gas entering the chlorination furnace 100.
The chlorine generating unit comprises a liquid chlorine storage tank 710, a first conveying branch pipe 720, a chlorine heater 730 and a pressure regulator 740 which are connected in sequence, wherein the liquid chlorine in the first conveying branch pipe 720 is heated by the chlorine heater 730 and then outputs chlorine; wherein the first delivery branch pipe 720 of the chlorine heater 730 is bent, thereby significantly improving the heating efficiency.
The first recovery unit comprises a middle gas tank and a second delivery branch pipe which sequentially deliver tail gas, and a second balance gas delivery pipeline 750 which inputs balance gas into the middle gas tank, wherein a fan 760 is arranged on the second delivery branch pipe.
The first conveying branch pipe 720 and the second conveying branch pipe are connected with the chlorination furnace 100 through a main conveying pipe.
The pressure control unit comprises a pressure detector 770 and a third control valve 780, the pressure detector 770 is used for detecting the pressure of the mixed gas at the gas outlet of the chlorination furnace 100, the third control valve 780 is arranged on the main conveying pipe, and the controller controls the opening and closing of the third control valve 780 according to the detection value of the pressure detector 770. Therefore, on the basis of fully utilizing chlorine, the working mode that the positive pressure of the treatment system is always maintained is ensured by controlling the air inlet pressure of the chlorine, so that not only is the filtering power and the air supply power required by the treatment system provided, but also the safety is obviously improved.
In the second and third embodiments of the mixed gas treatment system, the blowback gas used by the ash removal unit, the replacement gas used by the ash discharge unit, and the balance gas of the first recovery unit are all nitrogen provided by the nitrogen storage tank 510, and the hot gas in the first embodiment is hot nitrogen heated by the nitrogen heater 520.
The contents of the present invention have been explained above. Those skilled in the art will be able to implement the invention based on these teachings. All other embodiments, which can be derived by a person skilled in the art from the above description without inventive step, shall fall within the scope of protection of the present invention.
Claims (11)
1. The treatment method of the mixed gas is characterized in that the mixed gas is generated by reacting fly ash and chlorine at 950-1350 ℃, and comprises the following steps:
s0, primary separation: cooling the temperature of the mixed gas to a primary temperature, and then collecting solid particle impurities; the primary temperature is 450-550 ℃;
s1, primary separation: cooling the temperature of the mixed gas to a first temperature, condensing the first metal chloride gas in the mixed gas to a first solid at the first temperature, and then collecting the first solid; the first temperature is 250-280 ℃, and the first solid mainly comprises ferric chloride;
s2, secondary separation: cooling the temperature of the mixed gas to a second temperature, condensing the second metal chloride gas in the mixed gas to a second solid at the second temperature, and then collecting the second solid; the second temperature is 120-140 ℃, and the second solid mainly comprises aluminum chloride;
wherein the primary temperature > the first temperature > the second temperature and the primary temperature, the first temperature and the second temperature decrease in sequence according to a gradient of at least 50 ℃; the second metal chloride gas is in a gaseous state at the first temperature.
2. The method according to claim 1, wherein: the mixed gas is generated by the reaction of fly ash and surplus chlorine in chlor-alkali industry or PVC industry in a chlorination furnace (100).
3. The method according to claim 1, wherein: the mixed gas also has a third metal chloride gas, and the treatment method further comprises the steps of:
s3, three-stage separation: cooling the temperature of the mixed gas to a third temperature, condensing a third metal chloride gas in the mixed gas to a liquid at the third temperature, and then collecting the liquid; the third temperature is 0-30 ℃, and the liquid mainly comprises silicon chloride and titanium chloride.
4. The method according to claim 3, wherein: the solid particle impurities separated and collected primarily are input into the chlorination furnace (100) again for reaction; the tail gas output by the three-stage separation is input into the chlorination furnace (100) again for reaction.
5. The method according to claim 3, wherein:
the primary separation adopts a primary heat exchange structure (210) to cool the mixed gas, and adopts a primary filtering structure (310) to carry out gas-solid separation;
the primary separation adopts a primary heat exchange dust removal structure (401) to cool the mixed gas and collect part of first solids, and adopts a primary filtering structure (320) to collect the rest of the first solids;
the secondary separation adopts a secondary heat exchange dust removal structure (402) to cool the mixed gas and collect part of second solids, and adopts a secondary filtering structure (330) to collect the rest of second solids;
the three-stage separation adopts a three-stage heat exchange structure (220) to cool the mixed gas and collect liquid.
6. The method according to claim 5, wherein: the primary heat exchange dust removing structure (401) and/or the secondary heat exchange dust removing structure (402) is provided with:
a first passage (491) through which the mixed gas flows inside the first passage (491);
a second channel (492), the heat exchange medium flowing in the second channel (492) and passing through the second channel (492);
the separation mechanism is used for separating the first channel (491) from the second channel (492) and exchanging heat between the mixed gas in the first channel (491) and the heat exchange medium in the second channel (492);
wherein the flow direction of the mixed gas in the first passage (491) is different from the flow direction of the heat exchange medium in the second passage (492); part of the solids in the mixed gas is discharged from below the first passage (491).
7. The method according to claim 6, wherein: the primary separation is provided with at least two primary heat exchange dust removal structures (401) which are arranged at intervals in the horizontal direction, and the flow directions of mixed gas in every two adjacent primary heat exchange dust removal structures (401) are opposite; and/or the secondary separation is provided with at least two secondary heat exchange dust removing structures (402) which are arranged at intervals in the horizontal direction, and the flow directions of the mixed gas in the two adjacent secondary heat exchange dust removing structures (402) are opposite.
8. The method according to claim 7, wherein: the primary heat exchange and dust removal structure (401) adjacent to the primary filter structure (320) and the primary filter structure (320) share one ash bucket (441); and/or the secondary heat exchange dust removal structure (402) adjacent to the secondary filter structure (330) shares an ash hopper (441) with the secondary filter structure (330).
9. The method according to claim 7, wherein: at least the primary filtering structure (310) and the primary filtering structure (320) in the primary filtering structure (310), the primary filtering structure (320) and the secondary filtering structure (330) adopt filtering media made of metal materials; the filter medium is metal fiber felt, sintered metal porous film, metal net, ceramic film or ceramic fiber; the aperture of the filter medium is 1-100 μm.
10. The method for treating a mixed gas according to claim 9, wherein: the aperture of the filter medium is 5-50 μm.
11. The method according to claim 10, wherein: the aperture of the filter medium is 10-30 μm.
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| CN116282035A (en) * | 2023-03-03 | 2023-06-23 | 成都易态科技有限公司 | Production system of polycrystalline silicon |
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