CN110813050A - Method and device for treating solid combustion waste gas - Google Patents

Method and device for treating solid combustion waste gas Download PDF

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CN110813050A
CN110813050A CN201811011850.6A CN201811011850A CN110813050A CN 110813050 A CN110813050 A CN 110813050A CN 201811011850 A CN201811011850 A CN 201811011850A CN 110813050 A CN110813050 A CN 110813050A
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gas
adsorbent
air
ammonia
degassing section
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刘国锋
林学良
刘晓敏
李转丽
邓松林
徐增强
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Beijing ZHTD Environmental Protection Technology Co Ltd
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Beijing ZHTD Environmental Protection Technology Co Ltd
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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    • B01D53/02—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 adsorption, e.g. preparative gas chromatography
    • B01D53/06—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—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 adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
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    • B01D—SEPARATION
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/52—Hydrogen sulfide
    • B01D53/523—Mixtures of hydrogen sulfide and sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds
    • B01D53/685—Halogens or halogen compounds by treating the gases with solids
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    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
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    • B01D53/81—Solid phase processes
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/86—Catalytic processes
    • B01D53/8621—Removing nitrogen compounds
    • B01D53/8625—Nitrogen oxides
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
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    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/96—Regeneration, reactivation or recycling of reactants
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    • B01D2258/06—Polluted air

Abstract

A method and apparatus for treating solid combustion exhaust gas comprising removing at least a major amount of SOXAnd possibly other contaminant steps, pre-removal of NOXStep of removing NOXAnd/or other reaction product steps. The apparatus for treating solid combustion exhaust gas comprises a device for removing SO from the solid combustion exhaust gasX、NOXMoving bed reactor, NH, with possible other contaminants3A supply unit and a regeneration unit of the adsorbent; after flowing out of the cooling section of the regeneration unit, the air for cooling the adsorbent in the regeneration unit may be passed to a dilution fan in the NH3 supply unit. The method and the device for treating the solid combustion waste gas can realize simple and convenient NH production3The gas recycling during the regeneration of the adsorbent is realized, and the gas during the regeneration of the adsorbent can be used for NH3In the supply unit.

Description

Method and device for treating solid combustion waste gas
Technical Field
The invention relates to the technical field of waste gas treatment, in particular to a method and a device for treating solid combustion waste gas.
Background
In the combustion of ore material, the ore material is mixed with solids containing small particles of carbon and placed on a sinter band on which the ore is conveyed onwardsThe material is at least partially combusted, and the at least partially combusted material is delivered to the discharge end. During sintering, the material undergoes smoldering and at least partial combustion, whereby a large amount of gas is released, which gas has the component CO removed2And possibly CO, O2、H2O and/or N2It also contains a series of pollutants. In particular, the pollutants are nitrogen oxides (NOx), SO2HCl, dioxins, furans, dust and sublimable or condensable residues resulting from smoldering processes, heavy hydrocarbons and/or heavy metals.
The exhaust gases from the sintering belt represent a large proportion of all impurities produced in the metal production process, e.g. more than 90% of the corresponding emissions in the production of iron and steel are dioxins and furans. The current disposal of the off-gases from the sinter band is generally expensive, thereby increasing the overall cost of steel production. In addition, because of the different fractions of pollutants in the sintering belt exhaust gas and their composition, which vary greatly with the feed, and because of the different reactions and available purification methods of the pollutants, multiple purification steps must be taken to remove the different pollutant components.
Patents WO 01/17663, WO 2006/084671 a1 disclose purification methods for sintering exhaust gas, but the methods in the above two patents require expensive equipment and use of consumed materials, and thus patent CN 101605589B discloses a method and equipment for purifying sintering exhaust gas, but the method and equipment for supplying NH in the patent, which overcomes the above problems3The unit is complex and does not fully realize the recycling of resources.
Disclosure of Invention
The invention aims to provide a simpler method and a simpler device for solid combustion of waste gas, which can realize simple and convenient NH production3The gas recycling during the regeneration of the adsorbent is realized, and the gas during the regeneration of the adsorbent can be used for NH3In the supply unit.
In order to achieve the purpose, the invention provides the following technical scheme:
a method for treating solid combustion exhaust gas comprising,
removing at least a major amount of SOXAnd possibly other contaminant steps: passing flue gas into a moving bed reactor from below, horizontal gas inflow through said moving bed reactor and bulk material discharge from the lower plate, into a lower adsorbent layer, wherein the pore system of the adsorbent in said lower adsorbent layer is responsible for at least a major amount of SO in said flue gasXAdsorbing the purified gas with possible other pollutants to obtain primary purified gas;
preliminary removal of NOXThe method comprises the following steps: the primary purge gas leaves the lower adsorbent layer from its upper surface and is subsequently used to convert NOXContaining NH of3The mixture is fully mixed to obtain mixed gas;
removal of NOXAnd/or other reaction product steps: said mixed gas entering from below, a horizontal gas flow through said moving bed reactor and a bulk material discharge upper plate, entering an adsorbent upper layer, wherein at least a major amount of NOX and/or other reaction products are adsorbed on the adsorbent surface in said adsorbent upper layer, resulting in a repurified gas;
the repurified gas exits the upper adsorbent layer from an upper surface thereof and then exits the moving bed reactor.
Preferably, in the method for treating solid combustion exhaust gas, the method further comprises the following steps of:
adding an adsorbent: an adsorbent is supplied to the upper surface of the upper layer of the adsorbent from above through a bulk material distribution plate at the upper end of the moving bed reactor, and then passed through the upper and lower layers of the moving bed reactor from above downward, whereby the adsorbent is first loaded with NO on the surface thereofXOr N2 and water vapour, and secondly, the loading of SOX and possibly other contaminants in the pore system of the adsorbent, followed by a horizontal gas inflow through the moving bed reactor and bulk material discharge lower plate;
controlling the adsorbent: the transfer, discharge, and moving speed of the adsorbent, and the SO pair of the adsorbent in the upper layer of the moving bed reactorXAnd possibly other contaminantsThe load is controlled by a bulk material discharge unit that controls the load under or on the gas inflow and bulk material discharge lower plate.
Preferably, in the above method for treating solid combustion exhaust gas, the loading of the adsorbent on the upper layer of the moving bed reactor with SOX and possibly other pollutants is limited to within 10 wt.% of the weight of the adsorbent discharged on the bulk material discharge unit, which limitation may allow NO in the sintering exhaust gasXAn adsorbent that is highly deposited and does not hinder SOX and/or HCl removal by the lower adsorbent layer of the moving bed reactor.
Preferably, in the above method for treating a solid combustion exhaust gas, the NH is contained3The mixture being air/H2O steam/NH3A gas mixture.
Preferably, in the above method for treating solid combustion exhaust gas, the air/H2O steam/NH3The preparation method of the gas mixture comprises the following steps: firstly, ammonia water is evaporated by an ammonia water evaporator to form ammonia gas; secondly, mixing the ammonia gas and the hot air blown by the dilution fan through an ammonia gas/air mixer to obtain air/H2O steam/NH3A gas mixture.
Preferably, in the above method for treating solid combustion exhaust gas, the method further comprises the adsorbent regeneration step of:
loading SO from the moving bed reactor2Is introduced into the regeneration unit from above,
in the regeneration unit, the adsorbent first passes through a heated upper degassing section, then from above through a middle and rear degassing section to suck out the desorbed pollutant gas, and finally from above through a cooled cooling section.
Preferably, in the above method for treating a solid combustion exhaust gas, the upper degassing section is a tubular desorber.
Method for treating solid combustion exhaust gases, in which method NH-containing gas mixtures for obtaining NOx-converting gas mixtures are used3The mixture is emptygas/H2O steam/NH3A gas mixture.
A method of treating solid combustion exhaust gas, in which method the air/H is used2O steam/NH3The preparation method of the gas mixture comprises the following steps: firstly, ammonia water is evaporated by an ammonia water evaporator to form ammonia gas; secondly, mixing the ammonia gas and the hot air blown by the dilution fan through an ammonia gas/air mixer to obtain air/H2O steam/NH3A gas mixture.
A method of treating solid combustion exhaust gas comprising the adsorbent regeneration step of:
loading SO from the moving bed reactor2Is introduced into the regeneration unit from above,
in the regeneration unit, the adsorbent first passes through a heated upper degassing section, then from above through a middle and rear degassing section to suck out the desorbed pollutant gas, and finally from above through a cooled cooling section.
Preferably, in the above method for treating a solid combustion exhaust gas, the upper degassing section is a tubular desorber.
An apparatus for treating solid combustion exhaust gas comprising
For removing SO in solid combustion waste gasX、NOXAnd possibly other contaminants, in a moving bed reactor,
a NH3 supply unit for supplying a mixture comprising NH3 to the moving bed reactor and
a regeneration unit for regenerating the adsorbent which is discharged from the moving bed reactor and adsorbs the exhaust gas pollutants;
after the air for cooling the high-temperature adsorbent in the regeneration unit flows out of the cooling section of the regeneration unit, the hot air source which can be used as the NH3 supply unit is introduced into the dilution fan in the NH3 supply unit.
Preferably, in the above apparatus for treating solid combustion exhaust gas, the NH3 supply unit includes
An ammonia water evaporator for evaporating ammonia water into ammonia gas,
a dilution fan for blowing in the hot air,
an ammonia/air mixer for mixing ammonia and hot air,
the ammonia gas formed by the ammonia water evaporator and the hot air flowing out of the dilution fan flow into the ammonia gas/air mixer, and are mixed in the ammonia gas/air mixer to form NH-containing gas3And (3) mixing.
Preferably, the apparatus for treating solid combustion exhaust gas further comprises a regeneration unit for the adsorbent,
the regeneration unit comprises an upper degassing section, a middle rear degassing section, a cooling section and a hot combustion air circulation heating assembly;
the upper end of the middle rear degassing section is connected with the lower end of the upper degassing section, and the lower end of the middle rear degassing section is connected with the upper end of the cooling section;
the hot combustion air circulation heating assembly includes a heater through which air and gas enter the lower end of the upper degassing section after forming hot combustion air, after which the hot combustion air flows upward from the lower end of the upper degassing section, then flows out from the upper end of the upper degassing section, and finally, the hot combustion air flowing out from the upper end of the upper degassing section flows into the heater again.
Preferably, in the apparatus for treating solid combustion exhaust gas described above, the upper degassing section is a tubular desorber.
An apparatus for treating solid combustion exhaust gas, comprising an NH3 supply unit, wherein the NH3 supply unit comprises
An ammonia water evaporator for evaporating ammonia water into ammonia gas,
a dilution fan for blowing in the hot air,
an ammonia/air mixer for mixing ammonia and hot air,
the ammonia gas formed by the ammonia water evaporator and the hot air flowing out of the dilution fan flow into the ammonia gas/air mixer, and are mixed in the ammonia gas/air mixer to form NH-containing gas3And (3) mixing.
An apparatus for treating solid combustion exhaust gas comprising a regeneration unit for sorbent, said regeneration unit comprising an upper degassing section, a rear-middle degassing section, a cooling section, and a hot combustion air circulation heating assembly;
the upper end of the middle rear degassing section is connected with the lower end of the upper degassing section, and the lower end of the middle rear degassing section is connected with the upper end of the cooling section;
the hot combustion air circulation heating assembly includes a heater through which air and gas enter the lower end of the upper degassing section after forming hot combustion air, after which the hot combustion air flows upward from the lower end of the upper degassing section, then flows out from the upper end of the upper degassing section, and finally, the hot combustion air flowing out from the upper end of the upper degassing section flows into the heater again.
Preferably, in the apparatus for treating solid combustion exhaust gas described above, the upper degassing section is a tubular desorber.
The adsorbent can be a carbon-containing adsorbent which can enable pollutants to be removed in sintering waste gas to reach a high deposition degree, and preferably, the carbon-containing adsorbent can be formed active coke; preferably, the carbonaceous adsorbent may have a particle size of 1 to 10 mm.
Preferably, the height of the upper layer of the adsorbent is 1.5 to 4.5 mm.
Preferably, the height of the lower layer of the adsorbent may be 0.5 to 3.0 mm.
Preferably, the height of the upper layer of adsorbent is greater than the height of the lower layer.
Preferably, the gas purification temperature on the adsorbent is carried out at a temperature greater than 80 ℃.
Preferably, the sintering waste gas before entering the moving bed reactor can adopt calcium oxide, calcium hydroxide and/or similar alkali metal compound or alkali metal compound to react with SO in the sintering waste gasXHS and/or HCl in combination.
The above waste gas of the present invention is not limited to the sintering waste gas mentioned in the background art, and may be any waste gas generated in the steel manufacturing process, and the composition of the waste gas may be one or more of the components of the sintering waste gas in the background art, and is not limited thereto.
Compared with the prior art, the invention has the beneficial effects that:
1. the invention is provided with NH3A supply unit at the NH3In the supply unit, ammonia water is evaporated by an ammonia water evaporator to form ammonia gas, the ammonia gas and hot air blown by a dilution fan enter an ammonia gas/air mixer to form air/H2O steam/NH3Gas mixture, NH of the invention3The supply unit can supply NH-containing gas to the diversion area of the mobile reactor more simply and conveniently3And (3) mixing.
2. In the adsorbent regeneration unit of the present invention, hot combustion air formed by heating air and fuel gas by a heater is used to heat the active coke in the upper degassing section, and then the hot combustion air flows out from the upper end of the upper degassing section and flows into the heater again through a pipeline, thereby realizing the cyclic heating utilization of the hot combustion air.
3. In the adsorbent regeneration unit of the present invention, compressed air for the cooling stage flows out of the cooling stage and then flows into NH3Supply unit as NH3The hot air blown by the dilution fan is used in the supply unit, thereby realizing the reuse of the hot air and saving NH3The heating step of the hot air in the supply unit simplifies the process and saves the cost.
4. The invention greatly simplifies the method, can completely and fully deposit NOx, SOx and/or HCl and possible other pollutants by using a single counter-current moving bed reactor, has the utilization rate of the adsorption/absorption capacity of the used adsorbent as high as 100 percent, and can fully remove dust flowing to the moving bed reactor still existing in the sintering waste gas after pre-purification.
Drawings
FIG. 1 is a flowchart of example 1 of the present invention;
FIG. 2 is a schematic view of the structure of a moving bed reactor according to the present invention;
FIG. 3 is a schematic diagram of the construction of a regeneration unit according to the present invention.
In the figure: 1 is a sintering belt, 2 is an electric filter, 3 is a first air blower, 4 is a bag filter, 5 is a second air blower, 6 is a moving bed reactor, 6-1 is a horizontal gas inflow/bulk material discharge lower plate, 6-2 is a bulk material lower layer (adsorbent lower layer), 6-2-1 is an upper surface of the bulk material lower layer, 6-3 is a turning zone, 6-4 is a horizontal gas inflow/bulk material discharge upper plate, 6-5 is a bulk material upper layer (adsorbent upper layer), 6-5-1 is an upper surface of the bulk material upper layer, 6-6 is a storage hopper, 6-7 is an active coke passing bulk distribution plate material, 6-8 is a bulk material distribution pipe, 6-9 is a bulk material discharge pipe, 6-10 is an intermediate plate, 6-11 is a bulk material discharge pipe, 6-12 is a middle plate, 6-13 is an ejector, 6-14 is an exhaust funnel, 6-15 is an ammonia spraying grid, 7 is an NH3 supply unit, 7-1 is an ammonia water evaporator, 7-2 is a dilution fan, 7-3 is an ammonia gas/air mixer, 8 is a pipeline, 9 is screening equipment, 10 is a regeneration unit, 10-1 is an upper degassing section, 10-2 is a middle and rear degassing section, 10-3 is a cooling section, 10-4 is a storage section, 10-5 is an exhaust hopper, 10-6 is a heater, 10-7 is a fan, 10-8 and 10-9 are pipelines, 11 is a pipeline, 12 is a sulfuric acid blower production device, and 13 is a suction type.
Detailed Description
The technical solution in the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention.
Example 1
Referring to fig. 1, the exhaust gas generated on the sintering belt 1 is conveyed via a line to an electric filter (prior art), the dust generated by filtration by the electric filter 2 is conveyed via a line back to the sintering belt, and the exhaust gas flowing out of the electric filter 2 at about 150 ℃. sup.165 ℃ is passed in turn via a first blower 3 into a bag filter 4, wherein the blower 3 can provide sufficient pressurization for the operation of the apparatus. Calcium oxide, calcium hydroxide and/or similar alkali metal compounds or alkali metal compounds may also be added to the sintering waste gas before it exits the first blower 3 and flows into the bag filter 4 to react with the SO in the sintering waste gasXHS and or HCl to significantly reduce the consumption of the more expensive adsorbent.
The sintering waste gas leaving via the bag filter 4 is first cooled by evaporation to approximately 135 ℃ by means of water and is then conducted via a second blower 5 into a moving-bed reactor 6 which is operated in countercurrent, wherein, in order to cool the sintering waste gas leaving via the bag filter 4 to the desired temperature (for example 135 ℃), it is also possible to cool it by evaporation by mixing in ambient air and/or spraying in water.
Referring to fig. 2, the sintering offgas entering the moving bed reactor 6 first enters the horizontal gas inflow/bulk material discharge lower plate 6-1 and then enters the bulk material lower layer 6-2, which is an adsorbent lower layer and is composed of active coke particles 6-2. Dust residues in the exhaust gas, including mercury, other heavy metals and possibly other pollutants such as organic compounds, particularly heavy hydrocarbons, dioxins and furans, etc., are adsorbed, absorbed or adhered to deposit on the horizontal gas inflow/bulk material discharge lower plate 6-1 and the bulk material lower layer 6-2 thereon;
thereafter, the sintering offgas is sufficiently mixed with NH3 at the turning zone 6-3, and NH3 is supplied through the unique NH3 supply unit 7 of the present invention. The operation of the NH3 supply unit 7 is as follows: ammonia water is conveyed to the ammonia water evaporator 7-1 through a conveying pump to be evaporated to form ammonia gas, the ammonia gas is mixed with hot air blown in by a dilution fan 7-2 through an ammonia gas/air mixer 7-3, and NH is enabled to be carried out3The concentration is lower than the lower explosion limit, and the diluted ammonia gas is uniformly sprayed in a turning area 6-3 of the mobile reactor 6 through an ammonia spraying grid 6-15. The ammonia gas and the hot air blown by the dilution fan 7-2 are mixed by an ammonia gas/air mixer 7-3 to form air/H2O steam/NH3Gas mixture, air/H2O steam/NH3The gas mixture is fed via a feed line into the turn-around zone 6-3 of the moving bed reactor 6.
With air/H entering the turn-around zone 6-3 of the moving bed reactor 62O steam/NH3The horizontal gas inflow of the sintering waste gas mixed with the gas mixture into the moving bed reactor 6/bulk material discharge upper plate 6-4 and upward into the bulk material upper layer (i.e., adsorbent upper layer) 6-5 for denitrification. In the upper layer 6-5 of the sorbent, the sintering exhaust gas contains essentially only NOx, dioxins/furans or any other pollutants such as PCB and/or PAK, which are combined with fresh or regenerated sorbent from the storage hopper 6-6. The NOx and NH3 are substantially converted to water vapor and nitrogen by the catalytic action of an adsorbent, such as activated coke, and finally, the purified exhaust gas is discharged from above the upper layer of the moving bed reactor 6Finally, the waste gas is led out through a pipeline 8 and then can be directly sent into a waste gas chimney and discharged into the atmosphere.
Referring to fig. 2, the active coke is replenished from the upper end of the moving bed reactor 6 into the storage hopper 6-6 located above, after which the active coke reaches the bulk material upper layer (i.e., active coke upper layer) 6-5 through the bulk material distribution pipe 6-7 arranged in a matrix form 6-8. The above-mentioned active coke is completed without a blocking unit or without shutting down the equipment during the movement, so that the filling can be completed by the pure gravity of itself, and the filling is automatically completed when the upper surface 6-5-1 of the upper layer 6-5 of active coke reaches the discharge end of the bulk material distribution pipe 6-8. Between the bulk material distribution pipes 6-8, gas discharge spaces are formed in a manner known per se. At the lower end of the adsorbent upper layer (i.e., active coke upper layer) 6-5, there are provided a horizontal gas inflow and bulk material discharge upper plate 6-4 of the same structure as in WO 88/08746a 1. The bulk material (i.e., activated coke) moves downward by the horizontal gas inflow and bulk material discharge upper plate 6-4, and the sintering offgas flows upward by the horizontal gas inflow and bulk material discharge upper plate 6-4. The bulk material discharge pipe 6-9 arranged in a matrix form passes through the intermediate plate 6-10 and discharges the bulk material such as active coke to the upper surface 6-2-1 of the lower layer of bulk material (i.e., active coke lower layer) 6-2 therebelow, where a blocking unit for the active coke is not provided and the apparatus is not closed. At the lower end of the lower active coke layer 6-2 there is a horizontal gas inflow and bulk material discharge lower plate 6-1. The bulk material discharge pipes 6-11 arranged in a matrix form under the horizontal gas inflow and bulk material discharge lower plate 6-1 pass through the intermediate plate 6-12, and below the intermediate plate 6-12 there is provided a discharger 6-13 comprising a bulk material discharge unit, which is known from WO 90/14156a 1. The loaded active coke is discharged from the bulk material discharge pipe 6-11 passing through the intermediate plate 6-12 to the discharger 6-13, the discharge hopper 6-14, and finally discharged out of the moving bed reactor 6 in this order.
The spent active coke is fed to a screening device 9 where the screened out fine material (undersized material) can be re-fed to the sintering belt for fuel combustion, while the screened out coarse material is piped to a regeneration unit 10 (fig. 3). Referring to fig. 3, the regeneration unit 10 includes, from top to bottom, a stock section 10-4, an upper degassing section 10-1, a middle and rear degassing section 10-2, and a cooling section 10-3. The loaded activated coke passes from top to bottom through the regeneration unit 10, is heated to about 450 ℃ in the upper degassing stage 10-1, is held at a temperature of about 450 ℃ for about 1-2 hours in the middle and rear degassing stage 10-2, and the SO-enriched 2-enriched gas removed from the aggregate is sent via a line to a treatment unit, such as a sulfuric acid production unit 12 (fig. 1). From the regeneration unit 10, the regenerated adsorbent, such as activated coke, may also be returned to the moving bed reactor 6 via a line. The specific operation of the unique regeneration unit 10 of the present invention is as follows:
the spent activated coke from the moving bed reactor 6 passes through a screening device 9 and a pipeline to a storage section 10-4 located in the upper part of the regeneration unit 10. The upper degassing section 10-1 below the storage section 10-4 may be a tubular desorber into which the active coke enters from the storage section 10-4 and moves downwardly through the vertical tubes of the tubular desorber while these vertical tubes are heated by hot combustion air at about 450 ℃ outside thereof. Thereafter, the active coke enters the middle and rear degassing stage 10-2 having an enlarged cross section and stays at about 450 ℃ for about 1 to 2 hours in the middle and rear degassing stage 10-2, and then the active coke is indirectly cooled by passing through the lower end of the middle and rear degassing stage 10-2 to the cooling stage 10-3, which may be a tubular reactor in which room-temperature air as a cooling gas in the cooling stage 10-3 is used outside the vertical tubes in the tubular reactor. At the lower end of the regeneration section 10-3, the active coke enters a lower discharge hopper 10-5 through the lower end of the cooling tubes.
Specifically, in the regeneration unit 10 of the present embodiment, the hot combustion air at 450 ℃ in the upper degassing section 10-1 is provided by heating air and gas by the heater 10-6, the air and gas enter the heater 10-6 in the flowing direction shown in fig. 3 to form hot combustion air, and then are sent to the lower end of the upper degassing section 10-1, the hot combustion air flows from the lower end to the upper end of the upper degassing section 10-1, the hot combustion air in the upper degassing section 10-1 heats the active coke in the upper degassing section 10-1, and then the hot combustion air flows out from the upper end of the upper degassing section 10-1 and flows into the heater 10-6 again, so as to realize the cyclic heating utilization of the hot combustion air; the lower end of the cooling section 10-3 passes through a fan10-7 introduces 20 degrees of compressed air, and the 20 degrees of air is delivered to the upper end of the cooling section 10-3 without contacting with the active coke, and the active coke in the cooling section 10-3 is cooled while the compressed air flows from the lower end to the upper end of the cooling section 10-3, and then the air delivered to the upper end of the cooling section 10-3 is guided to NH through a pipeline 11 (in FIG. 1)3A supply unit;
contaminants that arrive at the upper degassing section 10-1 with the loaded activated coke are desorbed under the heat of the hot combustion air and leave the regeneration unit 10 in the mid-rear degassing section 10-2 via line 10-8 and via storage hopper 10-4 and line 10-9 as SO-rich 2 gas, the suction blower 13 generates the required reduced pressure and further passes the SO-rich 2 gas to the sulfuric acid production plant 12 (prior art) for further processing. The rising stripping gas via line 10-9 facilitates heat transfer to the active coke in the externally heated stripper tube in the mid-rear degassing section 10-2. Alternatively, a nitrogen-containing purge gas may be delivered to the storage section 10-4, after which the purge gas is directed through the vertical tubes of the desorber into the middle and rear degassing section 10-2 and finally to the sulfuric acid production plant 12 via line 10-8.
In actual production, two moving bed reactors 6 can also be used in a superposed manner.
In the present invention, the features in the drawings can be applied singly or in combination with each other, all within the scope of a single embodiment and various examples of the present invention.

Claims (16)

1. A method of treating solid combustion exhaust gas comprising,
removing at least a major amount of SOXAnd possibly other contaminant steps: passing flue gas into a moving bed reactor from below, horizontal gas inflow through said moving bed reactor and bulk material discharge from the lower plate, into a lower adsorbent layer, wherein the pore system of the adsorbent in said lower adsorbent layer is responsible for at least a major amount of SO in said flue gasXAdsorbing the purified gas with possible other pollutants to obtain primary purified gas;
preliminary removal of NOXThe method comprises the following steps: the primary purge gas exiting from the upper surface of the lower adsorbent layerSaid lower layer, in turn, being used for the conversion of NOXContaining NH of3The mixture is fully mixed to obtain mixed gas;
removal of NOXAnd/or other reaction product steps: the gas mixture enters from below, flows through the moving bed reactor horizontal gas inflow and bulk material discharge upper plate, enters the adsorbent upper layer, wherein at least the major amount of NOXAnd/or other reaction products are adsorbed on the surface of the adsorbent in the upper layer of the adsorbent to obtain secondary purified gas;
the repurified gas exits the upper adsorbent layer from an upper surface thereof and then exits the moving bed reactor.
2. The method for treating solid combustion exhaust gas of claim 1, further comprising the steps of adding and controlling an adsorbent:
adding an adsorbent: an adsorbent is supplied to the upper surface of the upper layer of the adsorbent from above through a bulk material distribution plate at the upper end of the moving bed reactor, and then passed through the upper and lower layers of the moving bed reactor from above downward, whereby the adsorbent is first loaded with NO on the surface thereofXOr N2 and water vapor, and secondly, loading SO in the pore system of the adsorbentXAnd possibly other contaminants, then through the horizontal gas inflow of the moving bed reactor and bulk material discharge lower plate;
controlling the adsorbent: the transfer, discharge, and moving speed of the adsorbent, and the SO pair of the adsorbent in the upper layer of the moving bed reactorXAnd possibly the loading of other pollutants, is controlled by a bulk material discharge unit, which controls the gas flow and bulk material discharge lower plate underneath or on top of it.
3. The method of treating solid combustion exhaust gas of claim 2,
the adsorbent is on the upper layer of the moving bed reactor to SOXAnd possibly other contaminants, is limited to within 10 weight percent of the weight of the adsorbent discharged on the bulk material discharge unit.
4. The method of treating solid combustion exhaust gas of claim 1,
said NH group3The mixture being air/H2O steam/NH3A gas mixture.
5. The method of treating solid combustion exhaust gas of claim 4,
the air/H2O steam/NH3The preparation method of the gas mixture comprises the following steps:
firstly, ammonia water is evaporated by an ammonia water evaporator to form ammonia gas; secondly, mixing the ammonia gas and the hot air blown by the dilution fan through an ammonia gas/air mixer to obtain air/H2O steam/NH3A gas mixture.
6. A method for treating solid combustion exhaust gases, characterized in that it is used for obtaining convertible NOXContaining NH of the gas mixture3The mixture being air/H2O steam/NH3A gas mixture.
7. The method of treating solid combustion exhaust gas of claim 6,
the air/H2O steam/NH3The preparation method of the gas mixture comprises the following steps:
firstly, ammonia water is evaporated by an ammonia water evaporator to form ammonia gas; secondly, mixing the ammonia gas and the hot air blown by the dilution fan through an ammonia gas/air mixer to obtain air/H2O steam/NH3A gas mixture.
8. A method of treating solid combustion exhaust gas comprising the adsorbent regeneration step of:
loading from the moving bed reactorCarrying SO2Is introduced into the regeneration unit from above,
in the regeneration unit, the adsorbent first passes through a heated upper degassing section, then from above through a middle and rear degassing section to suck out the desorbed pollutant gas, and finally from above through a cooled cooling section.
9. The method of treating a solid combustion exhaust gas of claim 1, further comprising the adsorbent regeneration step of:
loading SO from the moving bed reactor2Is introduced into the regeneration unit from above,
in the regeneration unit, the adsorbent first passes through a heated upper degassing section, then from above through a middle and rear degassing section to suck out the desorbed pollutant gas, and finally from above through a cooled cooling section.
10. The method of treating solid combustion exhaust gas according to claim 8 or 9,
the upper degassing section is a tubular desorber.
11. An apparatus for treating solid combustion exhaust gas, comprising
For removing SO in solid combustion waste gasX、NOXAnd possibly other contaminants, in a moving bed reactor,
a NH3 supply unit for supplying a mixture comprising NH3 to the moving bed reactor and
a regeneration unit for regenerating the adsorbent which is discharged from the moving bed reactor and adsorbs the exhaust gas pollutants;
after flowing out of the cooling section of the regeneration unit, the air for cooling the adsorbent in the regeneration unit may be passed to a dilution fan in the NH3 supply unit.
12. An apparatus for treating solid combustion exhaust gas, comprising a supply unit of NH3, wherein the supply unit of NH3 comprises
An ammonia water evaporator for evaporating ammonia water into ammonia gas,
a dilution fan for blowing in the hot air,
an ammonia/air mixer for mixing ammonia and hot air,
the ammonia gas formed by the ammonia water evaporator and the hot air flowing out of the dilution fan flow into the ammonia gas/air mixer, and are mixed in the ammonia gas/air mixer to form NH-containing gas3And (3) mixing.
13. The apparatus for treating solid combustion exhaust gas of claim 11, wherein the NH3 supply unit includes
An ammonia water evaporator for evaporating ammonia water into ammonia gas,
a dilution fan for blowing in the hot air,
an ammonia/air mixer for mixing ammonia and hot air,
the ammonia gas formed by the ammonia water evaporator and the hot air flowing out of the dilution fan flow into the ammonia gas/air mixer, and are mixed in the ammonia gas/air mixer to form NH-containing gas3And (3) mixing.
14. A device for treating solid combustion exhaust gas, comprising a regeneration unit for an adsorbent, characterized in that,
the regeneration unit comprises an upper degassing section, a middle rear degassing section, a cooling section and a hot combustion air circulation heating assembly;
the upper end of the middle rear degassing section is connected with the lower end of the upper degassing section, and the lower end of the middle rear degassing section is connected with the upper end of the cooling section;
the hot combustion air circulation heating assembly includes a heater through which air and gas enter the lower end of the upper degassing section after forming hot combustion air, after which the hot combustion air flows upward from the lower end of the upper degassing section, then flows out from the upper end of the upper degassing section, and finally, the hot combustion air flowing out from the upper end of the upper degassing section flows into the heater again.
15. The apparatus for treating solid combustion exhaust gas of claim 11, further comprising a regeneration unit for the sorbent,
the regeneration unit comprises an upper degassing section, a middle rear degassing section, a cooling section and a hot combustion air circulation heating assembly;
the upper end of the middle rear degassing section is connected with the lower end of the upper degassing section, and the lower end of the middle rear degassing section is connected with the upper end of the cooling section;
the hot combustion air circulation heating assembly includes a heater through which air and gas enter the lower end of the upper degassing section after forming hot combustion air, after which the hot combustion air flows upward from the lower end of the upper degassing section, then flows out from the upper end of the upper degassing section, and finally, the hot combustion air flowing out from the upper end of the upper degassing section flows into the heater again.
16. The apparatus for treating solid combustion exhaust gas of claim 14 or 15,
the upper degassing section is a tubular desorber.
CN201811011850.6A 2018-08-14 2018-08-31 Method and device for treating solid combustion waste gas Pending CN110813050A (en)

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023020694A1 (en) * 2021-08-19 2023-02-23 Horst Grochowski Method for cleaning industrial exhaust gases containing at least sox and nox, and exhaust-gas cleaning device for carrying out said method

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2023020694A1 (en) * 2021-08-19 2023-02-23 Horst Grochowski Method for cleaning industrial exhaust gases containing at least sox and nox, and exhaust-gas cleaning device for carrying out said method

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