CN111389221A - Device and process for removing sludge-doped flue gas pollutants of coal-fired boiler - Google Patents
Device and process for removing sludge-doped flue gas pollutants of coal-fired boiler Download PDFInfo
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- CN111389221A CN111389221A CN202010332060.9A CN202010332060A CN111389221A CN 111389221 A CN111389221 A CN 111389221A CN 202010332060 A CN202010332060 A CN 202010332060A CN 111389221 A CN111389221 A CN 111389221A
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- 239000003546 flue gas Substances 0.000 title claims abstract description 73
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims abstract description 71
- 239000003344 environmental pollutant Substances 0.000 title claims abstract description 42
- 231100000719 pollutant Toxicity 0.000 title claims abstract description 41
- 238000000034 method Methods 0.000 title claims abstract description 15
- 230000008569 process Effects 0.000 title claims abstract description 10
- 239000007788 liquid Substances 0.000 claims abstract description 53
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 50
- 230000003647 oxidation Effects 0.000 claims abstract description 47
- 239000003054 catalyst Substances 0.000 claims abstract description 39
- 238000010521 absorption reaction Methods 0.000 claims abstract description 25
- 239000010802 sludge Substances 0.000 claims abstract description 21
- 239000000779 smoke Substances 0.000 claims abstract description 14
- 230000004888 barrier function Effects 0.000 claims abstract description 13
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 11
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 9
- 239000001301 oxygen Substances 0.000 claims abstract description 9
- 239000007921 spray Substances 0.000 claims description 47
- 239000007789 gas Substances 0.000 claims description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 239000000243 solution Substances 0.000 claims description 23
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- 239000012153 distilled water Substances 0.000 claims description 5
- 229940099596 manganese sulfate Drugs 0.000 claims description 5
- 239000011702 manganese sulphate Substances 0.000 claims description 5
- 235000007079 manganese sulphate Nutrition 0.000 claims description 5
- SQQMAOCOWKFBNP-UHFFFAOYSA-L manganese(II) sulfate Chemical compound [Mn+2].[O-]S([O-])(=O)=O SQQMAOCOWKFBNP-UHFFFAOYSA-L 0.000 claims description 5
- 239000011259 mixed solution Substances 0.000 claims description 5
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- 229910000033 sodium borohydride Inorganic materials 0.000 claims description 5
- 239000012279 sodium borohydride Substances 0.000 claims description 5
- YTVQIZRDLKWECQ-UHFFFAOYSA-N 2-benzoylcyclohexan-1-one Chemical compound C=1C=CC=CC=1C(=O)C1CCCCC1=O YTVQIZRDLKWECQ-UHFFFAOYSA-N 0.000 claims description 4
- 238000009835 boiling Methods 0.000 claims description 4
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- 150000003254 radicals Chemical class 0.000 description 13
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 11
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- VEXZGXHMUGYJMC-UHFFFAOYSA-N Hydrochloric acid Chemical compound Cl VEXZGXHMUGYJMC-UHFFFAOYSA-N 0.000 description 9
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- 229910052753 mercury Inorganic materials 0.000 description 9
- 238000000746 purification Methods 0.000 description 7
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 description 6
- AMWRITDGCCNYAT-UHFFFAOYSA-L hydroxy(oxo)manganese;manganese Chemical compound [Mn].O[Mn]=O.O[Mn]=O AMWRITDGCCNYAT-UHFFFAOYSA-L 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- HYHCSLBZRBJJCH-UHFFFAOYSA-M sodium hydrosulfide Chemical compound [Na+].[SH-] HYHCSLBZRBJJCH-UHFFFAOYSA-M 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 239000012855 volatile organic compound Substances 0.000 description 6
- 229910000359 iron(II) sulfate Inorganic materials 0.000 description 5
- 230000001590 oxidative effect Effects 0.000 description 5
- 239000011592 zinc chloride Substances 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 4
- 235000011114 ammonium hydroxide Nutrition 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
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- 229910001385 heavy metal Inorganic materials 0.000 description 3
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- 229910052979 sodium sulfide Inorganic materials 0.000 description 3
- GRVFOGOEDUUMBP-UHFFFAOYSA-N sodium sulfide (anhydrous) Chemical compound [Na+].[Na+].[S-2] GRVFOGOEDUUMBP-UHFFFAOYSA-N 0.000 description 3
- VGVRPFIJEJYOFN-UHFFFAOYSA-N 2,3,4,6-tetrachlorophenol Chemical class OC1=C(Cl)C=C(Cl)C(Cl)=C1Cl VGVRPFIJEJYOFN-UHFFFAOYSA-N 0.000 description 2
- YLQBMQCUIZJEEH-UHFFFAOYSA-N Furan Chemical compound C=1C=COC=1 YLQBMQCUIZJEEH-UHFFFAOYSA-N 0.000 description 2
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 2
- 230000009471 action Effects 0.000 description 2
- 230000004913 activation Effects 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 150000008422 chlorobenzenes Chemical class 0.000 description 2
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- 230000001976 improved effect Effects 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 150000005181 nitrobenzenes Chemical class 0.000 description 2
- 150000003071 polychlorinated biphenyls Chemical class 0.000 description 2
- 125000005575 polycyclic aromatic hydrocarbon group Chemical group 0.000 description 2
- -1 polytetrafluoroethylene Polymers 0.000 description 2
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- 238000004088 simulation Methods 0.000 description 2
- KVGZZAHHUNAVKZ-UHFFFAOYSA-N 1,4-Dioxin Chemical compound O1C=COC=C1 KVGZZAHHUNAVKZ-UHFFFAOYSA-N 0.000 description 1
- 229910002971 CaTiO3 Inorganic materials 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 239000000809 air pollutant Substances 0.000 description 1
- 231100001243 air pollutant Toxicity 0.000 description 1
- 238000003915 air pollution Methods 0.000 description 1
- 238000000889 atomisation Methods 0.000 description 1
- 229910002113 barium titanate Inorganic materials 0.000 description 1
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- AIRPJJGSWHWBKS-UHFFFAOYSA-N hydroxymethylphosphanium;chloride Chemical compound [Cl-].OC[PH3+] AIRPJJGSWHWBKS-UHFFFAOYSA-N 0.000 description 1
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 150000002894 organic compounds Chemical class 0.000 description 1
- NFBOHOGPQUYFRF-UHFFFAOYSA-N oxanthrene Chemical class C1=CC=C2OC3=CC=CC=C3OC2=C1 NFBOHOGPQUYFRF-UHFFFAOYSA-N 0.000 description 1
- NFHFRUOZVGFOOS-UHFFFAOYSA-N palladium;triphenylphosphane Chemical compound [Pd].C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1.C1=CC=CC=C1P(C=1C=CC=CC=1)C1=CC=CC=C1 NFHFRUOZVGFOOS-UHFFFAOYSA-N 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 150000003021 phthalic acid derivatives Chemical class 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
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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
- B01D53/34—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
- B01D53/8671—Removing components of defined structure not provided for in B01D53/8603 - B01D53/8668
- B01D53/8675—Ozone
-
- 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
- B01D53/14—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 absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
-
- 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
- B01D53/14—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 absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- 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
- B01D53/32—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 electrical effects other than those provided for in group B01D61/00
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8665—Removing heavy metals or compounds thereof, e.g. mercury
-
- 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
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/8678—Removing components of undefined structure
- B01D53/8687—Organic components
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/10—Inorganic absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/80—Employing electric, magnetic, electromagnetic or wave energy, or particle radiation
- B01D2259/818—Employing electrical discharges or the generation of a plasma
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Environmental & Geological Engineering (AREA)
- Health & Medical Sciences (AREA)
- Biomedical Technology (AREA)
- Treating Waste Gases (AREA)
- Exhaust Gas Treatment By Means Of Catalyst (AREA)
Abstract
The invention relates to the field of flue gas pollutant treatment, and provides a device and a process for removing sludge flue gas pollutants mixed in a coal-fired boiler, which are characterized in that: comprises a plasma oxidation reactor and a plasma absorption processor; one end of the plasma oxidation reactor is provided with a flue gas inlet, the other end of the plasma oxidation reactor is communicated with the plasma absorption processor, and the other end of the plasma absorption processor is provided with a flue gas outlet; the plasma oxidation reactor is a dielectric barrier plasma linear cylinder type reactor; the plasma oxidation reactor is provided with an air inlet device for providing oxygen for the plasma oxidation reactor; the pulse power supply is connected with the wire barrel type reactor; and a net-loaded catalyst layer is arranged in the wire barrel type reactor. The invention realizes the catalytic removal of the smoke pollutants by combining the plasma technology with the catalyst and the adsorption liquid.
Description
Technical Field
The invention relates to the field of flue gas pollutant treatment, in particular to a device and a process for removing sludge flue gas pollutants mixed in a coal-fired boiler.
Background
Practice proves that coal-fired coupled sludge power generation is one of the most promising treatment modes in the current treatment of sludge, however, the sludge usually contains Chlorophenols (CPs), Chlorobenzenes (CBs), Nitrobenzenes (NBs), polychlorinated biphenyls (PCBs), polychlorinated dibenzodioxin/furan (PCDD/Fs), complex Volatile Organic Compounds (VOCs) such as phthalic acid esters (PEs) and Polycyclic Aromatic Hydrocarbons (PAHs) and heavy metals, and the secondary pollution problem of incineration flue gas is concerned widely. Compared with the flue gas discharged by a coal-fired power plant, the flue gas generated by blending and burning the sludge has the advantages of small flue gas amount, high HCl concentration and SO2Low concentration, high water content, high concentration of heavy metals, dioxin and benzene series, etc. Although pollutants such as fine particle smoke dust and heavy metal mercury generated by mixing and burning sludge in the coal-fired boiler can be collected and treated by air pollution control equipment such as a dust remover, for example, most of Hg generated by oxidation2+And Hg in particulate formPBut a third form of mercury, Hg0Because the low reactivity and the indissolvability of the sludge are difficult to capture compared with other two forms, the secondary pollutants generated by the co-combustion sludge can not be well removed by the traditional flue gas purification technology.
In recent years, low temperature plasma (NTP) technology has been used for air pollutant removal, particularly for removal of NOx、SO2And VOCs and the like. The NTP technology is an electrochemical process under the comprehensive actions of electrons, chemistry, catalysis and the like, and the purification principle is as follows: 1. the plasma is used for ionizing and cracking chemical bond energy of harmful gas by virtue of strong electric field energy instantaneously generated by the plasma, so that the molecular structure of the waste gas is damaged to achieve the purpose of purification; 2. activating, ionizing or cracking H in gaseous pollutants2O、O2Molecules are equi-molecularly generated to generate oxidative active species and free radicals (e.g. O, O)3OH radicals, HO2Free radical) and pollutants to CO2、H2O or other organic substances, and achieves the purpose of removing pollutants. However, this technique also has some problems: 1. the pollutant removal efficiency needs to be improved; 2. active particles react with free radicals actively, but lack selectivity, and are easy to produce incomplete oxidation products or polymers; 3. the generated ozone can not only corrode candle equipment, but also be harmful to the environment and human health when being discharged into the atmosphere.
Disclosure of Invention
In view of the above, the present invention provides a coal-fired boiler mixed-combustion sludge flue gas pollutant removal device for catalytically removing flue gas pollutants by using a plasma technology in combination with a catalyst and an adsorption solution.
The invention is realized by adopting the following mode, and the device for removing the sludge-doped flue gas pollutants of the coal-fired boiler is characterized in that: comprises a plasma oxidation reactor and a plasma absorption processor; one end of the plasma oxidation reactor is provided with a flue gas inlet, the other end of the plasma oxidation reactor is communicated with the plasma absorption processor, and the other end of the plasma absorption processor is provided with a flue gas outlet; the plasma oxidation reactor is provided with an air inlet device for providing oxygen for the plasma oxidation reactor; the plasma oxidation reactor comprises a pulse alternating-current high-voltage power supply and a dielectric barrier plasma linear barrel type reactor which are connected with each other, the plasma absorption processor comprises a pulse power supply, a linear barrel type reactor and a circulating liquid supply device, and the pulse power supply is connected with the linear barrel type reactor; and a net-loaded catalyst layer is arranged in the wire barrel type reactor.
Furthermore, a first non-conductor layer, a gap layer and a microporous plate layer are sequentially arranged on the wall of the dielectric barrier plasma linear barrel type reactor from outside to inside, and a plurality of small holes are formed in the microporous plate layer; the micro-porous plate layer is internally and symmetrically embedded with a high-voltage electrode layer and a grounding electrode layer, and the lower end of the high-voltage electrode layer is provided with a dielectric layer.
Further, the air inlet device comprises an air blower, the air blower is communicated with the gap layer through an air inlet pipe, and a valve is arranged on the air inlet pipe.
Furthermore, a second non-conductive layer and an anticorrosive layer are sequentially arranged on the wall of the linear barrel type reactor from outside to inside.
Further, the circulating liquid supply device comprises an atomizing spray head, a spray liquid storage tank and a spray liquid circulating pump; the atomizing spray heads are arranged at the top of the linear barrel type reactor at equal distances and are connected with the spray liquid storage tank through connecting pipes, and the spray liquid circulating pump is arranged on the connecting pipes; the spray liquid storage tank comprises a groove, and a filtering cover plate is arranged on the groove.
Furthermore, a guide rail for fixing the net-loaded catalyst layer is arranged on the inner side wall of the linear barrel type reactor, a fixing plate is arranged at one end of the net-loaded catalyst layer, and a bolt for fixing the net-loaded catalyst layer on the linear barrel type reactor is arranged on the fixing plate; the net-supported catalyst layer comprises a supporting net and a catalyst, and the catalyst is uniformly attached to the supporting net by adopting a sol-gel method.
Further, the aperture of the small hole is 2 mm.
Further, the sol-gel method for preparing the catalyst-supported mesh layer comprises the following steps:
step S1.1: placing the honeycomb ceramic into a 5% dilute nitric acid solution, heating and boiling for 1h, washing with distilled water for several times, drying at constant temperature of 100 ℃ for 1h, and cooling for later use;
step S1.2: the preparation method of the gold sol comprises the following steps: respectively adding a sodium borohydride solution and tetrakis (hydroxymethyl) phosphonium chloride into deionized water, then adding a freshly prepared tetrachloroauric acid solution, and stirring by a stirrer to obtain brown gold sol;
step S1.3: dissolving potassium permanganate and manganese sulfate in water according to a proportion, uniformly mixing to form a reddish brown solution, and then uniformly mixing with gold sol by stirring;
step S1.4: and (3) soaking the honeycomb ceramic obtained by the treatment in the step (S1.1) in the mixed solution obtained in the step (S1.3) for 1h, taking out, drying at the constant temperature of 80 ℃ for 3h, then putting into a muffle furnace, calcining at the temperature of 500 ℃ for 2h, and cooling for later use.
Another object of the present invention is to provide a process for removing sludge-doped flue gas pollutants in a coal-fired boiler, which is convenient for operators to remove sludge-doped flue gas pollutants in the coal-fired boiler, and is characterized in that: the method comprises the following steps:
step S2.1: starting the pulse alternating-current high-voltage power supply and the blower, and opening the valve;
step S2.2: introducing the flue gas after being treated by an air preheater, an economizer and a dust remover into the dielectric barrier plasma linear barrel type reactor from the flue gas inlet, and carrying out oxidation treatment on the flue gas through high-voltage discharge to obtain primarily purified gas and gas oxidation byproducts;
step S2.3: starting the pulse power supply and the spraying liquid circulating pump;
step S2.4: introducing the primarily purified gas and the gas oxidation by-products obtained in the step S2.2 into the plasma absorption processor, and further purifying the flue gas through the reaction between the primarily purified gas and the net-loaded catalyst layer and the spray liquid; the evolved smoke is discharged from the smoke outlet; meanwhile, the dust contained in the flue gas and the reaction products which are soluble in water are combined with water and fall into a liquid storage tank at the bottom of the device for collection and treatment after circulating spraying liquid.
The invention has the beneficial effects that:
(1) in the invention, H in the smoke pollutants can be caused by pulse alternating-current high-voltage discharge2O、O2Equimolecular activation, ionization or cleavage to produce O3、·OH、·O、·HO2Isooxidative active particles and free radicals, in which OH radicals formed are capable of reacting with SO2Reaction to HSO3、H2SO4NO in flue gasxOxidizing into nitric acid to remove Hg in flue gas0Oxidation to Hg2+And the subsequent capture and salt-forming absorption of the mercury in the flue gas are facilitated. The molecules of harmful gas of volatile organic compound undergo directional chain reaction through active electrons with strong oxidizing property and are cracked into CO2Etc. harmless gasAnd the pollutant removal efficiency is improved.
(2) The invention pumps oxygen by the blower, increases O in the flue gas2The volume fraction of (3) increases the content of free radicals and active particles such as O and ozone generated by discharge, and the removal efficiency of pollutants can be enhanced. Meanwhile, after the microporous plate layer structure on the inner wall of the plasma oxidation reactor is subjected to air inlet, an air film is formed on the surface of the microporous plate layer structure, so that solid powder can be prevented from being adhered to the microporous plate layer structure, and the effects of dust prevention, corrosion prevention and self-cleaning can be achieved on the surface of equipment.
(3) The invention can make full use of hydrochloric acid pollutant commonly existing in flue gas, and can generate Cl free radical or Cl through discharging2Gas, promoting Hg0Oxidation to HgCl2Can remove hydrochloric acid pollutants and is helpful for increasing Hg in gas0The removal efficiency of (1).
(4) Oxidation by-products, such as HSO, produced in a dielectric barrier plasma line barrel reactor as described in the present invention3、H2SO4NH generated by electrolyzing ammonia water in the linear cylinder type reactor2Reduction of active radicals, NH, OH, etc., to harmless products, Hg2+Can be mixed with Na in the spray liquid2S or NaHS and FeSO4Or ZnCl2The solution is coprecipitated and separated out.
(5) The net-loaded catalyst layer arranged in the invention can effectively remove the byproduct ozone and simultaneously realize the high-efficiency removal of mercury and volatile organic compounds.
(6) The invention adopts dielectric barrier discharge, avoids the discharge between two electrodes of the pulse alternating-current high-voltage power supply to form arc discharge or spark discharge under high air pressure by arranging the dielectric layer, and can work in a large air pressure range; the existence of the dielectric layer can ensure that the discharge is uniformly distributed in the whole discharge space.
Drawings
FIG. 1 is a diagram of the process steps for removing the pollutants in the mixed-combustion sludge flue gas of the coal-fired boiler.
FIG. 2 is a diagram of a sol-gel process for preparing a supported catalyst layer.
Fig. 3 is a schematic structural diagram according to an embodiment of the present invention.
FIG. 4 is a schematic diagram of the structure of the catalyst layer supported on a mesh according to the present invention.
Fig. 5 is a cross-sectional view of the plasma oxidation reactor of fig. 1.
Detailed Description
The invention is further described below with reference to the accompanying drawings.
Referring to fig. 3, in an embodiment of the present invention, a device for removing pollutants from sludge mixed combustion flue gas of a coal-fired boiler includes a plasma oxidation reactor 1 and a plasma absorption processor 2; a flue gas inlet 3 is formed in one end of the plasma oxidation reactor 1, the other end of the plasma oxidation reactor 1 is communicated with the plasma absorption processor 2, and a flue gas outlet 4 is formed in the other end of the plasma absorption processor 2; the plasma oxidation reactor 1 is provided with an air inlet device 5 for providing oxygen for the plasma oxidation reactor 1; the plasma oxidation reactor 1 comprises a pulse alternating-current high-voltage power supply 6 and a dielectric barrier plasma line cylinder type reactor 7 which are connected with each other, wherein the pulse alternating-current high-voltage power supply 6 provides electricity for the reaction of the flue gas in the plasma oxidation reactor 1; the plasma absorption processor 2 comprises a pulse power supply 8, a wire barrel type reactor 9 and a circulating liquid supply device 10, wherein the pulse power supply 8 is connected with the wire barrel type reactor 9, and the pulse power supply 8 is used for supplying power to the plasma absorption processor 2 and supplying power required by reaction; the inside of the bobbin type reactor 9 is provided with a net-supported catalyst layer 11. When the device is used, the flue gas after being treated by the air preheater, the economizer and the dust remover is introduced into the plasma oxidation reactor 1 from the flue gas inlet 3 to carry out high-voltage discharge through the pulse alternating-current high-voltage power supply 6 so as to oxidize molecules contained in flue gas pollutants, and gas oxidation byproducts after primary purification are obtained. The gas and the gas oxidation by-products after the preliminary purification are introduced into the plasma absorption processor 2, the flue gas is further purified by fully reacting with the spray liquid provided by the circulating liquid supply device 10 and the net-loaded catalyst layer 11, and the purified flue gas is treated by the flue gasThe outlet 4 exits the device. In the plasma oxidation reactor, the reaction principle of the flue gas is as follows: h in smoke pollutants can be generated by high-voltage discharge2O、O2Equimolecular activation, ionization or cleavage to produce O3、·OH、·O、·HO2Isooxidative active particles and free radicals, in which OH radicals formed are capable of reacting with SO2Reaction to HSO3、H2SO4The active particles with strong oxidizing property can be used for removing NO from smokexOxidizing the Hg0 in the flue gas into Hg by nitric acid2+And the subsequent capture and salt-forming absorption of the mercury in the flue gas are facilitated. The molecules of harmful gas of volatile organic compound undergo directional chain reaction through active electrons with strong oxidizing property and are cracked into CO2And the like, harmless gas molecules. The flue gas generally contains pollutants such as hydrochloric acid and the like, and Cl radicals or Cl can be generated in the low-temperature plasma discharge process2Gas capable of promoting the oxidation of Hg0 to HgCl2This removes both the hydrochloric acid contaminant and helps to increase the Hg in the gas0The removal efficiency of (1). The flue gas is post-treated by the plasma oxidation reactor 1 to remove SO2、 Hg0And some complex organic compounds, and the flue gas after primary purification also contains HSO3、H2SO4、Hg2+And harmful substances such as nitrogen oxides and ozone. And the flue gas treated by the plasma oxidation reactor 1 enters the plasma absorption processor 2 for further removal.
Referring to fig. 5, in an embodiment of the present invention, a non-conductive layer 12, a gap layer 13 and a microporous plate layer 14 are sequentially disposed on a wall of the dielectric barrier plasma linear-cylindrical reactor 7 from outside to inside, and a plurality of pores 15 are disposed on the microporous plate layer 14; the microporous plate layer 14 is made of heat-resistant stainless steel, when the gas inlet device 5 introduces oxygen into the plasma oxidation reactor 1, the introduced oxygen can form a gas film at the microporous plate layer 14, so that solid powder can be prevented from being adhered to the microporous plate, the dustproof, anticorrosive and self-cleaning effects on the surface of equipment can be achieved, and the service life of the equipment can be effectively prolonged in severe environments such as dust, corrosive gas and the like; the microporous board layer 14 is internally symmetricalThe high-voltage electrode layer 16 and the grounding electrode layer 17 are embedded, and a dielectric layer 18 is arranged at the lower end of the high-voltage electrode layer 16. The dielectric layer 18 is made of an insulating medium with excellent discharge resistance and large relative dielectric constant, and comprises BaTiO3、TiO2、CaTiO3、A12O3Or ceramic, the greater the relative dielectric constant of the dielectric layer 18, the more oxidizing substances may be generated to promote the decomposition of organic substances. By arranging the dielectric layer 18, the discharge between the two electrodes avoids arc discharge or spark discharge under high air pressure, and the invention can work in a large air pressure range; the existence of the dielectric layer 18 can ensure that discharge is uniformly distributed in the whole discharge space; the presence of the medium prevents the electrode from directly contacting the discharge plasma, avoiding the electrode from corroding.
Referring to fig. 3, in an embodiment of the present invention, the air intake device 5 includes a blower 19, the blower 19 is communicated with the gap layer 13 through an air intake pipe 20, and a valve 21 is disposed on the air intake pipe 20. The blower 19 pumps oxygen or air into the dielectric barrier plasma linear barrel type reactor 7, so that O in the flue gas is increased2The volume fraction of (3) increases the content of free radicals and active particles such as O and ozone generated by discharge, and the removal efficiency of pollutants can be enhanced. Meanwhile, the introduced oxygen can form an air film at the microporous plate layer 14, so that solid powder can be prevented from being adhered to the microporous plate, the dustproof, anticorrosive and self-cleaning effects on the surface of equipment can be achieved, and the service life of the equipment can be effectively prolonged in severe environments such as dust, corrosive gas and the like.
In an embodiment of the present invention, a second non-conductive layer and an anti-corrosion layer are sequentially disposed on the wall of the wire-barrel reactor 9 from outside to inside, and the anti-corrosion layer is made of polytetrafluoroethylene.
Referring to fig. 3, in an embodiment of the present invention, the circulating liquid supply device 6 includes an atomizing spray header 22, a spray liquid storage tank 23, and a spray liquid circulating pump 24; the spray liquid storage tank 23 is used for collecting and storing recyclable spray liquid, so that the consumption of the spray liquid is reduced, and the cost is reduced; the spray liquid contains Na2S and FeSO4、Na2S and ZnCl2NaHS and FeSO4Or NaHS and ZnCl2Absorbent dissolved in ammonia water, Na in the spray liquid2The S or NaHS is used for removing oxidized bivalent mercury and adding FeSO4Or ZnCl2The coprecipitation of the catalyst and HgS can be enhanced by the ammonia water, and NH is generated under the action of pulsed plasma discharge of the ammonia water2And NH, OH, etc., hydroxyl radicals, which dominate in the treatment of gaseous pollutants, promote the conversion of pollutants into harmless substances for the removal of nitrogen oxides and acidic by-products generated by the plasma oxidation reactor 1. The pH value of the spray liquid is kept in the range of 6-8, and the HgS precipitate is difficult to completely remove because the HgS precipitate is in a colloidal state when the pH value of the solution is more than 10; if Na is added2When S or NaHS is excessive, HgS is produced as [ HgS ]2]2-The precipitate is easily dissolved; therefore, it should be added to FeSO4Or ZnCl2And Hg2+1 of the concentration of (A): 1 equivalent of Na2S·9H2O or NaHS. The atomizing spray headers 22 are equidistantly arranged at the top of the linear barrel type reactor 9, the atomizing spray headers 22 are connected with the spray liquid storage tank 23 through a connecting pipe 25, and the spray liquid circulating pump 24 is arranged on the connecting pipe 25; the atomization spray header 22 atomizes the spray liquid pumped by the spray liquid circulating pump 24, and the atomized spray liquid can play a role in accelerating reaction efficiency and uniformity, and strengthen the washing absorption and catalytic chemical reaction of pollutants in gas; the spray liquid storage tank 23 comprises a groove, and a filter cover plate is arranged on the groove and used for filtering solid reaction products and fine particle smoke dust. The spray liquid circulating pump 24 is started, the spray liquid in the spray liquid storage tank 23 is pumped to the atomizing spray header 22, the spray liquid is atomized by the atomizing spray header 22 to be sprayed, and the spray liquid and the flue gas entering the linear barrel type reactor 9 are subjected to convection type absorption reaction during spraying, so that the time for full contact between the flue gas and the spray liquid is provided, and the effect of full purification can be achieved.
Referring to fig. 3 to 4, in an embodiment of the present invention, a guide rail 26 for fixing the catalyst layer 11 is disposed on an inner side wall of the bobbin type reactor 9, a fixing plate 27 is disposed at one end of the catalyst layer 11, a bolt for fixing the catalyst layer 11 to the bobbin type reactor 9 is disposed on the fixing plate 27, so as to facilitate subsequent replacement of the catalyst layer 11, and the fixing plate 27 plays a role in sealing after the catalyst layer 11 is locked and fixed to the bobbin type reactor 9; the net carries catalyst layer 11 including carrying net and catalyst, the net carries is honeycomb, and honeycomb is for guaranteeing that the flue gas can pass through smoothly, has great surface area again simultaneously, increases the reaction area of catalyst, the catalyst adopts gold doping manganese oxide, can be used for removing mercury, ozone and volatile organic pollutant, the catalyst adopts the sol-gel method evenly to adhere to carry the net.
In one embodiment of the present invention, the aperture of the small hole 15 is 2 mm.
Referring to fig. 2, in an embodiment of the present invention, the sol-gel method for preparing the catalyst-supported mesh layer includes the following steps:
step S1.1: placing the honeycomb ceramic into a 5% dilute nitric acid solution, heating and boiling for 1h, washing with distilled water for several times, drying at constant temperature of 100 ℃ for 1h, and cooling for later use;
step S1.2: the preparation method of the gold sol comprises the following steps: respectively adding a sodium borohydride solution and tetrakis (hydroxymethyl) phosphonium chloride into deionized water, then adding a freshly prepared tetrachloroauric acid solution, and stirring by a stirrer to obtain brown gold sol;
step S1.3: dissolving potassium permanganate and manganese sulfate in water according to a proportion, uniformly mixing to form a reddish brown solution, and then uniformly mixing with gold sol by stirring;
step S1.4: and (3) soaking the honeycomb ceramic obtained by the treatment in the step (S1.1) in the mixed solution obtained in the step (S1.3) for 1h, taking out, drying at the constant temperature of 80 ℃ for 3h, then putting into a muffle furnace, calcining at the temperature of 500 ℃ for 2h, and cooling for later use.
Referring to fig. 1, in an embodiment of the present invention, a process for removing pollutants from sludge mixed with flue gas of a coal-fired boiler includes the following steps:
step S2.1: starting the pulse alternating-current high-voltage power supply and the blower, and opening the valve;
step S2.2: introducing the flue gas after being treated by an air preheater, an economizer and a dust remover into the dielectric barrier plasma linear barrel type reactor from the flue gas inlet, and carrying out oxidation treatment on the flue gas through high-voltage discharge to obtain primarily purified gas and gas oxidation byproducts;
step S2.3: starting the pulse power supply and the spraying liquid circulating pump;
step S2.4: introducing the primarily purified gas and the gas oxidation by-products obtained in the step S2.2 into the plasma absorption processor, and further purifying the flue gas through the reaction between the primarily purified gas and the net-loaded catalyst layer and the spray liquid; the evolved smoke is discharged from the smoke outlet; meanwhile, the dust contained in the flue gas and the reaction products which are soluble in water are combined with water and fall into a liquid storage tank at the bottom of the device for collection and treatment after circulating spraying liquid.
The present invention is further described with reference to the following examples, which should be construed as being without limitation to the scope of the invention as claimed. The stirrer used in the invention is: shanghai Biao model JB200-D powerful electric blender, but is not limited thereto.
In embodiment 1, according to an embodiment of the present invention, the preparing of the au-doped mn oxide catalyst layer includes:
(1) putting the honeycomb ceramic into a 5% dilute nitric acid solution, heating and boiling for 1h to remove organic matters possibly remaining on the surface of the ceramic; washing with distilled water for several times, drying at 100 deg.C for 1h, and cooling.
(2) The preparation method of the gold sol comprises the steps of respectively adding 3.75m L sodium borohydride solution and 1.5m L0.96 wt% tetrakis (hydroxymethyl) phosphonium chloride into deionized water with a certain volume, adding a proper amount of freshly prepared tetrachloroauric acid solution with the concentration of 25 mmol/L, and stirring by a stirrer at the rotating speed of 900r/min to obtain brown gold sol.
(3) Dissolving potassium permanganate and manganese sulfate in water according to the mass ratio of 2.5: 1, uniformly mixing to form a reddish brown solution, and then mixing and stirring with the gold sol.
(4) And (3) soaking the treated honeycomb ceramic in the mixed solution for 1h, taking out, and drying at the constant temperature of 80 ℃ for 3 h. Then putting the mixture into a muffle furnace to calcine for 2 hours at 500 ℃, and cooling the mixture for standby. And loading a layer of gold-doped manganese oxide film on the carrier once each impregnation-drying-calcination process is completed.
Spray liquor Na2The S concentration is 0.10 mol/L4 concentration is 0.10 mol/L, and the ammonia water concentration is 0.15 mol/L.
Laboratory simulation smoke nitrogen oxide 395mg/m32930mg/m of sulfur dioxide3Mercury 104. mu.g/m3(ii) a The power supply operating parameters used were: the peak voltage is 40kV, the pulse rising edge is 7.5 mus, and the frequency is 30-120 Hz.
The results show that: the denitration efficiency is about 79.85%, the desulfurization efficiency is about 95.14%, and the demercuration efficiency is about 89.24%.
In embodiment 2, in an embodiment of the present invention, the preparing of the au-doped mn oxide catalyst layer includes:
(1) the honeycomb ceramic is put into a dilute nitric acid solution with the concentration of 8% and heated and boiled for 1h to remove possible residual organic matters on the surface of the ceramic. Washing with distilled water for several times, drying at 100 deg.C for 1h, and cooling.
(2) The preparation method of the gold sol comprises the steps of respectively adding 4.15m L sodium borohydride solution and 0.92 wt% tetrakis hydroxymethyl phosphonium chloride 2m L into deionized water with a certain volume, then adding a proper amount of freshly prepared 30 mmol/L tetrachloroauric acid solution, and stirring by a stirrer at the rotating speed of 955r/min to obtain brown gold sol.
(3) Dissolving potassium permanganate and manganese sulfate in water according to the mass ratio of 2: 1.5, uniformly mixing to form a reddish brown solution, and then mixing and stirring with the gold sol.
(4) And (3) soaking the treated honeycomb ceramic in the mixed solution for 1h, taking out, and drying at the constant temperature of 80 ℃ for 3 h. Then putting the mixture into a muffle furnace to calcine for 2 hours at 500 ℃, and cooling the mixture for standby. And loading a layer of gold-doped manganese oxide film on the carrier once each impregnation-drying-calcination process is completed.
The concentration of the NaHS in the spray liquid is 0.20 mol/L2The concentration is 0.20 mol/L,the ammonia concentration was 0.10 mol/L.
Laboratory simulation smoke contains nitric oxide 468mg/m33068mg/m of sulfur dioxide3Mercury 151. mu.g/m3(ii) a The power supply operating parameters used were: the peak voltage is 60kV, the pulse rising edge is 8.5 mus, and the frequency is 50-140 Hz.
The results show that: the denitration efficiency is about 83.59%, the desulfurization efficiency is about 99.24%, and the demercuration efficiency is about 92.04%.
The above description is only a preferred embodiment of the present invention, and all equivalent changes and modifications made in accordance with the claims of the present invention should be covered by the present invention.
Claims (9)
1. The utility model provides a coal fired boiler mixes burning mud flue gas pollutant remove device which characterized in that: comprises a plasma oxidation reactor and a plasma absorption processor; one end of the plasma oxidation reactor is provided with a flue gas inlet, the other end of the plasma oxidation reactor is communicated with the plasma absorption processor, and the other end of the plasma absorption processor is provided with a flue gas outlet; the plasma oxidation reactor is provided with an air inlet device for providing oxygen for the plasma oxidation reactor; the plasma oxidation reactor comprises a pulse alternating-current high-voltage power supply and a dielectric barrier plasma linear barrel type reactor which are connected with each other, the plasma absorption processor comprises a pulse power supply, a linear barrel type reactor and a circulating liquid supply device, and the pulse power supply is connected with the linear barrel type reactor; and a net-loaded catalyst layer is arranged in the wire barrel type reactor.
2. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 1, characterized in that: the wall of the dielectric barrier plasma line drum type reactor is sequentially provided with a first non-conductor layer, a gap layer and a microporous plate layer from outside to inside, and a plurality of small holes are formed in the microporous plate layer; the micro-porous plate layer is internally and symmetrically embedded with a high-voltage electrode layer and a grounding electrode layer, and the lower end of the high-voltage electrode layer is provided with a dielectric layer.
3. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 1, characterized in that: the air inlet device comprises an air blower, the air blower is communicated with the gap layer through an air inlet pipe, and a valve is arranged on the air inlet pipe.
4. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 1, characterized in that: and a second non-conductor layer and an anticorrosive layer are sequentially arranged on the wall of the linear drum reactor from outside to inside.
5. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 1, characterized in that: the circulating liquid supply device comprises an atomizing spray head, a spray liquid storage tank and a spray liquid circulating pump; the atomizing spray heads are arranged at the top of the linear barrel type reactor at equal distances and are connected with the spray liquid storage tank through connecting pipes, and the spray liquid circulating pump is arranged on the connecting pipes; the spray liquid storage tank comprises a groove, and a filtering cover plate is arranged on the groove.
6. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 1, characterized in that: a guide rail for fixing the net-loaded catalyst layer is arranged on the inner side wall of the wire barrel type reactor, a fixing plate is arranged at one end of the net-loaded catalyst layer, and a bolt for fixing the net-loaded catalyst layer on the wire barrel type reactor is arranged on the fixing plate; the net-supported catalyst layer comprises a supporting net and a catalyst, and the catalyst is uniformly attached to the supporting net by adopting a sol-gel method.
7. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 2, characterized in that: the aperture of the small hole is 2 mm.
8. The coal-fired boiler sludge mixed combustion flue gas pollutant removal device according to claim 6, characterized in that: the preparation method of the net-supported catalyst layer by the sol-gel method comprises the following steps:
step S1.1: placing the honeycomb ceramic into a 5% dilute nitric acid solution, heating and boiling for 1h, washing with distilled water for several times, drying at constant temperature of 100 ℃ for 1h, and cooling for later use;
step S1.2: the preparation method of the gold sol comprises the following steps: respectively adding a sodium borohydride solution and tetrakis (hydroxymethyl) phosphonium chloride into deionized water, then adding a freshly prepared tetrachloroauric acid solution, and stirring by a stirrer to obtain brown gold sol;
step S1.3: dissolving potassium permanganate and manganese sulfate in water according to a proportion, uniformly mixing to form a reddish brown solution, and then uniformly mixing with gold sol by stirring;
step S1.4: and (3) soaking the honeycomb ceramic obtained by the treatment in the step (S1.1) in the mixed solution obtained in the step (S1.3) for 1h, taking out, drying at the constant temperature of 80 ℃ for 3h, then putting into a muffle furnace, calcining at the temperature of 500 ℃ for 2h, and cooling for later use.
9. The process for removing the pollutants in the sludge mixed with the coal-fired boiler flue gas, which is disclosed by the claim, is characterized in that: the method comprises the following steps:
step S2.1: starting the pulse alternating-current high-voltage power supply and the blower, and opening the valve;
step S2.2: introducing the flue gas after being treated by an air preheater, an economizer and a dust remover into the dielectric barrier plasma linear barrel type reactor from the flue gas inlet, and carrying out oxidation treatment on the flue gas through high-voltage discharge to obtain primarily purified gas and gas oxidation byproducts;
step S2.3: starting the pulse power supply and the spraying liquid circulating pump;
step S2.4: introducing the primarily purified gas and the gas oxidation by-products obtained in the step S2.2 into the plasma absorption processor, and further purifying the flue gas through the reaction between the primarily purified gas and the net-loaded catalyst layer and the spray liquid; the evolved smoke is discharged from the smoke outlet; meanwhile, the dust contained in the flue gas and the reaction products which are soluble in water are combined with water and fall into a liquid storage tank at the bottom of the device for collection and treatment after circulating spraying liquid.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112495148A (en) * | 2020-12-15 | 2021-03-16 | 西安建筑科技大学 | Experimental device for low temperature plasma and wet-type washing jointly get rid of VOCs |
| CN114874816A (en) * | 2022-04-11 | 2022-08-09 | 北京卓控科技有限公司 | Combined process for treating pyrolysis waste gas |
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| CA2888538A1 (en) * | 2015-04-21 | 2016-10-21 | Hisham Younis | A non-selective and non-catalytic flue gas treatment system and method |
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| CN212039863U (en) * | 2020-04-24 | 2020-12-01 | 福建省锅炉压力容器检验研究院 | Coal fired boiler mixes burning mud smoke pollutants desorption device |
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| CN101703875A (en) * | 2009-11-09 | 2010-05-12 | 南京师范大学 | Oxidizing method for removing gaseous elemental mercury in boiler fume |
| CA2888538A1 (en) * | 2015-04-21 | 2016-10-21 | Hisham Younis | A non-selective and non-catalytic flue gas treatment system and method |
| CN107020004A (en) * | 2017-05-25 | 2017-08-08 | 浙江富春江环保热电股份有限公司 | A kind of apparatus and method of plasmaassisted ammonia absorption coal-fired flue-gas simultaneous SO_2 and NO removal decarburization |
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| CN114874816A (en) * | 2022-04-11 | 2022-08-09 | 北京卓控科技有限公司 | Combined process for treating pyrolysis waste gas |
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