CN113444546A - Purification treatment method for coke oven crude gas and tar ammonia water mixture - Google Patents
Purification treatment method for coke oven crude gas and tar ammonia water mixture Download PDFInfo
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- CN113444546A CN113444546A CN202110854662.5A CN202110854662A CN113444546A CN 113444546 A CN113444546 A CN 113444546A CN 202110854662 A CN202110854662 A CN 202110854662A CN 113444546 A CN113444546 A CN 113444546A
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- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 title claims abstract description 85
- 235000011114 ammonium hydroxide Nutrition 0.000 title claims abstract description 85
- 239000000571 coke Substances 0.000 title claims abstract description 58
- 239000000203 mixture Substances 0.000 title claims abstract description 45
- 238000000034 method Methods 0.000 title claims abstract description 38
- 238000000746 purification Methods 0.000 title claims abstract description 24
- 239000010802 sludge Substances 0.000 claims abstract description 79
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 77
- 239000007789 gas Substances 0.000 claims abstract description 66
- 239000002351 wastewater Substances 0.000 claims abstract description 42
- 239000003034 coal gas Substances 0.000 claims abstract description 16
- 238000004065 wastewater treatment Methods 0.000 claims abstract description 14
- BFNBIHQBYMNNAN-UHFFFAOYSA-N ammonium sulfate Chemical compound N.N.OS(O)(=O)=O BFNBIHQBYMNNAN-UHFFFAOYSA-N 0.000 claims abstract description 12
- 229910052921 ammonium sulfate Inorganic materials 0.000 claims abstract description 12
- 235000011130 ammonium sulphate Nutrition 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 11
- 239000002912 waste gas Substances 0.000 claims abstract description 11
- 239000012535 impurity Substances 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims abstract description 5
- 239000002699 waste material Substances 0.000 claims abstract description 5
- 239000012716 precipitator Substances 0.000 claims abstract description 4
- 238000007599 discharging Methods 0.000 claims abstract description 3
- 239000011269 tar Substances 0.000 claims description 92
- 238000004062 sedimentation Methods 0.000 claims description 34
- 239000011273 tar residue Substances 0.000 claims description 31
- 239000003245 coal Substances 0.000 claims description 24
- 239000010865 sewage Substances 0.000 claims description 24
- 239000000463 material Substances 0.000 claims description 21
- 238000004939 coking Methods 0.000 claims description 15
- 239000012528 membrane Substances 0.000 claims description 15
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims description 14
- 238000000926 separation method Methods 0.000 claims description 13
- CDBYLPFSWZWCQE-UHFFFAOYSA-L Sodium Carbonate Chemical compound [Na+].[Na+].[O-]C([O-])=O CDBYLPFSWZWCQE-UHFFFAOYSA-L 0.000 claims description 12
- 230000005484 gravity Effects 0.000 claims description 12
- 244000005700 microbiome Species 0.000 claims description 12
- 239000003921 oil Substances 0.000 claims description 12
- JMANVNJQNLATNU-UHFFFAOYSA-N oxalonitrile Chemical compound N#CC#N JMANVNJQNLATNU-UHFFFAOYSA-N 0.000 claims description 12
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 11
- 239000001301 oxygen Substances 0.000 claims description 11
- 229910052760 oxygen Inorganic materials 0.000 claims description 11
- 239000000126 substance Substances 0.000 claims description 11
- 238000005188 flotation Methods 0.000 claims description 9
- 239000007787 solid Substances 0.000 claims description 9
- 229910021529 ammonia Inorganic materials 0.000 claims description 7
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 claims description 6
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 claims description 6
- 230000015556 catabolic process Effects 0.000 claims description 6
- 238000006731 degradation reaction Methods 0.000 claims description 6
- 230000018044 dehydration Effects 0.000 claims description 6
- 238000006297 dehydration reaction Methods 0.000 claims description 6
- 238000002156 mixing Methods 0.000 claims description 6
- 238000011268 retreatment Methods 0.000 claims description 6
- 239000002893 slag Substances 0.000 claims description 6
- 235000017550 sodium carbonate Nutrition 0.000 claims description 6
- 229910000029 sodium carbonate Inorganic materials 0.000 claims description 6
- 229910002651 NO3 Inorganic materials 0.000 claims description 5
- 238000001914 filtration Methods 0.000 claims description 5
- 238000011001 backwashing Methods 0.000 claims description 4
- 230000000694 effects Effects 0.000 claims description 4
- 238000001704 evaporation Methods 0.000 claims description 4
- 230000008020 evaporation Effects 0.000 claims description 4
- KSSNXJHPEFVKHY-UHFFFAOYSA-N phenol;hydrate Chemical compound O.OC1=CC=CC=C1 KSSNXJHPEFVKHY-UHFFFAOYSA-N 0.000 claims description 4
- 238000004064 recycling Methods 0.000 claims description 4
- 239000004484 Briquette Substances 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 3
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 claims description 3
- 238000005276 aerator Methods 0.000 claims description 3
- 230000003851 biochemical process Effects 0.000 claims description 3
- 229910052799 carbon Inorganic materials 0.000 claims description 3
- 239000000919 ceramic Substances 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 238000005352 clarification Methods 0.000 claims description 3
- 239000000701 coagulant Substances 0.000 claims description 3
- 238000007255 decyanation reaction Methods 0.000 claims description 3
- 238000010790 dilution Methods 0.000 claims description 3
- 239000012895 dilution Substances 0.000 claims description 3
- 238000009826 distribution Methods 0.000 claims description 3
- 239000003814 drug Substances 0.000 claims description 3
- 235000003891 ferrous sulphate Nutrition 0.000 claims description 3
- 239000011790 ferrous sulphate Substances 0.000 claims description 3
- 239000000945 filler Substances 0.000 claims description 3
- 238000005189 flocculation Methods 0.000 claims description 3
- 230000016615 flocculation Effects 0.000 claims description 3
- 239000000295 fuel oil Substances 0.000 claims description 3
- 230000002706 hydrostatic effect Effects 0.000 claims description 3
- BAUYGSIQEAFULO-UHFFFAOYSA-L iron(2+) sulfate (anhydrous) Chemical compound [Fe+2].[O-]S([O-])(=O)=O BAUYGSIQEAFULO-UHFFFAOYSA-L 0.000 claims description 3
- 229910000359 iron(II) sulfate Inorganic materials 0.000 claims description 3
- 238000010525 oxidative degradation reaction Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims description 3
- 238000010791 quenching Methods 0.000 claims description 3
- 230000000171 quenching effect Effects 0.000 claims description 3
- 238000010992 reflux Methods 0.000 claims description 3
- 238000005245 sintering Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000005507 spraying Methods 0.000 claims description 3
- 238000009628 steelmaking Methods 0.000 claims description 3
- 239000006228 supernatant Substances 0.000 claims description 3
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims description 2
- 238000010521 absorption reaction Methods 0.000 claims description 2
- 238000005273 aeration Methods 0.000 claims description 2
- 239000003513 alkali Substances 0.000 claims description 2
- 238000006477 desulfuration reaction Methods 0.000 claims description 2
- 230000023556 desulfurization Effects 0.000 claims description 2
- 239000011259 mixed solution Substances 0.000 claims description 2
- 238000006396 nitration reaction Methods 0.000 claims description 2
- 230000003647 oxidation Effects 0.000 claims description 2
- 238000007254 oxidation reaction Methods 0.000 claims description 2
- 239000011574 phosphorus Substances 0.000 claims description 2
- 229910052698 phosphorus Inorganic materials 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000003756 stirring Methods 0.000 claims description 2
- 239000008400 supply water Substances 0.000 claims description 2
- 238000005406 washing Methods 0.000 claims description 2
- 239000002918 waste heat Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 125000004122 cyclic group Chemical group 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 2
- 241000894006 Bacteria Species 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 239000000306 component Substances 0.000 description 1
- 239000002131 composite material Substances 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000003203 everyday effect Effects 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000004519 manufacturing process Methods 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
- 239000011148 porous material Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000001488 sodium phosphate Substances 0.000 description 1
- 229910000162 sodium phosphate Inorganic materials 0.000 description 1
- RYFMWSXOAZQYPI-UHFFFAOYSA-K trisodium phosphate Chemical compound [Na+].[Na+].[Na+].[O-]P([O-])([O-])=O RYFMWSXOAZQYPI-UHFFFAOYSA-K 0.000 description 1
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Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/12—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors
- C10K1/121—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids alkaline-reacting including the revival of the used wash liquors containing NH3 only (possibly in combination with NH4 salts)
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F11/00—Treatment of sludge; Devices therefor
- C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
- C02F11/14—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents
- C02F11/147—Treatment of sludge; Devices therefor by de-watering, drying or thickening with addition of chemical agents using organic substances
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/18—Nature of the water, waste water, sewage or sludge to be treated from the purification of gaseous effluents
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/14—Maintenance of water treatment installations
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Activated Sludge Processes (AREA)
Abstract
The invention discloses a purification treatment method of a mixture of coke oven crude gas and tar ammonia water, which mainly comprises the following steps: the method comprises the following steps: and S1 waste gas treatment step: separating a mixture of raw coke oven gas and tar ammonia water from a coke oven through a gas-liquid separator, discharging the raw coke oven gas from the upper part, entering a horizontal pipe primary cooler operated in parallel, and cooling the gas to 20-23 ℃ by respectively using waste hot water, circulating water and low-temperature water; the coal gas discharged from the lower part of the transverse pipe primary cooler enters an electric tar precipitator which is operated in parallel to remove tar entrained in the coal gas, and then is pressurized and conveyed to an ammonium sulfate operation area by a coal gas blower; s2 wastewater treatment step: the waste water produced in the ammonium sulfate operation area is pretreated, biochemically treated, precipitated, biologically filtered and treated with sludge. The method disclosed by the invention can completely solve the problem of purification and recovery of the mixture of the raw coke oven gas and the tar ammonia water, the purified gas has low impurity content, the wastewater can be recycled, and the method is environment-friendly and energy-saving.
Description
Technical Field
The invention relates to the field of coke oven waste gas purification, and particularly discloses a purification treatment method for a mixture of coke oven crude gas and tar ammonia water.
Background
Coal is the main fossil energy of China and also is the raw material of many important chemicals, and the coal chemical industry occupies an important position in the fields of energy and chemical industry. The coal chemical industry can produce a large amount of harmful waste, such as coal tar residues produced in the coking and gas liquefaction processes, which are formed by mixing high-boiling-point organic compounds generated under the high-temperature condition with coal dust and the like during coal coking or gas liquefaction. Raw gas. It is characterized by that several kinds of bituminous coals are made into the coking coal, and after the coking coal is undergone the process of high-temp. dry distillation in the coking furnace, at the same time of producing coke and tar product a combustible gas is produced, and is a by-product of coking industry. The coke oven gas is a mixture, the yield and the composition of the coke oven gas are different due to different coking coal quality and coking process conditions, and the coke oven gas can be produced to be 300-350 m per ton of dry coal generally3(standard state). The hydrogen-methane composite material mainly comprises 55-60% of hydrogen and 23-27% of methane, and also comprises a small amount of carbon monoxide (5-8%), unsaturated hydrocarbon (2-4%) above C2, carbon dioxide (1.5-3%), oxygen (0.3-0.8%), and nitrogen (3-7%). Wherein hydrogen, methane, carbon monoxide and unsaturated hydrocarbon above C2 are combustible components, and carbon dioxide, nitrogen and oxygen are non-combustible components. With the development of coal chemical industry and the expansion of production capacity, the amount of coal tar residue is also increasing. In the coal gas purification process, a tar residue separator is usually adopted to primarily separate tar ammonia water from tar residue, and the separated tar residue is sent to a coal yard for coal blending. However, the tar residue contains a large amount of oil and water, which is not beneficial to coal blending and needs to be dehydrated and deoiled again; and the tar residue contains a plurality of small residues, which can not be separated from the large residues with high efficiency, thus increasing the energy consumption of the subsequent secondary deoiling treatment.
At present, a complete set of purification, recovery and reutilization process of the mixture of the raw coke oven gas and the tar ammonia water is lacked, and the problem is urgently needed to be solved.
Disclosure of Invention
Aiming at the situation, the invention discloses a purification treatment method of a mixture of coke oven raw gas and tar ammonia water, which can completely solve the problem of purification and recovery of the mixture of coke oven raw gas and tar ammonia water, and has the advantages of low impurity content of purified gas, cyclic utilization of waste water, environmental protection and energy saving.
The technical scheme of the invention is as follows:
a purification treatment method for a mixture of coke oven crude gas and tar ammonia water comprises the following steps:
and S1 waste gas treatment step: separating a mixture of raw coke oven gas and tar ammonia water from a coke oven through a gas-liquid separator, discharging the raw coke oven gas from the upper part, entering a horizontal pipe primary cooler operated in parallel, and cooling the gas to 20-23 ℃ by respectively using waste hot water, circulating water and low-temperature water; the coal gas discharged from the lower part of the transverse pipe primary cooler enters an electric tar precipitator which is operated in parallel to remove tar entrained in the coal gas, and then is pressurized and conveyed to an ammonium sulfate operation area by a coal gas blower;
s2 wastewater treatment step: the waste water produced in the ammonium sulfate operation area is pretreated, biochemically treated, precipitated, biologically filtered and treated with sludge.
Further, in the purification treatment method of the mixture of the raw coke oven gas and the tar ammonia water, the top of the horizontal pipe primary cooler in the step of treating the waste gas of S1 is irregularly washed by hot ammonia water to remove tar and naphthalene impurities on the pipe wall; the hot ammonia water after washing is sent to a desulfurization operation area for recycling through a transverse pipe primary cooler by a waste heat water pump.
Further, in the purification treatment method of the mixture of the raw coke oven gas and the tar ammonia water, the cross-tube primary cooler in the step of treating the waste gas of S1 is provided with a tower breaking disc, and the primary cooler is divided into an upper section and a lower section; the condensate discharged from the upper section flows into the condensate tank at the upper section through the water seal tank, a part of the condensate is sent to the upper section of the transverse pipe primary cooler by using a condensate pump at the upper section for spraying, and the rest is sent to the tar residue pre-separator; the condensate discharged from the lower section flows into the lower section condensate tank through the water seal tank, the condensate is pumped to the lower section of the primary cooler by the lower section condensate pump and sprayed, and the redundant part flows into the upper section condensate tank through the cross pipe.
Further, according to the purification treatment method of the coke oven crude gas and tar ammonia water mixture, in the step of processing the waste gas of S1, the tar ammonia water mixture discharged from the lower part of the gas-liquid separator firstly enters the tar residue pre-separator, and the tar ammonia water and the tar residue are separated; and settling the solid tar residues larger than 8mm to the conical bottom of the pre-separator, crushing the solid tar residues by a tar squeezing pump, and sending the crushed solid tar residues back to the upper part of the tar residue pre-separator.
Further, in the method for purifying the mixture of the raw coke oven gas and the tar ammonia water, the tar ammonia water discharged from the tar residue pre-separator enters the tar ammonia water separation tank, and the ammonia water and the tar are separated; the lower part of the tar-ammonia water separation tank is provided with a conical bottom plate, tar sinks to the bottom by utilizing the difference of temperature and specific gravity, is pumped out by a tar intermediate pump and is sent to a super centrifuge for further dehydration and slag removal; the tar after dehydration and deslagging automatically flows to a tar tank, the tar is pumped to an oil depot operation area through a tar pump, and the separated tar slag is conveyed to a coal briquette system through a forklift and is mixed into coking coal.
Further, according to the purification treatment method of the mixture of the coke oven crude gas and the tar ammonia water, the ammonia water flowing out of the upper part of the tar ammonia water separation tank flows into the circulating ammonia water intermediate tank below the conical bottom plate, and is pumped to the coke oven gas collecting pipe by the circulating ammonia water pump to circularly spray and cool the gas; and the residual ammonia water flows out from the upper part of the circulating ammonia water intermediate tank, automatically flows to the residual ammonia water intermediate tank to precipitate and separate heavy oil, is subjected to tar removal by a tar remover, automatically flows into the residual ammonia water tank, and is pumped to an ammonium sulfate operation area by a residual ammonia water pump to distill ammonia.
Further, in the purification treatment method of the mixture of the coke oven crude gas and the tar ammonia water, the pretreatment in the S2 wastewater treatment step specifically comprises the following steps:
coking wastewater and other wastewater generated in an ammonium sulfate operation area after ammonia evaporation treatment enter a mechanical clarification tank, are subjected to decyanation by adding ferrous sulfate, are sent into a gravity oil removal tank for treatment, enter a flotation system for air flotation oil removal, are transported out, and effluent of the flotation tank automatically flows into an equalizing tank.
Further, in the purification treatment method of the mixture of the coke oven crude gas and the tar ammonia water, the biochemical treatment in the S2 wastewater treatment step specifically comprises the following steps:
1) the pretreated wastewater firstly enters an anoxic water supply water absorption well, is mixed with approximately 3 times of return water in a return sedimentation tank, and is pumped to the anoxic tank through an anoxic tank water supply pump;
2) in an anoxic pond, microorganisms take organic matters in inlet water as a denitrification carbon source and energy source, take nitrate nitrogen in return water as a denitrification oxygen source, perform denitrification reaction under the action of a biological film on combined filler in the pond, reduce NO2 & lt- & gt and NO3 & lt- & gt in sewage into N2 gas, and escape from wastewater to achieve the aim of denitrification;
3) the effluent of the anoxic tank automatically flows into an aerobic tank (O1) by virtue of gravity, is fully mixed with activated sludge and dilution water which are lifted by a sludge pump and then sent back to the aerobic tank in a return sedimentation tank, phenol, cyanogen and other harmful substances in the wastewater are removed by the degradation action of microorganisms, and NH4+ in the wastewater is oxidized into NO 2-and NO 3-;
4) part of the effluent of the aerobic tank (O1) enters a return sedimentation tank, the sewage is subjected to mud-water separation in the return sedimentation tank, part of the separated water is removed by a distribution well and flows back to the anoxic tank, and the rest of the separated water flows to the aerobic tank (O2); the rest part of the effluent of the aerobic tank (O1) automatically flows into the aerobic tank (O2) by gravity, in the aerobic tank (O2), the sewage is fully mixed with the return sludge of the secondary sedimentation tank, and the phenol, the cyanogen and other harmful substances in the wastewater are further removed by the degradation of microorganisms;
5) arranging a microporous aerator to increase dissolved oxygen in the wastewater of the aerobic tank, providing oxygen for microorganisms, stirring the mixed solution, and adding soda ash and phosphorus alkali; adding sodium carbonate in sections according to the flow direction of the mixed liquid in the aerobic tank, wherein the amount of the returned sludge is 3 times of the amount of the treated water in the aerobic tank;
6) the effluent of the aerobic tank (O2) enters a secondary sedimentation tank, mud and water are separated in the secondary sedimentation tank, and the effluent automatically flows into a water supply and suction well of the biological filter; the sludge settled at the bottom of the return sedimentation tank and the secondary sedimentation tank is respectively sent back to the aerobic tank (O1) and the aerobic tank (O2) through a return sludge pump, and the rest part is used as the residual sludge generated in the biochemical process and is sent to a sludge concentration tank for further concentration treatment.
Further, in the purification treatment method of the mixture of the coke oven crude gas and the tar ammonia water, the biological filter treatment in the step of S2 wastewater treatment specifically comprises the following steps:
1) purifying: ceramic filter materials are filled in the filter tank, high-performance biological membranes grow on the surfaces of the filter materials, and aeration is carried out in the filter tank; when sewage flows through, organic matters in the sewage are quickly purified by utilizing the oxidative degradation capability of a high-concentration biological membrane brought by the high specific surface area of a filter material;
2) and (3) filtering: when sewage flows through the filter material, the filter material is in a compacted state, and suspended matters in the sewage are intercepted by utilizing the characteristic of smaller particle size of the filter material and the biological flocculation effect of the biological membrane, and the fallen biological membrane is ensured not to float out along with the water;
3) backwashing: after a certain time of operation, because of the increase of the loss of the water pressure head, the filter chamber needs to be back-flushed to release the trapped suspended matters and update the biological membrane; lifting the backwash wastewater by a water pump and then sending the wastewater back to the system for retreatment; a certain amount of suspended matters are remained in the effluent of the biological filter, so that a pressure filter is arranged behind the biological filter, a pipeline mixer is arranged on a main water inlet pipe of the filter, coagulant DM301 and PAM are added, sewage mixed with the medicament forms fine floccules, the fine floccules are intercepted by filter materials in the filter, and the effluent of the filter is delivered to sintering, steelmaking, coal yards and coke quenching users and is subjected to advanced treatment.
Further, in the purification treatment method of the mixture of the coke oven crude gas and the tar ammonia water, the sludge treatment in the S2 wastewater treatment step specifically comprises the following steps:
pumping the residual sludge discharged from the reflux sedimentation tank and the secondary sedimentation tank to a sludge concentration tank, concentrating the sludge in the concentration tank, collecting separated supernatant through a water outlet tank, and automatically flowing back to other phenol water wells for retreatment through a pipeline; the water content of the sludge after the sludge discharge operation and the concentration of the concentration tank are not more than 97 percent; the concentrated sludge is conveyed into a concentrated sludge well by virtue of hydrostatic pressure through a pipeline, a stirrer is arranged in the sludge well to prevent the sludge from hardening, the sludge is lifted by a pump and conveyed into a sludge dewatering machine for dewatering, and PAM is added on the sludge dewatering machine to improve the dewatering performance of the sludge; the dehydrated sludge cake is stored in a sludge hopper and is periodically loaded and conveyed to a coal blending system.
According to the technical scheme, the invention has the following beneficial effects:
the invention discloses a purification treatment method of a mixture of coke oven crude gas and tar ammonia water, which completely solves the problem of purification and recovery of the mixture of coke oven crude gas and tar ammonia water, and has the advantages of low impurity content of purified gas, cyclic utilization of waste water, environmental protection and energy saving.
Drawings
FIG. 1 is a schematic view of the waste gas treatment step in the present invention;
FIG. 2 is a schematic view showing the steps of wastewater treatment in the present invention.
Detailed Description
The invention will be further elucidated by means of several specific examples, which are intended to be illustrative only and not limiting.
Example 1
As shown in figures 1 and 2.
The process of purifying the mixture of crude gas and tar ammonia water from a coke oven comprises the following steps:
1 exhaust gas treatment
After the mixture of the raw gas from the coke oven and the tar ammonia water is separated by a gas-liquid separator, the raw gas flows out from the upper part and enters a horizontal pipe primary cooler which is operated in parallel, and the gas is cooled to 20-23 ℃ by respectively using waste hot water, circulating water and low-temperature water. The coal gas discharged from the lower part of the horizontal pipe primary cooler enters an electric tar precipitator which is operated in parallel to remove tar entrained in the coal gas, and then the coal gas is pumped to an ammonium sulfate operation area by a coal gas blower.
In order to ensure the cooling effect of the primary cooler, the top of the primary cooler is irregularly washed by hot ammonia water to remove impurities such as tar, naphthalene and the like on the tube wall.
The residual heat water is sent to the desulphurization operation area for recycling through the horizontal pipe primary cooler by a residual heat water pump.
The primary cooler is provided with a tower breaking disc, and is divided into an upper section and a lower section. And (3) allowing the condensate discharged from the upper section to flow into the condensate tank of the upper section through the water seal tank, conveying a part of the condensate to the upper section of the primary cooler by using a condensate pump of the upper section for spraying, and conveying the rest of the condensate to the tar residue preseparator. The condensate discharged from the lower section flows into the lower section condensate tank through the water seal tank, the condensate is pumped to the lower section of the primary cooler by the lower section condensate pump and sprayed, and the redundant part flows into the upper section condensate tank through the cross pipe.
The tar ammonia water mixture from the lower part of the gas-liquid separator enters a tar residue pre-separator firstly, and the tar ammonia water and the tar residue are separated. And settling the solid tar residues larger than 8mm to the conical bottom of the pre-separator, crushing the solid tar residues by a tar squeezing pump, and sending the crushed solid tar residues back to the upper part of the tar residue pre-separator.
And (4) the tar ammonia water from the tar residue pre-separator enters a tar ammonia water separation tank, and the ammonia water and the tar are separated. The lower part of the tar-ammonia water separation tank is provided with a conical bottom plate, tar sinks to the bottom by utilizing the difference of temperature and specific gravity, is pumped out by a tar intermediate pump and is sent to a super centrifuge for further dehydration and slag removal. The tar after dehydration and deslagging automatically flows to a tar tank, the tar is pumped to an oil depot operation area through a tar pump, and the separated tar slag is conveyed to a coal briquette system through a forklift and is mixed into coking coal.
The ammonia water flowing out of the upper part of the tar ammonia water separation tank flows into a circulating ammonia water intermediate tank below the conical bottom plate, and is pumped to a coke oven gas collecting pipe by a circulating ammonia water pump to circularly spray cooling coal gas. And the residual ammonia water flows out from the upper part of the circulating ammonia water intermediate tank, automatically flows to the residual ammonia water intermediate tank to precipitate and separate heavy oil, is subjected to tar removal by a tar remover, automatically flows into the residual ammonia water tank, and is pumped to an ammonium sulfate operation area by a residual ammonia water pump to distill ammonia.
And taking out a tar-ammonia water mixture at the interface of the tar-ammonia water separation tank, wherein the tar-ammonia water mixture contains about 30-50% of tar and automatically flows to a lower section condensation liquid tank.
2 treatment of waste water
The phenol-cyanogen wastewater treatment station comprises pretreatment, biochemical treatment, precipitation treatment, a biological filter, sludge treatment and the like. The biological treatment of the wastewater adopts an anoxic-aerobic (A-O-O) internal circulation process flow.
The coking wastewater and other wastewater after ammonia evaporation treatment enter a mechanical clarification tank, are subjected to decyanation pretreatment by adding ferrous sulfate, are sent into a gravity oil removal tank for treatment, then enter a flotation system for air flotation oil removal, and the effluent of the flotation tank automatically flows into an equalizing tank. The oil in the wastewater is removed in the pretreatment part, so that conditions are created for the next stage of biochemical treatment. The separated oil in the system is transported out. The regulating reservoir is mainly used for internal regulation of the coking wastewater treatment station, when the indexes of ammonia evaporation wastewater are unqualified due to unstable biological treatment process or system failure, the regulating reservoir stores the inflow amount, and the wastewater is treated after the system runs normally.
The pretreated wastewater firstly enters an anoxic water supply suction well, is mixed with approximately 3 times of return water in the return sedimentation tank, and is pumped to the anoxic tank through an anoxic tank water supply pump. In the anoxic pond, microorganisms take organic matters in the inlet water as a carbon source and an energy source for denitrification, take nitrate nitrogen in the return water as an oxygen source for denitrification, carry out denitrification reaction under the action of a biological film (facultative bacteria group) on the combined filler in the pond, and take NO in the sewage as2 -And NO3 -Reduction to N2The gas escapes from the waste water to achieve the aim of denitrification. The effluent of the anoxic tank automatically flows into an aerobic tank (O1) by gravity, is fully mixed with activated sludge and dilution water which are lifted by a sludge pump and then sent back to the aerobic tank by a return sedimentation tank, phenol, cyanogen and other harmful substances in the wastewater are removed by the degradation of microorganisms, and NH in the wastewater is subjected to nitration reaction4 +Oxidation to NO2 -And NO3 -. Part of the effluent of the aerobic tank (O1) enters a return sedimentation tank, the sewage is subjected to mud-water separation in the return sedimentation tank, part of the separated water is removed by a distribution well and flows back to the anoxic tank, and the rest of the separated water flows to the aerobic tank (O2); the rest part of the effluent of the aerobic tank (O1) automatically flows into the aerobic tank (O2) by gravity, in the aerobic tank (O2), the sewage is fully mixed with the return sludge of the secondary sedimentation tank, and the phenol, the cyanogen and other harmful substances in the wastewater are further removed by the degradation of microorganisms. In order to meet biochemical requirements, the micro-pore aerator is arranged to increase the dissolved oxygen in the wastewater in the aerobic tank, provide oxygen for microorganisms and feed mixed liquidStirring, and adding sodium carbonate and sodium phosphate in addition, wherein the sodium carbonate is added in sections according to the flow direction of the mixed liquid in the aerobic tank, and the amount of the return sludge is about 3 times of the amount of the treated water in the aerobic tank. The effluent of the aerobic tank (O2) enters a secondary sedimentation tank, mud and water are separated in the secondary sedimentation tank, and the effluent automatically flows into a feed water suction well of the biological filter. The sludge settled at the bottom of the return sedimentation tank and the secondary sedimentation tank is respectively sent back to the aerobic tank (O1) and the aerobic tank (O2) through a return sludge pump, and the rest part is used as the residual sludge generated in the biochemical process and is sent to a sludge concentration tank for further concentration treatment.
In order to further remove suspended matters and COD in the wastewater, the effluent of the secondary sedimentation tank is pressurized by a phenol water lift pump and then sent to a biological filter for filtration. The biological filter comprises three processes of purification, filtration and back flushing. Purifying: the filter chamber is filled with a certain amount of ceramic filter material, a high-performance biological membrane grows on the surface of the filter material, and the interior of the filter chamber is aerated. When sewage flows through, organic matters in the sewage are quickly purified by utilizing the oxidative degradation capability of a high-concentration biological membrane brought by the high specific surface area of a filter material; and (3) filtering: when sewage flows through the filter material, the filter material is in a compacted state, and suspended matters in the sewage are intercepted by utilizing the characteristic of smaller particle size of the filter material and the biological flocculation effect of the biological membrane, and the fallen biological membrane is ensured not to float out along with the water; backwashing: after a certain time of operation, the filter chamber needs to be backwashed to release the trapped suspended matters and update the biological membrane due to the increase of the loss of the water head. And the backwashing wastewater is lifted by a water pump and then is sent back to the system for retreatment. A certain amount of suspended matters are remained in the effluent of the biological filter, so that a pressure filter is arranged behind the biological filter, a pipeline mixer is arranged on a main water inlet pipe of the filter, coagulant (DM301 and PAM) is added, sewage mixed with the medicament forms fine floccules, the fine floccules are intercepted by filter materials in the filter, and the effluent of the filter is sent to users for sintering, steelmaking, coal yards, coke quenching and the like and is subjected to advanced treatment.
And residual sludge discharged from the reflux sedimentation tank and the secondary sedimentation tank is pumped to a sludge concentration tank, the sludge is concentrated in the concentration tank, and separated supernatant is collected by a water outlet tank and automatically flows back to other phenol water wells for retreatment through a pipeline. The sludge discharge operation of the concentration tank is carried out according to actual conditions, and the water content of the concentrated sludge is not more than 97%. The concentrated sludge is sent into a concentrated sludge well by hydrostatic pressure through a pipeline, and a stirrer is arranged in the sludge well to prevent the sludge from hardening. And then the sludge is lifted by a pump and sent into a sludge dewatering machine for dewatering, and PAM is added on the sludge dewatering machine to improve the dewatering performance of the sludge. The dehydrated sludge cake is stored in a sludge hopper and is periodically loaded and conveyed to a coal blending system.
Example of detection
The impurity contents of the coal gas before and after purification in example 1 were measured and shown in Table 1 below
TABLE 1 impurity content in the purified front and rear gases
(ii) temperature; the temperature of the coke oven is about 600 ℃ and 700 ℃, the temperature of the coke oven is 85 ℃ after the ammonia water is sprayed, and the coke oven is purified and then sent out at the temperature of 28-30 ℃.
The composition of the purified coke oven gas is shown in Table 2 below
Table 2 composition of the purified coke oven gas:
| CO2 | heavy hydrocarbon | O2 | CO | CH4 | H2 | N2 | Heat value |
| ％ | ％ | ％ | ％ | ％ | ％ | ％ | (KJ/m3) |
| 1.84 | 1.40 | 0.11 | 5.34 | 23.93 | 64.10 | 1.82 | 17183 |
The amount of the tar residue and the sludge is unchanged, the amount of the sludge is more than 20 tons every day, 20 days of sludge discharge are carried out in one month, and 10 days of sludge discharge are not carried out. The tar residue is 8 tons a day.
The technical scheme of the invention completely solves the problem of purifying and recycling the mixture of the raw coke oven gas and the tar ammonia water, the purified gas has low impurity content, the wastewater can be recycled, and the method is environment-friendly and energy-saving.
The above are only preferred embodiments of the present invention, and the scope of the present invention should not be limited thereby, and all the equivalent changes and modifications made by the claims and the summary of the invention should be covered by the protection scope of the present patent application.
Claims (10)
1. A purification treatment method for a mixture of coke oven crude gas and tar ammonia water is characterized by comprising the following steps:
and S1 waste gas treatment step: separating a mixture of raw coke oven gas and tar ammonia water from a coke oven through a gas-liquid separator, discharging the raw coke oven gas from the upper part, entering a horizontal pipe primary cooler operated in parallel, and cooling the gas to 20-23 ℃ by respectively using waste hot water, circulating water and low-temperature water; the coal gas discharged from the lower part of the transverse pipe primary cooler enters an electric tar precipitator which is operated in parallel to remove tar entrained in the coal gas, and then is pressurized and conveyed to an ammonium sulfate operation area by a coal gas blower;
s2 wastewater treatment step: the waste water produced in the ammonium sulfate operation area is pretreated, biochemically treated, precipitated, biologically filtered and treated with sludge.
2. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 1, wherein the top of the horizontal tube primary cooler in the step of S1 waste gas treatment is irregularly flushed with hot ammonia water to remove tar and naphthalene impurities on the tube wall; the hot ammonia water after washing is sent to a desulfurization operation area for recycling through a transverse pipe primary cooler by a waste heat water pump.
3. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 1, wherein the cross tube primary cooler in the step of S1 waste gas treatment is provided with a broken tray, dividing the primary cooler into an upper section and a lower section; the condensate discharged from the upper section flows into the condensate tank at the upper section through the water seal tank, a part of the condensate is sent to the upper section of the transverse pipe primary cooler by using a condensate pump at the upper section for spraying, and the rest is sent to the tar residue pre-separator; the condensate discharged from the lower section flows into the lower section condensate tank through the water seal tank, the condensate is pumped to the lower section of the primary cooler by the lower section condensate pump and sprayed, and the redundant part flows into the upper section condensate tank through the cross pipe.
4. The method for purifying a mixture of raw coke oven gas and tar ammonia water as claimed in claim 1, wherein the tar ammonia water mixture from the lower part of the gas-liquid separator in the step of processing the S1 waste gas first enters a tar residue pre-separator, where the tar ammonia water and tar residue are separated; and settling the solid tar residues larger than 8mm to the conical bottom of the pre-separator, crushing the solid tar residues by a tar squeezing pump, and sending the crushed solid tar residues back to the upper part of the tar residue pre-separator.
5. The method for purifying a mixture of raw coke oven gas and tar ammonia water as claimed in claim 4, wherein the tar ammonia water from the tar residue pre-separator enters a tar ammonia water separation tank, where the ammonia water and tar are separated; the lower part of the tar-ammonia water separation tank is provided with a conical bottom plate, tar sinks to the bottom by utilizing the difference of temperature and specific gravity, is pumped out by a tar intermediate pump and is sent to a super centrifuge for further dehydration and slag removal; the tar after dehydration and deslagging automatically flows to a tar tank, the tar is pumped to an oil depot operation area through a tar pump, and the separated tar slag is conveyed to a coal briquette system through a forklift and is mixed into coking coal.
6. The method for purifying the mixture of the coke oven crude gas and the tar ammonia water as claimed in claim 5, wherein the ammonia water flowing out from the upper part of the tar ammonia water separation tank flows into the circulating ammonia water intermediate tank under the conical bottom plate, and is pumped to the coke oven gas collecting pipe by the circulating ammonia water pump to circularly spray cooled gas; and the residual ammonia water flows out from the upper part of the circulating ammonia water intermediate tank, automatically flows to the residual ammonia water intermediate tank to precipitate and separate heavy oil, is subjected to tar removal by a tar remover, automatically flows into the residual ammonia water tank, and is pumped to an ammonium sulfate operation area by a residual ammonia water pump to distill ammonia.
7. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 1, wherein the pretreatment in the S2 wastewater treatment step specifically comprises the following steps:
coking wastewater and other wastewater generated in an ammonium sulfate operation area after ammonia evaporation treatment enter a mechanical clarification tank, are subjected to decyanation by adding ferrous sulfate, are sent into a gravity oil removal tank for treatment, enter a flotation system for air flotation oil removal, are transported out, and effluent of the flotation tank automatically flows into an equalizing tank.
8. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 1, wherein the biochemical treatment in the S2 wastewater treatment step specifically comprises the following steps:
1) the pretreated wastewater firstly enters an anoxic water supply water absorption well, is mixed with approximately 3 times of return water in a return sedimentation tank, and is pumped to the anoxic tank through an anoxic tank water supply pump;
2) in the anoxic pond, microorganisms take organic matters in the inlet water as a carbon source and an energy source for denitrification, take nitrate nitrogen in the return water as an oxygen source for denitrification, perform denitrification reaction under the action of a biological film on the combined filler in the pond, and enable NO in the sewage to be2 -And NO3 -Reduction to N2Gas escapes from the wastewater to achieve the aim of denitrification;
3) the effluent of the anoxic tank automatically flows into an aerobic tank (O1) by gravity, is fully mixed with activated sludge and dilution water which are lifted by a sludge pump and then sent back to the aerobic tank by a return sedimentation tank, phenol, cyanogen and other harmful substances in the wastewater are removed by the degradation of microorganisms, and NH in the wastewater is subjected to nitration reaction4 +Oxidation to NO2 -And NO3 -；
4) Part of the effluent of the aerobic tank (O1) enters a return sedimentation tank, the sewage is subjected to mud-water separation in the return sedimentation tank, part of the separated water is removed by a distribution well and flows back to the anoxic tank, and the rest of the separated water flows to the aerobic tank (O2); the rest part of the effluent of the aerobic tank (O1) automatically flows into the aerobic tank (O2) by gravity, in the aerobic tank (O2), the sewage is fully mixed with the return sludge of the secondary sedimentation tank, and the phenol, the cyanogen and other harmful substances in the wastewater are further removed by the degradation of microorganisms;
5) arranging a microporous aerator to increase dissolved oxygen in the wastewater of the aerobic tank, providing oxygen for microorganisms, stirring the mixed solution, and adding soda ash and phosphorus alkali; adding sodium carbonate in sections according to the flow direction of the mixed liquid in the aerobic tank, wherein the amount of the returned sludge is 3 times of the amount of the treated water in the aerobic tank;
6) the effluent of the aerobic tank (O2) enters a secondary sedimentation tank, mud and water are separated in the secondary sedimentation tank, and the effluent automatically flows into a water supply and suction well of the biological filter; the sludge settled at the bottom of the return sedimentation tank and the secondary sedimentation tank is respectively sent back to the aerobic tank (O1) and the aerobic tank (O2) through a return sludge pump, and the rest part is used as the residual sludge generated in the biochemical process and is sent to a sludge concentration tank for further concentration treatment.
9. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 8, wherein the biofilter treatment in the S2 wastewater treatment step specifically comprises the following steps:
1) purifying: ceramic filter materials are filled in the filter tank, high-performance biological membranes grow on the surfaces of the filter materials, and aeration is carried out in the filter tank; when sewage flows through, organic matters in the sewage are quickly purified by utilizing the oxidative degradation capability of a high-concentration biological membrane brought by the high specific surface area of a filter material;
2) and (3) filtering: when sewage flows through the filter material, the filter material is in a compacted state, and suspended matters in the sewage are intercepted by utilizing the characteristic of smaller particle size of the filter material and the biological flocculation effect of the biological membrane, and the fallen biological membrane is ensured not to float out along with the water;
3) backwashing: after a certain time of operation, because of the increase of the loss of the water pressure head, the filter chamber needs to be back-flushed to release the trapped suspended matters and update the biological membrane; lifting the backwash wastewater by a water pump and then sending the wastewater back to the system for retreatment; a certain amount of suspended matters are remained in the effluent of the biological filter, so that a pressure filter is arranged behind the biological filter, a pipeline mixer is arranged on a main water inlet pipe of the filter, coagulant DM301 and PAM are added, sewage mixed with the medicament forms fine floccules, the fine floccules are intercepted by filter materials in the filter, and the effluent of the filter is delivered to sintering, steelmaking, coal yards and coke quenching users and is subjected to advanced treatment.
10. The method for purifying a mixture of coke oven crude gas and tar ammonia water as claimed in claim 9, wherein the sludge treatment in the S2 wastewater treatment step comprises the following steps:
pumping the residual sludge discharged from the reflux sedimentation tank and the secondary sedimentation tank to a sludge concentration tank, concentrating the sludge in the concentration tank, collecting separated supernatant through a water outlet tank, and automatically flowing back to other phenol water wells for retreatment through a pipeline; the water content of the sludge after the sludge discharge operation and the concentration of the concentration tank are not more than 97 percent; the concentrated sludge is conveyed into a concentrated sludge well by virtue of hydrostatic pressure through a pipeline, a stirrer is arranged in the sludge well to prevent the sludge from hardening, the sludge is lifted by a pump and conveyed into a sludge dewatering machine for dewatering, and PAM is added on the sludge dewatering machine to improve the dewatering performance of the sludge; the dehydrated sludge cake is stored in a sludge hopper and is periodically loaded and conveyed to a coal blending system.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114395428A (en) * | 2021-12-31 | 2022-04-26 | 新兴铸管股份有限公司 | Method for reducing tar content in coke oven crude gas |
| CN114653108A (en) * | 2022-04-15 | 2022-06-24 | 山东钢铁集团日照有限公司 | Separation process of coal coking tar residues |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06136366A (en) * | 1992-10-22 | 1994-05-17 | Nippon Steel Corp | Method and apparatus for separating tar from ammonia liquor contained in waste coke-oven-gas cleaning liquid |
| CN101037602A (en) * | 2007-04-20 | 2007-09-19 | 武汉钢铁(集团)公司 | Gas transverse pipe initial cooler for coking oven |
| CN103496825A (en) * | 2013-09-27 | 2014-01-08 | 苏州国环环境检测有限公司 | Three-phase biological fluidized bed A/O/O process for treating coking wastewater |
| CN107021590A (en) * | 2017-04-24 | 2017-08-08 | 莱芜市泰山焦化有限公司 | The method for separating reduction distilled ammonia wastewater harmful components step by step based on the destructive distillation of briquette height |
| CN108503141A (en) * | 2018-04-11 | 2018-09-07 | 宝钢工程技术集团有限公司 | A kind of processing method of coking wastewater removing total nitrogen |
-
2021
- 2021-07-28 CN CN202110854662.5A patent/CN113444546A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06136366A (en) * | 1992-10-22 | 1994-05-17 | Nippon Steel Corp | Method and apparatus for separating tar from ammonia liquor contained in waste coke-oven-gas cleaning liquid |
| CN101037602A (en) * | 2007-04-20 | 2007-09-19 | 武汉钢铁(集团)公司 | Gas transverse pipe initial cooler for coking oven |
| CN103496825A (en) * | 2013-09-27 | 2014-01-08 | 苏州国环环境检测有限公司 | Three-phase biological fluidized bed A/O/O process for treating coking wastewater |
| CN107021590A (en) * | 2017-04-24 | 2017-08-08 | 莱芜市泰山焦化有限公司 | The method for separating reduction distilled ammonia wastewater harmful components step by step based on the destructive distillation of briquette height |
| CN108503141A (en) * | 2018-04-11 | 2018-09-07 | 宝钢工程技术集团有限公司 | A kind of processing method of coking wastewater removing total nitrogen |
Non-Patent Citations (4)
| Title |
|---|
| 中国炼焦行业协会: "《创新发展中的中国焦化业》", 31 January 2017, 冶金工业出版社 * |
| 吴军等: "《村镇生活污水处理技术及管理维护》", 31 July 2019, 冶金工业出版社 * |
| 浙江省安全生产协会: "《安全生产论文集》", 30 April 2019, 浙江工商大学出版社 * |
| 环境保护部环境工程评估中心: "《钢铁行业环境保护政策法规》", 28 February 2017, 中国环境出版社 * |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN114395428A (en) * | 2021-12-31 | 2022-04-26 | 新兴铸管股份有限公司 | Method for reducing tar content in coke oven crude gas |
| CN114653108A (en) * | 2022-04-15 | 2022-06-24 | 山东钢铁集团日照有限公司 | Separation process of coal coking tar residues |
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