CN118164651B - Coking strong brine evaporation crystallization processing system - Google Patents
Coking strong brine evaporation crystallization processing system Download PDFInfo
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- CN118164651B CN118164651B CN202410592135.5A CN202410592135A CN118164651B CN 118164651 B CN118164651 B CN 118164651B CN 202410592135 A CN202410592135 A CN 202410592135A CN 118164651 B CN118164651 B CN 118164651B
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- coking
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- 238000002425 crystallisation Methods 0.000 title claims abstract description 167
- 230000008025 crystallization Effects 0.000 title claims abstract description 167
- 239000012267 brine Substances 0.000 title claims abstract description 81
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 title claims abstract description 81
- 238000004939 coking Methods 0.000 title claims abstract description 67
- 238000001704 evaporation Methods 0.000 title claims abstract description 18
- 230000008020 evaporation Effects 0.000 title claims abstract description 17
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 claims abstract description 82
- 238000010791 quenching Methods 0.000 claims abstract description 52
- 230000000171 quenching effect Effects 0.000 claims abstract description 52
- 239000011780 sodium chloride Substances 0.000 claims abstract description 40
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 33
- 239000003546 flue gas Substances 0.000 claims abstract description 33
- 238000010438 heat treatment Methods 0.000 claims abstract description 33
- 238000001223 reverse osmosis Methods 0.000 claims abstract description 17
- 238000001728 nano-filtration Methods 0.000 claims abstract description 10
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 10
- 238000004062 sedimentation Methods 0.000 claims abstract description 7
- 239000007788 liquid Substances 0.000 claims description 63
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 47
- 238000001035 drying Methods 0.000 claims description 26
- 238000007599 discharging Methods 0.000 claims description 20
- 230000000694 effects Effects 0.000 claims description 17
- 150000003839 salts Chemical class 0.000 claims description 17
- 239000007789 gas Substances 0.000 claims description 16
- 238000009826 distribution Methods 0.000 claims description 14
- 238000009827 uniform distribution Methods 0.000 claims description 9
- 239000012452 mother liquor Substances 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 239000007921 spray Substances 0.000 claims description 6
- 230000001174 ascending effect Effects 0.000 claims description 5
- 230000000712 assembly Effects 0.000 claims description 2
- 238000000429 assembly Methods 0.000 claims description 2
- 238000011084 recovery Methods 0.000 claims description 2
- 238000009434 installation Methods 0.000 claims 2
- 238000009792 diffusion process Methods 0.000 claims 1
- 230000009977 dual effect Effects 0.000 abstract description 7
- 208000028659 discharge Diseases 0.000 description 9
- 239000002351 wastewater Substances 0.000 description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 239000000571 coke Substances 0.000 description 7
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 6
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 description 6
- 235000011114 ammonium hydroxide Nutrition 0.000 description 6
- KRHYYFGTRYWZRS-UHFFFAOYSA-M Fluoride anion Chemical compound [F-] KRHYYFGTRYWZRS-UHFFFAOYSA-M 0.000 description 5
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 5
- 238000005265 energy consumption Methods 0.000 description 5
- 229910052710 silicon Inorganic materials 0.000 description 5
- 239000010703 silicon Substances 0.000 description 5
- 238000004821 distillation Methods 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 229910021529 ammonia Inorganic materials 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000005855 radiation Effects 0.000 description 3
- 229910002651 NO3 Inorganic materials 0.000 description 2
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 description 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 2
- 239000003245 coal Substances 0.000 description 2
- 239000000084 colloidal system Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 230000003111 delayed effect Effects 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N phenol group Chemical group C1(=CC=CC=C1)O ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 2
- 238000003860 storage Methods 0.000 description 2
- XFXPMWWXUTWYJX-UHFFFAOYSA-N Cyanide Chemical compound N#[C-] XFXPMWWXUTWYJX-UHFFFAOYSA-N 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 229910045601 alloy Inorganic materials 0.000 description 1
- 239000000956 alloy Substances 0.000 description 1
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 230000002528 anti-freeze Effects 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005422 blasting Methods 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000000498 cooling water Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 229910052759 nickel Inorganic materials 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 238000000197 pyrolysis Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001502 supplementing effect Effects 0.000 description 1
- 239000002918 waste heat Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01D—COMPOUNDS OF ALKALI METALS, i.e. LITHIUM, SODIUM, POTASSIUM, RUBIDIUM, CAESIUM, OR FRANCIUM
- C01D3/00—Halides of sodium, potassium or alkali metals in general
- C01D3/04—Chlorides
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/16—Treatment of water, waste water, or sewage by heating by distillation or evaporation using waste heat from other processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B39/00—Cooling or quenching coke
- C10B39/02—Dry cooling outside the oven
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/441—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/442—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by nanofiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
- C02F2001/5218—Crystallization
-
- 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
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Materials Engineering (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The invention discloses a coking strong brine evaporation crystallization treatment system, which comprises a strong brine collecting tank, wherein strong brine is sequentially conveyed to a high-density sedimentation tank for concentrating strong brine, a multi-medium filter, a conveying pump, ultrafiltration, nanofiltration, a high-pressure pump and high-pressure reverse osmosis along a pipeline by a lifting pump for treatment, and a high-pressure reverse osmosis outlet is respectively conveyed to a sodium chloride dual-effect concentration system and a plurality of tubular crystallizers arranged in an annular flue gas chamber at the upper part of a coking dry quenching furnace by a strong brine pipeline for crystallization treatment; according to the invention, the concentrated brine produced by the zero-emission unit concentration section is respectively conveyed to the sodium chloride double-effect concentration system and the tubular crystallizers arranged in the annular flue gas chamber at the upper part of the coking dry quenching furnace for crystallization treatment, and the high-temperature flue gas of the coking dry quenching furnace is utilized for direct heating crystallization, so that the load of the double-effect concentration system is greatly reduced, and the high-efficiency utilization of the flue gas heat energy of the coking dry quenching furnace is realized.
Description
Technical Field
The invention relates to the field of coking strong brine treatment, in particular to a coking strong brine evaporation crystallization treatment system.
Background
The waste water produced by the coking plant mainly takes the residual ammonia water produced in the helium distillation process as a main source. The ammonia distillation wastewater is wastewater discharged after the distillation of the mixed residual ammonia water. The residual ammonia water is the most important phenolic cyanide wastewater source in the coking plant, is high-concentration phenolic water containing ammonia, is discharged by a circulating ammonia water pump in a condensing and blasting section and is sent to a residual ammonia water storage tank. The residual ammonia water mainly comprises three parts, namely wet water on the surface of the charging coal, combined water generated by dry distillation of the charging coal and oily process wastewater added into a gas suction pipeline and a gas collecting pipe circulating oxygen water pump.
The ammonia distillation wastewater is treated by a biochemical treatment unit, a zero discharge treatment unit (comprising three parts of recycling, concentration and evaporative crystallization), hardness, silicon and fluoride suspended matters in the wastewater are removed by a high-density sedimentation tank in a zero discharge recycling water treatment section, and then the biochemical treated wastewater is sent to an ultrafiltration and reverse osmosis system (recovery rate is 70%) to remove pollutants such as salt, COD, ammonia nitrogen and the like in the wastewater, and the produced water is used as circulating cooling water for supplementing water; the concentrated water is sent to concentrated brine for concentration treatment.
The concentrated water enters a concentrated water collecting tank 1 of a concentrated brine concentration treatment working section to be collected (shown in figure 9), a large amount of hardness, fluoride and silicon (the hardness of the discharged water is about 150mg/L, the fluoride is 20mg/L and the silicon is 10 mg/L) are further removed by a high-density sedimentation tank, the discharged water enters a multi-medium filter 3 to remove suspended matters, the discharged water after removing suspended matters enters an ultrafiltration system to remove colloid substances, the discharged water after ultrafiltration filtration enters nanofiltration to separate salt and nitrate, and after the nanofiltration produced water with high sodium chloride/low sulfate and low COD is concentrated and recycled by high-pressure reverse osmosis, the concentrated brine produced by high-pressure reverse osmosis enters a sodium chloride dual-effect concentration system to be crystallized and separated, but the steam amount used by the sodium chloride dual-effect concentration system is large, and the sodium chloride dual-effect concentration system consumes 0.6 to 0.7 ton of steam by evaporating one ton of water, and the steam needs to be additionally provided by a self-contained boiler, so that the energy consumption is large and the steam water resource is wasted; the sodium chloride crystals discharged from the crystallizer at the tail end of the sodium chloride two-effect concentration system also have certain moisture, and an additional dryer is needed for drying treatment in the follow-up process; the coke produced in the coke plant is required to be cooled by using a dry quenching furnace, high-temperature nitrogen generated by heat exchange and cooling can enter an annular flue gas chamber at the upper part and can not be fully utilized by heat exchange with a waste heat boiler along a flue gas pipeline, and the high-temperature flue gas generated by the dry quenching furnace has the problem of heat energy waste, so that a coking strong brine evaporation and crystallization treatment system is required to be studied to solve the problem.
Disclosure of Invention
In order to solve the problems, the invention provides a coking strong brine evaporation crystallization treatment system.
The invention is realized by the following technical scheme:
the concentrated water in the concentrated water collecting tank is sequentially conveyed to a high-concentration sedimentation tank for concentrating the concentrated brine, a multi-medium filter, a conveying pump, ultrafiltration, nanofiltration, a high-pressure pump and high-pressure reverse osmosis for treatment through a lifting pump, and a high-pressure reverse osmosis outlet is respectively conveyed to a sodium chloride two-effect concentration system and a plurality of tubular crystallizers arranged in an annular flue gas chamber at the upper part of a coking dry quenching furnace through a concentrated brine pipeline for crystallization treatment; the steam generated by heating the tubular crystallizer is conveyed to a sodium chloride two-effect concentration system through a gas collecting pipeline for heating and recycling; the crystallized salt generated by heating the tubular crystallizers is conveyed to a drying jacket arranged on the outer wall of the coking dry quenching furnace through a salt discharging assembly arranged in the tubular crystallizers for drying.
Further alternatively, the tubular crystallizer comprises a crystallization tube obliquely arranged in the annular flue gas chamber, one end of the crystallization tube is fixed with an end frame fixed on the inner wall of the annular flue gas chamber, and the other end of the crystallization tube is connected and fixed with an extension shell which is communicated with the outside of the annular flue gas chamber.
Further alternatively, the outer side of the crystallization pipe is connected with a drying jacket through a discharging pipe, a plurality of discharging pipes are arranged at the bottom of the drying jacket, a plurality of gas diffusing holes are formed at the top of the drying jacket, a control valve is arranged on the discharging pipe, and a cut-off valve is arranged at the root of the discharging pipe.
Further alternatively, the salt discharging assembly comprises a rotating shaft rotatably supported in the crystallization tube, a spiral blade is arranged on the rotating shaft, and one end of the rotating shaft is connected with a main shaft of a driving motor arranged on the outer side of the crystallization tube.
Further alternatively, the continuous liquid supply system is arranged on the upper portions of the crystallization tubes, the continuous liquid supply system comprises a liquid supply ring tube, the liquid supply ring tube is connected with a strong brine main tube of the high-pressure reverse osmosis outlet, the lower portion of the liquid supply ring tube is connected with the corresponding uniform distribution assemblies arranged on the crystallization tubes through the liquid supply tubes, and the crystallization tubes are uniformly divided into a first crystallization area and a second crystallization area which are alternately subjected to liquid supply crystallization.
Further alternatively, the uniform distribution assembly comprises a mounting cover which is arranged at the top of the crystallization tube and communicated with the crystallization tube, a distribution tube is fixed in the mounting cover, a plurality of spray heads are arranged at the lower part of the distribution tube, and the distribution tube is connected with the outlet of the liquid inlet tube.
Further alternatively, the gas collecting pipeline comprises a steam ring pipe arranged at the upper part of the coking dry quenching furnace, the bottom of the steam ring pipe is connected with the corresponding crystallization pipe through a plurality of ascending pipes, the steam ring pipe is connected with a steam inlet of the sodium chloride two-effect concentration system through a steam main pipe, and the steam main pipe is connected with an antifreezing pipe arranged in the concentrated water collecting tank through a bypass steam branch pipe.
Further alternatively, the sodium chloride two-effect concentration system comprises an effect heater connected through a strong brine branch pipe, an inlet of the strong brine branch pipe is connected with a strong brine main pipe in a bypass mode, strong brine from the strong brine branch pipe sequentially passes through the effect heater, the effect separator, a front end circulating pump, a two-effect heater, the two-effect separator, a rear end circulating pump, a crystallizer and a mother liquor tank, the tops of the effect separator and the two-effect separator heat jackets of the two-effect heater and the crystallizer respectively through steam pipes, a steam inlet of the effect heater is connected with the steam main pipe, the mother liquor tank is conveyed to the effect heater through a pressurizing pump for circulating treatment, and condensate water generated by the jackets of the effect heater, the two-effect heater and the crystallizer is recycled through pipelines.
Further optionally, the crystallization control system of the coking dry quenching furnace is further included, and the crystallization control system comprises a PLC controller, wherein the PLC controller is electrically connected with a liquid inlet valve of a liquid inlet pipe of the first crystallization zone and a liquid inlet pipe of the second crystallization zone, a driving motor, a cut-off valve, a flowmeter at the inlet end of a liquid supply ring pipe and a discharge valve on a discharge pipe.
Further alternatively, the main brine pipe, the branch brine pipe, the main steam pipe, the branch steam pipe and the pipelines are all provided with control valves.
Compared with the prior art, the invention has the beneficial effects that: according to the invention, concentrated brine produced by the zero-emission unit concentration section is respectively conveyed to a sodium chloride double-effect concentration system and a plurality of tubular crystallizers arranged in an annular flue gas chamber at the upper part of the coking dry quenching furnace for crystallization treatment, and high-temperature flue gas of the coking dry quenching furnace is utilized for direct heating crystallization, so that the load of the double-effect concentration system is greatly reduced, and the high-efficiency utilization of the flue gas heat energy of the coking dry quenching furnace is realized; the steam generated by heating and crystallizing the tubular crystallizer of the coking dry quenching furnace is transmitted to the two-effect concentration system to provide heating steam, so that the energy consumption and water resource of the two-effect concentration system are reduced; a plurality of tubular crystallizers are divided into a first crystallization area and a second crystallization area which alternately feed liquid for crystallization, a liquid supply evaporation section and a heating crystallization discharging section which pass through the first crystallization area and the second crystallization area are alternately used in a certain period by utilizing an automatic control system, so that the continuous liquid supply and crystallization discharging stability of the coking dry quenching furnace is realized, and the stable operation of the system is realized without intermittent operation in the whole process.
Drawings
FIG. 1 is a system diagram of the present invention;
FIG. 2 is a schematic perspective view of a coking dry quenching furnace according to the present invention;
FIG. 3 is a cut-away top view of the annular flue gas chamber of FIG. 2;
FIG. 4 is a front view of the coking dry quenching furnace of the present invention;
FIG. 5 is a schematic view of the structure of the crystallization tube salt removal assembly of the present invention;
FIG. 6 is a schematic diagram of the configuration of the distribution assembly of the crystallization tube of the present invention;
FIG. 7 is a schematic diagram of a crystallization control system according to the present invention;
FIG. 8 is a flow chart of the operation of the first crystallization zone and the second crystallization zone of the present invention;
FIG. 9 is a prior art schematic of the present invention;
In the figure: concentrated water collection tank 1, lift pump 101, antifreeze pipe 102, dense settling tank 2, multi-media filter 3, transfer pump 301, ultrafiltration 4, nanofiltration 5, high pressure pump 501, high pressure reverse osmosis 6, concentrated brine main pipe 61, concentrated brine branch pipe 62, sodium chloride two-effect concentration system 7, one-effect heater 71, one-effect separator 72, front-end circulation pump 73, two-effect heater 74, two-effect separator 75, rear-end circulation pump 76, crystallizer 77, mother liquor tank 78, coker dry quenching furnace 8, flue gas pipe 9, circulation fan 10, nitrogen hood 11, annular flue gas chamber 12, crystallization pipe 13, rotary shaft 131, spiral vane 132, mounting hood 133, distribution pipe 134, spray head 135, end frame 14, extension housing 15, drive motor 16, liquid feed loop 17, flow meter 171, liquid feed pipe 18, liquid feed valve 181, vapor loop 19, lift pipe 20, blanking pipe 21, drying jacket 22, discharge pipe 23, discharge valve 24, shut-off valve 25, vapor 26, vapor branch pipe 27, controller 28.
Detailed Description
The invention is described in further detail below with reference to the attached drawings and detailed description:
As shown in fig. 1, the coking strong brine evaporation crystallization treatment system comprises a strong brine collecting tank 1, wherein strong brine in the strong brine collecting tank 1 is sequentially conveyed to a high-density sedimentation tank 2, a multi-medium filter 3, a conveying pump 31, an ultrafiltration 4, a nanofiltration 5, a high-pressure pump 501 and a high-pressure reverse osmosis 6 for treatment along a pipeline through a lifting pump 101, sodium chloride water in the strong brine is separated and concentrated through the treatment of the concentration section, and a high-pressure reverse osmosis 6 outlet is respectively conveyed to a sodium chloride two-effect concentration system 7 and a plurality of tubular crystallizers arranged in an annular flue gas chamber 12 at the upper part of a coking dry quenching furnace 8 through a strong brine pipeline for crystallization treatment; the concentrated water is divided into two parts and is conveyed to the two-effect concentration system 7 and the coking dry quenching furnace 8 for heating crystallization treatment, so that the load of the two-effect concentration system 7 is greatly reduced, the running stability of the crystallization system is improved, and meanwhile, the coking dry quenching furnace 8 is heated and crystallized by utilizing the 810-890 ℃ high-temperature flue gas heat from the annular flue gas chamber 12, so that the maximum utilization and filtration of the flue gas heat of the coking dry quenching furnace 8 are realized;
The steam generated by heating the tubular crystallizer is conveyed to a sodium chloride two-effect concentration system 7 through a gas collecting pipeline for heating and recycling; the steam generated by heating and crystallizing the tubular crystallizer of the coking dry quenching furnace 8 is conveyed to the two-effect concentration system 7 to provide heating steam, so that the energy consumption and water saving resources of the two-effect concentration system 7 are reduced, the crystallized salt generated by heating the tubular crystallizers is conveyed to the drying jacket 22 arranged on the outer wall of the coking dry quenching furnace 8 through the salt discharging component arranged in the tubular crystallizer to be dried, the radiant heat of the outer wall of the coking dry quenching furnace 8 is utilized to dry the crystallized sodium chloride, an additional dryer is not required to be used for drying, the ambient temperature of the coking dry quenching furnace 8 can be reduced, and the operating environment of operators is greatly improved.
When the coking dry quenching furnace 8 works, red coke with the temperature of 920-1030 ℃ is filled in from the top of the coking dry quenching furnace 8, low-temperature inert nitrogen is led out from a nitrogen hood 11 at the bottom of the dry quenching furnace, the red coke is reversely contacted with red coke in a cooling chamber in the coking dry quenching furnace 8 to absorb red Jiao Reliang, cooled coke with the temperature of less than 200 ℃ is discharged from the bottom of the coking dry quenching furnace 8, 810-890 ℃ high-temperature inert gas from an annular flue gas chamber 12 at the upper part of the coking dry quenching furnace 8 enters a dry quenching boiler along a flue gas pipeline 9 to exchange heat, and the cooled inert gas with the temperature of about 130 ℃ is re-blown into the dry quenching furnace by a circulating fan 10 for recycling, and the tubular crystallizer is heated by using heat of the 810-890 ℃ high-temperature inert gas from the annular flue gas chamber 12 to realize crystallization;
As shown in fig. 3, the tubular crystallizer comprises a crystallization tube 13 obliquely arranged in the annular flue gas chamber 12, the inclined crystallization tube 13 can prolong the arrangement length of the crystallization tube 13 in the annular flue gas chamber 12 of the coking dry quenching furnace 8 so as to improve the heating area, one end of the crystallization tube 13 is fixed with an end frame 14 fixed on the inner wall of the annular flue gas chamber 12, the other end of the crystallization tube 13 is fixedly connected with an extension shell 15 which is communicated with the outside of the annular flue gas chamber 12, and the extension shell 15 is convenient for arranging and installing the crystallization tube 13.
As shown in fig. 2, the outside of the crystallization tube 13 is connected with a drying jacket 22 through a blanking tube 21, a plurality of discharging tubes 23 are arranged at the bottom of the drying jacket 22, a plurality of gas diffusing holes are arranged at the top of the drying jacket 22, a control valve 24 is arranged on the discharging tube 23, and a cut-off valve 25 is arranged at the root of the blanking tube 21.
As shown in fig. 5, the salt discharging assembly comprises a rotating shaft 131 rotatably supported inside the crystallization tube 13, a helical blade 132 is arranged on the rotating shaft 131, one end of the rotating shaft 131 is connected with a main shaft of a driving motor 16 arranged outside the crystallization tube 13, the concentrated brine material can be stirred by the rotating helical blade 132 to uniformly disperse the concentrated brine to the inner wall of the crystallization tube 13, so that the heat dissipation area is increased, the rapid discharging of the crystalline sodium chloride is realized in the discharging stage, the material adhesion and blockage are avoided, the crystallization tube 13, the rotating shaft 131 and the helical blade 132 are manufactured by adopting nickel base alloys, and the high strength and certain oxidation corrosion resistance can still be maintained at the high temperature of 650-1000 ℃, so that the service life of the tubular crystallizer is prolonged.
As shown in fig. 2 and 4, a continuous liquid supply system is arranged at the upper part of the crystallization tubes 13, the continuous liquid supply system comprises a liquid supply ring tube 17, the liquid supply ring tube 17 is connected with a concentrated brine main tube 61 at the outlet of the high-pressure reverse osmosis 6, the lower part of the liquid supply ring tube 17 is connected with uniform distribution components arranged on the corresponding crystallization tubes 13 through a plurality of liquid inlet tubes 18, the crystallization tubes 13 are uniformly divided into a first crystallization region and a second crystallization region which are alternately subjected to liquid inlet crystallization, the liquid supply crystallization in the first crystallization region and the second crystallization region are divided into a liquid supply evaporation section and a heating crystallization discharge section, and the liquid supply evaporation section and the heating crystallization discharge section of the first crystallization region and the second crystallization region are alternately used at a certain period (as shown in fig. 8), so that the continuous liquid supply and crystallization discharge stability of the coking dry quenching furnace 8 are realized, and the stable operation of the system is realized without intermittent operation in the whole process.
As shown in fig. 6, the uniform distribution assembly includes a mounting cover 133 disposed at the top of the crystallization tube 13 and communicated with the crystallization tube, a distribution tube 134 is fixed in the mounting cover 133, a plurality of spray nozzles 135 are mounted at the lower part of the distribution tube 134, the distribution tube 134 is connected with the outlet of the liquid inlet tube 18, and strong brine can be uniformly sprayed on the crystallization tube 13 through the distribution tube 134 and the spray nozzles 135, so as to realize efficient heating crystallization evaporation, and the mounting cover 133 is arranged to avoid the interference phenomenon between the rotation of the distribution tube 134 and the helical blade.
As shown in fig. 1 and 2, the gas collecting pipeline comprises a steam ring pipe 19 arranged at the upper part of the coking dry quenching furnace 8, the bottom of the steam ring pipe 19 is connected with a corresponding crystallization pipe 13 through a plurality of ascending pipes 20, a gas one-way valve can be installed on the ascending pipes 20 to avoid the interference of evaporated gas in a first crystallization area and a second crystallization area, the steam ring pipe 19 is connected with a steam inlet of the sodium chloride dual-effect concentration system 7 through a steam main pipe 26, high-temperature steam generated by the crystallization pipe 13 is led to the sodium chloride dual-effect concentration system 7 through the gas collecting pipeline for heating, the reutilization of the high-temperature steam is realized, the energy consumption of the sodium chloride dual-effect concentration system 7 is reduced, the steam main pipe 26 is connected with an anti-freezing pipe 102 installed inside the concentrated water collection tank 1 through a bypass steam branch pipe 27, the control valve on the steam branch pipe 27 can be opened in winter to realize the heating of the concentrated water collection tank 1 in order to avoid the excessive low concentrated water temperature, and the stability of the concentrated water temperature and the running of the equipment is improved.
As shown in fig. 1, the sodium chloride two-effect concentration system 7 comprises an effect heater 71 connected through a strong brine branch pipe 62, an inlet of the strong brine branch pipe 62 is connected with a strong brine main pipe 61 in a bypass way, strong brine from the strong brine branch pipe 62 sequentially passes through the effect heater 71, an effect separator 72, a front-end circulating pump 73, a two-effect heater 74, a two-effect separator 75, a rear-end circulating pump 76, a crystallizer 77 and a mother liquor tank 78, the tops of the effect separator 72 and the two-effect separator 75 respectively heat jackets of the two-effect heater 74 and the crystallizer 77 through steam pipes, a steam inlet of the effect heater 71 is connected with a steam main pipe 26, a mother liquor tank 78 is conveyed to the effect heater 71 through a pressurizing pump for circulating treatment, and condensed water generated by the jackets of the effect heater 71, the two-effect heater 74 and the crystallizer 77 is recovered through pipelines.
Steam at 300-350 ℃ from a gas collecting pipeline enters into an effective heater 71 to heat strong brine entering into an effective heater 71, the strong brine liquid is pushed to be heated and boiled, the boiling strong brine enters into an effective separator 72 to realize gas-liquid separation, the generated steam enters into a secondary heater 74 to continue heating, liquid at the lower part of the effective separator 72 is conveyed to the secondary heater 74 through a front-end circulating pump 73 to be heated and boiled, the brine with higher concentration entering into the bottom of the secondary separator 75 is conveyed to a crystallizer 77 through a rear-end circulating pump 76 to be heated to realize crystallization, and the crystallized sodium chloride crystalline salt is dried and dehydrated through a dryer to realize evaporation crystallization.
As shown in fig. 7, the crystallization control system of the coking dry quenching furnace 8 is further included, the crystallization control system comprises a PLC controller 28, the PLC controller 28 is electrically connected with a liquid inlet valve 181 of a liquid inlet pipe 18 of the first crystallization zone and the second crystallization zone, a driving motor 16, a cut-off valve 25, a flowmeter 171 at the inlet end of a liquid supply ring pipe 17 and a discharge valve 24 on a discharge pipe 23, and the tubular crystallizers of the first crystallization zone and the second crystallization zone are automatically controlled by the crystallization control system, so that alternate continuous liquid supply crystallization is realized, and stable operation of crystallization of the coking dry quenching furnace is improved.
As shown in fig. 1, control valves are installed on the main brine pipe 61, the branch brine pipe 62, the main steam pipe 26, the branch steam pipe 27, and the respective pipes.
The implementation principle of the coking strong brine evaporation crystallization treatment system provided by the embodiment of the application is as follows:
36 m/h of concentrated water treated by a recycling working section enters a concentrated water collecting tank 1 for storage, a large amount of hardness, fluoride and silicon (the hardness of the discharged water is about 150mg/L, the fluoride is 20mg/L and the silicon is 10 mg/L) are further removed by a lifting pump 101 and conveyed to a high-density sedimentation tank 2, then the discharged water enters a multi-medium filter 3 to remove suspended matters, the discharged water after the suspended matters are removed enters an ultrafiltration 4 to remove colloid matters, the discharged water after the ultrafiltration 4 is pressurized by a conveying pump 31 and enters a nanofiltration 5 to separate salt and nitrate, high sodium chloride and low COD (NaCL: 10490mg/L; COD:50 mg/L) are generated by nanofiltration, the nanofiltration generated water is pressurized by a high-pressure pump 501 and conveyed to a high-pressure reverse osmosis 6, and concentrated to form 4m of concentrated brine (NaCL: 83920mg/L; COD:400 mg/L);
Part of the strong brine generated by the high-pressure reverse osmosis 6 is directly conveyed to the coking dry quenching furnace 8 along the strong brine main pipe 61 for direct heating crystallization, and the other part of the strong brine is conveyed to the sodium chloride double-effect concentration system 7 along the strong brine branch pipe 62 for crystallization, and the flow of the two parts of the strong brine can be uniformly distributed and controlled by the control valve;
the strong brine entering the coking dry quenching furnace 8 passes through a flowmeter 171 at the front end of the inlet of the liquid supply ring pipe 17, a signal detected by the flowmeter 171 is transferred to the PLC 28, the PLC 28 controls all liquid inlet valves 181 of the first crystallization zone to be opened, all liquid inlet valves 181 of the second crystallization zone to be closed, the strong brine entering the liquid supply ring pipe 17 enters a plurality of tubular crystallizers of the first crystallization zone along a plurality of liquid inlet pipes 18 to be heated and evaporated, and liquid supply is delayed for 15 minutes (as shown in fig. 8), and the PLC 28 controls a driving motor 16 of the first crystallization zone to drive a spiral blade 132 to perform forward and reverse rotation (10 seconds are respectively and alternately performed);
When entering the corresponding tubular crystallizer of the first crystallization zone along the liquid inlet pipe 18, the concentrated brine enters the uniform distribution assembly firstly, and is uniformly dispersed in the crystallization pipe 13 by splashing from a plurality of spray heads 135 of the distribution pipe 134 of the uniform distribution assembly, and is heated by 810-890 ℃ high-temperature inert gas coming out of the annular flue gas chamber 12 at the upper part of the coking dry quenching furnace 8, so that most of water of the concentrated brine uniformly dispersed in the crystallization pipe 13 is evaporated in a liquid supply evaporation section for 15 minutes, and meanwhile, the concentrated brine in the crystallization pipe 13 is stirred by the spiral blades 132 in positive and negative rotation, so that the uniform distribution of the concentrated brine in the crystallization pipe 13 is ensured, and the heating evaporation efficiency is improved;
After the liquid in the first crystallization area is evaporated for 15 minutes, the PLC 28 controls to close all liquid inlet valves 181 of the first crystallization area and open all liquid inlet valves 181 of the second crystallization area, the liquid supply ring pipe 17 continues to supply liquid for 15 minutes in a delayed manner to the tubular crystallizer in the second crystallization area, during the period, the plurality of crystallization pipes 13 in the first crystallization area continuously heat for 14 minutes to gradually separate out residual moisture and evaporate solute, sodium chloride crystals gradually form to realize crystallization, and the spiral blades 132 in positive and negative rotation perform overturning movement to the separated salt, so that not only can the heating uniformity be improved, but also the crystallization efficiency can be improved, and the adhesion of crystallization salt and the inner wall of the crystallization pipe 13 can be avoided, so that the subsequent discharging is facilitated;
After heating for 14 minutes, the PLC 28 synchronously controls the driving motors 16 of the multiple tubular crystallizers in the first crystallization zone to reversely rotate and the cut-off valves 25 on the blanking pipes 21 corresponding to the crystallization pipes 13 to be opened for 1 minute, and the driving motors 16 drive the rotating shafts 131 and the spiral blades 132 to rotate so as to discharge the crystalline sodium chloride in the tubular crystallizers to the outside, and the crystalline sodium chloride is discharged to the drying jacket 22 at the lower part along the blanking pipes 21;
The PLC controller 28 controls the cut-off valve 25 and the driving motor 16 of the section of the first crystallization zone to be closed and enter the next liquid supply evaporation section after all the first crystallization zone is discharged within 1 minute, and the second crystallization zone enters the heating crystallization section and the discharging section to operate, so that the first crystallization zone and the second crystallization zone circularly and alternately operate for crystallization, continuous liquid supply and crystallization discharge are integrally realized, and the stable operation of heating crystallization of the coking dry quenching furnace 8 is realized.
The water content of the crystallization material entering into the drying jacket 22 is 5-10%, the drying jacket 22 is subjected to heat radiation of red coke heat exchange of a cooling chamber in the coking dry quenching furnace 8, the radiation temperature of the drying jacket 22 on the outer wall of the coking dry quenching furnace 8 is 80-120 ℃, the crystallization sodium chloride in the drying jacket 22 is subjected to the radiation of the heat of the outer wall of the coking dry quenching furnace 8 to evaporate the residual moisture and discharge the residual moisture from a plurality of gas discharge holes at the top of the drying jacket, so that the drying and heating of the crystallization sodium chloride are realized, and the PLC 28 controls the discharge valve 24 on the discharge pipe 23 to discharge the crystallization sodium chloride at intervals of 8-10 hours, so that not only can the drying of the crystallization sodium chloride be more thorough, but also the high-level crystallization sodium chloride in the drying jacket 22 can be prevented from radiating to the surrounding environment, the outer temperature of the coking dry quenching furnace 8 is reduced, and the operation environment around the coking dry quenching furnace 8 is greatly improved;
The concentrated brine in the crystallization tubes 13 of the first crystallization zone and the second crystallization zone is evaporated to generate steam with the temperature of 300-350 ℃ which enters the steam loop 19 along the ascending tube 20, and the steam enters the one-effect heater 71 of the sodium chloride two-effect concentration system 7 along the main steam tube 26 to supply heat, so that the requirement of the sodium chloride two-effect concentration system 7 on heating steam is met, the two-effect concentration system 7 does not need to be provided with additional steam, and the energy consumption is greatly reduced, and water resources are saved.
The foregoing has shown and described the basic principles, principal features and advantages of the invention. It will be understood by those skilled in the art that the present invention is not limited to the embodiments described above, and that the above embodiments and descriptions are merely illustrative of the principles of the present invention, and various changes and modifications may be made without departing from the spirit and scope of the invention, which is defined in the appended claims. The scope of the invention is defined by the appended claims and equivalents thereof.
Claims (10)
1. The utility model provides a coking strong brine evaporation crystallization processing system, includes strong water collecting vat (1), and this strong water collecting vat (1) strong water is carried along pipeline concentrated high-density sedimentation tank (2), multi-media filter (3), delivery pump (301), ultrafiltration (4), nanofiltration (5), high-pressure pump (501) and high-pressure reverse osmosis (6) in proper order through elevator pump (101) and is handled its characterized in that: the outlet of the high-pressure reverse osmosis (6) is respectively conveyed to a sodium chloride double-effect concentration system (7) and a plurality of tubular crystallizers arranged in an annular flue gas chamber (12) at the upper part of the coking dry quenching furnace (8) through a concentrated salt water pipeline for crystallization treatment; steam generated by heating the tubular crystallizer is conveyed to a sodium chloride double-effect concentration system (7) through a gas collecting pipeline for heating and recycling; and the crystallized salt generated by heating the tubular crystallizers is conveyed to a drying jacket (22) arranged on the outer wall of the coking dry quenching furnace (8) through a salt discharging assembly arranged in the tubular crystallizers for drying.
2. The coking strong brine evaporative crystallization processing system according to claim 1, wherein: the tubular crystallizer comprises a crystallization tube (13) obliquely arranged in the annular flue gas chamber (12), one end of the crystallization tube (13) is fixed with an end frame (14) fixed on the inner wall of the annular flue gas chamber (12), and the other end of the crystallization tube (13) is connected and fixed with an extension shell (15) which is communicated with the outside of the annular flue gas chamber (12).
3. The coking strong brine evaporative crystallization processing system according to claim 2, wherein: the outside of crystallization pipe (13) is connected with drying jacket (22) through unloading pipe (21), drying jacket (22) top sets up a plurality of gas diffusion holes, drying jacket (22) bottom is provided with a plurality of discharging pipes (23), install control valve (24) on discharging pipe (23), trip valve (25) are installed at the root of unloading pipe (21).
4. The coking strong brine evaporative crystallization processing system according to claim 1, wherein: the salt discharging assembly comprises a rotating shaft (131) rotatably supported inside the crystallization tube (13), a spiral blade (132) is arranged on the rotating shaft (131), and one end of the rotating shaft (131) is connected with a main shaft of a driving motor (16) arranged outside the crystallization tube (13).
5. The coking strong brine evaporative crystallization processing system according to claim 2, wherein: the crystallization device comprises a plurality of crystallization tubes (13), wherein a continuous liquid supply system is arranged on the upper portions of the crystallization tubes (13), the continuous liquid supply system comprises a liquid supply ring tube (17), the liquid supply ring tube (17) is connected with a concentrated brine main tube (61) at an outlet of a high-pressure reverse osmosis (6), the lower portions of the liquid supply ring tube (17) are connected with uniform distribution assemblies arranged on the corresponding crystallization tubes (13) through a plurality of liquid inlet tubes (18), and the crystallization tubes (13) are uniformly divided into a first crystallization zone and a second crystallization zone which are crystallized by two alternate liquid inlets.
6. The coking strong brine evaporative crystallization processing system according to claim 5, wherein: the uniform distribution assembly comprises an installation cover (133) which is arranged at the top of the crystallization tube (13) and communicated with the crystallization tube, a distribution tube (134) is fixed in the installation cover (133), a plurality of spray heads (135) are arranged at the lower part of the distribution tube (134), and the distribution tube (134) is connected with the outlet of the liquid inlet tube (18).
7. The coking strong brine evaporative crystallization processing system according to claim 1, wherein: the gas collecting pipeline comprises a steam loop pipe (19) arranged on the upper portion of the coking dry quenching furnace (8), the bottom of the steam loop pipe (19) is connected with a corresponding crystallization pipe (13) through a plurality of ascending pipes (20), the steam loop pipe (19) is connected with a steam inlet of a sodium chloride double-effect concentration system (7) through a steam main pipe (26), and the steam main pipe (26) is connected with an antifreezing pipe (102) arranged inside the concentrated water collecting tank (1) through a bypass steam branch pipe (27).
8. The coking strong brine evaporative crystallization processing system according to claim 1, wherein: the sodium chloride two-effect concentration system (7) comprises an effect heater (71) connected through a strong brine branch pipe (62), wherein an inlet of the strong brine branch pipe (62) is connected with a strong brine main pipe (61) in a bypass mode, strong brine from the strong brine branch pipe (62) sequentially passes through the effect heater (71), an effect separator (72), a front end circulating pump (73), a two-effect heater (74), a two-effect separator (75), a rear end circulating pump (76), a crystallizer (77) and a mother liquor tank (78), the tops of the two-effect separator (72) and the two-effect separator (75) are respectively used for heating jackets of the two-effect heater (74) and the crystallizer (77) through steam pipes, a steam inlet of the one-effect heater (71) is connected with a steam main pipe (26), the mother liquor tank (78) is conveyed to the one-effect heater (71) through a pressurizing pump for circulating treatment, and steam generated by the jackets of the one-effect heater (71), the two-effect heater (74) and the crystallizer (77) are subjected to condensate water recovery treatment through pipelines.
9. The coking strong brine evaporative crystallization processing system according to claim 1, wherein: the crystallization control system of the coking dry quenching furnace (8) is further included, the crystallization control system comprises a PLC (28), and the PLC (28) is electrically connected with a liquid inlet valve (181), a driving motor (16), a cut-off valve (25) and a flowmeter (171) at the inlet end of a liquid supply ring pipe (17) and a discharge valve (24) on a discharge pipe (23) of the liquid inlet pipe (18) of the first crystallization zone and the second crystallization zone.
10. The coking strong brine evaporative crystallization processing system according to claim 8, wherein: the main brine pipe (61), the strong brine branch pipe (62), the main steam pipe (26), the branch steam pipe (27) and the control valves are respectively arranged on the pipelines.
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| CN110813006A (en) * | 2019-12-02 | 2020-02-21 | 中冶焦耐(大连)工程技术有限公司 | Waste gas waste heat recovery and purification process of coke oven gas heating system |
| CN113185048A (en) * | 2021-05-20 | 2021-07-30 | 金能科技股份有限公司 | Triple-effect evaporation system and process for evaporating and extracting salt from coking wastewater |
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| JPH08218074A (en) * | 1995-02-17 | 1996-08-27 | Sumitomo Metal Ind Ltd | Gas recovery in dry coke quencher and plant therefor |
| CN113955888A (en) * | 2020-07-21 | 2022-01-21 | 蓝星工程有限公司 | Integrated treatment system and process for recycling concentrated brine in coking wastewater |
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| CN110813006A (en) * | 2019-12-02 | 2020-02-21 | 中冶焦耐(大连)工程技术有限公司 | Waste gas waste heat recovery and purification process of coke oven gas heating system |
| CN113185048A (en) * | 2021-05-20 | 2021-07-30 | 金能科技股份有限公司 | Triple-effect evaporation system and process for evaporating and extracting salt from coking wastewater |
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