CN105408452A - Coal dry distillation device - Google Patents
Coal dry distillation device Download PDFInfo
- Publication number
- CN105408452A CN105408452A CN201480042493.3A CN201480042493A CN105408452A CN 105408452 A CN105408452 A CN 105408452A CN 201480042493 A CN201480042493 A CN 201480042493A CN 105408452 A CN105408452 A CN 105408452A
- Authority
- CN
- China
- Prior art keywords
- unit
- coal
- heated air
- oxygen concentration
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000003245 coal Substances 0.000 title claims abstract description 189
- 238000000197 pyrolysis Methods 0.000 title claims abstract description 153
- 239000007789 gas Substances 0.000 claims abstract description 218
- 239000001301 oxygen Substances 0.000 claims abstract description 218
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 218
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 210
- 239000000446 fuel Substances 0.000 claims description 128
- 238000002485 combustion reaction Methods 0.000 claims description 40
- 238000010000 carbonizing Methods 0.000 claims description 35
- 238000010438 heat treatment Methods 0.000 claims description 34
- 238000005086 pumping Methods 0.000 claims description 17
- 238000006477 desulfuration reaction Methods 0.000 claims description 5
- 230000023556 desulfurization Effects 0.000 claims description 5
- 238000003756 stirring Methods 0.000 claims description 4
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 claims description 4
- 239000000284 extract Substances 0.000 claims description 2
- 238000000605 extraction Methods 0.000 abstract description 33
- 230000001737 promoting effect Effects 0.000 abstract description 10
- 238000000034 method Methods 0.000 abstract description 7
- 239000011261 inert gas Substances 0.000 abstract description 2
- 239000002912 waste gas Substances 0.000 description 152
- 230000000740 bleeding effect Effects 0.000 description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 8
- 238000009413 insulation Methods 0.000 description 7
- 238000002156 mixing Methods 0.000 description 7
- 238000000926 separation method Methods 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000004215 Carbon black (E152) Substances 0.000 description 6
- 229930195733 hydrocarbon Natural products 0.000 description 6
- 150000002430 hydrocarbons Chemical class 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 150000002926 oxygen Chemical class 0.000 description 5
- 235000009508 confectionery Nutrition 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 239000003345 natural gas Substances 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 3
- 235000011089 carbon dioxide Nutrition 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 239000000567 combustion gas Substances 0.000 description 3
- 239000000428 dust Substances 0.000 description 3
- 230000001535 kindling effect Effects 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 3
- 239000010970 precious metal Substances 0.000 description 3
- 229910052717 sulfur Inorganic materials 0.000 description 3
- 239000011593 sulfur Substances 0.000 description 3
- NLXLAEXVIDQMFP-UHFFFAOYSA-N Ammonia chloride Chemical compound [NH4+].[Cl-] NLXLAEXVIDQMFP-UHFFFAOYSA-N 0.000 description 2
- VTYYLEPIZMXCLO-UHFFFAOYSA-L Calcium carbonate Chemical compound [Ca+2].[O-]C([O-])=O VTYYLEPIZMXCLO-UHFFFAOYSA-L 0.000 description 2
- KDLHZDBZIXYQEI-UHFFFAOYSA-N Palladium Chemical compound [Pd] KDLHZDBZIXYQEI-UHFFFAOYSA-N 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 description 2
- 239000003077 lignite Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000002161 passivation Methods 0.000 description 2
- BASFCYQUMIYNBI-UHFFFAOYSA-N platinum Chemical compound [Pt] BASFCYQUMIYNBI-UHFFFAOYSA-N 0.000 description 2
- 230000003252 repetitive effect Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000003476 subbituminous coal Substances 0.000 description 2
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 1
- 241000264877 Hippospongia communis Species 0.000 description 1
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 1
- 239000000443 aerosol Substances 0.000 description 1
- 235000019270 ammonium chloride Nutrition 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910000019 calcium carbonate Inorganic materials 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000002817 coal dust Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000006866 deterioration Effects 0.000 description 1
- 238000010980 drying distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 238000004898 kneading Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 229910052763 palladium Inorganic materials 0.000 description 1
- 229910052697 platinum Inorganic materials 0.000 description 1
- 231100000572 poisoning Toxicity 0.000 description 1
- 230000000607 poisoning effect Effects 0.000 description 1
- 150000003254 radicals Chemical class 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 230000002269 spontaneous effect Effects 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 239000000758 substrate Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
Classifications
-
- 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
- C10B21/00—Heating of coke ovens with combustible gases
- C10B21/10—Regulating and controlling the combustion
- C10B21/18—Recirculating the flue gases
-
- 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
- C10B21/00—Heating of coke ovens with combustible gases
- C10B21/02—Heating of coke ovens with combustible gases with lean gas
-
- 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
- C10B47/00—Destructive distillation of solid carbonaceous materials with indirect heating, e.g. by external combustion
- C10B47/28—Other processes
- C10B47/30—Other processes in rotary ovens or retorts
-
- 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
- C10B57/00—Other carbonising or coking processes; Features of destructive distillation processes in general
- C10B57/18—Modifying the properties of the distillation gases in the oven
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/20—Reductants
- B01D2251/206—Ammonium compounds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2251/00—Reactants
- B01D2251/40—Alkaline earth metal or magnesium compounds
- B01D2251/404—Alkaline earth metal or magnesium compounds of calcium
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0283—Flue gases
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/48—Sulfur compounds
- B01D53/50—Sulfur oxides
- B01D53/501—Sulfur oxides by treating the gases with a solution or a suspension of an alkali or earth-alkali or ammonium compound
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/54—Nitrogen compounds
- B01D53/56—Nitrogen oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
- B01D53/86—Catalytic processes
- B01D53/869—Multiple step processes
Abstract
The purpose of the present invention is to enable low-cost acquisition of an inert gas (low-oxygen concentration gas) promoting the release of a dry distillation gas from coal. The invention is provided with: a coal dry distillation device main body (110) utilizing the rotary kiln method; exhaust means (118, 118a to 118c, 130), connected to an outer cylinder (113) of the coal dry distillation device main body (110), for exhausting an exhaust gas present inside the outer cylinder (113); gas extraction means (141, 141a, 141b, 143, 144, 144a) for extracting a portion of the exhaust gas exhausted by the exhaust means; and low-oxygen concentration gas supply means (141, 141a, 141b, 147, 142, 145, 145a, 146) for sending into the inner cylinder (112) the exhaust gas extracted by the gas extraction means so that the oxygen concentration of the exhaust gas is lowered.
Description
Technical field
The present invention relates to a kind of dry distillation of coal device.
Background technology
The thermal value of the low-rank coal more due to the moisture content such as brown coal and sub-bituminous coal and low grade coal per unit weight is low, therefore while carrying out drying or destructive distillation in utilization heating, upgrading is implemented, make it in low-oxygen environment, reduce surfactivity, thus formation can prevent spontaneous combustion and improve the upgrading coal of the thermal value of per unit weight.
Herein, as the dry distillation of coal device that will the dried dry coal of above-mentioned low-rank coal made to carry out destructive distillation, there will be a known the indirect heating type device utilizing the direct-heating type device of heated air direct heating dry coal (referenced patent document 1,2) and utilize heated air indirect heating dry coal.Such as have rotary kiln type device as indirect heating type device, described rotary kiln type device possesses the urceolus (sleeve pipe) of fixing maintenance and the rotatable inner core be supported on inside this urceolus.In the dry distillation of coal device of this mode, heated air is supplied to (between urceolus and inner core) in urceolus, described dry coal is supplied to the end side of described inner core simultaneously, by making this inner cylinder rotating, this dry coal is moved from the end side of this inner core to the other end side, and stir while heat destructive distillation, send destructive distillation coal and carbonizing gas from another side of this inner core.
Prior art document
Patent documentation
Patent documentation 1: Japanese Patent Laid-Open No. Sho 61-64788 publication
Patent documentation 2: Japanese Patent Laid-Open 2012-241992 publication
Summary of the invention
Invent problem to be solved
But described carbonizing gas, not only containing water vapor, carbonic acid gas, low molecular hydrocarbon (such as methane and ethane etc.), tar etc., also contains Determination of Trace Sulfur contained in this dry coal.In order to promote trace ingredients release by this destructive distillation operation, need to increase the partial pressure difference of carbonizing gas composition and dry coal surface destructive distillation gaseous constituent in inner core environment gas.Such as, low oxygen concentration rare gas element can be supplied by externally in described inner core, reduce the carbonizing gas concentration in inner core environment.
Usually use nitrogen as described rare gas element, but produce nitrogen to be separated from air, and need PSA (PressureSwingAdsorption) or cryogenic separation device.The described nitrogen amount that described dry distillation of coal device consumes increases according to the size (the dry coal treatment capacity of this dry distillation of coal device) of this dry distillation of coal device, the capacity of described PSA or described cryogenic separation device also becomes large, and equipment cost and the power cost for the manufacture of nitrogen increase thereupon.
Therefore, the present invention forms for solving above-mentioned the project, its object is to provide a kind of dry distillation of coal device, and described dry distillation of coal device can obtain with low cost the rare gas element (low oxygen concentration gas) promoting that carbonizing gas discharges from coal.
For solving the method for problem
Solve the described dry distillation of coal device of the first invention of above-mentioned problem, it is characterized in that, possess: rotary kiln type dry distillation of coal apparatus main body, described rotary kiln type dry distillation of coal apparatus main body is by rotatable for the inner core inner side being supported on urceolus, heated air is supplied to the inside of described urceolus, coal is supplied to inside from the end side of described inner core simultaneously, by making this inner cylinder rotating, this coal is moved from the end side of this inner core to the other end side, and stir while heat destructive distillation, send destructive distillation coal and carbonizing gas from another side of this inner core; Exhaust unit, described exhaust unit is connected with described urceolus and arranges, and discharges the described heated air in this urceolus; Pumping cells, described pumping cells extracts a part for the described heated air of being discharged by described exhaust unit out; With, low oxygen concentration gas supply unit, this heated air is supplied in described inner core by described low oxygen concentration gas supply unit, and the concentration of the oxygen contained in the described heated air of being extracted out by described pumping cells is reduced.
The the second invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned first invention, it is characterized in that, described low oxygen concentration gas supply unit has: deacidification unit, and described deacidification unit removes in described heated air the described oxygen contained; With, low oxygen concentration gas transport unit, the low oxygen concentration gas obtained by described deacidification unit is delivered to described inner core by described low oxygen concentration gas transport unit.
The 3rd invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned second invention, and it is characterized in that, described deacidification unit possesses: fuel addition unit, and fuel is added into described heated air by described fuel addition unit; With, combustioncatalysts, described combustioncatalysts is arranged to contact with the described heated air of adding described fuel.
The 4th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned 3rd invention, and it is characterized in that possessing heating unit, described heating unit is arranged on described pumping cells, heats described heated air.
The 5th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned 3rd invention, and it is characterized in that possessing desulfurization unit, described desulfurization unit is arranged on described exhaust unit, removes the oxysulfide contained in described heated air.
The 6th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned 4th invention, it is characterized in that, possess: oxygen concentration testing unit, described oxygen concentration testing unit measures the oxygen concn of the described low oxygen concentration gas carried by described low oxygen concentration gas transport unit; With, amount of fuel addition control unit, described amount of fuel addition control unit, according to the information obtained by described oxygen concentration testing unit, controls the addition of the described fuel added by described fuel addition unit, makes the oxygen concn of described low oxygen concentration gas be less than 1.5%.
The 7th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned second invention, it is characterized in that, described deacidification unit possesses: alternate combustion device, described alternate combustion device have be transferred described heated air combustion chamber, be arranged on the burner in this combustion chamber and be arranged in this combustion chamber the alternative type heat exchanger being transferred described heated air position; With, fuel addition unit, fuel is added into described combustion chamber by described fuel addition unit.
The 8th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned 7th invention, it is characterized in that, possess: oxygen concentration testing unit, described oxygen concentration testing unit measures the concentration of the oxygen contained in the described heated air of being carried by described low oxygen concentration gas transport unit; With, amount of fuel addition control unit, described amount of fuel addition control unit, according to the information obtained by described oxygen concentration testing unit, controls the addition of the described fuel added by described fuel addition unit, makes the oxygen concn of described low oxygen concentration gas be less than 1.5%.
The 9th invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned first invention, it is characterized in that, described low oxygen concentration gas supply unit possesses: heated air supply unit, and the described heated air of being extracted out by described pumping cells is delivered in described inner core by described heated air supply unit; With, fuel addition unit, fuel is added into the described heated air be delivered to by described heated air supply unit in described inner core by described fuel addition unit.
The tenth invention described dry distillation of coal device solving above-mentioned problem is the described dry distillation of coal device of above-mentioned 9th invention, it is characterized in that, possess: heating gas flow measuring unit, described heating gas flow measuring unit measures the flow of the described heated air of being carried by described heated air supply unit; Oxygen concentration testing unit, described oxygen concentration testing unit measures the concentration of the oxygen contained in the described heated air of being carried by described heated air supply unit; With, amount of fuel addition control unit, described amount of fuel addition control unit is according to the information obtained by described heating gas flow measuring unit and described oxygen concentration testing unit, control the addition of the described fuel added by described fuel addition unit, make the oxygen concn of described low oxygen concentration gas be less than 1.5%.
Beneficial effect
According to dry distillation of coal device of the present invention, the rare gas element of the concentration reducing the oxygen contained in the heated air of indirect heating coal can be obtained by low oxygen concentration gas supply unit, low oxygen concentration gas supply unit itself and running cost thereof are compared comparatively cheap with PSA with cryogenic separation device etc., thus can obtain with low cost the rare gas element promoting that carbonizing gas discharges from coal.When the generation of described rare gas element is risen with the temperature of this rare gas element itself, by the coal in rare gas element heating dry distillation of coal apparatus main body, thus correspondingly can realize the miniaturization of dry distillation of coal apparatus main body.
Accompanying drawing explanation
Fig. 1 is the Sketch figure of dry distillation of coal device first embodiment of the present invention.
Fig. 2 is that the Sketch figure of dry distillation of coal device second embodiment of the present invention, Fig. 2 (a) represent that it is overall, and Fig. 2 (b) represents the summary possessing the alternate combustion device for deoxidizing of this structure.
Fig. 3 is the Sketch figure of dry distillation of coal device the 3rd embodiment of the present invention.
Embodiment
The embodiment of dry distillation of coal device of the present invention is described according to accompanying drawing, but the present invention is not limited in the following embodiment illustrated according to accompanying drawing.
[the first embodiment]
First embodiment of dry distillation of coal device of the present invention is described according to Fig. 1.
Dry distillation of coal device 100 described in present embodiment as shown in Figure 1, possesses the dry distillation of coal unit and the dry distillation of coal apparatus main body 110 that are obtained destructive distillation coal 2 by heated air 11 indirect heating dry coal 1.Dry distillation of coal apparatus main body 110 possesses hopper 111, inner core (main cavity portion) 112, urceolus (sleeve pipe) 113 and chute 114.Hopper 111 is the equipment receiving dry coal 1 and this dry coal 1 is supplied to end side (base end side) inside of inner core 112.The rotatable support of inner core 112.Inner core 112 is supplied to inner dry coal 1 while make it from end side to the equipment of the other end side movement by rotating to stir.Although urceolus 113 makes inner core 112 rotatable, but to cover the mode fixed support of this inner core 112 periphery.Urceolus 113 is equipment heating medium and heated air 11 being delivered to inner side and being heated inner core 112 by heated air 11.Chute 114 is connected with another side (front) of this inner core 112 to make inner core 112 rotatable, and the destructive distillation coal 2 of the indirect heating destructive distillation dry coal 1 by heated air 11 is fallen the equipment sent below the other end side direction of this inner core 112.That is, dry distillation of coal apparatus main body 110 is rotary kiln type device.
The dry coal obtained in the following manner such as can be used as described dry coal 1, the low-rank coal (low grade coal) many by the water content such as brown coal and sub-bituminous coal is supplied to moisture eliminator (not shown), and utilizes to be dried to the hot blast (150 DEG C ~ 500 DEG C) of this moisture eliminator internal circulation and make water ratio be 0% substantially.
The top of the chute 114 of dry distillation of coal apparatus main body 110 is connected with the end side (base end side) of carbonizing gas vent line 115.Another side (front) of carbonizing gas vent line 115 is connected with heated air generation unit and roasting kiln 116.Therefore, carbonizing gas (pyrolysis gas) 15 is discharged to roasting kiln 116 via chute 114 and carbonizing gas vent line 115 in inner core 112, described carbonizing gas (pyrolysis gas) 15 contains water vapor, carbonic acid gas, low molecular hydrocarbon, tar etc. by heated air 11 indirect heating dry coal 1 from the release of this dry coal 1, and containing Determination of Trace Sulfur.
Roasting kiln 116 is connected with the end side (base end side) of heated air line of pipes 117.Roasting kiln 116 is connected with another side (front) of details exhaust gas recirculation pipeline 121 described later.Another side (front) of heated air line of pipes 117 is connected with the inner side of the urceolus 113 of dry distillation of coal apparatus main body 110.Carbonizing gas 15 has 5 ~ 15MJ/Nm
3combustion heating amount, the described carbonizing gas 15 being delivered to roasting kiln 116 carries out burn processing with combustion-supporting fuel (ignition dope) 16 such as the Sweet natural gases being supplied to this roasting kiln 116 together with waste gas 13.Therefore, the heated air (combustion gases) 11 generated in roasting kiln 116 is delivered to the inner side of urceolus 113 via heated air line of pipes 117.
Urceolus 113 is connected with the end side (base end side) of exhausting waste gas pipeline 118.Exhausting waste gas pipeline 118 is provided with boiler 118a, flow control valve 118b and extraction fan 118c from end side.The used heat of the heated air 12 after heating inner core 112 is reclaimed by boiler 118a.By control flow check adjustable valve 118b and extraction fan 118c, the heated air 12 after heating inner core 112 circulates from the end side of exhausting waste gas pipeline 118 to another side (front).
The end side (base end side) of heated air by-pass line 119 is connected with between the base end side of heated air line of pipes 117 and front.Another side (front) of heated air by-pass line 119 and the flow control valve 118b of exhausting waste gas pipeline 118 are connected with between extraction fan 118c.Heated air by-pass line 119 is provided with boiler 119a and flow control valve 119b from end side.The used heat of heated air 11 is reclaimed by boiler 119a.By control flow check adjustable valve 119b and extraction fan 118c, a part for the heated air 11 generated in roasting kiln 116 circulates from heated air line of pipes 117 via heated air by-pass line 119 another side (front) to exhausting waste gas pipeline 118.
Therefore, by control flow check adjustable valve 118b, 119b and extraction fan 118c, heated air 11,12 mixed gass mixed and waste gas 13 circulate to another side (front) of exhausting waste gas pipeline 118.
Another side (front) of exhausting waste gas pipeline 118 is provided with the emission-control equipment 130 of process waste gas 13.
Emission-control equipment 130 possesses denitrification apparatus (denitration unit) 131, electric bag filter (dust removing units) 132 and desulfurizer (desulfurization unit) 133.
The oxynitride (NOx) contained in waste gas 13 is removed by denitrification apparatus 131.Such as can using by spraying aqueous ammonium chloride solution (not shown) aerosol to waste gas 13 as denitrification apparatus 131, the reduction of nitrogen oxides such as nitrogen protoxide being become the device etc. of nitrogen.
The fine particulate solids such as the dust contained in removing waste gas 13 are separated by electric bag filter 132.
The oxysulfide (SOx) contained in waste gas 13 is removed by desulfurizer 133.Such as can use as desulfurizer 133 and spray calcium carbonate suspension (not shown) to waste gas 13, the oxysulfides such as sulfurous gas are replaced as the wet type device etc. of calcium sulfate etc.So, the SOx concentration in waste gas 13 can be reduced to below 50ppm, thus the poisoning performance that causes of S because of aftermentioned combustioncatalysts can be suppressed to reduce, and suppress to cause running cost to increase because changing this combustioncatalysts.
Therefore, by processing with said apparatus 131 ~ 133, the NOx of waste gas 13, dust and SOx can be removed.Outside the waste gas 13 of this process is exhausted from system.
The end side (base end side) of exhaust gas recirculation pipeline 121 is connected with between the extraction fan 118c of exhausting waste gas pipeline 118 and denitrification apparatus 131.Another side (front) of exhaust gas recirculation pipeline 121 is connected with roasting kiln 116.Exhaust gas recirculation pipeline 121 is provided with flow control valve 121a.By controlling extraction fan 118c and flow control valve 121a, in exhausting waste gas pipeline 118 part of waste gas 13 for circulation via exhaust gas recirculation pipeline 121 to roasting kiln 116 recirculation.
Above-mentioned dry distillation of coal apparatus main body 110 also possesses rare gas element generating apparatus 140, and described rare gas element generating apparatus 140 generates the rare gas element 14 promoting that carbonizing gas 15 discharges from dry coal 1.
Rare gas element generating apparatus 140 possesses waste gas and to bleed pipeline 141, and the bleed end side (base end side) of pipeline 141 and another side (front) of exhausting waste gas pipeline 118 of described waste gas is arranged with being connected between desulfurizer 133.Bleed another side (front) of pipeline 141 of waste gas is connected with the gas receiving port of combustioncatalysts device for deoxidizing (device for deoxidizing) 142.Waste gas pipeline 141 of bleeding is provided with flow control valve 141a, extraction fan 141b and heat exchanger (heating unit) 143 from end side (base end side).By control flow check adjustable valve 141a and extraction fan 141b, the part of the waste gas 13 circulated in desulfurizer 133 via exhausting waste gas pipeline 118 circulates to waste gas pipeline 141 of bleeding.
Waste gas is bled and is connected with the end side (base end side) of exhaust gas bypass pipeline 144 between the extraction fan 141b of pipeline 141 and heat exchanger 143.The bleed heat exchanger 143 of pipeline 141 of another side (front) of exhaust gas bypass pipeline 144 and waste gas is connected with between combustioncatalysts device for deoxidizing 142.Exhaust gas bypass pipeline 144 is provided with flow control valve 144a.By control flow check adjustable valve 141a, 144a and extraction fan 141b, adjustable via the ratio of heat exchanger 143 to combustioncatalysts device for deoxidizing 142 waste gas 13 circulated and the waste gas 13 circulated to combustioncatalysts device for deoxidizing 142 via exhaust gas bypass pipeline 144, regulate the temperature of the waste gas 13 to combustioncatalysts device for deoxidizing 142 circulation.
The gas receiving port of combustioncatalysts device for deoxidizing 142 is connected with the end side (front) of oxygen depletion fuel feed line 145, described oxygen depletion fuel feed line 145 carries the hydrocarbon fuels such as such as Sweet natural gas, namely for consuming the oxygen depletion fuel 17 of oxygen in waste gas 13.Another side (base end side) of oxygen depletion fuel feed line 145 is connected with the tanks 146 of storage oxygen depletion fuel 17.Oxygen depletion fuel feed line 145 is provided with flow control valve 145a.
Combustioncatalysts device for deoxidizing 142 possesses: pre-mixing chamber (not shown), and described pre-mixing chamber can generate the pre-mixed gas of waste gas 13 with oxygen depletion fuel 17 pre-mixing; With, combustioncatalysts (not shown), described combustioncatalysts is filled in the position adjacent with this pre-mixing chamber, contacts with described pre-mixed gas, thus in waste gas 13, oxygen and oxygen depletion fuel 17 react this oxygen of post consumption.
Include, for example as described combustioncatalysts and provide the standby catalyzer being shaped to honey comb like base material and being arranged on the precious metal on base material.Trichroite base material is include, for example out as described base material.As described precious metals as can platinum, palladium etc. be listed.Such as impregnating supporting method, coating method etc. can be utilized as the method arranged on the substrate by described precious metal.
The gas of combustioncatalysts device for deoxidizing 142 sends the end side (base end side) that mouth is connected with rare gas element line of pipes 147, and described rare gas element line of pipes 147 is carried and to be obtained by this combustioncatalysts device for deoxidizing 142 and to reduce the rare gas element 14 of waste gas 13 oxygen concn.Another side (front) of rare gas element line of pipes 147 is connected with the end side (base end side) of the inner core 112 of dry distillation of coal apparatus main body 110 via heat exchanger 143.Details rare gas element 14 described later rises to 550 DEG C ~ 750 DEG C, utilizes rare gas element 14 waste gas 13 to be preheated to the kindling temperature 150 DEG C ~ 350 DEG C of fuel 17 by heat exchanger 143.Rare gas element 14 is delivered to the inner core 112 of dry distillation of coal apparatus main body 110.
Waste gas is bled between the front of pipeline 141 and heat exchanger 143 and is provided with thermometer 141c, and described thermometer 141c can measure the temperature of the waste gas 13 of circulation in waste gas bleeds pipeline 141.Thermometer 141c is connected with the flow control valve 144a of exhaust gas bypass pipeline 144 via temperature signal line.The aperture of flow control valve 144a can regulate according to the information obtained by thermometer 141c (temperature of waste gas 13).
Rare gas element line of pipes 147 is provided with oxygen sensor (oxygen concentration testing unit) 147a, and described oxygen sensor (oxygen concentration testing unit) 147a can measure the oxygen concn of the rare gas element 14 of circulation in rare gas element line of pipes 147.
Oxygen sensor 147a via oxygen concn signal wire be arranged on the flow control valve 145a of oxygen depletion in fuel feed line 145 and be connected.The aperture of flow control valve 145a can regulate according to the information obtained by oxygen sensor 147a (oxygen concn of rare gas element 14).Namely, dry distillation of coal device 100 possesses not shown control device (amount of fuel addition control unit), this control device can according to the information obtained by oxygen sensor 147a (oxygen concn of rare gas element 14), control the addition of the oxygen depletion fuel 17 added by oxygen depletion fuel feed line 145, flow control valve 145a and tanks 146, make the oxygen concn of rare gas element 14 be such as less than 1.5%.
In this present embodiment, form exhaust unit by described exhausting waste gas pipeline 118, described boiler 118a, described flow control valve 118b, described extraction fan 118c, described emission-control equipment 130 etc.Pumping cells is formed by bleed pipeline 141, described flow control valve 141a, described extraction fan 141b, described heat exchanger 143, described exhaust gas bypass pipeline 144, described flow control valve 144a etc. of described waste gas.Fuel addition unit is formed by described oxygen depletion fuel feed line 145, described flow control valve 145a, described tanks 146 etc.Deacidification unit is formed by described combustioncatalysts device for deoxidizing 142, described fuel addition unit etc.Low oxygen concentration gas transport unit is formed by bleed pipeline 141, described flow control valve 141a, described extraction fan 141b, described rare gas element line of pipes 147 etc. of described waste gas.Low oxygen concentration gas supply unit is formed by described low oxygen concentration gas transport unit, described deacidification unit etc.Described dry distillation of coal device 100 is formed by described dry distillation of coal apparatus main body 110, described exhaust unit, described pumping cells, described low oxygen concentration gas supply unit, described amount of fuel addition control unit etc.
Next to using the dry distillation of coal treatment process of dry distillation of coal device 100 destructive distillation dry coal 1 described in the present embodiment of so formation to be described.
After dry coal 1 is put into the hopper 111 of dry distillation of coal apparatus main body 110, the dry coal 1 in hopper 111 is supplied from end side (base end side) to the inside of inner core 112.Rotated by inner core 112, the dry coal 1 in inner core 112 moves from its end side (base end side) gradually to another side (front).Inner core 112 is heated by the heated air 11 be delivered in urceolus 113, when described dry coal 1 moves from the end side of described inner core 112 to the other end side, by described heated air 11 indirect heating (300 DEG C ~ 500 DEG C).So, discharge from described dry coal 1 and be separated removing carbonizing gas (pyrolysis gas) 15 and make destructive distillation coal 2, described carbonizing gas (pyrolysis gas) 15 containing water vapor, carbonic acid gas, low molecular hydrocarbon, tar etc., and contains Determination of Trace Sulfur.
Destructive distillation coal 2 falls downwards via chute 114 from another side of inner core 112 and sends.Fall by chute 114 the destructive distillation coal 2 sent such as to be provided to not shown water cooler and to carry out cooling (150 DEG C ~ 200 DEG C), by passivation device (not shown), Passivation Treatment is carried out to the active site (free radical) produced because of destructive distillation, mixing together with water with tackiness agent by kneading device (not shown), again by shaped device (not shown) compressed moulding, thus make shaped coal.
Discharge from described dry coal 1 and be separated the carbonizing gas 15 removed and be delivered to roasting kiln 116 via carbonizing gas vent line 115.
Heated air (combustion gases) 11 is generated after burn processing being carried out with described combustion-supporting fuel 16 together with described waste gas 13 to described carbonizing gas 15 in described roasting kiln 116.Roasting kiln 116 is controlled the ratio of combustion-supporting fuel 16 and air flow quantity than controlling by combustion air, for preventing that coal dust etc. does not fire composition and prevents efficiency of combustion from reducing, usually combustion air excess rate is set as more than 1.0.Therefore, the oxygen concn in heated air (combustion gases) 11 is about 2 ~ 5%.By control flow check adjustable valve 118b and extraction fan 118c, a part for described heated air 11 is delivered in urceolus 113 by heated air line of pipes 117 in roasting kiln 116, and the heated air 12 after heating inner core 112 circulates to the front of exhausting waste gas pipeline 118 in urceolus 113.The nubbin of described heated air 11 is delivered to exhausting waste gas pipeline 118 via heated air by-pass line 119.Heated air 12 reclaims the used heat of heated air 12 by boiler 118a, is adjusted to the temperature (such as 350 DEG C) of regulation.The heated air 11 of circulation in heated air by-pass line 119, by the used heat of boiler 119a recovery heated air 11, is adjusted to the temperature (such as 350 DEG C) of regulation.The described heated air 12 reclaiming used heat by boiler 118a and another side (front) being delivered to exhausting waste gas pipeline 118 by extraction fan 118c by the waste gas (mixed gas) 13 that the described heated air 11 that boiler 119a reclaims used heat mixes, processed by emission-control equipment 130.
By control flow check adjustable valve 121a, in exhausting waste gas pipeline 118 part of described waste gas 13 for circulation via exhaust gas recirculation pipeline 121 to roasting kiln 116 recirculation.
Circulating and do not remove NOx to the waste gas 13 of exhaust gas recirculation pipeline 121 recirculation by denitrification apparatus 131 in front to exhausting waste gas pipeline 118, removes solids, remove SOx by desulfurizer 133 by electric bag filter 132, and outside being exhausted from system.
When so manufacturing described destructive distillation coal 2 by described dry coal 1, promote that the amount of inert gas that carbonizing gas 15 discharges from dry coal 1 increases according to the turnout of described destructive distillation coal 2, the manufacture PSA of rare gas element or the capacity of cryogenic separation device become large thereupon, and equipment cost and power cost increase.
In view of the above problems, in dry distillation of coal device 100 described in present embodiment, in order to recycle by the waste gas 13 outside exhausting waste gas pipeline 118 discharge system, also following action can be carried out.
To bleed flow control valve 141a on pipeline 141 and extraction fan 141b by controlling to be arranged on waste gas, a part for the waste gas 13 circulate in desulfurizer 133 via exhausting waste gas pipeline 118 circulates through bleeding and does not discharge outside system in waste gas bleeds pipeline 141.By information (temperature of waste gas 13) the control flow check adjustable valve 144a that basis is obtained by thermometer 141c, adjustment to combustioncatalysts device for deoxidizing 142 waste gas 13 circulated and the ratio passing through the waste gas 13 that exhaust gas bypass pipeline 144 circulates to combustioncatalysts device for deoxidizing 142, makes the waste gas 13 being preheated to the kindling temperature 150 DEG C ~ 350 DEG C of oxygen depletion fuel 17 by this heat exchanger 143 circulate to combustioncatalysts device for deoxidizing 142 by heat exchanger 143.By arranging exhaust gas bypass pipeline 144 and flow control valve 144a, even if the combustioncatalysts of combustioncatalysts device for deoxidizing 142 through time deterioration after because performance reduce and cause the kindling temperature of oxygen depletion fuel 17 to rise, also can regulate the preheating temperature of waste gas 13 thereupon.
By according to information (oxygen concn of rare gas element 14) the control flow check adjustable valve 145a obtained by oxygen sensor 147a, the oxygen depletion fuel 17 of specified amount is delivered in combustioncatalysts device for deoxidizing 142.That is, this oxygen concn is reduced to below prescribed value by feedback control by rare gas element 14.Described prescribed value is preferably 1.5%.So, reacted by the oxygen in rare gas element 14 and dry coal 1 and can suppress destructive distillation loss.
By being contacted with described combustioncatalysts by the mixed gas of described waste gas 13 with the pre-mixing of described oxygen depletion fuel 17 in described combustioncatalysts device for deoxidizing 142, the burning of this oxygen depletion fuel 17 reduces the oxygen concn of waste gas 13 after consuming the oxygen in this waste gas 13.The rare gas element 14 being reduced the oxygen concn of waste gas 13 by reaction heat now rises to 550 DEG C ~ 750 DEG C.Rare gas element 14 is delivered in the inner core 112 of dry distillation of coal apparatus main body 110 via rare gas element line of pipes 147.Regulate the operational throughput of rare gas element 14, make it reach 0.1Nm relative to the 1kg dry coal 1 being supplied to inner core 112
3~ 0.3Nm
3.So, the dividing potential drop of the carbonizing gas 15 on dry coal 1 surface reduces, and promotes that carbonizing gas 15 discharges from dry coal 1.
Therefore, described dry distillation of coal device 100 according to the present embodiment, by combustioncatalysts device for deoxidizing 142, the waste gas 13 produced by dry distillation of coal apparatus main body 110 processed and obtain rare gas element 14, combustioncatalysts device for deoxidizing 142 itself and running cost thereof are compared comparatively cheap with PSA with cryogenic separation device etc., thus can obtain with low cost the rare gas element 14 promoting that carbonizing gas 15 discharges from dry coal 1.
In addition, the temperature of the rare gas element 14 obtained by combustioncatalysts device for deoxidizing 142 is 550 DEG C ~ about 750 DEG C, thus the dry coal 1 in inner core 112 is by heated air 11 indirect heating, and by this rare gas element 14 direct heating.That is, the thermal source (destructive distillation thermal source) during destructive distillation dry coal 1, except heated air 11, also can utilize rare gas element 14.So, destructive distillation thermal source can reduce the heat supplied from the outside of dry distillation of coal apparatus main body 110, can reduce the flow of heated air 11, can reduce the thermal load of dry distillation of coal apparatus main body 110.Its result, with only using heated air 11 compared with the situation of destructive distillation thermal source, the total length of urceolus 113 (dry distillation of coal apparatus main body 110) can be shortened.
[the second embodiment]
Second embodiment of dry distillation of coal device of the present invention is described according to Fig. 2.
The structure of present embodiment is for changing the device for deoxidizing possessed in above-mentioned first embodiment shown in Fig. 1.Other structures are roughly the same with the foregoing shown in Fig. 1, give same label, and suitably the repetitive description thereof will be omitted at this to same equipment.
Described in present embodiment, dry distillation of coal device 200 possesses rare gas element generating apparatus 240 as shown in Figure 2, and described rare gas element generating apparatus 240 generates the rare gas element 24 promoting that carbonizing gas 15 discharges from dry coal 1 from waste gas 13.
Rare gas element generating apparatus 240 possesses waste gas and to bleed pipeline 241, and the bleed end side (base end side) of pipeline 141 and another side (front) of exhausting waste gas pipeline 118 of described waste gas is arranged with being connected between desulfurizer 133.Bleed another side (front) of pipeline 241 of waste gas is connected with the gas receiving port of alternate combustion device for deoxidizing (device for deoxidizing) 242.Waste gas pipeline 241 of bleeding is provided with flow control valve 241a and extraction fan 241b from end side (base end side).By control flow check adjustable valve 241a and extraction fan 241b, the part of the waste gas 13 circulated in desulfurizer 133 via exhausting waste gas pipeline 118 circulates to waste gas pipeline 241 of bleeding.
The end side (front) of oxygen depletion fuel feed line 245 is connected with near the gas receiving port (the sidewall portion of the adjacent upper part of aftermentioned apparatus main body 242b) of alternate combustion device for deoxidizing 242, described oxygen depletion fuel feed line 245 carries the hydrocarbon fuels such as such as Sweet natural gas, namely for consuming the oxygen depletion fuel 27 of oxygen in waste gas 13.Another side (base end side) of oxygen depletion fuel feed line 245 is connected with the tanks 246 of storage oxygen depletion fuel 27.Oxygen depletion fuel feed line 245 is provided with flow control valve 245a.
Alternate combustion device for deoxidizing 242 possesses the apparatus main body 242b that inside is provided with combustion chamber 242a.The bottom of apparatus main body 242b is provided with burner 242c.Insulation fuel 28 and insulation fuel combustion air 29 is supplied to burner 242c.Insulation fuel 28 burns in burner 242c, and combustion chamber 242a envrionment temperature remains on the high temperature of roughly 1200 DEG C.So, even if the concentration of the oxygen contained in waste gas 13 is the lower concentration of 2 ~ 5%, the oxygen of the lower concentration contained in this waste gas 13 also can be utilized to make oxygen depletion fuel 27 stable burning.
Apparatus main body 242b is provided with alternative type heat exchanger 242d.Alternative type heat exchanger 242d is made up of the 1st heat exchanger body 242da be disposed adjacent and the 2nd heat exchanger body 242db.1st heat exchanger body 242da is connected with waste gas and bleeds another side (front) of pipeline 241.2nd heat exchanger body 242db is connected with the end side (base end side) of rare gas element line of pipes 247.Waste gas bleed pipeline 241 front near and rare gas element line of pipes 247 base end side near be provided with rotary valve 242e, to bleed the front of pipeline 241 and the base end side of rare gas element line of pipes 247 by rotary valve 242e switching waste gas.So, the waste gas 13 of alternate combustion device for deoxidizing 242 is delivered to from waste gas pipeline 241 of bleeding, after being preheated to 800 DEG C ~ 1000 DEG C by the alternative type heat exchanger 242d of the gas receiving port being arranged on alternate combustion device for deoxidizing 242, be supplied to the combustion chamber 242a of alternate combustion device for deoxidizing 242.
Burnt in burner 242c together with insulation fuel 28 by oxygen depletion fuel 27, the oxygen in waste gas 13 is consumed gas and the rare gas element 24 of rear generation low oxygen concentration.
Another side (front) of rare gas element line of pipes 247 is connected with the end side (base end side) of the inner core 112 of dry distillation of coal apparatus main body 110.So, the rare gas element 24 reaching 70 DEG C ~ 150 DEG C in the alternative type heat exchanger 242d of gas discharge outlet being arranged on alternate combustion device for deoxidizing 242 is delivered to the inner core 112 of dry distillation of coal apparatus main body 110.
Rare gas element line of pipes 247 is provided with oxygen sensor (oxygen concentration testing unit) 247a, and described oxygen sensor (oxygen concentration testing unit) 247a can measure the oxygen concn of the rare gas element 24 of circulation in rare gas element line of pipes 247.
Oxygen sensor 247a via oxygen concn signal wire be arranged on the flow control valve 245a of oxygen depletion in fuel feed line 245 and be connected.The aperture of flow control valve 245a can regulate according to the information obtained by oxygen sensor 247a (oxygen concn of rare gas element 24).Namely, dry distillation of coal device 200 possesses not shown control device (amount of fuel addition control unit), this control device can according to the information obtained by oxygen sensor 247a (oxygen concn of rare gas element 24), control the addition of the oxygen depletion fuel 27 added by oxygen depletion fuel feed line 245, flow control valve 245a and tanks 246, make the oxygen concn of rare gas element 24 be such as less than 1.5%.
In this present embodiment, form pumping cells by bleed pipeline 241, described flow control valve 241a, described extraction fan 241b etc. of described waste gas.Fuel addition unit is formed by described oxygen depletion fuel feed line 245, described flow control valve 245a, described tanks 246 etc.Deacidification unit is formed by described alternate combustion device for deoxidizing 242, described fuel addition unit etc.Low oxygen concentration gas transport unit is formed by bleed pipeline 241, described flow control valve 241a, described extraction fan 241b, described rare gas element line of pipes 247 etc. of described waste gas.Low oxygen concentration gas supply unit is formed by described low oxygen concentration gas transport unit, described deacidification unit etc.Described dry distillation of coal device 200 is formed by described dry distillation of coal apparatus main body 110, described exhaust unit, described pumping cells, described low oxygen concentration gas supply unit, described amount of fuel addition control unit etc.In addition each device is made up of the equipment identical with above-mentioned first embodiment.
Possessing in dry distillation of coal device 200 described in the present embodiment of this rare gas element generating apparatus 240, by carrying out the main operation identical with the dry distillation of coal device 100 in above-mentioned first embodiment, destructive distillation coal 2 can be manufactured by described dry coal 1.
And, to bleed flow control valve 241a on pipeline 241 and extraction fan 241b by controlling to be arranged on waste gas, a part for the waste gas 13 circulate in desulfurizer 133 via exhausting waste gas pipeline 118 circulates through bleeding and does not discharge outside system in waste gas bleeds pipeline 241.By according to information (oxygen concn of rare gas element 24) the control flow check adjustable valve 245a obtained by oxygen sensor 247a, the oxygen depletion fuel 27 of specified amount is delivered in alternate combustion device for deoxidizing 242.That is, this oxygen concn is reduced to below prescribed value by feedback control by rare gas element 24.Described prescribed value is preferably 1.5%.So, reacted by the oxygen in rare gas element 24 and dry coal 1 and can suppress destructive distillation loss.
In described alternate combustion device for deoxidizing 242, waste gas 13 is delivered in the 242a of combustion chamber after being preheated to 800 DEG C ~ 1000 DEG C by alternative type heat exchanger 242d, thus oxygen depletion fuel 27 burn together with insulation fuel 28 consume in waste gas 13 oxygen after reduce the oxygen concn of waste gas 13.The rare gas element 24 reducing the oxygen concn of waste gas 13 reaches 70 DEG C ~ 150 DEG C by alternative type heat exchanger 242d, is delivered in the inner core 112 of dry distillation of coal apparatus main body 110 via rare gas element line of pipes 247.Regulate the operational throughput of rare gas element 24, make it reach 0.1Nm relative to the 1kg dry coal 1 being supplied to inner core 112
3~ 0.3Nm
3.So, the dividing potential drop of the carbonizing gas 15 on dry coal 1 surface reduces, and promotes that carbonizing gas 15 discharges from dry coal 1.
So in the present embodiment, by alternate combustion device for deoxidizing 242, the waste gas 13 produced by dry distillation of coal apparatus main body 110 is processed, thus can be used as and promote that the rare gas element 24 that carbonizing gas 15 discharges from dry coal 1 utilizes.
Therefore, described dry distillation of coal device 200 according to the present embodiment, by alternate combustion device for deoxidizing 242, the waste gas 13 produced by dry distillation of coal apparatus main body 110 processed and obtain rare gas element 24, alternate combustion device for deoxidizing 242 itself and running cost thereof are compared comparatively cheap with PSA with cryogenic separation device etc., thus can obtain with low cost the rare gas element 24 promoting that carbonizing gas 15 discharges from dry coal 1.
In addition, the temperature of the rare gas element 24 obtained by alternate combustion device for deoxidizing 242 is 70 DEG C ~ about 150 DEG C, thus the dry coal 1 in inner core 112 is by heated air 11 indirect heating, and by this rare gas element 24 direct heating.That is, the thermal source (destructive distillation thermal source) during destructive distillation dry coal 1, except heated air 11, also can utilize rare gas element 24.So, destructive distillation thermal source can reduce the heat supplied from the outside of dry distillation of coal apparatus main body 110, can reduce the flow of heated air 11, can reduce the thermal load of dry distillation of coal apparatus main body 110.Its result, with only using heated air 11 compared with the situation of destructive distillation thermal source, the total length of urceolus 113 (dry distillation of coal apparatus main body 110) can be shortened.
[the 3rd embodiment]
3rd embodiment of dry distillation of coal device of the present invention is described according to Fig. 3.
The structure of present embodiment is for changing the device for deoxidizing possessed in above-mentioned first embodiment shown in Fig. 1.Other structures are roughly the same with the foregoing shown in Fig. 1, give same label, and suitably the repetitive description thereof will be omitted at this to same equipment.
Described in present embodiment, dry distillation of coal device 300 possesses rare gas element generating apparatus 340 as shown in Figure 3, and described rare gas element generating apparatus 340 generates the rare gas element (not shown) promoting that carbonizing gas 15 discharges from dry coal 1 from waste gas 13.
Rare gas element generating apparatus 340 possesses waste gas and to bleed pipeline 341, and the bleed end side (base end side) of pipeline 141 and another side (front) of exhausting waste gas pipeline 118 of described waste gas is arranged with being connected between desulfurizer 133.
Waste gas another side (front) of pipeline 341 of bleeding is connected with the end side (base end side) of the inner core 112 of dry distillation of coal apparatus main body 110.Waste gas pipeline 341 of bleeding is provided with flow control valve 341a and extraction fan 341b from base end side.
And, waste gas pipeline 341 of bleeding is provided with under meter (exhaust gas flow measuring unit) 341c measured the flow of waste gas 13 of circulation in pipeline 341 of bleeding at waste gas, and is provided with oxygen sensor (oxygen concentration testing unit) 341d measured the oxygen concn of the waste gas 13 circulated pipeline 341 of bleeding at waste gas in.
In addition, waste gas is bled and is connected with the end side (front) of oxygen depletion fuel feed line 345 between the oxygen sensor 341d of pipeline 341 and another side (front), described oxygen depletion fuel feed line 345 carries the hydrocarbon fuels such as such as Sweet natural gas, namely for consuming the oxygen depletion fuel 37 of oxygen in waste gas 13.Another side (base end side) of oxygen depletion fuel feed line 345 is connected with the tanks 346 of storage oxygen depletion fuel 37.Oxygen depletion fuel feed line 345 is provided with flow control valve 345a.
Rare gas element generating apparatus 340 also possesses control device (calculating machine) 348, described control device (calculating machine) 348 is connected with under meter 341c via flow signal line, be connected with oxygen sensor 341d via oxygen concn signal wire, be connected with flow control valve 345a via control signal wire.Control device 348 is according to the information obtained by under meter 341c (flow of waste gas 13) and the information (oxygen concn of waste gas 13) that obtained by oxygen sensor 341d, the aperture of control flow check adjustable valve 345a, regulates and is delivered to waste gas and bleeds the operational throughput of the oxygen depletion fuel 37 in pipeline 341.
In this present embodiment, form pumping cells by bleed pipeline 341, described flow control valve 341a, described extraction fan 341b etc. of described waste gas.Fuel addition unit is formed by described oxygen depletion fuel feed line 345, described flow control valve 345a, described tanks 346 etc.Heated air supply unit is formed by described pumping cells etc.Low oxygen concentration gas supply unit is formed by described heated air supply unit, described fuel addition unit etc.Amount of fuel addition control unit is formed by described control device 348.Described dry distillation of coal device 300 is formed by described dry distillation of coal apparatus main body 110, described exhaust unit, described pumping cells, described low oxygen concentration gas supply unit, described amount of fuel addition control unit etc.In addition each device is made up of the equipment identical with above-mentioned first embodiment.
Possessing in dry distillation of coal device 300 described in the present embodiment of this rare gas element generating apparatus 340, by carrying out the main operation identical with the dry distillation of coal device 100 in above-mentioned first embodiment, destructive distillation coal 2 can be manufactured by described dry coal 1.
And, to bleed flow control valve 341a on pipeline 341 and extraction fan 341b by controlling to be arranged on waste gas, a part for the waste gas 13 circulate in desulfurizer 133 via exhausting waste gas pipeline 118 circulates through bleeding and does not discharge outside system in waste gas bleeds pipeline 341.Control device 348 is according to the information obtained by under meter 341c (flow of waste gas 13) and information (oxygen concn of waste gas 13) the control flow check adjustable valve 345a that obtained by oxygen sensor 341d, thus the oxygen depletion fuel 37 of specified amount is delivered to the end side (base end side) of the inner core 112 of dry distillation of coal apparatus main body 110 via waste gas pipeline 341 of bleeding.Control device 348 calculates the oxygen flow of waste gas 13 according to the information obtained by under meter 341c (flow of waste gas 13) and the information (oxygen concn of waste gas 13) that obtained by oxygen sensor 341d, oxygen flow for the described waste gas 13 calculated carries out feedback control to the flow of oxygen depletion fuel 37, make described oxygen depletion fuel 37 for more than oxygen equivalents, in other words make the excessive oxygen rate of oxygen depletion fuel 38 be less than 1.0.
Inner core 112 is heated by the heated air 11 be delivered in urceolus 113, thus heated transportation is to the waste gas 13 in inner core 112 and oxygen depletion fuel 37, this waste gas 13 and oxygen depletion fuel 37 have precedence over this waste gas 13 and dry coal 1 reacts, and reduce the oxygen concn of waste gas 13 after consuming the oxygen in this waste gas 13.By reducing the oxygen concn of waste gas 13, can utilize as rare gas element in inner core 112.
So in the present embodiment, pre-mixing oxygen depletion fuel 37 in the waste gas 13 produced by dry distillation of coal apparatus main body 110, thermal source during destructive distillation dry coal 1 is utilized to heat, thus reduce oxygen concn after consuming the oxygen in waste gas 13, can be used as the rare gas element promoting carbonizing gas 15 to discharge from dry coal 1 and utilize.
Therefore, described dry distillation of coal device 300 according to the present embodiment, by the information (flow of waste gas 13 according to the waste gas 13 of circulation in waste gas bleeds pipeline 341, the oxygen concn of waste gas 13) regulate oxygen depletion fuel 37 to be delivered to the operational throughput of waste gas 13, oxygen in the inner core 112 of dry distillation of coal apparatus main body 110 in described waste gas 13 reduces oxygen concn after consuming this oxygen by oxygen depletion fuel 37 burning, rare gas element can be obtained, under meter 341c, oxygen sensor 341d, oxygen depletion fuel feed line 345, flow control valve 345a, control device 348 itself and running cost thereof are compared comparatively cheap with PSA with cryogenic separation device etc., thus can obtain with low cost the rare gas element promoting that carbonizing gas 15 discharges from dry coal 1.
Oxygen depletion fuel 37 generates heat in inner core 112 with after the oxygen reaction in waste gas 13, thus the thermal source (destructive distillation thermal source) during destructive distillation dry coal 1 is except heated air 11, also can utilize the reaction heat of oxygen in waste gas 13 and oxygen depletion fuel 37.So, destructive distillation thermal source can reduce the heat supplied from the outside of dry distillation of coal apparatus main body 110, can reduce the flow of heated air 11, can reduce the thermal load of dry distillation of coal apparatus main body 110.Its result, with only using heated air 11 compared with the situation of destructive distillation thermal source, the total length of urceolus 113 (dry distillation of coal apparatus main body 110) can be shortened.
[other embodiments]
In addition, above to the dry distillation of coal device 100,200 being provided with 1 extraction fan 118c on exhausting waste gas pipeline 118,300 are illustrated, but a part for exhausting waste gas pipeline 118 also can be set as 2 cover systems by dry distillation of coal device, and arranges extraction fan and flow control valve respectively.
Accompanying drawing explanation
1 dry coal
2 destructive distillation coals
11 heated air
12 heated air
13 waste gas (mixed gas)
14 rare gas elementes (low oxygen concentration gas)
15 carbonizing gas (pyrolysis gas)
16 combustion-supporting fuel (ignition dope)
17 oxygen depletion fuel
24 rare gas elementes (low oxygen concentration gas)
27 oxygen depletion fuel
28 insulation fuel
29 insulation fuel combustion air
37 oxygen depletion fuel
110 dry distillation of coal apparatus main bodies
111 hoppers
112 inner cores (main cavity portion)
113 urceolus (sleeve pipe)
114 chutes
115 carbonizing gas vent lines
116 roasting kilns
117 heated air line of pipes
118 exhausting waste gas pipelines
118a boiler
118b flow control valve
118c extraction fan (sending gas blower)
119 heated air by-pass lines
119a boiler
119b flow control valve
121 exhaust gas recirculation pipelines
121a flow control valve
130 emission-control equipments
131 denitrification apparatus
132 electric bag filters
133 desulfurizers
140 rare gas element generating apparatus
141 waste gas are bled pipeline
141a flow control valve
141b extraction fan (attraction fan)
141c thermometer
142 combustioncatalysts device for deoxidizing (device for deoxidizing)
143 heat exchangers
144 exhaust gas bypass pipelines
144a flow control valve
145 oxygen depletion fuel feed line
145a flow control valve
146 tanks
147 rare gas element line of pipes
147a oxygen sensor
240 rare gas element generating apparatus
241 waste gas are bled pipeline
241a flow control valve
241b extraction fan (attraction fan)
242 alternate combustion device for deoxidizing (device for deoxidizing)
242a combustion chamber
242b apparatus main body
242c burner
242d alternative type heat exchanger
242da the 1st heat exchanger body
242db the 2nd heat exchanger body
242e rotary valve
245 oxygen depletion fuel feed line
245a flow control valve
246 tanks
247 rare gas element line of pipes
247a oxygen sensor
340 rare gas element generating apparatus
341 waste gas are bled pipeline
341a flow control valve
341b extraction fan (attraction fan)
341c under meter
341d oxygen sensor
345 oxygen depletion fuel feed line
345a flow control valve
346 tanks
348 control device (calculating machine)
Claims (10)
1. a dry distillation of coal device, it is characterized in that, possess: rotary kiln type dry distillation of coal apparatus main body, described rotary kiln type dry distillation of coal apparatus main body is by rotatable for the inner core inner side being supported on urceolus, heated air is supplied to the inside of described urceolus, coal is supplied to inside from the end side of described inner core simultaneously, by making described inner cylinder rotating, described coal is moved from the end side of described inner core to the other end side, and stir while heat destructive distillation, send destructive distillation coal and carbonizing gas from another side of described inner core;
Exhaust unit, described exhaust unit is connected with described urceolus and arranges, and discharges the described heated air in described urceolus;
Pumping cells, described pumping cells extracts a part for the described heated air of being discharged by described exhaust unit out; With,
Low oxygen concentration gas supply unit, described heated air is supplied in described inner core by described low oxygen concentration gas supply unit, and the concentration of the oxygen contained in the described heated air of being extracted out by described pumping cells is reduced.
2. dry distillation of coal device according to claim 1, is characterized in that,
Described low oxygen concentration gas supply unit has: deacidification unit, and described deacidification unit removes in described heated air the described oxygen contained; With, low oxygen concentration gas transport unit, the low oxygen concentration gas obtained by described deacidification unit is delivered to described inner core by described low oxygen concentration gas transport unit.
3. dry distillation of coal device according to claim 2, is characterized in that,
Described deacidification unit possesses: fuel addition unit, and fuel is added into described heated air by described fuel addition unit; With, combustioncatalysts, described combustioncatalysts is arranged to contact with the described heated air of adding described fuel.
4. dry distillation of coal device according to claim 3, is characterized in that,
Possess heating unit, described heating unit is arranged on described pumping cells, heats described heated air.
5. dry distillation of coal device according to claim 3, is characterized in that,
Possess desulfurization unit, described desulfurization unit is arranged on described exhaust unit, removes the oxysulfide contained in described heated air.
6. dry distillation of coal device according to claim 4, is characterized in that,
Possess: oxygen concentration testing unit, described oxygen concentration testing unit measures the oxygen concn of the described low oxygen concentration gas carried by described low oxygen concentration gas transport unit; With,
Amount of fuel addition control unit, described amount of fuel addition control unit is according to the information obtained by described heating gas flow measuring unit and described oxygen concentration testing unit, control the addition of the described fuel added by described fuel addition unit, make the oxygen concn of described low oxygen concentration gas be less than 1.5%.
7. dry distillation of coal device according to claim 2, is characterized in that,
Described deacidification unit possesses: alternate combustion device, described alternate combustion device have be transferred described heated air combustion chamber, be arranged on the burner in described combustion chamber and be arranged in described combustion chamber the alternative type heat exchanger being transferred described heated air position; With, fuel addition unit, fuel is added into described combustion chamber by described fuel addition unit.
8. dry distillation of coal device according to claim 7, is characterized in that,
Possess: oxygen concentration testing unit, described oxygen concentration testing unit measures the concentration of the oxygen contained in the described heated air of being carried by described low oxygen concentration gas transport unit; With,
Amount of fuel addition control unit, described amount of fuel addition control unit is according to the information obtained by described heating gas flow measuring unit and described oxygen concentration testing unit, control the addition of the described fuel added by described fuel addition unit, make the oxygen concn of described low oxygen concentration gas be less than 1.5%.
9. dry distillation of coal device according to claim 1, is characterized in that,
Described low oxygen concentration gas supply unit possesses: heated air supply unit, and the described heated air of being extracted out by described pumping cells is delivered in described inner core by described heated air supply unit; With, fuel addition unit, fuel is added into the described heated air be delivered to by described heated air supply unit in described inner core by described fuel addition unit.
10. dry distillation of coal device according to claim 9, is characterized in that,
Possess: heating gas flow measuring unit, described heating gas flow measuring unit measures the flow of the described heated air of being carried by described heated air supply unit;
Oxygen concentration testing unit, described oxygen concentration testing unit measures the concentration of the oxygen contained in the described heated air of being carried by described heated air supply unit; With,
Amount of fuel addition control unit, described amount of fuel addition control unit is according to the information obtained by described heating gas flow measuring unit and described oxygen concentration testing unit, control the addition of the described fuel added by described fuel addition unit, make the oxygen concn of described low oxygen concentration gas be less than 1.5%.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2013-172952 | 2013-08-23 | ||
| JP2013172952A JP2015040273A (en) | 2013-08-23 | 2013-08-23 | Coal carbonization apparatus |
| PCT/JP2014/065176 WO2015025588A1 (en) | 2013-08-23 | 2014-06-09 | Coal dry distillation device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN105408452A true CN105408452A (en) | 2016-03-16 |
Family
ID=52483373
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201480042493.3A Pending CN105408452A (en) | 2013-08-23 | 2014-06-09 | Coal dry distillation device |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20160177183A1 (en) |
| JP (1) | JP2015040273A (en) |
| CN (1) | CN105408452A (en) |
| AU (1) | AU2014310093B2 (en) |
| DE (1) | DE112014003870T5 (en) |
| WO (1) | WO2015025588A1 (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110105971B (en) * | 2019-06-18 | 2024-01-26 | 华泰永创(北京)科技股份有限公司 | Coke oven regenerator |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4797091A (en) * | 1987-03-13 | 1989-01-10 | Krupp Polysius Ag | Method and apparatus for utilizing the heat energy of domestic and commercial refuse |
| CN1066459A (en) * | 1992-06-13 | 1992-11-25 | 煤炭科学研究总院北京煤化学研究所 | A kind of process of coal pyrogenic decomposition of multi-stage rotary |
| CN1227128A (en) * | 1998-02-20 | 1999-09-01 | 株式会社明电舍 | Process and system for treating material containing noxious components |
| JP2003262315A (en) * | 2002-03-08 | 2003-09-19 | Meidensha Corp | Heat treatment method and facility for water containing organic matter |
| CN101351532A (en) * | 2005-10-26 | 2009-01-21 | 德维雷奥克斯控股有限公司 | Process, system and apparatus for passivating carbonaceous materials |
| CN102712846A (en) * | 2009-07-14 | 2012-10-03 | C20技术有限责任公司 | Process for treating coal by removing volatile components |
| CN103160301A (en) * | 2013-03-21 | 2013-06-19 | 何建祥 | Low-temperature carbonization apparatus and method for oil sand, oil sludge, oil shale and biomass |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5279712A (en) * | 1991-04-05 | 1994-01-18 | Pasco Nominees Pty Limited | Process and apparatus for the pyrolysis of carbonaceous material |
| JP2011127010A (en) * | 2009-12-18 | 2011-06-30 | Mitsubishi Heavy Ind Ltd | Coal reforming equipment |
| JP4719298B1 (en) * | 2010-03-24 | 2011-07-06 | 三菱重工業株式会社 | Modified coal production equipment |
| JP5804972B2 (en) * | 2012-02-24 | 2015-11-04 | 三菱重工業株式会社 | Modified coal production facility and control method thereof |
-
2013
- 2013-08-23 JP JP2013172952A patent/JP2015040273A/en active Pending
-
2014
- 2014-06-09 DE DE112014003870.9T patent/DE112014003870T5/en not_active Withdrawn
- 2014-06-09 CN CN201480042493.3A patent/CN105408452A/en active Pending
- 2014-06-09 US US14/908,231 patent/US20160177183A1/en not_active Abandoned
- 2014-06-09 AU AU2014310093A patent/AU2014310093B2/en not_active Ceased
- 2014-06-09 WO PCT/JP2014/065176 patent/WO2015025588A1/en active Application Filing
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4797091A (en) * | 1987-03-13 | 1989-01-10 | Krupp Polysius Ag | Method and apparatus for utilizing the heat energy of domestic and commercial refuse |
| CN1066459A (en) * | 1992-06-13 | 1992-11-25 | 煤炭科学研究总院北京煤化学研究所 | A kind of process of coal pyrogenic decomposition of multi-stage rotary |
| CN1227128A (en) * | 1998-02-20 | 1999-09-01 | 株式会社明电舍 | Process and system for treating material containing noxious components |
| JP2003262315A (en) * | 2002-03-08 | 2003-09-19 | Meidensha Corp | Heat treatment method and facility for water containing organic matter |
| CN101351532A (en) * | 2005-10-26 | 2009-01-21 | 德维雷奥克斯控股有限公司 | Process, system and apparatus for passivating carbonaceous materials |
| CN102712846A (en) * | 2009-07-14 | 2012-10-03 | C20技术有限责任公司 | Process for treating coal by removing volatile components |
| CN103160301A (en) * | 2013-03-21 | 2013-06-19 | 何建祥 | Low-temperature carbonization apparatus and method for oil sand, oil sludge, oil shale and biomass |
Also Published As
| Publication number | Publication date |
|---|---|
| AU2014310093A1 (en) | 2016-02-11 |
| DE112014003870T5 (en) | 2016-05-25 |
| WO2015025588A1 (en) | 2015-02-26 |
| US20160177183A1 (en) | 2016-06-23 |
| JP2015040273A (en) | 2015-03-02 |
| AU2014310093B2 (en) | 2016-12-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103604133B (en) | A kind of flue gas purification system of multi-pollutant integration dry removal and technique | |
| JP6121158B2 (en) | Exhaust gas treatment apparatus and exhaust gas treatment method | |
| AU2008352209A1 (en) | Method and apparatus of controlling exhaust gas in oxyfuel combustion boiler | |
| CN107131770B (en) | A kind of agglomeration for iron mine waste heat recycling collaboration emission reduction SOxAnd NOxMethod | |
| CN106996702A (en) | A kind of agglomeration for iron mine flue gas segmentation enrichment and UTILIZATION OF VESIDUAL HEAT IN emission reduction SOxAnd NOxMethod | |
| AU2009284975B2 (en) | Method for processing coal and coal processing system | |
| CN106669418A (en) | Device and method for comprehensively carrying out desulfurization, denitration and dioxin removing on steel sintering flue gas | |
| CN108273370A (en) | A kind of combination flue gas takes off white wet type fume sweetening device and its application method | |
| CN102363095A (en) | Dry flue gas desulfurization process method and dry flue gas desulfurization system thereof | |
| CN205216582U (en) | Iron and steel sintering flue gas is synthesized desulfurization, denitration and is got rid of device of dioxin | |
| AU2010316285A1 (en) | Method and apparatus for treatment of exhaust gas | |
| WO2011162344A1 (en) | Fuel treatment system, method for utilization of exhaust gas, and apparatus for utilization of exhaust gas | |
| CN105408452A (en) | Coal dry distillation device | |
| CN205613259U (en) | Sintering flue gas desulfurization denitration integration system | |
| CN1327939C (en) | High-efficient catalyzing smoke desulfurizing and denitrifying method and apparatus thereof | |
| JP3384435B2 (en) | Fluidized bed furnace exhaust gas desulfurization method | |
| CN208275227U (en) | A kind of combination flue gas takes off white wet type fume sweetening device | |
| CN103301745A (en) | Cyclone separator desulfurization device | |
| CN104121590B (en) | exhaust gas treatment device | |
| CN104822436A (en) | Exhaust gas processing apparatus and exhaust gas processing method | |
| CN203400632U (en) | Flue gas purification device | |
| CN103864509A (en) | Manufacture equipment of sulfur-containing product and manufacture method of sulfur-containing product | |
| CN212166999U (en) | Energy-saving flue desulphurization unit | |
| CN109675431A (en) | CO coupling inhibits the method and device of white haze in a kind of purifying smoke | |
| CN204891599U (en) | Coal fired boiler flue gas dry desulfurization low temperature denitrification facility |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20160316 |
|
| WD01 | Invention patent application deemed withdrawn after publication |