CN1632379A - Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor - Google Patents
Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor Download PDFInfo
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- CN1632379A CN1632379A CN 200410044168 CN200410044168A CN1632379A CN 1632379 A CN1632379 A CN 1632379A CN 200410044168 CN200410044168 CN 200410044168 CN 200410044168 A CN200410044168 A CN 200410044168A CN 1632379 A CN1632379 A CN 1632379A
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Abstract
A double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor, which relates to a fluidized bed incinerator device processing high concentration organic waste liquor. Another end of the low temperature flue 21 of the invention connects with high temperature oxidization circulation bet 60, the two ends of a high temperature air passage 30 connect separately to high temperature air preheating device (15) and low temperature gasification fluidized bed 50. The combination of low temperature gasification of low temperature gasification fluidized bed and high temperature oxidization of the high temperature oxidization circulation fluidized bet resolve the problem of bed material clustering and coking, and effectively gets rid of harmful gas such as HCL, SO[2] and NO[x] generated after burning the high concentration organic waste liquor, and effectively restrains generation of dioxins, and can completely burn down poisonous organic matter in the waste liquor, the rate of burning down reach more than 99.99 percents.
Description
Technical field:
The present invention relates to a kind of fluidized bed combustion device of handling high concentrated organic waste liquid, be specifically related to fluid bed low temperature gasification and recirculating fluidized bed high-temperature oxydation are combined, handle the device of various poisonous and harmful high concentrated organic waste liquids.
Background technology:
In recent years, along with China's rapid economy development, the high concentrated organic waste liquid that produces and discharge increases year by year, and the high concentrated organic waste liquid that annual oil, chemical industry, pharmacy, printing and dyeing and paper industry produce reaches tens million of tons.High concentrated organic waste liquid is one of primary pollution source that causes water environment pollution, and its heavy damage of discharging wantonly ecological environment threatens human health.Because wherein quite a few high concentrated organic waste liquid easily biological-degradable not adopts conventional biochemistry or chemical oxidization method to handle, exist length consuming time, occupation area of equipment big, handle problems such as not thorough.The device that uses more burning high concentrated organic waste liquid at present both at home and abroad is that liquid sprays stove, but needs fuel oil or combustion gas as auxiliary fuel, can not remove SO in the stove
2, HCl, operating cost is higher, not too meets present China's national situation, by contrast, fluidized bed incinerator application of cold temperature (850～900 ℃) combustion technology, heating power type NO
xCan ignore, adopt fractional combustion, fuel type NO
xGeneration can reduce significantly, be fit to handle all kinds of organic liquid wastes.For the organic liquid waste of sulfur-bearing, chlorine, in order to control SO
2, HCl discharging, can in recirculating fluidized bed, add lime stone or dolomite, be 2 o'clock 850 ℃ of left and right sides Ca/S mol ratios, can slough 85～90% SO
2With section H Cl.Can to adopt coal be auxiliary fuel to fluidized bed incinerator in addition, can reduce operating cost significantly, relatively meets present national conditions.But, adopt fluidized combustion to handle high concentrated organic waste liquid and also have some problems: the inorganic sodium, the sylvite that contain variable concentrations in (1) common high concentrated organic waste liquid, can not form the bed material because of ashless behind the liquid waste incineration, need to adopt the medium fluid bed, usually medium adopt river sand or quartz sand, inorganic sodium, sylvite and SiO
2(main component of sand) reaction generates sodium metasilicate (glass), its fusing point is in 635～815 ℃ of scopes, under the fluid bed running temperature, be molten condition, cause the conglomeration of bed material easily, even serious coking, can't guarantee that fluid bed normally moves, so many advantages of fluidized bed incinerator can't be brought into play; (2) under the fluid bed normal operating temperature (850～900 ℃), absorbent (lime) dechlorination efficiency has only 20～30% when burning chloride high concentrated organic waste liquid, burn the back like this and produce concentration higher H Cl, can cause high temperature, the cold end corrosion of waste heat boiler on the one hand; The possibility that also can cause the bioxin growing amount to increase on the other hand.
Summary of the invention:
The purpose of this invention is to provide a kind of two temperature double bed gasification oxidation fluidized bed incinerators of handling high concentrated organic waste liquid, it has the bed material coking problem that the existing fluidized bed incinerator of solution takes place when burning contains the waste liquid of inorganic sodium, sylvite, and problem such as fluidized bed incinerator inner absorbent dechlorination efficiency is low, realize high-efficiency desulfurization, dechlorination, denitration, reduce the bioxin discharging, reach organic matter and destroy clearance by fire greater than 99.99% characteristics.The present invention comprises low temperature gasification fluid bed 50, high-temperature oxydation recirculating fluidized bed 60, cyclone separator 3, first feeding back device 4, low temperature flue 21, high temperature cyclone separator 11, second feeding back device 12, high-temperature exhaust air flue 23, high-temperature air preheater 15, economizer 17, first low-temperature air preheater 18, second low-temperature air preheater 24, auxiliary air pipeline 28, primary air pipeline 29, high temperature air pipeline 30; One side on cyclone separator 3 tops is fixedlyed connected with the top of low temperature gasification fluid bed 50, fixedly connected with a side of first feeding back device 4 in the lower end of cyclone separator 3, the opposite side of first feeding back device 4 is fixedlyed connected with the bottom of low temperature gasification fluid bed 50, one end of low temperature flue 21 is fixedlyed connected with the upper end of cyclone separator 3, the other end of low temperature flue 21 is connected with the bottom of high-temperature oxydation recirculating fluidized bed 60, one side on high temperature cyclone separator 11 tops is fixedlyed connected with top one side of high-temperature oxydation recirculating fluidized bed 60, fixedly connected with a side of second feeding back device 12 in the lower end of high temperature cyclone separator 11, the opposite side of second feeding back device 12 is fixedlyed connected with the bottom of high-temperature oxydation recirculating fluidized bed 60, the inlet of high-temperature exhaust air flue 23 is fixedlyed connected with the upper end of high temperature cyclone separator 11, high-temperature air preheater 15 is arranged on the top in the high-temperature exhaust air flue 23, first low-temperature air preheater 18 and second low-temperature air preheater 24 are separately positioned on the bottom in the high-temperature exhaust air flue 23, the two ends of auxiliary air pipeline 28 are connected with first low-temperature air preheater 18 with high-temperature oxydation recirculating fluidized bed 60, the two ends of primary air pipeline 29 are connected with second low-temperature air preheater 24 with high-temperature oxydation recirculating fluidized bed 60, economizer 17 is fixed in the high-temperature exhaust air flue 23 of first low-temperature air preheater, 18 upsides, economizer 17 is connected with the top of high-temperature oxydation recirculating fluidized bed 60, and the two ends of high temperature air pipeline 30 are connected with the bottom of high-temperature air preheater 15 with low temperature gasification fluid bed 50 respectively.Low temperature gasification fluid bed low temperature gasification of the present invention and the combination of high-temperature oxydation recirculating fluidized bed high-temp combustion have solved fluidized bed material conglomeration, coking problem, have removed the HCl, the SO that produce behind the high concentration organic waste liquid burning effectively
2And NO
xDeng pernicious gas, in stove, suppress the generation of bioxin fully, and the toxic organic compound in the waste liquid thoroughly can be destroyed by fire, destroy clearance by fire and reach more than 99.99%.This device has almost solved all difficult problems of utilizing the fluidized combustion high concentrated organic waste liquid to run into, and the high-temperature oxydation recirculating fluidized bed is auxiliary fuel with the coal, has reduced operating cost, meets the present national conditions of China.
Description of drawings:
Fig. 1 is an overall structure schematic diagram of the present invention.
The specific embodiment:
The specific embodiment one: (referring to Fig. 1) present embodiment is made up of low temperature gasification fluid bed 50, high-temperature oxydation recirculating fluidized bed 60, cyclone separator 3, first feeding back device 4, low temperature flue 21, high temperature cyclone separator 11, second feeding back device 12, high-temperature exhaust air flue 23, high-temperature air preheater 15, economizer 17, first low-temperature air preheater 18, second low-temperature air preheater 24, auxiliary air pipeline 28, primary air pipeline 29, high temperature air pipeline 30; One side on cyclone separator 3 tops is fixedlyed connected with the top of low temperature gasification fluid bed 50, fixedly connected with a side of first feeding back device 4 in the lower end of cyclone separator 3, the opposite side of first feeding back device 4 is fixedlyed connected with the bottom of low temperature gasification fluid bed 50, one end of low temperature flue 21 is fixedlyed connected with the upper end of cyclone separator 3, the other end of low temperature flue 21 is connected with the bottom of high-temperature oxydation recirculating fluidized bed 60, one side on high temperature cyclone separator 11 tops is fixedlyed connected with top one side of high-temperature oxydation recirculating fluidized bed 60, fixedly connected with a side of second feeding back device 12 in the lower end of high temperature cyclone separator 11, the opposite side of second feeding back device 12 is fixedlyed connected with the bottom of high-temperature oxydation recirculating fluidized bed 60, the inlet of high-temperature exhaust air flue 23 is fixedlyed connected with the upper end of high temperature cyclone separator 11, high-temperature air preheater 15 is arranged on the top in the high-temperature exhaust air flue 23, first low-temperature air preheater 18 and second low-temperature air preheater 24 are separately positioned on the bottom in the high-temperature exhaust air flue 23, the two ends of auxiliary air pipeline 28 are connected with first low-temperature air preheater 18 with high-temperature oxydation recirculating fluidized bed 60, the two ends of primary air pipeline 29 are connected with second low-temperature air preheater 24 with high-temperature oxydation recirculating fluidized bed 60, economizer 17 is fixed in the high-temperature exhaust air flue 23 of first low-temperature air preheater, 18 upsides, economizer 17 is connected with the top of high-temperature oxydation recirculating fluidized bed 60, and the two ends of high temperature air pipeline 30 are connected with the bottom of high-temperature air preheater 15 with low temperature gasification fluid bed 50 respectively.Low temperature gasification fluid bed 50 is made up of body of heater 32, lime silo and charging gear 19, first ash releasing tube 25, auxiliary burner 20, air distribution plate 31, waste liquid spray gun 51; Air distribution plate 31 is fixed on the bottom in the body of heater 32, fixedly connected with the downside of air distribution plate 31 in the upper end of first ash releasing tube 25, the lower end of first ash releasing tube 25 is located at the outside of body of heater 32 lower ends, bottom space in the downside of air distribution plate 31 and the body of heater 32 forms fluid bed air compartment 5, central space in the upside of air distribution plate 31 and the body of heater 32 forms fluid bed emulsion zone 1, upper space in the body of heater 32 forms fluid bed dilute-phase zone 2, auxiliary burner 20 is fixed on fluid bed air compartment 5 outer walls, lime silo and charging gear 19 are fixed on the outer wall of body of heater 32 on fluid bed emulsion zone 1 top, the outer end of auxiliary burner 20 is connected with an end of high temperature air pipeline 30, and waste liquid spray gun 51 is fixed on fluid bed emulsion zone 1 body of heater 32 outward.High-temperature oxydation recirculating fluidized bed 60 is by bed body 33, fluidized bed air distribution plate 34, second ash releasing tube 26, water-cooling wall 9, drum 10, coal bunker and feeding system 22, rotation overfiren air port 7, rotation smoke inlet 8 is formed, fluidized bed air distribution plate 34 is fixed on the bottom in the body 33, fixedly connected with the downside of fluidized bed air distribution plate 34 in the upper end of second ash releasing tube 26, the lower end of second ash releasing tube 26 is located at the outside of body of heater 33 lower ends, form air air compartment 13 between the bottom in the downside of fluidized bed air distribution plate 34 and the bed body 33, form high-temperature oxydation circulating fluidized bed combustor 6 in the bed body 33 of fluidized bed air distribution plate 34 upsides, rotation smoke inlet 8 is fixed in the bed body 33 of fluidized bed air distribution plate 34 upsides, and be connected with low temperature flue 21, primary air pipeline 29 is connected with air air compartment 13 in the bed body 33, coal bunker and feeding system 22 are fixed on the outer wall of the bed body 33 between rotation smoke inlet 8 and the fluidized bed air distribution plate 34, rotation overfiren air port 7 is fixed in the bed body 33 that rotates smoke inlet 8 upsides and with auxiliary air pipeline 28 and is connected, water-cooling wall 9 is fixed in the bed body 33 of rotation overfiren air port 7 upsides, water-cooling wall 9 is connected with the drum 10 of bed body 33 outsides, and drum 10 is connected by pipeline 27 with economizer 17.
The specific embodiment two: the difference of (referring to Fig. 1) present embodiment and the specific embodiment one is that increasing has high temperature superheater 14 on the high-temperature exhaust air flue 23 between high temperature cyclone separator 11 and the high-temperature air preheater 15.On the high-temperature exhaust air flue 23 between high-temperature air preheater 15 and the economizer 17, increase low temperature superheater 16 is arranged.Other composition is identical with the specific embodiment one with annexation.
The present invention can day processing organic liquid waste 200～1000t/d.After being preheating to 500～550 ℃ through high-temperature air preheater 15, cold air sends into fluid bed air compartment 5, inlet at fluid bed air compartment 5 is arranged auxiliary burner 20, when temperature is lower than 500 ℃ in the fluid bed emulsion zone 1, start, automatically stop when being higher than 600 ℃, guarantee that temperature is controlled at 500～600 ℃ in the fluid bed emulsion zone 1.High concentrated organic waste liquid is directly sent in the zone of positive pressure of fluid bed emulsion zone 1 after spray gun 51 atomizings.Air distribution plate 31 above the fluid bed air compartment 5 can adopt water-cooled, guarantees that air distribution plate 31 is indeformable under the higher air temperature.Add the CaO particulate absorbent of particle diameter in the bed material (river sand) on fluid bed emulsion zone 1 less than 2mm, be used to remove the HCl gas that chloride organic liquid waste gasification back produces, under 500～600 ℃, can remove about HCl85～90%, adopt bubbling bed mode of operation in the fluid bed emulsion zone 1, reduce the elutriation amount of bed material and additive, adopt cyclone separator 3 that bed material and the additive that flue gas carries out is transmitted back in the fluid bed by first feeding back device 4, improve the utilization rate of additive.When blast is increased to 15000Pa in the fluid bed air compartment 5,, keep the material balance in the fluid bed emulsion zone 1 from first ash releasing tube, the 25 discharge section bed material of fluid bed emulsion zone 1.In the upper fluid-bed dilute-phase zone 2 is the pressure-fired anoxycausis, and temperature is controlled at 500～600 ℃.The flue gas that removes 85～90%HCl enters in the high-temperature oxydation circulating fluidized bed combustor 6 through rotation smoke inlet 8 through cyclone separator 3 outlets.In high-temperature oxydation circulating fluidized bed combustor 6, the auxiliary fuel coal is sent in the high-temperature oxydation circulating fluidized bed combustor 6 by coal bunker and feeding system 22,850～900 ℃ of burnings down, in the combustion chamber, arrange tangential rotation overfiren air port 7, give burning required auxiliary air, wind-warm syndrome is about 150 ℃, and the heat that burning produces absorbs by water-cooling wall 9, and the combustor exit temperature remains on 850～900 ℃.When the blast of air air compartment 13 surpasses 14000Pa,, keep the material balance in the recirculating fluidized bed by second ash releasing tube, 26 discharge section bed material.Send into air air compartment 13 from the air of low-temperature air preheater 24, send into high-temperature oxydation circulating fluidized bed combustor 6 from the air of low-temperature air preheater 18 through rotation overfiren air port 7 and be used for strengthening mixing, guarantee fully burning.In high-temperature oxydation circulating fluidized bed combustor 6, adopt fractional combustion (being anoxycausis below the secondary wind, is oxygen-enriched combusting more than the secondary wind) control NO
xDischarging, NO
xConcentration of emission can be lower than 200mg/m
3By adding lime stone, when Ca/S=2.0, can remove the SO more than 80%
2, guaranteeing that simultaneously the toxic organics in the waste liquid thoroughly destroys by fire, the organic clearance that destroys by fire is greater than 99.99%.Enter back-end ductwork from the outlet of high-temperature oxydation circulating fluidized bed combustor, arrange high temperature superheater 14, high-temperature air preheater 15, low temperature superheater 16, economizer 17, low-temperature air preheater 18 and low-temperature air preheater 24 successively.Delivery temperature is 140～150 ℃ and enters atmosphere after entering deduster and chimney.The 3.82MPa that produces, 450 ℃ of superheated steams can be used for generating, join the 3000KW-12000KW generating set.1.6～2.45MPa the saturated vapor that produces when day handling the following organic liquid waste of 200t can be used for heating and process steam quantity of steam≤20t/h.
Claims (4)
1, handle two temperature double bed gasification oxidation fluidized bed incinerators of high concentrated organic waste liquid, it comprises low temperature gasification fluid bed (50), high-temperature oxydation recirculating fluidized bed (60), cyclone separator (3), first feeding back device (4), low temperature flue (21), high temperature cyclone separator (11), second feeding back device (12), high-temperature exhaust air flue (23), high-temperature air preheater (15), economizer (17), first low-temperature air preheater (18), second low-temperature air preheater (24), auxiliary air pipeline (28), primary air pipeline (29), high temperature air pipeline (30); A side that it is characterized in that cyclone separator (3) top is fixedlyed connected with the top of low temperature gasification fluid bed (50), fixedly connected with a side of first feeding back device (4) in the lower end of cyclone separator (3), the opposite side of first feeding back device (4) is fixedlyed connected with the bottom of low temperature gasification fluid bed (50), one end of low temperature flue (21) is fixedlyed connected with the upper end of cyclone separator (3), the other end of low temperature flue (21) is connected with the bottom of high-temperature oxydation recirculating fluidized bed (60), one side on high temperature cyclone separator (11) top is fixedlyed connected with top one side of high-temperature oxydation recirculating fluidized bed (60), fixedly connected with a side of second feeding back device (12) in the lower end of high temperature cyclone separator (11), the opposite side of second feeding back device (12) is fixedlyed connected with the bottom of high-temperature oxydation recirculating fluidized bed (60), the inlet of high-temperature exhaust air flue (23) is fixedlyed connected with the upper end of high temperature cyclone separator (11), high-temperature air preheater (15) is arranged on the top in the high-temperature exhaust air flue (23), first low-temperature air preheater (18) and second low-temperature air preheater (24) are separately positioned on the bottom in the high-temperature exhaust air flue (23), the two ends of auxiliary air pipeline (28) are connected with first low-temperature air preheater (18) with high-temperature oxydation recirculating fluidized bed (60), the two ends of primary air pipeline (29) are connected with second low-temperature air preheater (24) with high-temperature oxydation recirculating fluidized bed (60), economizer (17) is fixed in the high-temperature exhaust air flue (23) of first low-temperature air preheater (18) upside, economizer (17) is connected with the top of high-temperature oxydation recirculating fluidized bed (60), and the two ends of high temperature air pipeline (30) are connected with the bottom of high-temperature air preheater (15) with low temperature gasification fluid bed (50) respectively.
2, the two temperature double beds of processing high concentrated organic waste liquid according to claim 1 gasification oxidation fluidized bed incinerators is characterized in that low temperature gasification fluid bed (50) is made up of body of heater (32), lime silo and charging gear (19), first ash releasing tube (25), auxiliary burner (20), air distribution plate (31), waste liquid spray gun (51); Air distribution plate (31) is fixed on the bottom in the body of heater (32), fixedly connected with the downside of air distribution plate (31) in the upper end of first ash releasing tube (25), the lower end of first ash releasing tube (25) is located at the outside of body of heater (32) lower end, bottom space in the downside of air distribution plate (31) and the body of heater (32) forms fluid bed air compartment (5), central space in the upside of air distribution plate (31) and the body of heater (32) forms fluid bed emulsion zone (1), upper space in the body of heater (32) forms fluid bed dilute-phase zone (2), auxiliary burner (20) is fixed on fluid bed air compartment (5) outer wall, lime silo and charging gear (19) are fixed on the outer wall of body of heater (32) on fluid bed emulsion zone (1) top, the outer end of auxiliary burner (20) is connected with an end of high temperature air pipeline (30), and waste liquid spray gun (51) is fixed on the outer body of heater (32) of fluid bed emulsion zone (1).
3, two temperature double bed gasification oxidation fluidized bed incinerators of processing high concentrated organic waste liquid according to claim 1, it is characterized in that high-temperature oxydation recirculating fluidized bed (60) is by bed body (33), fluidized bed air distribution plate (34), second ash releasing tube (26), water-cooling wall (9), drum (10), coal bunker and feeding system (22), rotation overfiren air port (7), rotation smoke inlet (8) is formed, fluidized bed air distribution plate (34) is fixed on the bottom in the body (33), fixedly connected with the downside of fluidized bed air distribution plate (34) in the upper end of second ash releasing tube (26), the lower end of second ash releasing tube (26) is located at the outside of body of heater (33) lower end, form air air compartment (13) between the bottom in the downside of fluidized bed air distribution plate (34) and the bed body (33), form high-temperature oxydation circulating fluidized bed combustor (6) in the bed body (33) of fluidized bed air distribution plate (34) upside, rotation smoke inlet (8) is fixed in the bed body (33) of fluidized bed air distribution plate (34) upside, and be connected with low temperature flue (21), primary air pipeline (29) is connected with an air air compartment (13) that body (33) is interior, coal bunker and feeding system (22) are fixed on the outer wall of the bed body (33) between rotation smoke inlet (8) and the fluidized bed air distribution plate (34), rotation overfiren air port (7) is fixed in the bed body (33) that rotates smoke inlet (8) upside and with auxiliary air pipeline (28) and is connected, water-cooling wall (9) is fixed in the bed body (33) of rotation overfiren air port (7) upside, cold water wall (9) is connected with the drum (10) of bed body (33) outside, and drum (10) is connected by pipeline (27) with economizer (17).
4, two temperature double bed gasification oxidation fluidized bed incinerators of processing high concentrated organic waste liquid according to claim 1, it is characterized in that last the increasing of high-temperature exhaust air flue (23) between high temperature cyclone separator (11) and high-temperature air preheater (15) has high temperature superheater (14), the high-temperature exhaust air flue (23) between high-temperature air preheater (15) and low-temperature air preheater (18) is gone up to increase low temperature superheater (16) and economizer (17).
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410044168 CN1259523C (en) | 2004-12-24 | 2004-12-24 | Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200410044168 CN1259523C (en) | 2004-12-24 | 2004-12-24 | Double temperature double bed gasification, oxidization and fluidized bed incinerator for disposing high concentration organic effluent liquor |
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| CN1259523C CN1259523C (en) | 2006-06-14 |
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Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100398907C (en) * | 2006-01-04 | 2008-07-02 | 东南大学 | Fluidized bed incineration method for industrial organic waste liquid with high salt content |
| CN102997247A (en) * | 2012-12-25 | 2013-03-27 | 季栋梁 | System and method for incineration treatment of saliferous waste residue, saliferous waste water and stink waste gas |
| CN105240818A (en) * | 2015-11-10 | 2016-01-13 | 李聪 | Combustion boiler of power station |
| CN105258113A (en) * | 2015-10-26 | 2016-01-20 | 隋恒睿 | Low-heating-value liquid and solid fluidized bed boiler and combustion technology |
| CN105627319A (en) * | 2015-11-29 | 2016-06-01 | 集美大学 | Garbage incineration processing system and method for reducing toxicity of fly ash |
| CN105948150A (en) * | 2016-04-26 | 2016-09-21 | 天津理工大学 | Process and system for recycling high-chloride high-concentration non-degradable organic wastewater |
| CN109297037A (en) * | 2018-10-30 | 2019-02-01 | 大连科林能源工程技术开发有限公司 | A kind of environment-friendly type resource utilization system of organic exhaust gas containing chlorine |
| CN110160029A (en) * | 2019-05-28 | 2019-08-23 | 浙江大学 | A kind of system and method for biomass carbon vapour coproduction |
| CN110448854A (en) * | 2019-08-14 | 2019-11-15 | 杨皓 | A kind of method of toxic liquid organic mixture recycling |
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2004
- 2004-12-24 CN CN 200410044168 patent/CN1259523C/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100398907C (en) * | 2006-01-04 | 2008-07-02 | 东南大学 | Fluidized bed incineration method for industrial organic waste liquid with high salt content |
| CN102997247A (en) * | 2012-12-25 | 2013-03-27 | 季栋梁 | System and method for incineration treatment of saliferous waste residue, saliferous waste water and stink waste gas |
| CN102997247B (en) * | 2012-12-25 | 2015-03-18 | 季栋梁 | System and method for incineration treatment of saliferous waste residue, saliferous waste water and stink waste gas |
| CN105258113A (en) * | 2015-10-26 | 2016-01-20 | 隋恒睿 | Low-heating-value liquid and solid fluidized bed boiler and combustion technology |
| CN105240818A (en) * | 2015-11-10 | 2016-01-13 | 李聪 | Combustion boiler of power station |
| CN105627319A (en) * | 2015-11-29 | 2016-06-01 | 集美大学 | Garbage incineration processing system and method for reducing toxicity of fly ash |
| CN105948150A (en) * | 2016-04-26 | 2016-09-21 | 天津理工大学 | Process and system for recycling high-chloride high-concentration non-degradable organic wastewater |
| CN109297037A (en) * | 2018-10-30 | 2019-02-01 | 大连科林能源工程技术开发有限公司 | A kind of environment-friendly type resource utilization system of organic exhaust gas containing chlorine |
| CN109297037B (en) * | 2018-10-30 | 2023-12-15 | 大连科林能源工程技术开发有限公司 | Environment-friendly recycling system for chlorine-containing organic waste gas |
| CN110160029A (en) * | 2019-05-28 | 2019-08-23 | 浙江大学 | A kind of system and method for biomass carbon vapour coproduction |
| CN110160029B (en) * | 2019-05-28 | 2024-05-10 | 浙江大学 | System and method for co-production of biomass charcoal and steam |
| CN110448854A (en) * | 2019-08-14 | 2019-11-15 | 杨皓 | A kind of method of toxic liquid organic mixture recycling |
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| Publication number | Publication date |
|---|---|
| CN1259523C (en) | 2006-06-14 |
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