CN104560072A - Pyrolysis system and pyrolysis method for organic wastes - Google Patents
Pyrolysis system and pyrolysis method for organic wastes Download PDFInfo
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- CN104560072A CN104560072A CN201410831821.XA CN201410831821A CN104560072A CN 104560072 A CN104560072 A CN 104560072A CN 201410831821 A CN201410831821 A CN 201410831821A CN 104560072 A CN104560072 A CN 104560072A
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- 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
- C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
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- 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
- C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
- C10B49/02—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge
- C10B49/04—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge while moving the solid material to be treated
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- 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
- C10B57/08—Non-mechanical pretreatment of the charge, e.g. desulfurization
- C10B57/10—Drying
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Abstract
The invention provides a pyrolysis system and pyrolysis method for organic wastes. The pyrolysis system for the organic wastes comprises a crushing device, a drying device, a rotating-bed pyrolysis oven, a pyrolysis solid processing device, a cooling and purifying device, an oil storage tank, and a heat accumulating type rotary heat exchanger, wherein the rotating-bed pyrolysis oven is suitable for performing pyrolysis treatment on pyrolysis raw materials, and a rotatable material distributing tray for containing the pyrolysis raw materials is arranged in the rotating-bed pyrolysis oven, the material distributing tray divides the interior of the rotating-bed pyrolysis oven into a pyrolysis chamber positioned above the material distributing tray and a heat supply chamber positioned below the material distributing tray , wherein a plurality of through holes for enabling the pyrolysis chamber to be communicated with the heat supply chamber are formed in the material distributing tray; the heat accumulating type rotary heat exchanger is connected with the cooling and purifying device and a hot-air inlet of the rotating-bed pyrolysis oven for pyrolyzing heated non-condensable gases. Through the adoption of the pyrolysis system of organic wastes, disclosed by the embodiment of the invention, the organic wastes can be effectively pyrolyzed.
Description
Technical field
The present invention relates to pyrolysis art, specifically, the present invention relates to a kind of thermal decomposition of organic wastes system and method for pyrolysis.
Background technology
For a large amount of waste in the current whole world, the main method landfill of traditional process waste, compost, burning three kinds of technology, but along with the increasing fast of waste, these three kinds of technology demonstrate its defect day by day, as landfill takies tract, composting process treatment capacity is little, efficiency is low, burn and easily produce secondary pollution, obnoxious flavour can be produced, particularly produce dioxin (Dioxins) toxic pollutant, and be cause one of haze weather origin cause of formation, make it interrupted in industrial application.
Pyrolytic technique is that organism is heated to 500 ~ 1000 DEG C under the state of anaerobic or anoxic, make solid carbon thing (coal, biomass, rubbish, junked tire, waste and old organism, organic sludge etc.), be converted into based on the depot energy of combustion gas (pyrolysis gas), oil fuel and pyrolytic carbon.With in gas heating pyrolytic technique, multiplex high-temperature flue gas directly enters in pyrolysis oven as heating carrier and conducts heat through material bed realizations, is back to use in pyrolytic process mentions as the technology of gas heating carrier is rare for product pyrolysis gas.
Summary of the invention
The present invention is intended to solve one of technical problem in correlation technique at least to a certain extent.For this reason, it is high that one object of the present invention is to propose a kind of pyrolysis efficiency, the low thermal decomposition of organic wastes system of energy consumption and utilize this system to carry out the method for pyrolysis organic waste.
According to the thermal decomposition of organic wastes system of the embodiment of the present invention, comprising: shredder assembly, described shredder assembly is suitable for described organic waste to carry out break process, obtains granular pyrolysis feed, moisture eliminator, described moisture eliminator is connected with described shredder assembly and is suitable for carrying out drying and processing to the pyrolysis feed through described break process, rotating bed pyrolysis oven, described rotating bed pyrolysis oven is connected with described moisture eliminator and is suitable for carrying out pyrolysis processing to described pyrolysis feed, and have rotatable in described rotating bed pyrolysis oven, for holding the cloth tray of described pyrolysis feed, described cloth tray will be separated into the pyrolysis chamber be positioned at above described cloth tray in described rotating bed pyrolysis oven, be positioned at the heat supply chamber below described cloth tray, wherein, described cloth tray has the through hole of the described pyrolysis chamber of multiple connection and heat supply chamber, described heat supply chamber there is hot air intake, described pyrolysis chamber has opening for feed and air outlet, described opening for feed is connected with described pretreatment unit, pyrolysis solids treatment device, described solid product treatment unit is connected with described solid outlet, cooling and refining plant, described cooling is connected with described air outlet with refining plant, the oil gas product produced in described pyrolysis chamber is carried out gas-oil separation obtain oil and non-condensable gas, storage tank, described storage tank is connected with refining plant with described cooling, heat accumulating type rotary heat exchanger, described heat accumulating type rotary heat exchanger is connected with the hot air intake of refining plant with described rotating bed pyrolysis oven with described cooling respectively, after being heated by described non-condensable gas, be used for described pyrolysis processing.
According to the thermal decomposition of organic wastes system of the embodiment of the present invention, wherein rotating bed pyrolysis oven adopts the method for gas heat supply, first hot gas enters in the heat supply chamber of cloth tray bottom from hot air intake, secondly, hot gas enters multiple through holes cloth tray from the bottom even of cloth tray, and through the pyrolysis feed layer in cloth tray, contact heat-exchanging abundant with pyrolysis feed, pyrolysis feed issues raw pyrolytic reaction at the environment of starvation thus.Thus, the rotating bed pyrolysis oven with said structure adopts gas heating mode, and make hot gas make pyrolysis feed reach pyrolysis temperature from the bottom penetrator bed of material of pyrolysis feed layer, hot gas can be made thus fully to contact with the inner raw material of the layer of pyrolysis feed layer, the contact area of further raising thermal source and pyrolysis feed, thus the degree of being heated evenly improving pyrolysis feed.Therefore, the thermal decomposition of organic wastes system of the above embodiment of the present invention is adopted can to improve pyrolysis efficiency and the degree of pyrolysis of pyrolysis material.
In addition, thermal decomposition of organic wastes system according to the present invention also has following additional technical feature:
Particularly, described heat accumulating type rotary heat exchanger comprises: insulation shell, is limited with chamber in described housing, and described housing has the first entrance, the first outlet, the second entrance and the second outlet, dividing plate, described dividing plate to be located in described chamber and described chamber is separated into accumulation of heat chamber and heat release chamber, heat storage, described heat storage is located at the middle part of described heat release chamber and the middle part of accumulation of heat chamber, described second outlet is formed at the top of described heat release chamber, described second entrance is formed at the bottom of described heat release chamber, combustion chamber is formed at the top of described accumulation of heat chamber, combustion chamber and the first entrance conducting, first outlet is formed at the bottom of described accumulation of heat chamber, wherein, described first entrance and described cooling are connected with refining plant with non-condensable gas described in receiving unit, described second entrance is connected to accept non-condensable gas described in another part with refining plant with cooling, described second outlet is connected with described hot air intake.Adopt above-mentioned heat accumulating type rotary heat exchanger can significantly improve heat exchange efficiency between gas.
Further, described heat accumulating type rotary heat exchanger comprises denitration catalyst reaction chamber.
Further, described denitration catalyst reaction chamber comprises: spray ammonia or urea grid, ammonia or urea and SCR catalytic reaction chamber.
Further, described thermal decomposition of organic wastes system also comprises smoke eliminator, and described smoke eliminator is connected with described moisture eliminator.Avoid the direct exhaust emission environment of flue gas thus.
Preferentially, the through hole in described cloth tray is circular hole and/or fin square hole, and wherein, the diameter of described circular hole is 2 ~ 6 millimeters, and the long limit of described fin square hole is 10 ~ 15 millimeters, broadside is 3 ~ 5 millimeters.What can significantly improve hot gas thus passes the efficiency passed through, and then the heat transfer effect of raising and pyrolysis feed.
According to a second aspect of the invention, the invention allows for and utilize foregoing thermal decomposition of organic wastes system to carry out the method for pyrolysis organic waste, comprising:
Utilize described shredder assembly that described organic waste is carried out break process, obtain granular pyrolysis feed;
Moisture eliminator is utilized to carry out drying and processing to the pyrolysis feed through described break process;
Described pyrolysis feed particle through drying and processing is carried out cloth from the described opening for feed of the pyrolysis chamber of described rotating bed pyrolysis oven to described cloth tray, and in described heat supply chamber, pass into hot gas from described hot air intake, make described pyrolysis feed particle generation pyrolysis, obtain solid product and oil gas product;
In described pyrolysis solids treatment device, described solid product is carried out processing and collecting;
In described cooling and refining plant, described oil gas product is carried out gas-oil separation process, to obtain oil and non-condensable gas, and described oil is stored in described storage tank;
Described in the combustion chamber combustion part of described heat accumulating type rotary heat exchanger, non-condensable gas or the outer combustible gas liberated heat that supplies carry out heat treated to non-condensable gas described in another part, and the described non-condensable gas after heating is used for described pyrolysis.
In some embodiments of the invention, it is 600 ~ 950 degrees Celsius for heating the temperature of the high-temperature flue gas of non-condensable gas after the combustion chamber combustion of described heat accumulating type rotary heat exchanger.
In some embodiments of the invention, the temperature of the described non-condensable gas after heating is 550 ~ 850 degrees Celsius.
In some embodiments of the invention, described pyrolysis processing carries out 1 ~ 3 hour under 550 ~ 800 degrees Celsius.
Accompanying drawing explanation
Fig. 1 is the structural representation of thermal decomposition of organic wastes system according to an embodiment of the invention.
Fig. 2 is the structural representation of rotating bed pyrolysis oven according to an embodiment of the invention.
Fig. 3 is the structural representation of cloth tray in rotating bed pyrolysis oven according to an embodiment of the invention.
Fig. 4 is the structural representation of heat accumulating type rotary heat exchanger according to an embodiment of the invention.
Fig. 5 is the structural representation of heat accumulating type rotary heat exchanger in accordance with another embodiment of the present invention.
Fig. 6 is the structural representation of thermal decomposition of organic wastes system in accordance with another embodiment of the present invention.
Fig. 7 is the schema of method for pyrolysis in accordance with another embodiment of the present invention.
Embodiment
Be described below in detail embodiments of the invention, the example of described embodiment is shown in the drawings, and wherein same or similar label represents same or similar element or has element that is identical or similar functions from start to finish.Be exemplary below by the embodiment be described with reference to the drawings, be intended to for explaining the present invention, and can not limitation of the present invention be interpreted as.
In describing the invention, it will be appreciated that, term " " center ", " longitudinal direction ", " transverse direction ", " length ", " width ", " thickness ", " on ", D score, " front ", " afterwards ", " left side ", " right side ", " vertically ", " level ", " top ", " end " " interior ", " outward ", " clockwise ", " counterclockwise ", " axis ", " radial direction ", orientation or the position relationship of the instruction such as " circumference " are based on orientation shown in the drawings or position relationship, only the present invention for convenience of description and simplified characterization, instead of indicate or imply that the device of indication or element must have specific orientation, with specific azimuth configuration and operation, therefore limitation of the present invention can not be interpreted as.
In addition, term " first ", " second " only for describing object, and can not be interpreted as instruction or hint relative importance or imply the quantity indicating indicated technical characteristic.Thus, be limited with " first ", the feature of " second " can express or impliedly comprise one or more these features.In describing the invention, the implication of " multiple " is two or more, unless otherwise expressly limited specifically.
In the present invention, unless otherwise clearly defined and limited, the term such as term " installation ", " being connected ", " connection ", " fixing " should be interpreted broadly, and such as, can be fixedly connected with, also can be removably connect, or integral; Can be mechanical connection, also can be electrical connection; Can be directly be connected, also indirectly can be connected by intermediary, can be the connection of two element internals or the interaction relationship of two elements.For the ordinary skill in the art, above-mentioned term concrete meaning in the present invention can be understood as the case may be.
In the present invention, unless otherwise clearly defined and limited, fisrt feature second feature " on " or D score can be that the first and second features directly contact, or the first and second features are by intermediary indirect contact.And, fisrt feature second feature " on ", " top " and " above " but fisrt feature directly over second feature or oblique upper, or only represent that fisrt feature level height is higher than second feature.Fisrt feature second feature " under ", " below " and " below " can be fisrt feature immediately below second feature or tiltedly below, or only represent that fisrt feature level height is less than second feature.
According to an aspect of the present invention, the present invention proposes a kind of thermal decomposition of organic wastes system.According to the thermal decomposition of organic wastes system of the embodiment of the present invention, comprising: shredder assembly, shredder assembly is suitable for organic waste to carry out break process, obtains granular pyrolysis feed; Moisture eliminator, moisture eliminator is connected with shredder assembly and is suitable for carrying out drying and processing to the pyrolysis feed through break process; Rotating bed pyrolysis oven, rotating bed pyrolysis oven is suitable for carrying out pyrolysis processing to described pyrolysis feed, and have in rotating bed pyrolysis oven rotatable, for holding the cloth tray of pyrolysis feed, cloth tray is positioned at be separated in rotating bed pyrolysis oven in pyrolysis chamber above cloth tray, be positioned at heat supply chamber below cloth tray, wherein, cloth tray has the through hole of multiple connection pyrolysis chamber and heat supply chamber, heat supply chamber has hot air intake, and pyrolysis chamber has opening for feed, air outlet and solid outlet; Pyrolysis solids treatment device, pyrolysis solids treatment device is connected with solid outlet; Cooling and refining plant, cooling is connected with air outlet with refining plant, the oil gas product produced in pyrolysis chamber is carried out gas-oil separation obtain oil and non-condensable gas; Storage tank, storage tank is connected with refining plant with cooling; Heat accumulating type rotary heat exchanger, heat accumulating type rotary heat exchanger is connected with the hot air intake of refining plant with rotating bed pyrolysis oven with cooling respectively, after being heated by non-condensable gas, be used for pyrolysis processing.
According to the thermal decomposition of organic wastes system of the embodiment of the present invention, wherein rotating bed pyrolysis oven adopts the method for gas heat supply, first hot gas enters in the heat supply chamber of cloth tray bottom from hot air intake, secondly, hot gas enters multiple through holes cloth tray from the bottom even of cloth tray, and through the pyrolysis feed layer in cloth tray, contact heat-exchanging abundant with pyrolysis feed, pyrolysis feed issues raw pyrolytic reaction at the environment of starvation thus.Thus, the rotating bed pyrolysis oven with said structure adopts gas heating mode, hot gas can be made to make pyrolysis feed reach pyrolysis temperature from the bottom penetrator bed of material of pyrolysis feed layer, hot gas can be made thus fully to contact with the inner raw material of the layer of pyrolysis feed layer, the contact area of further raising thermal source and pyrolysis feed, thus the degree of being heated evenly improving pyrolysis feed.Therefore, the thermal decomposition of organic wastes system of the above embodiment of the present invention is adopted can to improve pyrolysis efficiency and the degree of pyrolysis of pyrolysis material.
The thermal decomposition of organic wastes system 100 of the above embodiment of the present invention is described in detail below with reference to Fig. 1-Fig. 5.This thermal decomposition of organic wastes system 100 is adopted to become solid matter as useful products such as carbon black, pyrolysis oil and pyrolysis gas complete for waste materials containing carbon pyrolysis.
According to the thermal decomposition of organic wastes system 100 of the embodiment of the present invention, as shown in Figure 1, comprise: shredder assembly 10, moisture eliminator 20, rotating bed pyrolysis oven 30, pyrolysis solids treatment device 40, cooling and refining plant 50, storage tank 60, heat accumulating type rotary heat exchanger 70.
According to a particular embodiment of the invention, as shown in Figure 1, shredder assembly 10 is suitable for organic waste to carry out break process, obtains granular pyrolysis feed; Moisture eliminator 20 is connected with shredder assembly 10 and is suitable for carrying out drying and processing to the pyrolysis feed through break process.Thus, utilize shredder assembly 10 and moisture eliminator 20 can carry out pre-treatment by the organic waste effectively before pyrolysis, removing moisture wherein, to improve pyrolysis efficiency.
According to a particular embodiment of the invention, as shown in Figure 2, have in rotating bed pyrolysis oven 30 rotatable, for holding the cloth tray 31 of pyrolysis feed, cloth tray is positioned at be separated in rotating bed pyrolysis oven in pyrolysis chamber 32 above cloth tray, be positioned at heat supply chamber 33 below cloth tray.The circular ring that cloth tray is arranged horizontally, the circular cavity that heat supply chamber is arranged horizontally, wherein, cloth tray 31 as shown in Figure 3 has the through hole 311 of multiple connection pyrolysis chamber and heat supply chamber, heat supply chamber there is hot air intake 34, described hot air intake 34 is multiple, and inside the annulus being evenly distributed in heat supply chamber cavity, pyrolysis chamber has opening for feed (not shown), air outlet 35 and solid outlet (not shown); Pyrolysis solids treatment device 40 is connected with solid outlet (not shown).According to a particular embodiment of the invention, above-mentioned rotating bed pyrolysis oven 30 is suitable for carrying out pyrolysis processing to pyrolysis feed.
According to a particular embodiment of the invention, the through hole 311 in above-mentioned rotating bed pyrolysis oven 30 in cloth tray 31 can be circular hole and/or fin square hole.According to a particular embodiment of the invention, the diameter of circular hole can be 2 ~ 6 millimeters, and the long limit of fin square hole can be 10 ~ 15 millimeters, broadside can be 3 ~ 5 millimeters.Therefore by adopting the through hole with above-mentioned size can prevent pyrolysis feed from draining in heat supply chamber, hot gas can be significantly improved simultaneously and enter speed in pyrolysis chamber, and then improving hot gas to the heating efficiency of pyrolysis material, improving pyrolysis efficiency.
According to a particular embodiment of the invention, cloth tray preferably has aperture and is preferably the stainless steel plate that the circular hole of 4 millimeters and aperture are the fin square hole (not providing in figure) of 3 millimeters * 12 millimeters.Advantageously bottom cloth tray, the hot gas of 550 ~ 800 degrees Celsius is directly contacted with the material in cloth tray by circular hole and/or fin square hole thus.In cloth tray, the selection of through-hole aperture size should be conducive to gas by pyrolysis feed layer and effectively avoid pyrolysis feed to be fallen heat supply chamber under cloth tray by this hole.Therefore, in cloth tray, the selection of through-hole aperture size determined by pyrolysis feed granular size, the selection gist of pyrolysis feed grain diameter obtained by actual production, when after material particular diameter is greater than 30 millimeters, the pyrolysis in 2 hours of material difficulty is saturating, when material particular diameter is less than 5 millimeters, individual layer material pyrolysis time is short, but fabric thickness is limited, because the thicker bed of material makes bed of material air resistance bigger than normal, unfavorable gas passes, and is also unfavorable for the pyrolysis of upper materials.Therefore, pyrolysis feed optimum grain-diameter is 5 ~ 30 millimeters, and fabric thickness is preferably 50 ~ 400 millimeters, and in the cloth tray of rotating bed pyrolysis oven, to be the circular hole of 4 millimeters and/or aperture be through hole that the fin square hole of 3 millimeters * 12 millimeters is best.Pyrolysis efficiency can be significantly improved thus.
According to a particular embodiment of the invention, the temperature being provided to the hot gas in heat supply chamber can be 550 ~ 850 degrees Celsius, can provide enough heats thus to pyrolysis feed and pyrolysis chamber, and then improves pyrolysis efficiency.According to a particular embodiment of the invention, the temperature of carrying out pyrolysis processing in pyrolysis chamber is 480 ~ 800 degrees Celsius.Therefore, temperature is provided to be that hot gas to the heat supply chamber of 550 ~ 850 degrees Celsius effectively can ensure that pyrolysis feed reaches 480 ~ 800 degrees Celsius of concurrent raw pyrolytic reactions.
According to a particular embodiment of the invention, above-mentioned rotating bed pyrolysis oven take hot gas as thermal source, and from the type of heating that the bottom of pyrolysis feed is passed, the contact area of hot gas and pyrolysis feed can be significantly improved thus, especially can contact with the pyrolysis feed of pyrolysis feed layer inside, improve the degree of being heated evenly of pyrolysis feed, therefore, adopt the rotating bed pyrolysis oven with said structure feature can significantly improve pyrolysis efficiency.
Thermal decomposition of organic wastes system according to the above embodiment of the present invention can also comprise: cooling and refining plant 50, storage tank 60.Cooling is connected with air outlet 35 with refining plant 50, the oil gas product produced in pyrolysis chamber is carried out gas-oil separation obtain oil and non-condensable gas; Storage tank 60 is connected with refining plant 50 with cooling, for storing the oil being separated and obtaining.
According to a particular embodiment of the invention, the oil gas product that in rotating bed pyrolysis oven, pyrolysis produces is discharged from the air outlet of pyrolysis chamber roof and is entered in cooling and refining plant 50, oil after cooling in oil gas product defines liquid oils and non-condensable gas, be separated by oil gas product thus, liquid oils is stored in storage tank 60.
According to a particular embodiment of the invention, thermal decomposition of organic wastes system can also comprise: heat accumulating type rotary heat exchanger 70, heat accumulating type rotary heat exchanger 70 is connected with the hot air intake 34 of rotating bed pyrolysis oven 30 with refining plant 50 with cooling respectively, after being heated by non-condensable gas, be used for pyrolysis processing.Therefore, return for pyrolytic reaction after the non-condensable gas that can be produced pyrolysis by heat accumulating type rotary heat exchanger 70 is heated.Adopt the thermal decomposition of organic wastes system of the above embodiment of the present invention to significantly improve energy utilization rate thus, reduce pyrolysis energy consumption.
According to a particular embodiment of the invention, as shown in Figure 4, above-mentioned heat accumulating type rotary heat exchanger 70 specifically comprises following assemblies: insulation shell 71, housing has the first entrance 72, second entrance 73, first outlet 74 and the second outlet 75, first entrance 72 is connected with receiving unit non-condensable gas with cooling with refining plant 70, second entrance 73 is connected to accept another part non-condensable gas with refining plant 40 with cooling, second outlet 75 is connected with hot air intake 14, one or more pairs of heat storage 76, multipair heat storage is positioned at housing 71; Combustion chamber 77, combustion chamber is positioned at described insulation shell and closes on described first entrance, and combustion chamber is suitable for the burning of part non-condensable gas.
Thus, first entrance 72 (high-temperature flue gas entry) front end of above-mentioned heat accumulating type rotary heat exchanger 70 has combustion chamber 77, pyrolysis produce the part non-condensable gas that obtains can directly in combustion chamber 77 burning produce high-temperature flue gas and enter heat storage 76 heat exchange, also combustible gas can be provided to replace non-condensable gas to burn in combustion chamber 77 as combustion gas by the external world to obtain high-temperature flue gas, can also directly provide high-temperature flue gas to enter heat storage 76 heat exchange by the external world.
According to a particular embodiment of the invention, the specific works principle of heat accumulating type rotary heat exchanger 70 as shown in Figure 5, when heat accumulating type rotary heat exchanger 70 runs, heat storage 76 is axle rotary motion longitudinally, other each equipment transfixions, part non-condensable gas from the first entrance 72 enter combustion chamber 77 combustion and by heat storage 76 time, heat storage 76 starts accumulation of heat, heat storage 76 constantly heats up, when the heat storage 76 after accumulation of heat heats up rotates to opposite side, another part non-condensable gas of normal temperature enters heat storage 76 from opposite side second entrance 73, non-condensable gas is by heat storage 76 process, heat exchange is carried out with heat storage 76, normal temperature non-condensable gas constantly heats up, finally leave heat accumulating type rotary heat exchanger 70 from the second outlet 75 to enter in rotating bed pyrolysis oven for pyrolysis.With heat storage 76 longitudinally axle continuous rotation rotation, combustion parts non-condensable gas and another normal temperature non-condensable gas reach Continuous Heat Transfer effect.According to a particular embodiment of the invention, the part non-condensable gas of burning also directly can release heat by outer for high-temperature flue gas is alternative, or is substituted for inflammable gas by outer, after burning, release heat.Therefore, above-mentioned heat accumulating type rotary heat exchanger 70 pairs of non-condensable gases adaptability of carrying out preheating is stronger.
In addition, adopt above-mentioned heat accumulating type rotary heat exchanger also can add corresponding catalyzer as requested in heat accumulating type rotary heat exchanger, the one-tenth changing non-condensable gas gas assigns to meet pyrolysis requirement, also directly can carry out denitration process to flue gas, reduces back segment operation cost of investment.
Thus, by adopting above-mentioned heat accumulating type rotary heat exchanger 70 can heat the non-condensable gas that pyrolysis produces, and then for the pyrolytic reaction of the pyrolysis feed in rotating bed pyrolysis oven.The non-condensable gas produced in thermal decomposition of organic wastes system can be returned the thermal source for thermal decomposition of organic wastes system thus, significantly can reduce energy consumption.
According to a particular embodiment of the invention, mainly containing the reducing gas of low-carbon (LC) hydro carbons in the non-condensable gas that pyrolysis produces, carbon monoxide, hydrogen and methane etc. are comprised.Therefore, amount of heat can be released for preheating another part non-condensable gas at the combustion chamber 77 combustion part non-condensable gas of heat accumulating type rotary heat exchanger 70, this save outer for combustible gas, save energy consumption.In addition, adopt the non-condensable gas of pyrolysis generation itself as the thermal source of pyrolytic reaction, not only can not affect the carrying out of pyrolytic reaction, also can not affect the quality of non-condensable gas, guarantee the calorific value of non-condensable gas.According to a particular embodiment of the invention, adopt gaseous heat-carrier, pyrolysis feed is heated evenly, temperature plateau, and fluctuation range is little, easy to control.The thermal decomposition of organic wastes system thus with said structure of the present invention improves utilization rate of heat value, and facility investment is few, easy handling.
As shown in Figure 5, according to a particular embodiment of the invention, above-mentioned heat accumulating type rotary heat exchanger 70 also comprises denitration catalyst reaction further, and out of stock reaction chamber is positioned at described insulation shell and closes on described first outlet 74.According to a particular embodiment of the invention, denitration catalyst reaction chamber comprises: ammonia-spraying grid or spray urea grid 78, ammonia or urea and SCR catalytic reaction chamber 79.Wherein, ammonia or urea are provided by import 781.Directly can carry out denitration process to flue gas thus, reduce back segment operation cost of investment.
As shown in Figure 6, according to a particular embodiment of the invention, above-mentioned thermal decomposition of organic wastes system comprises further: smoke eliminator 80 and chimney 90, and smoke eliminator 80 is connected with moisture eliminator 20, and moisture eliminator 20 exports 74 with first of heat accumulating type rotary heat exchanger 70 and is connected; Chimney 90 is connected with smoke eliminator 80.After can first utilizing the heat of the flue gas of discharge in heat accumulating type rotary heat exchanger 70 to carry out drying and processing to organic waste thus, then in smoke eliminator 80, carry out purifying treatment chimney 90 discharge, by, avoid contaminate environment.
According to a further aspect in the invention, the invention allows for a kind of method utilizing above-mentioned pyrolysis system to carry out pyrolysis.Specifically comprise the following steps: to utilize shredder assembly that described organic waste is carried out break process, obtain granular pyrolysis feed; Moisture eliminator is utilized to carry out drying and processing to the pyrolysis feed through break process; Described pyrolysis feed particle through drying and processing is carried out cloth from the opening for feed of the pyrolysis chamber of rotating bed pyrolysis oven to cloth tray, and in heat supply chamber, pass into hot gas from hot air intake, make pyrolysis feed particle generation pyrolysis, obtain solid product and oil gas product; In pyrolysis solids treatment device, solid product is carried out processing and collecting; In cooling and refining plant, oil gas product is carried out gas-oil separation process, to obtain oil and non-condensable gas, and oil is stored in described storage tank; Heat accumulating type rotary heat exchanger combustion chamber combustion part non-condensable gas or outer for combustible gas liberated heat, heat treated is carried out to another part non-condensable gas, and the non-condensable gas after heating is used for pyrolysis.
According to the method for pyrolysis of the embodiment of the present invention, wherein rotating bed pyrolysis oven adopts the method for gas heat supply, first hot gas enters in the heat supply chamber of cloth tray bottom from hot air intake, secondly, hot gas enters multiple through holes cloth tray from the bottom even of cloth tray, and through the pyrolysis feed layer in cloth tray, contact heat-exchanging abundant with pyrolysis feed, pyrolysis feed issues raw pyrolytic reaction at the environment of starvation thus.Thus, employing has above-mentioned rotating bed pyrolysis oven, hot gas can be made to make pyrolysis feed reach pyrolysis temperature from the bottom penetrator bed of material of pyrolysis feed layer, hot gas can be made thus fully to contact with the inner raw material of the layer of pyrolysis feed layer, the contact area of further raising thermal source and pyrolysis feed, thus the degree of being heated evenly improving pyrolysis feed.Therefore, the method for pyrolysis of the above embodiment of the present invention is adopted can to improve pyrolysis efficiency and the degree of pyrolysis of pyrolysis material.
The method for pyrolysis according to the embodiment of the present invention is described in detail below with reference to Fig. 7.
(1) raw materials pretreatment
First, using obtain after pre-treatment until the organic waste of pyrolysis can as the pyrolysis feed of pyrolysis.Pre-treatment can comprise following one or more step:
Break process: organic waste is carried out break process.
Drying and processing: broken good hot organic waste needed to dry before entering rotating bed pyrolysis oven, the temperature of oven dry can be 120 ~ 280 degrees Celsius.Current use more widely solid drying machine is rotary dryer, and dry thermal source can be the heat smoke from heat accumulating type rotary heat exchanger, by reverse with organic waste direct contact heat transfer, thus realizes the drying of organic waste.
(2) in rotating bed pyrolysis oven, pyrolysis processing is carried out
Secondly, the pyrolysis feed particle above-mentioned pre-treatment obtained carries out cloth from the opening for feed of the pyrolysis chamber of rotating bed pyrolysis oven to cloth tray, in heat supply chamber, pass into hot gas from hot air intake, make pyrolysis feed particle generation pyrolysis, obtain solid product and oil gas product.
According to a particular embodiment of the invention, above-mentioned pretreated pyrolysis feed particle is entered entrance storehouse by rotating bed pyrolysis oven upper feed inlet, in rotating bed pyrolysis oven under the effect of cloth scraper plate, pyrolysis feed particle is formed pyrolysis feed granular layer by cloth equably in rotating bed pyrolysis oven cloth tray.According to a particular embodiment of the invention, the thickness of pyrolysis feed granular layer can be correlated with according to the hole size in the size of pyrolysis feed particle and cloth tray, particularly, should suitably control relation between three, contriver finds, when pyrolysis feed optimum grain-diameter is 5 ~ 30 millimeters, fabric thickness is preferably 50 ~ 400 millimeters, through hole to be the circular hole of 4 millimeters and/or aperture the be fin square hole of 3 millimeters * 12 millimeters in the cloth tray of rotating bed pyrolysis oven.Can ensure that hot gas passes the speed of through hole and pyrolysis feed granular layer thus, and then raising fully contacts with pyrolysis feed particle, improve pyrolysis feed particles by heat uniformity coefficient, improve pyrolysis efficiency.
According to a particular embodiment of the invention, the temperature of the anti-raw pyrolytic reaction of above-mentioned pyrolysis feed is 480 ~ 800 degrees Celsius, and it is complete only to need to get final product pyrolysis in 1 ~ 3 hour at such a temperature.Pyrolysis efficiency can be significantly improved thus.
(3) thermal source presentation mode
Further, in rotating bed pyrolysis oven, supply thermal source and carry out pyrolytic reaction.According to another specific embodiment of the present invention, thermal source can provide according to following manner.Such as, utilize the non-condensable gas of generation in rotating bed pyrolysis oven as thermal source after preheating, wherein, preheating can adopt part non-condensable gas or outer combustible gas and the high-temperature flue gas of supplying to carry out.
According to a particular embodiment of the invention, utilization is outer supplies non-condensable gas after preheating as thermal source.First, when driving furnace lifting, external flammable gas produces high-temperature flue gas in the combustion chamber combustion of heat accumulating type rotary heat exchanger, also directly high-temperature flue gas can be provided by the external world, heat accumulating type rotary heat exchanger is oppositely entered respectively by the high-temperature flue gas entry of heat accumulating type rotary heat exchanger and non-condensable gas entrance with the outside non-condensable gas of normal temperature, heat exchange is carried out in rotation heat storage in heat accumulating type rotary heat exchanger, the high temperature non-condensable gas produced enters bottom the cloth tray of rotating bed pyrolysis oven, in heat supply chamber high temperature non-condensable gas being evenly distributed on bottom cloth tray by furnace bottom gas distributor, then high temperature non-condensable gas from bottom to top by the through hole in cloth tray as gaseous heat-carrier through the pyrolysis feed granular layer in cloth tray, with pyrolysis feed direct contact heat transfer, pyrolysis feed carries out pyrolysis under the environment of starvation, be that the heating material of 5 ~ 30 millimeters is to pyrolysis temperature 550 ~ 800 degrees Celsius by particle diameter.Pyrolysis feed destructive distillation is become gas, liquid, solid body carbonaceous products, left rotating bed pyrolysis oven by the solid product after pyrolysis by rotating bed pyrolysis oven solid outlet.
According to a particular embodiment of the invention, above-mentioned method for pyrolysis also comprises: be used for pyrolysis after being heated in heat accumulating type rotary heat exchanger by the non-condensable gas produced in rotating bed pyrolysis oven.The non-condensable gas that pyrolysis can be utilized to produce thus returns for pyrolytic reaction, not only can save energy consumption, can not affect the composition of non-condensable gas simultaneously, guarantee that non-condensable gas can continue recycle, reduce costs so that at utmost low.
According to a particular embodiment of the invention, above-mentioned method for pyrolysis also comprises: heat accumulating type rotary heat exchanger combustion chamber combustion part non-condensable gas or outer for combustible gas liberated heat, heat treated is carried out to another part non-condensable gas, and the non-condensable gas after heating is used for pyrolysis.The utilization ratio of non-condensable gas can be improved thus further, eliminate outer for combustible gas simultaneously, save energy consumption.In addition, adopt the non-condensable gas of pyrolysis generation itself as the thermal source of pyrolytic reaction, not only can not affect the carrying out of pyrolytic reaction, also can not affect the quality of non-condensable gas, guarantee the calorific value of non-condensable gas.According to a particular embodiment of the invention, adopt gaseous heat-carrier, pyrolysis feed is heated evenly, temperature plateau, and fluctuation range is little, easy to control.The thermal decomposition of organic wastes system thus with said structure of the present invention improves utilization rate of heat value, and facility investment is few, in operation.
According to a particular embodiment of the invention, in the above-mentioned non-condensable gas as heat accumulating type rotary heat exchanger thermal source, can be 1:1 for the part non-condensable gas of combustion heat release and the gas volume ratio of another part non-condensable gas.The in particular cases volume ratio 1:3 of both adjustable gas.Part non-condensable gas also can replace non-condensable gas directly to burn in a combustion chamber for combustible gas by outer.
According to a particular embodiment of the invention, it is 600 ~ 950 degrees Celsius for heating the temperature of the high-temperature flue gas of non-condensable gas after the combustion chamber combustion of heat accumulating type rotary heat exchanger, after heat storage heat exchange, flue-gas temperature is down to less than 300 degrees Celsius, the temperature of the above-mentioned non-condensable gas thermal source for rotating bed pyrolysis oven obtained through heat accumulating type rotary heat exchanger is 550 ~ 850, fully pyrolysis feed can be heated to 550 ~ 800 degrees Celsius thus and pyrolytic reactions occur.Further, enter in gas cleaning unit after cooling, removing flue dust and nitrogen sulfur compound, after reaching emission standard, flue gas is arranged outward by chimney.
According to another specific embodiment of the present invention, it is 700 ~ 950 degrees Celsius for heating the temperature of the high-temperature flue gas of non-condensable gas after heat accumulating type rotary heat exchanger combustion, after heat storage heat exchange, flue-gas temperature is down to less than 300 degrees Celsius, the temperature of the above-mentioned non-condensable gas thermal source for rotating bed pyrolysis oven obtained through heat accumulating type rotating commutator is 600 ~ 850 degrees Celsius, fully pyrolysis feed can be heated to 580 ~ 750 degrees Celsius thus and pyrolytic reactions occur.
(4) solid product process
According to a particular embodiment of the invention, solid product is carried out processing and collecting in pyrolysis solids treatment device.Particularly, in rotating bed pyrolysis oven, under the effect of discharging spiral, entered pyrolysis solids treatment device by feed opening by the solid product after pyrolysis to cool.The process of cooling of solid product can by spraying quenching or the cooling of band water-cooling jacket spiral, and solid product is cooled to less than 80 degrees Celsius by 450 DEG C-750 degrees Celsius, and cooling after product enters in solid resultant product collection storehouse and stores.Cool the high-temperature steam obtained and deliver to afterheat boiler system recycling.
(5) oil gas product process
According to a particular embodiment of the invention, the oil gas product produced in rotating bed pyrolysis oven is carried out gas-oil separation process in cooling and refining plant, to obtain oil and non-condensable gas, and oil is stored in storage tank.According to a particular embodiment of the invention, enter the temperature of oil gas product after in cooling and clean unit and be reduced to less than 28 degrees Celsius, portion gas is condensed into liquid.The oil product obtained after liquid separation can deep processing or to sell directly outward further, and the non-condensable gas obtained after cooling and purifying may be used for the thermal source of heat accumulating type rotary heat exchanger after preheating.Significantly can reduce energy consumption thus.
Thus, the above embodiment of the present invention thermal decomposition of organic wastes system and utilize the method for this system pyrolysis organic waste can bring following beneficial effect:
(1) adopt non-condensable gas as heat source, thus do not affect the quality of pyrolysis gas, guarantee non-condensable gas calorific value.
(2) adopt gaseous heat-carrier, rubbish is heated evenly temperature plateau, and fluctuation range is little, easy to control.
(3) heat storage is generally used for smoke pre-heating air, and select heat accumulating type rotating commutator, can be as required, the combustion chamber combustion that the non-condensable gas produced with a part of pyrolysis is arranged in heat accumulating type rotating commutator, provide the thermal source of system, on the one hand, the non-condensable gas that consequent high-temperature flue gas preheating another part pyrolysis produces or other gas (such as hydrogen, CO etc.) are as thermal source, and adaptability is stronger.
(4) separate unit heat accumulating type rotating commutator heat transfer effect is adopted more to be better than other heat exchange mode heat transfer effects, and set up denitrification apparatus at heat accumulating type rotating commutator exhanst gas outlet, directly utilize flue-gas temperature as denitration reaction temperature, structure is simple, denitration effect is good, reduces back segment operation cost of investment.
Embodiment 1
The somewhere domestic refuse in autumn (garbage raw material analytical data is in table 1) of granularity 5mm ~ 120mm, send into continuously in rotating bed with 1.6t/h, be the non-condensable gas direct contact heat transfer of about 800 DEG C with temperature and at 680 DEG C, pyrolysis occur, Heat of Formation solid is containing charcoal thing, oil vapour and combustible gas, the hot solids obtained containing charcoal thing temperature be about 620 DEG C enter cooling system carry out cooling reclaim heat, cooled solid containing charcoal thing feeding storage bin in.The oil gas produced and the non-condensable gas mixture of heat supply draw rotating bed by the multiple oil gas vent in rotating bed top, and the high-temperature oil gas of generation mixes temperature afterwards with non-condensable gas be 660 DEG C, to be converged by each oil gas vent oil gas enter in cooling and purifying unit by oil gas house steward.
Beijing area domestic refuse in autumn water ratio is low, and cooled tolerance is higher, and non-condensable gas is with 1:(1 ~ 2.4 as the case may be) be divided into two parts, first as band denitration heat accumulating type rotating commutator burning source of the gas; Second section for the non-condensable gas heat exchange use with denitration heat accumulating type rotating commutator, heat exchange Posterior circle to rotating bed as rubbish pyrolysis thermal source gas.And regularly outwards transport portion non-condensable gas supply waste heat boiler uses, and guarantees rotating bed heat balance.
Processing method of the present invention can long-term smooth operation, and the productive rate of the pyrolysis product obtained and main character are in table 2.
Table 1 domestic refuse raw material (butt) analytical results
Embodiment 2
The somewhere domestic refuse in autumn of granularity 5mm ~ 120mm, send into continuously in rotating bed with 1.3t/h, be the non-condensable gas direct contact heat transfer of about 800 DEG C with temperature and at 660 DEG C, pyrolysis occur, Heat of Formation solid is containing charcoal thing, tar steam and combustible gas, the hot solids obtained containing charcoal thing temperature be about 640 DEG C enter cooling system carry out cooling reclaim heat, cooled solid containing charcoal thing feeding storage bin in.The oil gas produced and the non-condensable gas mixture of heat supply draw rotating bed by the multiple oil gas vent in rotating bed top, the high-temperature oil gas produced mix afterwards temperature with non-condensable gas be 650 DEG C, to be converged by each oil gas vent oil gas to enter to cool and in purification system by oil gas house steward.
Hubei province domestic refuse in autumn water ratio is slightly high, and cooled tolerance is lower, and non-condensable gas is with 1:(1 ~ 1.8 as the case may be) be divided into two portions, first part is as band denitration heat accumulating type rotating commutator burning source of the gas; Second section for the non-condensable gas heat exchange use with denitration heat accumulating type rotating commutator, heat exchange Posterior circle to rotating bed as rubbish pyrolysis thermal source gas.And regularly outwards transport portion non-condensable gas supply waste heat boiler uses, and guarantees rotating bed heat balance.
Processing method of the present invention can long-term smooth operation, and the productive rate of the pyrolysis product obtained and main character are in table 2.
Table 2 data results
In the description of this specification sheets, specific features, structure, material or feature that the description of reference term " embodiment ", " some embodiments ", " example ", " concrete example " or " some examples " etc. means to describe in conjunction with this embodiment or example are contained at least one embodiment of the present invention or example.In this manual, to the schematic representation of above-mentioned term need not for be identical embodiment or example.And the specific features of description, structure, material or feature can combine in one or more embodiment in office or example in an appropriate manner.In addition, when not conflicting, the feature of the different embodiment described in this specification sheets or example and different embodiment or example can carry out combining and combining by those skilled in the art.
Although illustrate and describe embodiments of the invention above, be understandable that, above-described embodiment is exemplary, can not be interpreted as limitation of the present invention, and those of ordinary skill in the art can change above-described embodiment within the scope of the invention, revises, replace and modification.
Claims (10)
1. a thermal decomposition of organic wastes system, is characterized in that, comprising:
Shredder assembly, described shredder assembly is suitable for described organic waste to carry out break process, obtains granular pyrolysis feed;
Moisture eliminator, described moisture eliminator is connected with described shredder assembly and is suitable for carrying out drying and processing to the pyrolysis feed through described break process;
Rotating bed pyrolysis oven, described rotating bed pyrolysis oven is connected with described moisture eliminator and is suitable for carrying out pyrolysis processing to described pyrolysis feed, and have in described rotating bed pyrolysis oven rotatable, for holding the cloth tray of described pyrolysis feed, described cloth tray is positioned at be separated in described rotating bed pyrolysis oven in pyrolysis chamber above described cloth tray, be positioned at heat supply chamber below described cloth tray
Wherein, described cloth tray has the through hole of the described pyrolysis chamber of multiple connection and heat supply chamber,
Described heat supply chamber has hot air intake,
Described pyrolysis chamber has opening for feed and air outlet, and described opening for feed is connected with described pretreatment unit;
Pyrolysis solids treatment device, described solid product treatment unit is connected with described solid outlet;
Cooling and refining plant, described cooling is connected with described air outlet with refining plant, the oil gas product produced in described pyrolysis chamber is carried out gas-oil separation obtain oil and non-condensable gas;
Storage tank, described storage tank is connected with refining plant with described cooling;
Heat accumulating type rotary heat exchanger, described heat accumulating type rotary heat exchanger is connected with the hot air intake of refining plant with described rotating bed pyrolysis oven with described cooling respectively, after being heated by described non-condensable gas, be used for described pyrolysis processing.
2. thermal decomposition of organic wastes system according to claim 1, is characterized in that, described heat accumulating type rotary heat exchanger comprises:
Insulation shell, is limited with chamber in described housing, and described housing has the first entrance, the first outlet, the second entrance and the second outlet;
Dividing plate, described dividing plate to be located in described chamber and described chamber is separated into accumulation of heat chamber and heat release chamber;
Heat storage, described heat storage is located at the middle part of described heat release chamber and the middle part of accumulation of heat chamber, described second outlet is formed at the top of described heat release chamber, described second entrance is formed at the bottom of described heat release chamber, combustion chamber is formed at the top of described accumulation of heat chamber, combustion chamber and the first entrance conducting, the first outlet is formed at the bottom of described accumulation of heat chamber
Wherein, described first entrance and described cooling are connected with refining plant with non-condensable gas described in receiving unit, and described second entrance is connected to accept non-condensable gas described in another part with refining plant with cooling, and described second outlet is connected with described hot air intake.
3. thermal decomposition of organic wastes system according to claim 1 and 2, is characterized in that, described heat accumulating type rotary heat exchanger comprises denitration catalyst reaction chamber.
4. thermal decomposition of organic wastes system according to claim 3, is characterized in that, described denitration catalyst reaction chamber comprises:: ammonia-spraying grid or spray urea grid, ammonia or urea and SCR catalytic reaction chamber.
5. the thermal decomposition of organic wastes system according to any one of claim 1-4, is characterized in that, comprise further:
Smoke eliminator, described smoke eliminator is connected with described moisture eliminator.
6. the thermal decomposition of organic wastes system according to any one of claim 1-5, it is characterized in that, the through hole in described cloth tray is circular hole and/or fin square hole, wherein, the diameter of described circular hole is 2 ~ 6 millimeters, and the long limit of described fin square hole is 10 ~ 15 millimeters, broadside is 3 ~ 5 millimeters.
7. utilize the method for the system pyrolysis organic waste described in any one of claim 1-6, it is characterized in that, comprising:
Utilize described shredder assembly that described organic waste is carried out break process, obtain granular pyrolysis feed;
Moisture eliminator is utilized to carry out drying and processing to the pyrolysis feed through described break process;
Described pyrolysis feed particle through drying and processing is carried out cloth from the described opening for feed of the pyrolysis chamber of described rotating bed pyrolysis oven to described cloth tray, and in described heat supply chamber, pass into hot gas from described hot air intake, make described pyrolysis feed particle generation pyrolysis, obtain solid product and oil gas product;
In described pyrolysis solids treatment device, described solid product is carried out processing and collecting;
In described cooling and refining plant, described oil gas product is carried out gas-oil separation process, to obtain oil and non-condensable gas, and described oil is stored in described storage tank;
Described in the combustion chamber combustion part of described heat accumulating type rotary heat exchanger, non-condensable gas or the outer combustible gas liberated heat that supplies carry out heat treated to non-condensable gas described in another part, and the described non-condensable gas after heating is used for described pyrolysis.
8. the method for pyrolysis according to claim 7, is characterized in that, is 600 ~ 950 degrees Celsius for heating the temperature of the high-temperature flue gas of non-condensable gas after the combustion chamber combustion of described heat accumulating type rotary heat exchanger.
9. the method for pyrolysis according to claim 7 or 8, is characterized in that, the temperature of the described non-condensable gas after heating is 550 ~ 850 degrees Celsius.
10. the method for pyrolysis according to any one of claim 7-9, is characterized in that, described pyrolysis carries out 1 ~ 3 hour under 550 ~ 800 degrees Celsius.
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