WO2019085528A1 - 一种生活有机垃圾的裂解还原转化处理方法 - Google Patents

一种生活有机垃圾的裂解还原转化处理方法 Download PDF

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Publication number
WO2019085528A1
WO2019085528A1 PCT/CN2018/093427 CN2018093427W WO2019085528A1 WO 2019085528 A1 WO2019085528 A1 WO 2019085528A1 CN 2018093427 W CN2018093427 W CN 2018093427W WO 2019085528 A1 WO2019085528 A1 WO 2019085528A1
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Prior art keywords
cracking
organic waste
gas
reaction
reducing
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PCT/CN2018/093427
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English (en)
French (fr)
Inventor
董平年
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董平年
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Priority claimed from CN201711094259.7A external-priority patent/CN107626726A/zh
Application filed by 董平年 filed Critical 董平年
Priority to CN201880003660.1A priority Critical patent/CN109890943A/zh
Publication of WO2019085528A1 publication Critical patent/WO2019085528A1/zh

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B09—DISPOSAL OF SOLID WASTE; RECLAMATION OF CONTAMINATED SOIL
    • B09B—DISPOSAL OF SOLID WASTE NOT OTHERWISE PROVIDED FOR
    • B09B3/00—Destroying solid waste or transforming solid waste into something useful or harmless
    • 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
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/141—Feedstock
    • Y02P20/145—Feedstock the feedstock being materials of biological origin

Definitions

  • the invention relates to the technical field of domestic organic waste treatment, in particular to the technical field of cracking, reduction and transformation treatment of organic matter.
  • the main treatment methods for organic waste in China are mostly oxidative incineration decomposition technology (incineration power generation), incomplete oxidative cracking gasification technology, and biological fermentation landfill rot gasification technology. Due to the complex composition and low calorific value of organic waste in towns and cities in China, it is necessary to add auxiliary fuel when incineration power generation and cracking gasification, which increases the cost of treatment.
  • incineration power generation When incineration power generation is operated, harmful substances such as dioxins may be generated due to factors such as technology and operation. Landfill treatment takes up a large amount of land while seriously polluting the atmosphere and groundwater sources.
  • the cracking gasification and secondary combustion of organic waste is called the third generation processing technology.
  • the cracking gasification technology is an effective way to reduce organic waste, reduce pollution, and recycle resources.
  • the pyrolysis gasification technology as disclosed in the patent document CN101457147A, CN206219517U, and CN106949479A has no problem from a theoretical point of view. In practice, it will find that the implementation effect is not ideal, so the industry It has never been promoted.
  • the cracking gasifier eventually becomes a small incinerator, which inevitably brings environmental problems such as dioxin emissions.
  • the combustion of the combustion chamber mainly depends on the combustible gas generated by the dry distillation, the combustion of the combustion chamber is unstable, the combustion of the combustion chamber is unstable, and on the one hand, the incomplete combustion itself produces the emission of harmful substances; In the cracking furnace, a complete dry distillation reaction cannot be carried out, and finally the cracking furnace constitutes only a crucible furnace.
  • the object of the present invention is to overcome the deficiencies of the above-mentioned method and technology, and to provide a cleavage reduction conversion treatment method capable of realizing sufficient lysis and reduction reaction of domestic organic waste, and environmentally, efficiently and completely changing the living organic waste into resource materials.
  • the main technical solutions adopted by the present invention include:
  • a method for cracking and reducing treatment of domestic organic waste wherein the domestic organic waste comprises an organic material, characterized in that the organic material is placed in a closed cylinder to insulate air and continuously flip in the closed cylinder and The ground is evenly heated.
  • the heating includes:
  • the organic material is heated to 100 ° C ⁇ 200 ° C for drying;
  • the organic material is slowly heated to 450 ° C to 550 ° C and maintained, and the dried organic material is subjected to a dry distillation reaction;
  • the temperature is raised to 580 ° C to 640 ° C to gradually carbonize the organic material after the reaction.
  • the organic material is crushed to a size of 50 to 100 mm before being placed in the closed cylinder.
  • said continuous flipping comprises rotating the body of said closed barrel about its own horizontal axis.
  • the organic material is slowly heated at a rate of from 15 ° C to 20 ° C / min.
  • the gas phase product produced by the dry distillation reaction is collected, purified and separated into combustible gas, tar and water.
  • the gas phase product is collected via a gas collection conduit in communication with the closed barrel.
  • the separation is achieved by cooling the gas phase product to 10 °C.
  • the combustible gas is used to indirectly heat the closed cylinder and the organic material therein after combustion.
  • the rate of fuel gas passing into the combustor is adjusted in accordance with the temperature requirements of the organic material within the closed barrel, the fuel gas comprising the combustible gas.
  • the ratio of air to fuel gas entering the combustor is adjusted in accordance with the amount of carbon monoxide emissions detected on-line, the carbon monoxide emissions are always minimized, and the fuel gas comprises the combustible gas.
  • the humidity in the closed cylinder is detected, and when the humidity is lowered to the set humidity, it is judged that the drying is completed.
  • the pH of the closed cylinder is detected, and when the pH is deviated from the set pH, an acid or a base is added to the closed cylinder to stabilize the pH at a set pH.
  • the pressure in the closed cylinder is detected, and when a pressure drop is detected, it is judged that the dry distillation reaction is completed.
  • the method of the invention can fully carry out the cracking and reduction treatment reaction, and simulates the formation process of coal, oil and natural gas in nature, not only the reaction process which takes hundreds of years in nature, but also at the appropriate temperature, pressure and time. Under the condition of pH and pH, it can be reproduced within a few hours, and the organic material can be sufficiently subjected to the above reaction to avoid environmental problems caused by insufficient reaction.
  • the amount of harmful gas generated during the treatment is lower than international standards and national standards.
  • the dioxin emission standard is 0.1 ng
  • the emission of dioxins from living organic waste using the apparatus of the present invention is less than 0.02 ng, in some samples.
  • the condition is only 0.005 ng, which is far superior to the emission standard.
  • the method of the invention can truly achieve the theoretical effect of the cracking and reduction treatment reaction, and can completely transform the living organic waste into a harmless physical state through a harmless way, and convert into "oil, gas, gas according to its own organic molecular composition.
  • Resource materials such as carbon.
  • beneficial effects of the present invention further include:
  • the cracking reduction conversion reaction is carried out in a rotating closed cylinder, and the organic material is continuously stirred in the reaction device, uniformly heated, so that the reaction is fully completed, and the resource products such as combustible gas and tar can be produced to the greatest extent, and other harmful products are made.
  • the production has reached a minimum and is truly harmless;
  • the whole process from cracking to gas treatment adopts closed cycle operation to isolate the organic material from air, the treatment process and discharge are completely controlled, and the reaction process of organic materials is stable and the output is stable;
  • the burner for providing heat to the closed cylinder is independently provided, and only heat is supplied to the closed cylinder, that is, indirect heating, and no open flame is introduced therein. This approach facilitates the placement of an environmental information collection device within the barrel and in turn facilitates precise control of the internal environment within the barrel.
  • the fuel gas used for burner combustion is at least partially derived from a closed rotary cracking reduction conversion reaction. Since the cracking reduction conversion reaction is sufficiently stable, the output of the combustible gas can be maximized, the quality is high, and the flow rate is stable, thereby effectively ensuring the combustion stability of the burner, and the self-production output satisfies the self-energy demand to the greatest extent.
  • the entire system achieves a stable energy cycle, and the system itself minimizes the need for external fuel supply, thereby greatly reducing energy consumption and operating costs.
  • the method further comprises receiving environmental data feedback, and performing precise parameter control on the process of the cleavage reduction conversion reaction to ensure sufficient circulation balance and reaction of the entire process. For example, by collecting temperature, pressure, humidity, and pH data in the cylinder, the internal environment in the cylinder is controlled to maintain an ideal state or reacted according to an ideal control process; for example, by controlling the cooling temperature of the gas phase product to make the tar oil and gas The separation is more thorough, avoiding undesired mixing resulting in a decrease in the quality of the combustible gas obtained after separation, undesired harmful products in subsequent combustion, and even affecting the temperature in the reaction chamber.
  • the data feedback and processing method enables all the process steps in the process to be automated, without the need for human intervention, and the operator's requirements are very low.
  • the process method can automatically perform material sorting and crushing, and the composition and form of the material can be effectively controlled, thereby providing an ideal material for the cracking reaction, and can avoid the influence of the uneven quality of the material on the degree of reaction, and is suitable for recycling. Biomass-containing household waste of various qualities.
  • the pyrolysis reduction conversion treatment method can directly discharge and/or recover the solid product “carbon”, and is not mixed with the gas phase product, and is convenient for separation and recycling.
  • the gas treatment process can completely separate the gas phase product obtained by the cracking reduction conversion reaction device, and separate it into "tar, combustible gas and water", thereby facilitating separate recycling.
  • FIG. 1 is a process diagram of a cracking and reduction treatment of living organic waste in an embodiment of the present invention.
  • Figure 2 is a schematic illustration of a cracking reduction conversion reaction treatment apparatus for living organic waste used in the treatment of the present invention.
  • the invention relates to a method for cracking and reducing treatment of domestic organic waste, which provides a condition for guiding material to be naturally reduced and decomposed according to its most original attribute by providing a cracking reduction conversion reaction treatment environment, and returning to the organic substance before returning to the organic substance. Harmless physical state. Specific practice: the domestic organic waste is subjected to a pretreatment system, a cracking reduction conversion reaction system, a gas treatment system, parameter control, etc., to treat domestic organic waste to become a resource substance.
  • the cracking and reduction conversion treatment method of the domestic organic waste of the present invention generally comprises the following steps:
  • organic waste ie, domestic organic waste
  • pretreatment including but not limited to removal of inorganic waste such as metal batteries by a magnetic separation device.
  • the obtained organic material is spirally advanced into a cracking reduction reaction unit for reaction, and the reaction includes a drying step, a dry distillation reaction step, and a carbonization step.
  • the gas phase product obtained by the crack reduction reaction is then subjected to a gas treatment in which oil, water, and gas are separated, and the condensation system is connected to a circulating water tank to ensure that the condensation system supplies the gas phase product with an appropriate temperature.
  • the separated tar storage is the main product of the domestic organic waste, and can be sold to the market;
  • the obtained non-condensable gas (the main component is a combustible gas) is purified by the purification system to obtain a high-purity combustible gas, and is introduced into a heating device to generate heat. It is supplied to a cracking reduction reaction unit for use in a cracking reduction treatment.
  • the gas products after combustion of the combustible gas can be discharged by the dust removal.
  • the solid phase product obtained by the cleavage reduction reaction is organic carbon, which is separately cooled, recovered, and stored in the form of solid organic carbon after cooling.
  • the whole process of the above-mentioned cracking reduction reaction is controlled by the parameter control system to ensure that the reaction is carried out under ideal conditions.
  • the reaction is made uniform, fully carried out, and the recovered combustible gas is fully utilized as a fuel to provide heat for the material reaction.
  • the above-mentioned cracking and reduction treatment method is realized by the cracking and reducing treatment equipment of the living organic garbage shown in FIG. 2, and the detailed process of realizing the cracking and reduction treatment of the living organic waste by the cracking reduction treatment equipment will be described in combination with the composition of the equipment.
  • the living organic garbage referred to in the present invention refers to garbage which is mainly composed of bio-organic matter, such as fruit and vegetable skin stalks, food residues, straws, dead branches and leaves, which are produced in daily life of human beings.
  • bio-organic matter such as fruit and vegetable skin stalks, food residues, straws, dead branches and leaves
  • these domestic organic wastes will inevitably be doped with some inorganic waste materials, such as glass bottles, construction waste, metals, batteries and so on.
  • the present invention needs to pretreat the collected domestic organic waste to obtain an organic material, so that the organic material finally entering the equipment is composed of three elements of carbon, hydrogen and oxygen.
  • the pretreatment system equipment includes: a weighbridge 1, a gripper 2, a belt conveying magnetic separator 3, and a crusher 4.
  • the magnetic separator 3 is transported to the belt to remove components such as metal and batteries; and is conveyed to the crusher 4 to be crushed into uniform block-shaped organic materials having a thickness of 50 to 100 mm and a thickness of less than 15 mm.
  • this pretreatment system equipment By means of this pretreatment system equipment, a good quality organic material is obtained, which facilitates the subsequent cleavage reduction conversion reaction. Of course, it is not excluded that the quality of the organic domestic waste itself is good. In this case, the pretreatment system equipment can be omitted. According to the actual situation, some or all of the devices of the pre-processing system device may be omitted without affecting the processing.
  • the cracking reduction conversion reaction system apparatus includes a belt conveyor 5, a feed hopper 6, a material propulsion device 7, a closed-rotation cracking reduction conversion reaction device 8, a discharge screw conveyor 30, and a heating device 16.
  • the belt conveyor 5 is for conveying the organic material obtained after the pretreatment to the feed hopper 6 on the side of the closed rotary cleavage reduction conversion reaction device 8.
  • the material enters the material propulsion device 7 from the feed hopper 6 and is pushed by the material propulsion device 7 into the closed rotary cleavage reduction conversion reaction device 8.
  • the material propulsion device 7 includes a screw disposed in a horizontal direction in the casing, and a first end of the casing is connected to the feed bin 6 and a second end is connected to the closed rotary type.
  • the cleavage reduction conversion reaction device 8 is carried out.
  • the horizontal screw extends from the first end to the second end, and even extends to the inside of the cracking reduction conversion reaction device 8, and a continuous blade disposed along the Archimedes spiral is formed on the screw for
  • the Archimedes screw advancement mode advances the organic material received from the feed hopper 6 into the closed rotary cracking reduction conversion reaction unit 8.
  • the material propulsion device can also hydraulically propel the material. The material is pushed laterally by the material propulsion unit 7 to the inside of the closed rotary cracking reduction conversion reaction unit 8.
  • An operable closing device is disposed at the first end of the material propulsion device 7 or on the feed bin 6 after the expected weight or volume of organic material enters the closed rotary cracking reduction conversion reaction device 8 Before the reaction is started, the closing device is closed to form a closed oxygen-free space inside the closed rotary cracking reduction conversion reaction device 8.
  • the closed rotary cracking reduction conversion reaction device 8 comprises a horizontal cylinder 9 which rotates around a horizontal axis during operation to ensure that the material maintains a balanced distribution in the cylinder at all times and ensures the cylinder
  • the material in any part of the material has the same or substantially the same temperature at the same time.
  • the rotation comprises a clockwise rotation and/or a counterclockwise rotation, ie the barrel 9 can be rotated forward and reversed.
  • the barrel has a circular, polygonal or the like cross-section that is centrally symmetric about the horizontal axis.
  • the cylinder 9 is designed to be horizontal, on the one hand, to facilitate the rotation of the cylinder; on the other hand, when the horizontal cylinder 9 rotates around the horizontal axis, the organic material is thrown and dropped, and this rotation form It is especially advantageous to stir the organic material evenly.
  • the horizontal axis referred to herein is not limited to a strict level. It is conceivable that the cylinder is set to be slightly inclined as long as it does not affect the turning and stirring of the material in the cylinder, and is in the invention. Within the scope of protection. Similarly, horizontal screws for feeding and discharging are not necessarily critical. The horizontal setting is only a preferred solution.
  • the rotation of the cylinder 9 is achieved by means of a motor and a toothed ring drive driven by a motor.
  • a toothed ring may be fixedly provided on the outer surface of the cylindrical body 9, and the center line of the toothed ring is the rotational axis of the cylindrical body 9.
  • the motor is engaged with the ring gear through a transmission to drive the cylinder 9 to rotate.
  • the ring gears are arranged one, two or more depending on the scale of the cylinder 9.
  • the motor allows the barrel 9 to rotate in the forward or reverse direction when needed, so that when rotated in one direction causes material accumulation in the barrel, the reverse rotation causes the material to be more evenly dispersed in the barrel, thereby further promoting uniform heating.
  • the feeding port and the discharging port of the cylinder 9 are respectively located at two ends of the cylinder body, and the feeding port is sealedly connected with the casing of the material propelling device 7 by a sealing device 11.
  • the sealing device is a bellows mechanical combination sealing device 11.
  • the discharge port is also sealedly connected to the housing of the discharge screw conveyor 30 by a bellows mechanical combination sealing device 11.
  • the screw of the material advancing device 7 extends into the cylinder 9 through the feed port of the cylinder 9.
  • the inner wall of the cylinder 9 is provided with a spiral material guide plate 12 for guiding the material from the inside of the cylinder 9 to the discharge opening by means of the rotating action of the cylinder 9.
  • the discharge screw conveyor 30 serves as a discharge conveying device for discharging and/or recovering the solid product after the reaction from the discharge port.
  • the discharge screw conveyor 30 includes a casing and a screw disposed in the casing in a horizontal direction. As described above, one end of the casing is sealingly connected to the discharge port of the cylinder 9 and passes through the The discharge port communicates with the inside of the cylindrical body 9, and one end of the screw extends into the cylindrical body 9, and the other end extends in a direction away from the cylindrical body 9. Similar to the structure of the material advancing device 7, the screw of the discharge screw conveyor 30 is formed with continuous blades arranged along the Archimedes spiral for propelling the material inside the cylinder 9 by Archimedes screw propulsion. External output.
  • An end of the housing of the discharge screw conveyor 30 remote from the barrel 9 includes a downwardly closable discharge opening.
  • the discharge port is closed during the reaction, and after the reaction is completed, the organic carbon for discharging the reaction is opened.
  • the discharge opening is connected to the vertically downward water-cooled discharge conveyor 13 by means of a discharge seal 15.
  • the water-cooled discharge conveyor 13 includes a water jacket disposed outside the discharge conduit to provide water jacketed water circulation cooling to the organic carbon in the discharge conduit, and the organic carbon carbon discharge temperature is lowered to a safe temperature and then transported to the organic carbon storage device. 27 in.
  • the interior of the barrel 9 is in communication with a gas collection conduit for collecting gaseous products produced during the dry distillation reaction.
  • the gas collection conduit is coupled to the sidewall of the housing of the material advancement device 14 to be in gaseous communication with the interior of the cartridge 9.
  • the gas collecting duct is not disposed on the side wall of the rotating cylinder 9, but is disposed on the side wall of the casing of the stationary material propulsion device 14 to reduce the complexity of the connecting structure.
  • the gas phase product is produced in the cylinder 9, there is almost no material in the material propulsion device 14, and there is no risk of blockage of the pipe inlet.
  • the heating device 16 is used for heating the cracking reduction conversion reaction device 8 to remove moisture in the material inside the cylinder 9, so that the heat value of the material is improved, and the occurrence of the cracking reduction conversion reaction is promoted.
  • the heating device 16 may be provided with one or more, and in the case where a plurality of heating devices are provided, one or more of them may be activated according to the demand of the heating. In this way, flexible heating of the cracking reduction conversion reaction device 8 can be achieved, and the temperature requirement of the organic material in the cylinder 9 can be satisfied.
  • the heating device 16 includes a thermally conductive chamber 17 that is capable of transferring heat to at least a portion of the barrel 9.
  • the heat transfer chamber 17 is disposed at the bottom of the cylindrical body 9, covers the bottom of the cylindrical body in the direction of the bus bar of the cylindrical body, and transfers heat generated in the heat transfer chamber 17 to the cylindrical body 9 by heat conduction, thereby realizing Indirect heating of the material in the cylinder. As the barrel 9 rotates, heat can be transferred from the different locations on the surface of the barrel 9 to the contents of the barrel.
  • the heat in the heat conducting chamber 17 is generated by combustion of a fuel (for example, a combustible gas obtained by separating the gas phase product of the cracking reduction conversion reaction device 8) by means of a self-aligning gas burner 18, and the oxygen supply fan 26 is used for the burner 18. Air or oxygen is supplied inside.
  • a fuel for example, a combustible gas obtained by separating the gas phase product of the cracking reduction conversion reaction device 8
  • the oxygen supply fan 26 is used for the burner 18.
  • Air or oxygen is supplied inside.
  • the interior of the thermally conductive chamber 17 is made of a refractory insulating material to ensure that the greatest proportion of heat will be transferred to the barrel 9 rather than being dissipated.
  • a gas control pipe or an air pipe connected to the burner 18 is provided with a proportional control valve 19 for controlling the ratio of air and gas entering, and capable of controlling the amount of heat generated by the combustion, thereby accurately controlling the heat transfer chamber 17 according to a predetermined temperature profile. Internal temperature. When the heat balance is reached in the burner and in the barrel, the temperatures are the same.
  • the proportional control valve 19 is connected to a PLC controller which controls the proportional control valve 19 in accordance with the following temperature reaction conditions of the material in the cylinder 9.
  • the flue gas generated by the combustion of the combustible gas in the furnace of the burner 18 is discharged directly by the cooling dust removal tower 24 to remove impurities.
  • a wet filtration device is further included, and the acid harmful gas in the flue gas is removed by mixing reaction with the alkali liquid sprayed at 5% concentration.
  • a carbon monoxide detector is preferably disposed in the exhaust pipe, and is connected to the PLC controller to detect the carbon monoxide emission contained in the flue gas in real time, and adjust the burner proportional control valve according to the carbon monoxide emission. 19. Increase the oxygen supply or increase the ratio of oxygen to fuel gas when the carbon monoxide emissions are above a certain threshold; maintain the oxygen supply or maintain the ratio of oxygen to fuel gas when the carbon monoxide emissions are below a certain threshold, in short To keep carbon monoxide emissions to a minimum, so that the fuel gas can be fully burned in the burner.
  • the fuel gas includes the recovered combustible gas.
  • the temperature profile can be divided into chronological order:
  • the temperature in the cylinder 9 is maintained at 100-200 ° C.
  • the function is to evaporate the moisture of the material in the cylinder, so that the material is uniformly heated and gradually dried to meet the material drying standard.
  • Uniform heating as used herein and hereinafter means that the organic material at any part of the cylinder is at the same or substantially the same temperature at the same time. Uniform heating is one of the key technologies emphasized by the present invention, both in the drying stage and in the dry distillation stage. Or in the carbonization stage, it is desirable that the material is uniformly heated in the cylinder. Uniform heating in the present invention is achieved by continuously turning the material over the barrel. By continuous reversal is meant that the material is continuously inverted continuously or at known time intervals throughout the various stages of drying, dry distillation or carbonization.
  • continuous flipping does not mean that the cylinder must be continuously rotated, or it can be rotated at a certain time interval, for example, by rotating for 2 minutes at intervals of 0.5 minutes, and then continuing to rotate in the same direction or in the opposite direction for 2 minutes, and then at intervals of 0.5 minutes.
  • the drying standard of the material that normally satisfies the conditions of the dry distillation reaction is about 20% of the water content, and the duration of this stage is adjusted according to the water content of the material to be treated.
  • the material is continuously heated uniformly and slowly heated to 450 ° C to 550 ° C and maintained.
  • the role of this stage is to produce a large amount of flammable gas and tar oil and gas.
  • the temperature is continuously raised at a temperature rising rate of 15 ° C to 20 ° C / min from the holding temperature in the drying stage. Increasing the temperature at this rate ensures stable stabilization of the subsequent retorting reaction.
  • the dry distillation reaction begins to occur, the main products are methane, ethylene, ethane and carbon monoxide.
  • the reaction time at this stage varies depending on the composition of the materials. The invention assists in judging whether the reaction is completed by monitoring the pressure inside the cylinder.
  • the pressure gradually increases during the reaction, and the reaction end pressure gradually decreases.
  • the control device detects a decrease in pressure, it judges that the reaction is over.
  • the pressure is reduced to stabilize, the reaction is completely complete and the resulting gas phase product is substantially completely recovered.
  • the temperature in the cylinder 9 is maintained at 580 ° C to 640 ° C, preferably 600 ° C. During this process, it is still continued to ensure that the material is evenly heated. The material after the full dry distillation reaction no longer produces a gas phase product, but gradually carbonizes to form a solid phase product organic carbon.
  • the three-stage temperature control can be achieved by controlling the pressure in the heat-conducting chamber by the number of heating devices.
  • the pressure in the heat transfer chamber and the temperature of the heat transfer chamber directly control the temperature stability in the cylinder to achieve the best three-stage work process and efficiency.
  • the material in the reaction chamber can be fully subjected to a cracking reduction conversion reaction. Since the organic material reacts under the anaerobic condition in the sealed cylinder, the material does not burn and does not generate harmful gases such as dioxins. Ying et al., because the entire cylinder is sealed, does not emit dust and other particulate pollutants into the environment, and all organic materials are fully converted into "oil, gas and carbon".
  • the gaseous fuel used in the heating device 16 is derived from the gas phase product of the closed rotary cracking reduction conversion reaction unit 8.
  • the gas phase product is not used directly as the heating device 16, but requires a series of gas treatments, which will be described below.
  • the apparatus of the present invention further comprises a gas treatment system apparatus, comprising: a steam separator 23, a dust purification purifier 21, a gas phase condensation bundling device 22, and an oil and gas water separator. 25.
  • the gas collection pipe on the cracking reduction conversion reaction device 8 is provided with a steam separator 23, and the acidic toxic and harmful gas such as HCl, SOx and HF generated during the cracking reduction reaction is removed by wet absorption, for example, by Ca(OH). 2, NaOH and other alkaline substances are absorbed and removed, and the remaining gas phase products are pressure buffered to facilitate gas entry into subsequent processing procedures.
  • the gas phase product enters the dust purifier 21 from the steam separator 23, and under the action of centrifugal force, the particles of the mixture of dust and oil and gas sink, and the gas escapes through the upper outlet, thereby removing the solid particles entrained in the gas phase product.
  • the structure of the vapor phase condensation bundling device 22 is a conventional bundling device structure, which is externally cooled by a circulating water tank 29 to condense the steam therein to obtain a gas-liquid mixture after condensation.
  • the temperature in the gas phase condensation bundling device 22 needs to be controlled, on the one hand, a temperature sensor is provided, and on the other hand, a temperature adjusting device is provided, which is connected to the parameter control system device, so that the temperature of the gas phase condensation bundling device 22 is controlled at At 10 ° C, tar oil and gas and combustible gas can be completely separated under this temperature condition. It is conceivable that a constant temperature water tank can be used instead of the temperature sensor and the temperature adjusting device, and the temperature of the gas phase condensation bundling device 22 can also be controlled at 10 °C. These temperature control means are all within the scope of the invention.
  • the gas-liquid mixture enters the oil-water separator 25, and the tar, water, and combustible gas are separated.
  • the tar is stored in the oil storage device 28, and can be recycled; the water can be discharged or recycled; the combustible gas is purified by the gas purifier 20 as a heating device 16
  • the fuel is recycled, and the heat generated by the combustion of the combustible gas is used to maintain the temperature required for the cracking reduction conversion reaction.
  • the recovered combustible gas may be passed directly to the heating device 16, or may be stored and passed to the heating device 16 as needed.
  • the fuel gas for combustion in the heating device 16 to generate heat includes the recovered combustible gas and other fuel gases, which are supplemented by the combustible gas.
  • the flue gas generated by the combustion of the fuel gas (including the combustible gas) in the furnace of the burner 18 is discharged by the cooling dust removal tower 24 to remove the impurities.
  • a wet filtration device is further included, and the acid harmful gas in the flue gas is removed by mixing reaction with the alkali liquid sprayed at 5% concentration.
  • the material in the cylinder 9 is uniformly heated according to the ideal temperature profile to ensure efficient operation of the system, and the present invention also includes a parameter control system device.
  • the parameter control system device includes a temperature sensor, a pressure sensor, a humidity sensor, a pH meter, a carbon monoxide detector, a motor that drives the cylinder 9 to rotate, a burner proportional control valve 19, and/or an oxygen supply fan disposed in the barrel 9. 26, and a control device connected to these devices.
  • the control device is configured to adjust the drying and holding time and the pH of the organic material according to the humidity sensor and the data fed back by the pH meter.
  • the control device includes a variable frequency controller and a PLC controller.
  • the variable frequency controller is used to adjust the air volume of the oxygen supply fan 26, and the PLC controller can adjust the burner proportional control valve 19.
  • the fuel gas rate to the burner, and the fuel gas and air can be determined according to the temperature requirement of the organic material in the closed cylinder.
  • the ratio is adjusted. For example, collecting the real-time temperature in the closed cylinder, compared with the set temperature, increasing the rate of the fuel gas flowing into the combustor when the real-time temperature is lower than the set temperature, that is, increasing the fuel gas supply amount; When the real-time temperature is higher than the set temperature, the rate of the fuel gas that is introduced into the combustor is reduced, that is, the fuel gas supply amount is reduced. And based on the fuel gas supply amount, the ratio of the fuel gas to the air is adjusted in a desired ratio.
  • the PLC controller is also coupled to a carbon monoxide detector that monitors the carbon monoxide emissions emitted by the combustor and adjusts the combustor proportional control valve 19 based on the carbon monoxide emissions.
  • the PLC controller is used to control the motor, temperature control, pressure control, humidity control, reaction time control and pH control.
  • the control of the motor includes control of the start and stop of the motor and control of the rotational speed and the rotational direction of the cylinder 9 to achieve uniform heating and feed and discharge of the material in the cylinder.
  • the temperature control includes detecting and controlling the temperature of the organic material in the cylinder and the heating or cooling rate to ensure that the organic material in the cylinder always meets the temperature requirement; and according to the temperature of the organic material in the cylinder and the rate of temperature rise or fall, The amount, rate and ratio of oxygen and fuel gases that pass into the burner are adjusted so that the temperature is always at the desired value.
  • the pressure control includes detection and/or control of the pressure inside the cylinder of the closed rotary cracking reduction conversion reaction device 8, and detection and/or control of the pressure in the heat transfer chamber, and if a pressure drop is detected in the dry distillation reaction phase, it is determined as The dry distillation reaction ends.
  • the humidity control includes controlling the humidity inside the cylinder of the closed rotary cracking reduction conversion reaction device 8, and determining whether the first drying phase is completed based on the humidity. For example, in the drying stage, the humidity in the closed cylinder is detected, and when the humidity is lowered to the set humidity, it is judged that the drying is completed.
  • the pH control includes controlling the organic material in the barrel of the closed rotary cleavage reduction conversion reaction device 8. If the pH is deviated, an appropriate amount of acid or base may be applied to the barrel to adjust the pH. In particular, in the dry distillation reaction stage, the pH of the closed cylinder is detected. When the pH is deviated from the set pH, an acid or a base is added to the closed cylinder to stabilize the pH at a set pH, for example, setting a pH. It is 7-8 to facilitate the occurrence of the dry distillation reaction.
  • control is precisely controlled, so that the material in the cylinder of the closed rotary cracking reduction conversion reaction device 8 is uniformly heated, and the predetermined reaction conditions of cracking, reduction and transformation are satisfied, and the continuous and efficient operation of the system is effectively ensured.

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Abstract

一种生活有机垃圾的裂解还原处理方法，生活有机垃圾包括有机物料，将有机物料置入封闭筒体，并以持续翻转和间接加热的方式，使有机物料隔绝空气、均匀受热。该方法可以使有机物料在反应装置中持续搅拌，均匀受热，使反应充分完全，能够最大程度地产出可燃气体、焦油等资源产物，且使其他有害产物的产生达到最低，真正做到了无害化；从裂解到气体处理的全过程采用封闭循环运行，使所述有机物料隔绝空气，处理过程和排放完全受控，有机物料的反应过程稳定、产出稳定；整个系统达到稳定的能量循环，系统自身对外部供给燃料的需求量降至最低，从而大大降低了能源消耗和运行成本。

Description

一种生活有机垃圾的裂解还原转化处理方法 技术领域
本发明涉及一种生活有机垃圾处理技术领域，尤其是有机质的裂解还原转化处理技术领域。
背景技术
随着人口的快速增长城镇的不断扩大，生活有机垃圾产生量与日增大，严重污染了城镇及周边环境，而且还会对周围居民的身体造成严重损害，生活有机垃圾的处理已经是迫在眉睫。然而，降低有机垃圾的综合处理成本，提高有机垃圾的经济效益，将其无害化、减量化、资源化，是全社会推进有机垃圾处理的重要关键问题。
当前我国生活有机垃圾主要的处理方法大都是全氧化焚烧分解技术(焚烧发电)、不完全氧化裂解气化技术、生物发酵填埋腐烂气化技术。由于我国城镇的有机垃圾的成分复杂、热值低，焚烧发电、裂解气化时需要添加辅助燃料，使得处理成本费用加大。焚烧发电运行时因技术、操作等因素会产生二噁英等有害物质。填埋处理占用大量的土地，同时严重污染大气和地下水源。
而对有机垃圾进行裂解气化和二次燃烧被称为第三代处理技术，然而经研究实践表明裂解气化技术处理有机垃圾是减量化、无害化、资源化的有效途径，但要使这个技术达到实用性还有很多技术难题。如公开号为CN101457147A、公开号为CN206219517U、公开号为CN106949479A的专利文献所阐述的裂解气化技术从理论角度是没有问题的，在实践中就会发现普遍存在实施效果不理想的问题，因此产业上始终无法推广。
一些设备中由于无法在干馏反应过程中完全隔绝氧气，使裂解气化炉最终实际变成了小焚烧炉，仍然不可避免地带来二噁英排放等环境问题。
还有一些设备中由于有机垃圾所包含的组分复杂多变，含水量不同、 密度不同的材料对裂解反应的要求不同，而设备却无法识别这些组分的差异，并相应地调整工艺参数；另外，自身设计的缺陷常导致处理过程中，燃烧层堆压，阻隔氧气供应，造成燃烧不匀，使得炉内能量循环中断甚至死火，导致干馏反应不稳定。干馏反应不稳定的情况下，可燃气体产出也时快时慢，使气流极不稳定。进一步地，由于燃烧室的燃烧主要依赖于干馏产生的可燃气体，因而又导致燃烧室燃烧不稳定，燃烧室燃烧不稳定，一方面本身不完全燃烧产生了有害物质的排放；另一方面进一步导致裂解炉中无法进行完全的干馏反应，最终使裂解炉仅仅构成了焖烧炉。
发明内容
(一)要解决的技术问题
本发明的目的就是要克服上述方法技术的缺陷，提供一种能够实现生活有机垃圾充分裂解还原处理反应、将生活有机垃圾环保、高效、完全地变为资源物质的裂解还原转化处理方法。
(二)技术方案
为了达到上述目的，本发明采用的主要技术方案包括：
一种生活有机垃圾的裂解还原处理方法，所述生活有机垃圾包括有机物料，其特征在于，将有机物料置入封闭筒体使其隔绝空气，并使其在所述封闭筒体中持续翻转和间接地均匀受热。
所述受热包括：
干燥阶段，将所述有机物料加热至100℃～200℃进行干燥；
干馏反应阶段，将所述有机物料缓慢升温至450℃～550℃并保持，使干燥后的所述有机物料进行干馏反应；
碳化阶段，在所述干馏反应结束后，升温至580℃～640℃，使反应后的所述有机物料逐渐碳化。
优选地，所述有机物料在置入所述封闭筒体中之前经破碎尺寸大小为50～100毫米。
优选地，所述持续翻转包括所述封闭筒体的本体绕其自身的水平轴线转动。
优选地，在所述干馏反应阶段，所述有机物料缓慢升温的速率为15℃～20℃/分钟。
优选地，所述干馏反应产生的气相产物被收集、净化和分离为可燃气体、焦油和水。
优选地，所述气相产物经由与所述封闭筒体连通的集气管道被收集。
优选地，所述分离通过将所述气相产物冷却至10℃实现。
优选地，所述可燃气体用于燃烧后间接加热所述封闭筒体及其中的有机物料。
优选地，通入燃烧器的燃料气体的速率依据所述封闭筒体内所述有机物料的温度要求进行调节，所述燃料气体包括所述可燃气体。
优选地，通入燃烧器的空气和燃料气体的比例依据在线检测的一氧化碳排放量进行调节，始终使所述一氧化碳排放量最小，所述燃料气体包括所述可燃气体。
优选地，在干燥阶段，检测所述封闭筒体内的湿度，在湿度下降到设定湿度时判断为干燥完成。
优选地，在干馏反应阶段，检测所述封闭筒体内的酸碱度，当酸碱度偏离设定PH值时，向所述封闭筒体内添加酸或碱，使酸碱度稳定在设定PH值。
优选地，在干馏反应阶段，检测所述封闭筒体内的压力，当检测到压力下降，则判断为干馏反应结束。
(三)有益效果
本发明的方法能够充分进行裂解还原处理反应，模拟自然界的煤、石油和天然气的生成过程，不仅仅是将这一在自然界需要数百年时间的反应过程，通过在适当的温度、压力、时间和酸碱度(PH值)条件下， 数小时内再现，而且能够将有机物料充分进行上述反应，避免反应不充分带来的环境问题。处理过程中有害气体生成量低于国际标准和国家标准，例如二噁英排放标准是0.1ng，而采用本发明的设备进行生活有机垃圾产生二噁英的排放量低于0.02ng，在一些样品条件下仅为0.005ng，远优于排放标准。
本发明的方法能够真正达到裂解还原处理反应理论效果，能够完全地将生活有机垃圾通过无害的途径转变为无害物性状态，并按照其自身包含的有机分子构成，转化为“油、气、碳”类等资源物质。
更具体地，本发明的有益效果还包括：
1、使裂解还原转化反应在旋转的封闭筒体内进行，有机物料在反应装置中持续搅拌，均匀受热，使反应充分完全，能够最大程度地产出可燃气体、焦油等资源产物，且使其他有害产物的产生达到最低，真正做到了无害化；
2、从裂解到气体处理的全过程采用封闭循环运行，使所述有机物料隔绝空气，处理过程和排放完全受控，有机物料的反应过程稳定、产出稳定；
3、用于为封闭筒体提供热量的燃烧器独立设置，仅对封闭筒体提供热量，即间接加热，而不会将明火引入其中。这种方式便于在筒体内设置环境信息采集装置并继而有助于对筒体内的内部环境进行精确控制。
4、燃烧器燃烧所用的燃料气体至少部分来自封闭旋转式的裂解还原转化反应。由于裂解还原转化反应充分稳定，可燃气体的产出能够达到最大、品质高且流量稳定，从而有效保证了燃烧器的燃烧稳定，自体产出最大程度满足了自体能源需求。整个系统达到稳定的能量循环，系统自身对外部供给燃料的需求量降至最低，从而大大降低了能源消耗和运行成本。
5、本方法还包括接收环境数据反馈，对裂解还原转化反应的过程进行精确的参数控制，以保证整个工艺的循环平衡和反应充分。例如，通 过采集筒体中的温度、压力、湿度和酸碱度数据，控制筒体中的内环境保持理想状态或按照理想的控制过程进行反应；又例如，通过控制气相产物的冷却温度，使焦油油气的分离更彻底，避免不期望的混杂造成分离后获得的可燃气体品质下降，在后续的燃烧中产生不期望的有害产物，甚至影响反应腔内的温度。
6、自动化程度高、易操作。数据反馈和处理的方法能够使工艺中所有的程序步骤全部自动化完成，无需人为介入，对操作人员的要求很低。
7、本工艺方法能够自动进行物料的分选、破碎，物料的成分和形态得到有效的控制，从而为裂解反应提供理想的物料，能够避免物料品质参差不齐对反应程度造成影响，适用于回收各种品质的含有生物质的生活垃圾。
8、本裂解还原转化处理方法能够直接将固体产物“碳”单独排放和/或回收，不与气相产物混杂，便于分离、回收利用。
9、其中的气体处理过程能够将裂解还原转化反应装置得到的气相产物进行完全分离，将其分离为“焦油、可燃气体和水”，从而便于各自单独进行回收利用。
附图说明
附图1是本发明实施例中生活有机垃圾的裂解还原处理工艺图。
附图2是实施本发明的处理所采用的生活有机垃圾的裂解还原转化反应处理设备的示意图。
【附图标记】
1：地磅；2：抓装机；3：皮带输送磁选机；4：破碎机；5：皮带输送机；6：送料仓斗；7：物料推进装置；8：封闭旋转式裂解还原转化反应装置；9：筒体；10：齿环传动机构；11：密封采用波纹管机械组合密封装置；12：螺旋物料导料板；13：水冷出料输送机；14：进料密封装置；15：出料密封装置；16：加热装置；17：导热室；18：自配风燃烧 器；19：比例控制阀；20：燃气净化器；21：降尘净化器；22：气相冷凝集束装置；23：分汽包；24：冷却除尘塔；25：油气水分离器；26：供氧风机；27：有机碳储存装置；28：储油装置；29：循环水箱；30、出料螺旋输送机。
具体实施方式
为了更好的解释本发明，以便于理解，下面结合附图，通过具体实施方式，对本发明作详细描述。
本发明涉及一种生活有机垃圾的裂解还原处理方法，该方法通过提供一种裂解还原转化反应处理环境，创造条件引导物质按照其最原本的属性自然地进行还原分解，重新回到有机物质前的无害物性状态。具体作法：将生活有机垃圾经过预处理系统、裂解还原转化反应系统、气体处理系统、参数控制等，处理生活有机垃圾使其变为资源物质。
如图1所示，本发明的生活有机垃圾的裂解还原转化处理方法大致包括如下步骤：
首先，有机废料(即生活有机垃圾)进场后经计量仓储后作为待用原料，先进行前置处理，包括但不限于经磁选装置去除金属电池等无机类废弃物。
其次，得到的有机物料经螺旋推进进入裂解还原反应装置中进行反应，反应包括干燥步骤、干馏反应步骤和碳化步骤。
然后，裂解还原反应得到的气相产物进行燃气处理，在冷凝系统中进行油、水、气分离，该冷凝系统与循环水池相连，以确保冷凝系统给气相产物提供适当的温度。
继而，分离所得焦油存储作为本生活有机垃圾的主要产品，可向市场销售；所得的不凝气(主要成分是可燃气体)经过净化系统的净化获得高纯度可燃气体，导入加热装置燃烧产生热量，供应给裂解还原反应装置供裂解还原处理所用。可燃气体燃烧后的气体产物经除尘可达标排放。
另一方面，裂解还原反应得到的固相产物为有机质碳，单独进行冷却、回收，冷却后以固态有机质碳的形态储存。
上述裂解还原反应的全过程均由参数控制系统进行参数控制，以保证反应按照理想的条件进行。使反应均匀、充分进行，并充分利用回收的可燃气体作为燃料，为物料反应提供热量。
上述裂解还原处理方法，由图2所示的生活有机垃圾的裂解还原处理设备实现，生活有机垃圾由所述裂解还原处理设备实现裂解还原处理的详细过程将结合设备的构成进行描述。
生活有机垃圾和有机物料
本发明中涉及的生活有机垃圾，指的是人类日常生活中产生的果蔬皮梗、食物残渣、秸秆、枯枝、树叶等以生物有机质为主要成分的垃圾。在当前国内垃圾分类不完全、不精细的条件下，这些生活有机垃圾不可避免会掺杂一些无机物废物物料，例如玻璃瓶罐、建筑垃圾、金属、电池等。为了更好地实施本发明，本发明需要对收集的生活有机垃圾进行预处理以获取有机物料，使最终进入设备的有机物料由碳、氢、氧三元素所构成。
预处理系统设备
图2所示生活有机垃圾的裂解还原处理设备中，预处理系统设备包括：地磅1、抓装机2、皮带输送磁选机3和破碎机4。
运转车载生活有机垃圾进场，经地磅1计量重量后卸入仓储室；借助于人工或分选设备去除生活有机垃圾中的非有机物，例如建筑垃圾、瓶、罐等；采用抓装机2上料给皮带输送磁选机3除去金属和电池等成分；输送给破碎机4破碎成50～100毫米大小、小于15毫米厚度的均匀块状的有机物料。
借助于这一预处理系统设备，获得品质良好的有机物料，有助于后续裂解还原转化反应的进行。当然，也不排除收集到了有机生活垃圾本 身的品质良好，这种情况下，预处理系统设备可以省略。根据实际情况，在不影响处理的前提下，预处理系统设备的部分或全部装置可以省略。
裂解还原转化反应系统设备
裂解还原转化反应系统设备包括：皮带输送机5、进料仓斗6、物料推进装置7、封闭旋转式的裂解还原转化反应装置8、出料螺旋输送机30、和加热装置16。
所述皮带输送机5用于将预处理后获得的有机物料输送到位于封闭旋转式裂解还原转化反应装置8一侧的进料仓斗6。物料自进料仓斗6进入物料推进装置7并由所述物料推进装置7推动进入所述封闭旋转式的裂解还原转化反应装置8。
物料推进装置7
所述物料推进装置7包括在壳体和设置在壳体中沿水平方向布置的螺杆，所述壳体的第一端连接所述进料仓斗6，第二端连接所述封闭旋转式的裂解还原转化反应装置8。所述水平的螺杆一直从所述第一端延伸到第二端，甚至一直延伸到裂解还原转化反应装置8的内部，螺杆上形成有沿阿基米德螺旋线设置的连续叶片，用以以阿基米德螺旋推进方式将从进料仓斗6接收的有机物料推进到所述封闭旋转式的裂解还原转化反应装置8内。或者可选地，物料推进装置也可以采用液压方式推进物料。物料由物料推进装置7横向地推送到封闭旋转式裂解还原转化反应装置8内部。
在所述物料推进装置7的第一端或者在所述进料仓斗6上设置有可操作的封闭装置，在预期重量或体积的有机物料进入封闭旋转式裂解还原转化反应装置8中后、开始反应前，关闭所述封闭装置，使封闭旋转式裂解还原转化反应装置8内部形成封闭无氧空间。
所述封闭旋转式裂解还原转化反应装置8
所述封闭旋转式裂解还原转化反应装置8包括卧式的筒体9，所述筒体9在工作时绕着水平轴线旋转，以保证物料在筒体中始终动态保持均 衡的分布以及保证筒体中任何部位的物料在同一时刻具有相同或基本相同的温度。所述旋转包括顺时针旋转和/或逆时针旋转，即所述筒体9能够正转和翻转。
优选地，筒体具有圆形、多边形等围绕所述水平轴线中心对称的横截面。将所述筒体9设计为卧式，一方面，方便实现筒体的旋转；另一方面，卧式筒体9在绕水平轴线旋转时，会带动有机物料抛起、落下，这种旋转形式尤其有利于将有机物料搅拌均匀。需要指出的是，此处所指的水平轴线，并不限定为严格的水平，可以想见的是，将筒体设置为略微倾斜，只要不影响物料在筒体内的翻转搅拌，都在本发明的保护范围之内。类似地，进料和出料的水平螺杆也并非必需严格的水平。水平设置仅为优选的方案。
筒体9的旋转借助于电机和由电机驱动的齿环传动装置实现。具体地，可以在筒体9的外表面固定设置齿环，所述齿环的中心线即筒体9的旋转轴线。电机通过传动装置与所述齿环接合，带动筒体9旋转。所述齿环根据筒体9的规模设置一个、两个或多个。
电机允许筒体9在需要的时候正向或反向旋转，从而在一个方向旋转导致筒体内物料堆积时，转为反向旋转使物料更均匀地分散在筒体内，从而进一步促进均匀受热。
筒体9的进料口和出料口分别位于筒体两端，进料口采用密封装置11与物料推进装置7的壳体密封连接。优选地，所述密封装置为波纹管机械组合密封装置11。出料口同样采用波纹管机械组合密封装置11与出料螺旋输送机30的壳体密封连接。
物料推进装置7的螺杆穿过筒体9的进料口伸入筒体9内。筒体9内壁设有螺旋物料导料板12，用于借助于筒体9的旋转动作将物料从筒体9内部导向出料口。
出料螺旋输送机30作为出料输送装置用于将反应后的固体产物从出料口排出和/或回收。所述出料螺旋输送机30包括壳体和设置在壳体中沿 水平方向布置的螺杆，如前所述，其壳体的一端与所述筒体9的出料口密封连接并通过所述出料口与所述筒体9内部连通，螺杆一端伸入在筒体9中，另一端朝向远离筒体9的方向延伸。类似于物料推进装置7的结构，出料螺旋输送机30的螺杆上形成有沿阿基米德螺旋线设置的连续叶片，用以以阿基米德螺旋推进方式将筒体9内部的物料向外输出。
所述出料螺旋输送机30的壳体上远离所述筒体9的一端包括向下的可封闭的排料口。所述排料口在反应期间封闭，在反应完成后打开用于排出反应生成的有机质碳。
排料口借助于出料密封装置15连接垂直向下的水冷出料输送机13。水冷出料输送机13包括设置在出料管道外部的水套，向出料管道内的有机质碳提供水套式水循环冷却，使有机质碳的出料温度降低到安全温度后输送到有机质碳储存装置27中。
筒体9内部与一集气管道连通，用于收集干馏反应过程中产生的气相产物。在图示的实施例中，集气管道连接在物料推进装置14的壳体侧壁上，从而与筒体9的内部气体连通。集气管道不设置在旋转的筒体9的侧壁上，而是设置在固定不动的物料推进装置14的壳体侧壁上可以降低连接结构的复杂度。同时，在筒体9中产生气相产物时，物料推进装置14中几乎没有物料，不存在管道入口堵塞的风险。
加热装置
加热装置16用于对裂解还原转化反应装置8进行加热，以去除筒体9内部的物料中的水分，使物料的热值得到提高，促进裂解还原转化反应的发生。所述加热装置16可以设置一个或多个，在加热装置设置多个的情况下，能够根据加热的需求启动其中的一个或多个。这样，能够实现对裂解还原转化反应装置8的灵活加热，满足筒体9内有机物料对温度的要求。
所述加热装置16包括能够对筒体9的至少一部分进行热量传递的导热室17。例如，导热室17设置在筒体9的底部，沿筒体的母线方向覆盖 所述筒体的底部，并通过热传导的方式将导热室17内产生的热量传递到筒体9内，从而实现对筒内物料的间接加热。在筒体9转动时，热量可以从筒体9表面的不同位置传递给筒内物料。
所述导热室17内的热量由燃料(例如从裂解还原转化反应装置8的气相产物中分离获得的可燃气体)借助于自配风燃烧器18燃烧产生，供氧风机26用于向燃烧器18内供应空气或氧气。导热室17的内部由耐火保温材料制成，以保证最大比例的热量都将被传递至筒体9而非逸散。
与燃烧器18相连接的燃气管道或空气管道中设置有比例控制阀19用来控制空气和燃气进入的比例，能够控制燃烧产生的热量大小，从而按照既定的温度曲线精准地控制导热室17的内部温度。在燃烧器内和筒体内达到热平衡时，二者的温度相同。
比例控制阀19与一PLC控制器连接，PLC控制器根据筒体9内物料的下述温度反应条件来控制比例控制阀19。
可燃气体在燃烧器18的炉膛中燃烧所产生的烟气经冷却除尘塔24除去杂质后直接达标排放。可选地，还包括湿法过滤装置，通过与5％浓度喷淋的碱液混合反应去除烟气当中的酸性有害气体。
在除尘过滤排放之前，优选在排气管道中设置一氧化碳检测器，并与所述PLC控制器连接，在线实时检测烟气中所包含的一氧化碳排放量，并根据一氧化碳排放量调节燃烧器比例控制阀19。当一氧化碳排放量高于某一阈值时增大供氧量或增大氧气和燃料气体的比例；当一氧化碳排放量低于某一阈值时，保持供氧量或保持氧气和燃料气体的比例，总之，使一氧化碳排放量保持最小，使燃料气体在燃烧器中达到充分燃烧。所述燃料气体包括回收的所述可燃气体。
筒体9内的温度反应条件
具体而言，在物料的整个处理过程中，温度曲线沿时间先后顺序可分为：
第一段干燥阶段，筒体9内温度保持100～200℃，其作用是使筒体内物料的水分蒸发，使物料均匀受热、逐渐干燥达到物料干燥标准。
此处及下文中所述的均匀受热，是指筒体内任何部位的有机物料在同一时刻的温度相同或基本相同，均匀受热是本发明强调的其中一个关键技术，无论在干燥阶段、干馏反应阶段或是碳化阶段，均期望物料在筒体中均匀受热。本发明中的均匀受热通过使物料在筒体内持续翻转来实现。所谓持续翻转是指物料在干燥、干馏反应或碳化的各个阶段全程连续地或者以已知时间间隔间断地翻转。即，持续翻转并不意味着筒体必需连续转动，也可以以一定时间间隔地转动，例如转动2分钟，间隔0.5分钟，然后继续同向或反向地转动2分钟，再间隔0.5分钟等。
通常满足干馏反应条件的物料干燥标准是含水量20％左右，此阶段持续的时间根据待处理物料自身的含水量有所调整。
在此阶段中可以通过观察集气管道中气相冷凝集束装置上的观察窗来辅助检测物料的干燥程度。如果物料湿润，将在气相冷凝集束装置的观察窗上观察到冷凝水，随着物料的干燥，冷凝水逐渐减少，至观察窗干燥，物料达到干燥标准。
第二段干馏反应阶段，继续使物料均匀受热并缓慢升温至450°C～550℃并保持。此阶段的作用是产生大量的可燃气体和焦油油气。从干燥阶段的保持温度开始以15℃～20℃/分钟的升温速率持续升温。以这一速率升温，能够保证后续干馏反应的稳定发生。升温到300℃后，干馏反应开始发生，主要的产物是甲烷、乙烯、乙烷和一氧化碳。此阶段反应的时间根据物料的组分不同而有所不同。本发明通过监测筒体内压力来辅助判断反应是否完成，具体而言，反应过程中压力逐渐增大，反应尾声压力逐渐减小。控制装置在检测到压力减小时，判断反应结束。优选地，当压力减小至趋于稳定时，反应完全结束，且产生的气相产物基本全部被回收。
第三阶段碳化阶段，筒体9内的温度保持在580℃～640℃，优选 600℃。在此过程中仍然继续保证物料均匀受热。其中经过充分干馏反应后的物料不再产生气液相产物，而逐渐碳化，生成固相产物有机质碳。
三个阶段温度的控制，可通过加热装置的数量，控制导热室内的压力实现。导热室内的压力和导热室的温度直接控制着筒体内温度的稳定，以达到三个阶段工作进程和效率最佳。
借助于上述控制过程，能够使反应腔室中的物料充分发生裂解还原转化反应，由于有机物料在密封筒体中的无氧条件下进行反应，物料不燃烧，不会产生有害气体，如二噁英等，由于整个筒体密封，不会向环境中排放粉尘等颗粒污染物，所有的有机物料充分转化为“油、气和碳”。
加热装置16所使用的气体燃料来自于所述封闭旋转式裂解还原转化反应装置8的气相产物。所述气相产物并非直接用作加热装置16，而是需要进行一系列的气体处理，将在下文进行描述。
气体处理系统设备
为了分离和收集上述裂解还原转化反应中的油、气产物，本发明的设备还包括一气体处理系统设备，包括：分汽包23、降尘净化器21、气相冷凝集束装置22、油气水分离器25、燃气净化器20、和循环水箱29。
具体地，裂解还原转化反应装置8上的集气管道中设置有分汽包23，将裂解还原反应过程中产生的HCl、SOx和HF等酸性有毒有害气体通过湿法吸收去除，例如由Ca(OH)2、NaOH等碱性物质吸收去除，并将其余的气相产物进行压力缓冲，便于气体进入后续处理程序。
气相产物从分汽包23进入降尘净化器21，在离心力的作用下粉尘和油气的混合物颗粒下沉，气体经上面的出口逸出，从而将气相产物中夹带的固体颗粒物去除。
经除尘净化后，所述气相产物中全部为高温有机物蒸汽，包括油气混合物。这些蒸汽被输送到气相冷凝集束装置22中。所述气相冷凝集束装置22的结构为常规的集束装置结构，由循环水箱29进行外部冷却，使其中的蒸汽得以冷凝，冷凝后得到气液混合物。
所述气相冷凝集束装置22中的温度需要进行控制，一方面设置温度传感器，另一方面设置温度调节装置，均与参数控制系统设备相连接，使所述气相冷凝集束装置22的温度被控制在10℃，在这一温度条件下焦油油气和可燃气体能够得到彻底的分离。可以想见的是，也可以采用恒温水箱代替温度传感器和温度调节装置，同样也可以将所述气相冷凝集束装置22的温度控制在10℃。这些温度控制手段均在本发明的范围之内。
所述气液混合物进入油水气分离器25，对焦油、水和可燃气体进行分离。经所述油、水、气分离器25分离后，焦油被储存到储油装置28中，可获回收利用；水可进行排放或回收利用；可燃气体经燃气净化器20净化后作为加热装置16的燃料进行循环利用，可燃气体燃烧产生的热量，用于维持裂解还原转化反应所需的温度。
回收的所述可燃气体可以直接通入加热装置16，也可以储存起来，在需要时通入加热装置16。用于在加热装置16中燃烧产生热量的燃料气体包括回收的所述可燃气体以及其他燃料气体，所述其他燃料气体作为所述可燃气体的补充。
燃料气体(包括可燃气体)在燃烧器18的炉膛中燃烧所产生的烟气经冷却除尘塔24除去杂质后直接达标排放。可选地，还包括湿法过滤装置，通过与5％浓度喷淋的碱液混合反应去除烟气当中的酸性有害气体。
参数控制系统设备
为了能够精确地控制裂解还原转化反应的条件，使筒体9内的物料按照理想的温度曲线均匀受热，保证系统的高效运行，本发明还包括一个参数控制系统设备。
所述参数控制系统设备包括设置在筒体9中的温度传感器、压力传感器、湿度传感器、酸碱度计、一氧化碳检测器、驱动筒体9旋转的电机、燃烧器比例控制阀19和/或供氧风机26，以及与这些装置相连接的控制装置。
所述控制装置用于根据所述湿度传感器和或酸碱度计反馈的数据对有机物料的干燥保温时间和酸碱度进行调节。
所述控制装置包括变频控制器和PLC控制器。
变频控制器用来调节供氧风机26的风量，PLC控制器能够调节燃烧器比例控制阀19。通过调节供氧风机26的风量以及调节燃烧器比例控制阀19，能够所述依据所述封闭筒体内所述有机物料的温度要求，对通入燃烧器的燃料气体速率、以及燃料气体和空气的比例进行调节。例如，采集所述封闭筒体内的实时温度，与设定温度对比，当实时温度低于设定温度时，增大通入燃烧器的所述燃料气体的速率，也就是增大燃料气体供给量；当实时温度高于设定温度时减小通入燃烧器的所述燃料气体的速率，也就是减少燃料气体供给量。并且基于燃料气体供给量，按理想比例调节燃料气体和空气的比例。
再例如，PLC控制器还与一氧化碳检测器相连接，在线监测燃烧器排放的一氧化碳排放量并根据一氧化碳排放量调节燃烧器比例控制阀19。当一氧化碳排放量高于某一阈值时增大供氧量或增大氧气和燃料气体的比例；当一氧化碳排放量低于某一阈值时，保持供氧量或保持氧气和燃料气体的比例，总之，使一氧化碳排放量保持最小。
PLC控制器用来控制电机、温度控制、压力控制、湿度控制、反应时间控制及酸碱度控制等。
所述对电机的控制包括对电机启停的控制和对筒体9的旋转转速和旋转方向的控制，以实现物料在筒体内的均匀受热和进排料。
所述温度的控制包括对筒体内有机物料的温度以及升温或降温速率的检测和控制，以确保筒体内有机物料始终满足温度要求；以及根据筒体内有机物料的温度以及升温或降温的速率要求，对通入燃烧器的氧气和燃料气体的气量、速率和比例进行调节，以使温度始终处于理想数值。
所述压力控制包括对封闭旋转式裂解还原转化反应装置8的筒体内压力的检测和/或控制，以及导热室内压力的检测和/或控制，如果在干馏 反应阶段检测到压力下降，则判断为干馏反应结束。
所述湿度控制包括对封闭旋转式裂解还原转化反应装置8的筒体内湿度进行控制，并根据湿度确定第一干燥阶段是否完成。例如，在干燥阶段，检测所述封闭筒体内的湿度，在湿度下降到设定湿度时判断为干燥完成。
所述酸碱度控制包括对封闭旋转式裂解还原转化反应装置8的筒体内的有机物料进行控制，如果酸碱度偏离，可以向筒体内投放适量的酸或碱以调节PH值。尤其需要在干馏反应阶段，检测所述封闭筒体内的酸碱度，当酸碱度偏离设定PH值时，向所述封闭筒体内添加酸或碱，使酸碱度稳定在设定PH值，例如设定PH值为7-8，以有利于干馏反应发生的。
上述控制均为精准控制，使封闭旋转式裂解还原转化反应装置8的筒体内的物料受热均匀，满足其预定的发生裂解还原转化的反应条件，有效地保证系统的连续高效运行。
以上内容仅为本发明的较佳实施例，对于本领域的普通技术人员，依据本发明的思想，在具体实施方式及应用范围上均会有改变之处，本说明书内容不应理解为对本发明的限制。

Claims (14)

  1. 一种生活有机垃圾的裂解还原处理方法，所述生活有机垃圾包括有机物料，其特征在于，将有机物料置入封闭筒体使其隔绝空气，并使其在所述封闭筒体中持续翻转和间接地均匀受热。
  2. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，
    所述受热包括：
    干燥阶段，将所述有机物料加热至100℃～200℃进行干燥；
    干馏反应阶段，将所述有机物料缓慢升温至450℃～550℃并保持，使干燥后的所述有机物料进行干馏反应；
    碳化阶段，在所述干馏反应结束后，升温至580℃～640℃，使反应后的所述有机物料逐渐碳化。
  3. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述有机物料在置入所述封闭筒体中之前经破碎尺寸大小为50～100毫米。
  4. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述持续翻转包括所述封闭筒体的本体绕其自身的水平轴线转动。
  5. 根据权利要求3所述的生活有机垃圾的裂解还原处理方法，其特征在于，在所述干馏反应阶段，所述有机物料缓慢升温的速率为15℃～20℃/分钟。
  6. 根据权利要求3所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述干馏反应产生的气相产物被收集、净化和分离为可燃气体、焦油和水。
  7. 根据权利要求6所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述气相产物经由与所述封闭筒体连通的集气管道被收集。
  8. 根据权利要求6所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述分离通过将所述气相产物冷却至10℃实现。
  9. 根据权利要求6所述的生活有机垃圾的裂解还原处理方法，其特征在于，所述可燃气体用于在燃烧器内燃烧后间接加热所述封闭筒体及其中的有机物料。
  10. 根据权利要求9所述的生活有机垃圾的裂解还原处理方法，其特征在于，通入燃烧器的燃料气体的速率依据所述封闭筒体内所述有机物料的温度要求进行调节，所述燃料气体包括所述可燃气体。
  11. 根据权利要求9所述的生活有机垃圾的裂解还原处理方法，其特征在于，通入燃烧器的空气和燃料气体的比例依据在线检测的一氧化碳排放量进行调节，使所述一氧化碳排放量最小，所述燃料气体包括所述可燃气体。
  12. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，在干燥阶段，检测所述封闭筒体内的湿度，在湿度下降到设定湿度时判断为干燥完成。
  13. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，在干馏反应阶段，检测所述封闭筒体内的酸碱度，当酸碱度偏离设定PH值时，向所述封闭筒体内添加酸或碱，使酸碱度稳定在设定PH值。
  14. 根据权利要求1所述的生活有机垃圾的裂解还原处理方法，其特征在于，在干馏反应阶段，检测所述封闭筒体内的压力，当检测到压力下降，则判断为干馏反应结束。
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