WO2020192221A1 - Dispositif et procédé de gazéification supercritique - Google Patents

Dispositif et procédé de gazéification supercritique Download PDF

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Publication number
WO2020192221A1
WO2020192221A1 PCT/CN2019/129801 CN2019129801W WO2020192221A1 WO 2020192221 A1 WO2020192221 A1 WO 2020192221A1 CN 2019129801 W CN2019129801 W CN 2019129801W WO 2020192221 A1 WO2020192221 A1 WO 2020192221A1
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furnace
heat exchange
supercritical
gasification
pressure
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PCT/CN2019/129801
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English (en)
Chinese (zh)
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楼龙春
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楼龙春
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Publication of WO2020192221A1 publication Critical patent/WO2020192221A1/fr

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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • 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
    • Y02P20/10—Process efficiency
    • 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
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids

Definitions

  • the invention relates to a gasification device and method, in particular to a supercritical gasification device and method.
  • Soluble in supercritical water it can form a single-phase reaction. Usually within a few seconds of reaction time, a destruction rate of over 99.9% can be achieved. It can be used to treat difficult-to-decompose organic chlorides, sludge, dioxins in fly ash, and other dangerous organic substances. Inorganic substances, especially salts, have very low solubility in supercritical water, and can be separated almost insoluble, and become a general fluid aqueous solution after returning to normal temperature and pressure, so there is no concern about secondary pollution.
  • Supercritical Water Oxidation (Supercritical Water Oxidation for short SCWO) method is a technology with extremely clean treatment efficiency and does not require post-treatment equipment. In addition, when the organic content exceeds 2%, the SCWO process can form self-heating without additional heat supply. These characteristics make SCWO have its unique advantages compared with traditional wastewater treatment technologies such as biochemical treatment, Wet Air Oxidation (WAO), and combustion. For wastewater systems that are difficult to treat by traditional methods, SCWO has become A new environmental protection technology with great potential advantages. The supercritical water oxidation method was first proposed by American scholar Modell and others in the mid-1980s and has been unable to enter the market for more than 30 years.
  • WAO Wet Air Oxidation
  • the previous SCWO technology reaction system includes: feed system, pump, preheater , Reactor, cooler (or heat recovery system), separator, etc.
  • the connection between the material preheating system, the supercritical water medium heating system, the oxidant preheating system and the reactor is too complicated, and the equipment material requirements are very high. Not only the equipment construction and production and operation costs are high, but also the entire The system is very unreliable.
  • the first technical problem to be solved by the present invention is to provide a supercritical gasification device with a simple and reasonable structure, convenient to achieve a supercritical state, high conversion efficiency and reasonable operating cost in view of the above-mentioned current state of the art.
  • the second technical problem to be solved by the present invention is to provide a supercritical gasification method with reasonable and practical technology, high efficiency and energy saving, which can effectively reduce operating costs.
  • a supercritical gasification device including a supercritical gasification furnace. It is characterized in that: the supercritical gasification furnace includes a heat exchange device and a furnace chamber for supplying materials for gasification reaction, the heat exchange device is connected with the furnace chamber, and the heat exchange device is provided with materials for the input of materials before gasification
  • the material inlet of the heat exchange device is connected to the material outlet through the furnace, and the material inlet and the material outlet are both exposed outside the supercritical gasification furnace.
  • the furnace is provided with an oxygen nozzle for the input of oxidant and a gas nozzle for the input of combustible gas, and an ignition device for ignition is arranged between the oxygen nozzle and the gas nozzle in the furnace.
  • part of the feed heat exchange tube group of the heat exchange device is in the furnace, so that the furnace and the heat exchange device are integrated into one. In this way, the production process of material gasification from non-supercritical to supercritical state and then from supercritical to non-supercritical state is completed in the supercritical gasifier.
  • the material inlet and the material outlet are located on the same side of the heat exchange device, and the oxygen inlet and fuel gas inlet are located on the side away from the material inlet , And adjacent to the oxygen inlet is provided with an oxygen nozzle to facilitate the introduction of oxygen into the furnace, and adjacent to the fuel gas inlet is provided with a gas nozzle to facilitate the introduction of combustible gas into the furnace, and
  • the fire device is arranged between the oxygen nozzle and the gas nozzle, so that it is convenient to realize the ignition in the furnace.
  • the existing external heating method is changed to directly spray combustible gas and pure oxygen into the furnace to start heating, and continue to input appropriate amount of oxygen during operation to maintain the temperature of the entire system.
  • the tube shape is adopted to better integrate heat preservation Measures to achieve better energy-saving effects; in addition, prepare for the follow-up furnace to reach and maintain a supercritical state.
  • the supercritical gasification furnace includes a first shell, and the furnace core composed of the hearth and the heat exchange device is located in the first shell.
  • the shell is provided with a nitrogen inlet for nitrogen input and a nitrogen outlet for nitrogen outflow, and both the material inlet and the material outlet are exposed outside the first shell.
  • the first shell usually adopts a high-pressure-resistant protective shell structure to better meet the pressure requirements of the supercritical gasification reaction.
  • the materials, motors and gearboxes in the supercritical gasification furnace are all in In a nearly equal pressure environment with dry pure nitrogen, it is like working under normal pressure, which solves the safety sealing problem caused by the huge pressure difference of the equipment made of multiple parts.
  • a pressure sensor is provided in the first housing, a signal output end of the pressure sensor is connected to a pressure signal input end of an automated control system, and a signal output end of the automated control system is connected to a nitrogen supply system.
  • the furnace is provided with a pressure sensor for testing its internal pressure and a temperature sensor for testing its internal temperature.
  • the signal output terminals of the temperature sensor and the pressure sensor are connected to the corresponding signal input terminals of the automation control system.
  • the signal output terminal of the automation control system is connected with the oxidant supply system, and the signal output terminal of the automation control system is also connected with the nitrogen supply system.
  • the signal is transmitted to the automatic control system through the pressure sensor during operation, and the automatic control system controls the nitrogen supply system to input dry pure nitrogen into the supercritical gasification furnace, so that the nitrogen pressure in the supercritical gasification furnace is consistent with the supercritical gas
  • the pressure in the furnace is kept equal, and the error is less than 0.5MPa;
  • the signal of the temperature sensor is connected to the automatic control system, and the automatic control system controls the oxygen supply system to spray an appropriate amount of oxygen into the furnace to maintain the furnace temperature.
  • the temperature sensor signal of the material outlet is output to the automatic control system, and the automatic control system instructs the material feeding system to control the feed flow rate to control the temperature difference between the material inlet and outlet.
  • a second shell is provided in the first shell as an insulation layer shell of the furnace and the heat exchange device to form the furnace core, the heat exchange device is partially located in the second shell, and the heat exchange device includes
  • the feed tube group with the material inlet and the discharge tube group with the material outlet, the feed tube group and the discharge tube group are composed of heat exchange tubes with built-in spiral blades, the first shell and the second
  • the space between the shells is provided with a motor for driving the spiral blades to rotate.
  • the power output end of the motor is transformed into a plurality of drive shafts through a variable speed gear box, and the drive shafts are connected with the spiral shafts of the corresponding spiral blades.
  • the spiral blade is driven by the motor and the variable speed gear box to slowly rotate around its own spiral axis (for example, one rotation per minute) to clean the inner wall of the heat exchange tube, so that the material will not affect the heat exchange device during the reaction process. It causes blockage and at the same time, the material advances spirally in the heat exchange tube, which can not only make the particles have the effect of scouring and descaling on the heat exchange tube wall, but also has a better heat exchange effect.
  • the heat exchange tubes in the feed heat exchange tube group are feed heat exchange tubes, and the heat exchange tubes in the discharge heat exchange tube group
  • the heat exchange tube is a discharging heat exchange tube
  • the feeding heat exchange tube and the discharging heat exchange tube are arranged side by side at intervals
  • a heat conducting layer is arranged between the adjacent feeding heat exchange tube and the discharging heat exchange tube .
  • the composition of the thermally conductive layer has various forms.
  • the thermally conductive layer includes at least one of silicon carbide, aluminum oxide, silicon dioxide, and at least one of pure metal copper, iron, and nickel. Thermally conductive medium.
  • the furnace core composed of the second shell and the furnace chamber and the heat exchange device is filled with insulation materials.
  • the supercritical gasification device also includes a material feeding system useful for supplying materials into the supercritical gasification furnace.
  • the material feeding system includes a buffer constant pressure material tank, a first material tank and a second material tank.
  • the lower part of the first material tank can be communicated with the lower part of the second material tank through a pump.
  • the second material tank are provided with a first connection port communicating with the buffer constant pressure material tank and a second connection port for the input of normal pressure materials at positions adjacent to the upper part of the second material tank.
  • the material output valve is connected to the material inlet, and the buffer constant pressure material tank is also provided with a gas constant pressure valve for maintaining a constant pressure of the material subsequently entering the furnace.
  • the first material tank and the second material tank supply 25MPa material into the buffer constant pressure material tank
  • the first material tank and the second material tank are respectively provided with a first sliding partition and a second Sliding partitions, the materials and clean water in the first material tank and the second material tank are separated by respective sliding partitions and arranged up and down.
  • the technical solution adopted by the present invention to solve the above-mentioned second technical problem is: a method for realizing supercritical gasification in the above-mentioned supercritical gasification device, which is characterized by including the following steps:
  • Start-up phase by passing combustible gas and oxygen into the supercritical gasifier and igniting it, the combustible gas and oxygen are burned in the furnace to increase the temperature and the pressure at the same time, so that the furnace of the supercritical gasifier reaches Supercritical state
  • step 2) The gasified material in step 2) enters the gas-liquid separator through the material outlet of the supercritical gasifier for separation.
  • step 2) the normal pressure material is pressurized by the material feeding system and then buffered and constant pressure is performed by the buffer constant pressure material tank, and then enters the heat exchange device in the supercritical gasifier in step 1) for preheating .
  • step 3 there are two gas-liquid separators, namely the first-stage gas-liquid separator and the second-stage gas-liquid separator.
  • the gasified material enters the first stage through the material outlet.
  • the first-stage gas-liquid separator the combustible gas separated by the first-stage gas-liquid separator is collected in a combustible gas storage tank for use; and the separated mixture of carbon dioxide, ash and water is decompressed or After the hydraulic turbine is decompressed, it enters the second-stage gas-liquid separator, the carbon dioxide gas separated by the second-stage gas-liquid separator is compressed to form liquid carbon dioxide, and the remaining mixed liquid separated by the second-stage gas-liquid separator is precipitated Afterwards, it is directly discharged or reused. In this way, it is easier to obtain the required fuel gas, liquid carbon dioxide, ash and clean water containing inorganic salts through various levels of gas-liquid separators.
  • step 1) the combustible gas and oxygen are burned in the furnace to increase the temperature and increase the pressure at the same time. It is necessary to input dry pure nitrogen into the supercritical gasification furnace, so that the nitrogen pressure between the first shell and the second shell in the critical gasification furnace is always equal to the pressure in the furnace, and the pressure error is less than 0.5MPa until When the temperature in the furnace reaches 600°C ⁇ 1000°C and the pressure reaches 23MPa ⁇ 27MPa, the supercritical gasifier enters the normal operating state. The material stays in the furnace for 10 seconds to 300 seconds. The material before gasification is in the supercritical gas The difference T between the temperature at the material inlet of the chemical furnace and the temperature of the gasified material at the material outlet of the supercritical gasifier is 10°C-50°C.
  • the material is a material slurry with a mass ratio of solid to liquid material of more than 40%.
  • step 2) the temperature in the furnace is 800°C, the temperature in the furnace is maintained by controlling the amount of oxygen injected into the furnace, the furnace of the supercritical gasification furnace
  • the internal operating pressure is 25MPa, the residence time of the material in the furnace is 60 seconds, and the temperature difference T before and after gasification of the material is 30°C.
  • the integration of the device of the present invention greatly simplifies the process route, greatly reduces the construction and operating costs of the supercritical gasification device, greatly improves the production efficiency, and the operation of the entire system becomes extremely stable and reliable, because of the material feeding of the present invention.
  • the system can crush coal, agricultural and forestry wastes, domestic garbage and even floating organic wastes in rivers, lakes and seas into particles or small fragments and mix them with organic toxic waste water to form a slurry, which can easily enter the supercritical heat exchange device for gasification , So as to realize the energy conversion and the efficient production process of harmless thermal decomposition of organic toxic substances.
  • Figure 1 is a schematic diagram of a supercritical gasification device and method according to an embodiment of the present invention
  • Figure 2 is a schematic diagram of the structure of the supercritical gasifier in Figure 1;
  • Fig. 3 is a schematic diagram of the structure of the material feeding system in Fig. 1.
  • the supercritical gasification device includes supercritical gasification furnace 1.1, material feeding system 1.2, oxidant supply system 1.3, nitrogen supply system 1.4, gas-liquid separator, carbon dioxide liquefaction system 1.64, ash and slag water precipitation Separation tank 1.63 and automatic control system 1.7.
  • the material feed system 1.2 is connected to the supercritical gasification furnace 1.1 through the constant pressure material output valve 1.21, and the oxidant supply system 1.3 is connected to the supercritical gasification furnace 1.1 through the buffer constant pressure oxygen tank output valve 1.31; in addition, gas-liquid separation There are two devices, namely the first-stage gas-liquid separator 1.5 and the second-stage gas-liquid separator 1.6; the supercritical gasifier 1.1 is connected to the nitrogen supply system 1.4 through the nitrogen output control valve 1.41, and the supercritical gas The chemical furnace 1.1 is connected to the first-stage gas-liquid separator 1.5. One end of the first-stage gas-liquid separator 1.5 is connected to the combustible gas storage tank 1.54 through the combustible gas output control valve 1.51.
  • the other end of the first-stage gas-liquid separator 1.5 One end is connected to the second stage gas-liquid separator 1.6 through the first discharge control valve 1.52 (or through the hydraulic turbine 1.53), and one port of the second stage gas-liquid separator 1.6 is connected to the carbon dioxide liquefaction system 1.64 through the carbon dioxide emission control valve 1.61 The other port of the second stage gas-liquid separator 1.6 is connected to the ash slag water sedimentation separation tank 1.63 through the second discharge control valve 1.62.
  • the aforementioned material feeding system 1.2 includes a first material tank 3.2a, a second material tank 3.2b, a pump 3.1, a clean water tank 3.3, and a buffer constant pressure material tank 3.5. among them:
  • the lower part of the first material tank 3.2a can be communicated with the lower part of the second material tank 3.2b through the pump 3.1.
  • the first material tank 3.2a and the second material tank 3.2b are equipped with a buffer constant pressure material tank adjacent to the upper part.
  • the connected first connection port and the second connection port for the input of normal pressure materials, the buffer constant pressure material tank 3.5 is provided with a gas constant pressure valve 3.51 that is useful to keep the material entering the furnace 2.1 at a constant pressure.
  • Constant pressure valve 3.51 is mainly a constant pressure valve that maintains a constant pressure of materials through combustible gas.
  • the buffer constant pressure material tank 3.5 communicates with the first material tank 3.2a through the first pressure limiting check valve 3.24, and the buffer constant pressure material tank 3.5 communicates with the second material tank 3.2b through the second pressure limiting check valve 3.25.
  • the first pressure limiting check valve 3.24 is opened, the material in the first material tank 3.2a can be input into the buffer constant pressure material tank 3.5.
  • the second pressure limiting check valve 3.25 is opened, the second The materials in the material tank 3.2b can be input into the buffer constant pressure material tank 3.5.
  • the first material tank 3.2a is provided with a first sliding partition 3.21a to separate clean water and materials; the second material tank 3.2b is filled with materials, and the second material tank 3.2b is also provided with a separate partition for clean water and materials
  • the second sliding partition 3.21b; the first sliding partition 3.21a and the second sliding partition 3.21b can both move up and down, and the materials and clean water in the first material tank 3.2a and the second material tank 3.2b pass through each The sliding partitions are separated and arranged up and down.
  • Normal pressure materials are connected to the first material tank 3.2a through the first one-way valve 3.22, and normal pressure materials are connected to the second material tank 3.2b through the second one-way valve 3.23, that is, the first one-way Valve 3.22, normal pressure materials can be input into the first material tank 3.2a, open the second one-way valve 3.23, normal pressure materials can be input into the second material tank 3.2b.
  • the pump 3.1 closes the fourth valve 3.14 and the second valve 3.12, opens the third valve 3.13 and the first valve 3.11, and presses the clean water in the first material tank 3.2a into the second material tank 3.2b; the pump 3.1 closes The first valve 3.11 and the third valve 3.13, the fourth valve 3.14 and the second valve 3.12 are opened, and the clean water in the second material tank 3.2b is pressed into the first material tank 3.2a.
  • the working process of the material feeding system is as follows:
  • the third valve 3.13, the first valve 3.11 and the pump 3.1 When working, open the third valve 3.13, the first valve 3.11 and the pump 3.1. At this time, the material of about 0.2MPa enters the first material tank 3.2a through the first one-way valve 3.22, and the clean water part in the first material tank 3.2a The material in the second material tank 3.2b is pressed under the second sliding partition 3.21b of the second material tank 3.2b. Under the action of the clear water pressure under the second sliding partition 3.21b, the material in the second material tank 3.2b quickly reaches 25MPa. The second pressure limiting check valve 3.25 automatically opens, and the second material tank 3.21b inputs 25MPa material to the buffer constant pressure material tank 3.5.
  • the second material tank 3.2b When the second material tank 3.2b is almost filled with clean water and the first material tank 3.2a is almost filled with about 0.2MPa material, close the third valve 3.13 and the first valve 3.11, and then open the fourth valve 3.14 and the second Valve 3.12, at this time, the normal pressure material of about 0.2MPa enters the second material tank 3.2b through the second one-way valve 3.23, and the clean water is pressed into the first material tank 3.2a from the second material tank 3.2b via the pump 3.1 Below the first sliding partition 3.21a, the material in the first material tank 3.2a is pressed by the clear water under the sliding partition 3.21a, and the pressure quickly reaches 25MPa, and the first pressure limiting check valve 3.24 opens automatically.
  • the material in the first material tank 3.2a is fed with 25MPa material to the buffer constant pressure material tank 3.5, so that the circulating operation can continuously input the 25MPa material into the supercritical gasifier through the buffer constant pressure material tank 3.5.
  • the above-mentioned supercritical gasification furnace 1.1 (that is, an integrated gasification and heat exchange reactor) includes a first shell 2.10, a second shell 2.7 located in the first shell 2.10, and part of it
  • the above-mentioned first shell 2.10 is a high-pressure resistant shell
  • the second shell 2.7 serves as the furnace 2.1 and heat exchange
  • the supercritical gasification furnace 1.1 includes a heat exchange device 2.2 and a furnace 2.1 for material gasification reaction.
  • the furnace 2.1 is connected with the heat exchange device 2.2, and the heat exchange device 2.2 is the feed material
  • the heat exchange tube group 2.3 may be partly located in the furnace 2.1 to integrate the furnace 2.1 and the heat exchange device 2.2.
  • the heat exchange device 2.2 has a material inlet 2.15 for material input before gasification and a material after gasification.
  • the outflowing material outlet 2.16, the material inlet 2.15 is connected to the material outlet 2.16 through the furnace 2.1, the material inlet 2.15 is connected with the material output valve 3.52 of the buffer constant pressure material tank 3.5, and the material outlet 2.16 is connected to the first stage gas-liquid separator 1.5 connection.
  • the first shell 2.10 is provided with a nitrogen inlet 2.17 for nitrogen input and a nitrogen outlet 2.18 for nitrogen outflow. Both the material inlet 2.15 and the material outlet 2.16 are exposed outside the first shell 2.10, and obviously also exposed in the furnace 2.1 and replacement
  • the heating device 2.2 jointly constitutes outside the furnace core.
  • a pressure sensor is arranged in the first housing 2.10, the signal output end of the pressure sensor is connected to the pressure signal input end of the automation control system 1.7, and the signal output end of the automation control system 1.7 is connected to the nitrogen supply system 1.4.
  • the furnace 2.1 is equipped with a pressure sensor for testing its internal pressure and a temperature sensor for testing its internal temperature.
  • the signal output terminals of the pressure sensor and temperature sensor in the furnace are connected to the corresponding signal input terminals of the automation control system 1.7, automation
  • the signal output end of the control system 1.7 is connected to the oxidant supply system 1.3, and the signal output end of the automation control system 1.7 is connected to the nitrogen supply system 1.4.
  • a motor 2.9 and a transmission gear box 2.8 are arranged in the space between the inner peripheral wall of the first housing 2.10 and the outer peripheral wall of the second housing 2.7.
  • the first housing 2.10 is a high-pressure resistant protective housing, and the second housing 2.7
  • An insulation layer 2.6 is set between the inner peripheral wall of the furnace 2.1 and most of the outer peripheral wall of the heat exchange device 2.2; the material inlet 2.15 and the material outlet 2.16 are located on the same side of the heat exchange device 2.2, on the other side of the furnace 2.1 away from the material inlet 2.15
  • An oxygen inlet 2.13 for oxidant input and a gas inlet 2.14 for flammable gas input are provided on the side.
  • An oxygen nozzle 2.11 is provided adjacent to the oxygen inlet 2.13 to facilitate oxygen input into the furnace 2.1, and an adjacent gas inlet 2.14 is provided for convenient
  • the combustible gas is input into the gas nozzle 2.12 in the furnace 2.1, and a ignition device for ignition is provided in the furnace.
  • the oxygen nozzle 2.11 and the gas nozzle 2.12 are provided between the ports in the furnace for ignition Lighter.
  • the heat exchange device 2.2 includes a feed heat exchange tube group 2.3 with a material inlet 2.15 and a discharge heat exchange tube group 2.4 with a material outlet 2.16. Both the feed heat exchange tube group and the discharge heat exchange tube group include a built-in spiral
  • the blades are composed of heat exchange tubes.
  • the space between the first shell 2.10 and the second shell 2.7 is provided with a motor 2.9 for driving the rotation of the spiral blade.
  • the power output end of the motor 2.9 is changed into multiple drives through a variable speed gear box 2.8
  • the drive shaft is connected with the screw shaft of the corresponding screw blade.
  • the heat exchange tubes in the feed heat exchange tube group 2.3 are feed heat exchange tubes
  • the feed heat exchange tube group 2.3 includes a feed connection pipe 2.31 with a material inlet 2.15
  • the feed heat exchange tube group 2.3 has The inlet end connected by the feeding connecting pipe 2.31
  • the heat exchange tube in the discharging heat exchange tube group 2.4 is the discharging heat exchange tube
  • the discharging heat exchange tube group 2.4 includes the discharging connecting pipe 2.41 with the material outlet 2.16
  • the heat exchange tube group 2.4 has an outlet end connected to the discharge connecting pipe 2.41.
  • each feed heat exchange tube 2.3 has an inlet end connected to the feed connection pipe 2.31, the feed connection pipe 2.31 is connected to the material inlet 2.15, and the outlet end of each feed heat exchange tube 2.3 extends into the furnace 2.1 Inside and adjacent to the ports of the oxygen nozzle 2.11 and the gas nozzle 2.12.
  • the material inlet 2.15 of the above-mentioned feeding heat exchange tube group and the material outlet 2.16 of the discharging heat exchange tube group are both located on the same side of the heat exchange device 2.2.
  • the discharging heat exchange tube and the feeding heat exchange tube are both There are two, but in practical applications, the number of the discharge heat exchange tube and the feed heat exchange tube is not limited to two.
  • the heat exchange tubes in the above-mentioned feed heat exchange tube group 2.3 and the discharge heat exchange tube group 2.4 are composed of heat exchange tubes with built-in spiral blades, and the spiral blades in each heat exchange tube pass through their respective spiral shafts.
  • the motor 2.9 is transformed into multiple drive shafts through the transmission gearbox 2.8, and the multiple drive shafts are respectively connected to the spiral shafts in the heat exchange tubes.
  • the spiral blades in each heat exchange tube rotate around their respective spiral shafts under the drive of the motor 2.9. Thereby cleaning the inner tube wall of the heat exchange tube.
  • the spiral leaf is made of pure nickel or pure iron, and the material is added with a proper amount of alkaline material (preferably calcium carbonate powder) to make it alkalescent, and when the material contains agricultural and forestry waste as the main feed into the system, it will naturally appear alkalescent , Pure metallic nickel and pure metallic iron have good corrosion resistance in alkaline state and reducing atmosphere, while pure metallic nickel has excellent oxidation and corrosion resistance, and pure metallic nickel is preferred.
  • alkaline material preferably calcium carbonate powder
  • a heat transfer layer 2.5 is cast between adjacent heat exchange tubes.
  • a thermally conductive layer 2.5 is also casted between the inner peripheral wall of the inner wall and the adjacent feed heat exchange tube or the adjacent discharge heat exchange tube.
  • the medium of the above-mentioned thermal conductive layer 2.5 includes at least one of silicon carbide, aluminum oxide, silicon dioxide, and at least one of high-temperature-resistant pure metals such as copper, iron, nickel, etc.
  • the heat-conducting medium of the heat-conducting layer is preferably silicon carbide and pure metallic copper cast into a composite material with high thermal conductivity.
  • the above-mentioned material is a slurry containing solids and liquid substances with a mass ratio of up to 40% or more.
  • the material contains a mass ratio of 0-30% coal powder and 0-15% combustible waste.
  • the powder is mixed with 50%-95% sewage and an appropriate amount of calcium carbonate powder to form a slurry.
  • the waste material powder can be agricultural and forestry waste material powder or fine fragments of organic waste such as domestic garbage.
  • the material in this embodiment is made by mixing 30% coal powder, 10% agricultural and forestry waste powder, 60% sewage and appropriate amount of calcium carbonate powder. Slurry.
  • the constant pressure material output valve 1.21 in the high pressure feeding system (the constant pressure material output valve 1.21 is also the material output valve 3.52 in the material feeding system), it is input from the material inlet 2.15 through the feeding heat exchange tube group 2.3 To the furnace 2.1, and then from the furnace 2.1 to the first-stage gas-liquid separator 1.5 through the discharge heat exchange tube group 2.4 and the material outlet 2.16.
  • the working principle of the oxidant supply system only needs to be input from the liquid oxygen storage tank through the low temperature and high pressure liquid pump to the liquid oxygen expander.
  • the automatic control system 1.7 can provide 25MPa oxygen to the furnace of the supercritical gasifier.
  • the working principle of the nitrogen supply system is similar to that of the oxidant (oxygen) supply system.
  • the supercritical gasification method is as follows:
  • the supercritical gasification device when the second discharge control valve 1.62 has clear water flowing out, the supercritical gasification device is full of clear water at this time, close the constant pressure material output valve 1.21; then open the gas through the gas inlet 2.14 from the gas nozzle 2.12 to the furnace 2.1 Enter the combustible gas (the combustible gas is a carbon monoxide hydrogen mixture or methane gas), and after the second emission control valve 1.62 has combustible gas flow out, the second emission control valve 1.62 is closed.
  • the combustible gas is a carbon monoxide hydrogen mixture or methane gas
  • Step 1) The start-up procedure is also the start-up stage: first start the ignition device of the supercritical gasifier 1.1, so that the oxygen nozzle 2.11 and the gas nozzle 2.12 in the furnace continuously have high-voltage electric sparks between the ports in the furnace. Then open the buffer constant pressure oxygen tank output valve 1.31 and input pure oxygen from the oxygen nozzle 2.11 to the furnace 2.1 through the oxygen inlet 2.13. The furnace 2.1 is ignited, and the combustible gas and pure oxygen are continuously input.
  • the pressure sensor, temperature sensor and automation The control system 1.7 controls the nitrogen input to make the entire supercritical gasification device slowly and synchronously heat up and increase the pressure, so that the supercritical gasification furnace reaches the supercritical state.
  • Step 2) Normal operation procedure: As shown in Figure 1, turn on the material feeding system 1.2, adjust it to reach the normal operating flow, and combine the materials (such as: 30% coal powder, 10% agricultural and forestry waste powder, 60% sewage and appropriate amount Calcium carbonate powder is mixed to form a slurry) After being pressurized, it is introduced into the heat exchange device 2.2 of the supercritical gasifier 1.1 for preheating. There are many ways to achieve pressurization. In this embodiment, the buffer constant pressure material tank 3.5 After being pressurized, it is introduced into the heat exchange device 2.2 of the supercritical gasifier 1.1 for preheating.
  • the preheated material enters the furnace 2.1 of the supercritical gasifier 1.1; the gas constant pressure valve 3.51 is opened to ensure that it enters the furnace 2.1
  • the oxidant supply system 1.3 so that oxygen enters the furnace 2.1 through the buffer constant pressure oxygen tank output valve 1.31 to the oxygen nozzle 2.11 to a proper flow rate, and then the furnace 2.1 maintains a working temperature of 800 through the automatic control system 1.7 °C, the pressure is 25MPa
  • the carbon monoxide, hydrogen and a small amount of methane gas produced by the gasification reaction and a small amount of nitrogen generated by the reaction it is gaseous under the environment of temperature ⁇ 374.3°C and pressure of 25MPa, and supercritical gasification
  • the carbon dioxide produced by the furnace and a small amount of hydrogen sulfide may be mixed with water in a liquefied state) in the first stage gas-liquid separator 1.5 through the combustible gas output control valve 1.51 into the combustible gas storage tank 1.54 for later
  • the carbon dioxide gas enters the carbon dioxide liquefaction system 1.64 through the carbon dioxide discharge control valve 1.61 to make liquid.
  • Carbon dioxide, ash and slag water and a small amount of hydrogen sulfide (dissolved in ash and slag water) are discharged to the ash and slag water precipitation separation tank 1.63 through the second discharge control valve 1.62.
  • the solid matter in the material can account for more than 40% by mass, which solves the problem that the existing high-pressure plunger sewage pump can only input the particle size ⁇ 300 microns and the weight ratio of the particulate matter to water ⁇ 3%.
  • the above gasified materials enter the first-stage gas-liquid separator 1.5 through the material outlet 2.16, and the combustible gas separated by the first-stage gas-liquid separator 1.5 is collected into the combustible gas storage tank 1.54 for use.
  • the separated mixture of carbon dioxide, ash and water is decompressed or decompressed by a hydraulic turbine 1.53 (recovered pressure potential energy), and then enters the second-stage gas-liquid separator 1.6, and passes through the second-stage gas-liquid separator
  • the separated carbon dioxide gas is compressed to form liquid carbon dioxide, and the inorganic salt-containing clean water after precipitation of the ash and water mixture separated by the second-stage gas-liquid separator can be directly discharged or reused. In this way, it is easier to obtain the required fuel gas, liquid carbon dioxide, ash and clean water containing inorganic salts through various levels of gas-liquid separators.
  • the residence time of the material in the furnace of the supercritical gasifier 1.1 60 seconds;
  • the running material feed system 1.2 is changed from material feed to clean water, and at the same time, the oxidant supply system 1.3 is closed for the oxygen flow into the supercritical gasifier, and the system quickly cools down.
  • the temperature of the supercritical gasifier 1.1 drops below 200°C
  • the material feeding system 1.2 is closed.
  • the automatic control system 1.7 cooperates to control the nitrogen pressure for equalizing pressure reduction, so that the temperature and pressure of the entire system are reduced. Under pressure, all valves and equipment power supplies can be closed.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

La présente invention concerne un dispositif et un procédé de gazéification supercritique. Le dispositif comprend un four (1.1) de gazéification supercritique, qui comprend un dispositif (2.2) d'échange thermique et un foyer (2.1) pour la réaction de gazéification d'un matériau. Le dispositif (2.2) d'échange thermique est relié au foyer (2.1). Le dispositif (2.2) d'échange thermique est pourvu d'une entrée (2,15) de matériau pour l'entrée du matériau avant gazéification et d'une sortie (2,16) de matériau pour la récupération du matériau après gazéification. L'entrée (2.15) de matériau du dispositif d'échange thermique (2.2) est reliée à la sortie (2,16) de matériau au moyen du foyer (2.1), et l'entrée (2.15) de matériau et la sortie (2,16) de matériau sont exposées hors du four (1.1) de gazéification supercritique. Le foyer (2.1) est pourvu d'une buse (2.11) d'oxygène pour l'entrée d'oxydant et d'une buse (2.12) de gaz pour une entrée de gaz combustible. Un dispositif d'allumage permettant l'allumage est prévu entre les orifices des buses d'oxygène et de gaz dans le foyer (2.1). L'intégration d'un système de préchauffage, d'un système de chauffage de milieu à eau supercritique et d'un système de gazéification facilite la prise de mesures d'isolation thermique efficaces, ce qui permet d'obtenir un effet d'économie d'énergie plus efficace, et d'atteindre facilement les conditions de mise en œuvre les plus suffisantes requises pour une gazéification supercritique.
PCT/CN2019/129801 2019-03-27 2019-12-30 Dispositif et procédé de gazéification supercritique WO2020192221A1 (fr)

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CN110513167B (zh) * 2019-08-27 2022-05-13 中国科学院广州能源研究所 一种热质混合多级发电系统
CN112594695A (zh) * 2020-11-17 2021-04-02 光大环境科技（中国）有限公司 一种用于工业垃圾的超临界水气化装置
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