WO2020006994A1 - 一种带辐射换热的气化炉及气化方法 - Google Patents

一种带辐射换热的气化炉及气化方法 Download PDF

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Publication number
WO2020006994A1
WO2020006994A1 PCT/CN2018/122284 CN2018122284W WO2020006994A1 WO 2020006994 A1 WO2020006994 A1 WO 2020006994A1 CN 2018122284 W CN2018122284 W CN 2018122284W WO 2020006994 A1 WO2020006994 A1 WO 2020006994A1
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Prior art keywords
heat exchange
chamber
gasification
radiant heat
chilling
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PCT/CN2018/122284
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English (en)
French (fr)
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毛炜
黄萍
张燕
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北京航天迈未科技有限公司
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Publication of WO2020006994A1 publication Critical patent/WO2020006994A1/zh

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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
    • C10J3/485—Entrained flow gasifiers
    • 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
    • C10J3/02—Fixed-bed gasification of lump fuel
    • C10J3/20—Apparatus; Plants
    • 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
    • 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
    • C10J3/52—Ash-removing devices
    • 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
    • C10J3/52—Ash-removing devices
    • C10J3/526—Ash-removing devices for entrained flow gasifiers
    • 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
    • C10J3/72—Other features
    • 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
    • C10J3/72—Other features
    • C10J3/74—Construction of shells or jackets
    • C10J3/76—Water jackets; Steam boiler-jackets
    • 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
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1861—Heat exchange between at least two process streams
    • C10J2300/1884—Heat exchange between at least two process streams with one stream being synthesis gas

Definitions

  • the invention belongs to the technical field of coal chemical industry, and particularly relates to a gasification furnace with radiant heat exchange and a gasification method.
  • entrained bed gasification technology Divided from the perspective of energy recovery and temperature reduction measures of crude syngas, entrained bed gasification technology includes chilling process and waste pot process.
  • the chilling process means that the crude synthesis gas at 1300-1600 ° C is directly entered into the water bath at 200-250 ° C from the outlet of the gasification chamber, and the high-temperature crude synthesis gas is rapidly cooled to a low temperature.
  • the process is characterized by stable equipment, simple operation, and long-term operation of the gasification furnace.
  • the gasification process does not make full use of the high-temperature sensible heat of the crude synthesis gas, and directly quenches the crude synthesis gas at 1300 to 1600 ° C to 220. Around °C, the sensible heat at high temperature is converted into saturated steam at low temperature, and the energy efficiency index is low.
  • Waste pot process includes full waste pot process and semi-waste pot process.
  • Full waste pan process means that the crude synthesis gas at 1300 ⁇ 1600 °C passes the radiation waste pan and convection waste pan successively from the gasification chamber outlet, and the temperature at the outlet of the convection waste pan is reduced to about 350 ° C.
  • Effective gas per thousand standard square (CO + H 2 ) The high-temperature superheated steam can be co-produced from 0.7 to 0.9t, and the energy efficiency index is optimal.
  • the water-to-gas ratio (water vapor / dry gas) in the synthesis gas in this process is only 0.2 to 0.3, which is more suitable for IGCC combined power generation.
  • the existing full waste pan process has extremely strict requirements on the quality of raw coal, including ash content, volatile content, ash melting point, viscosity temperature characteristics, silicon-aluminum ratio, potassium-sodium content and other parameters that need to pass a variety of coal. Coal blending is stable in a very narrow range, and localization of raw coal cannot be achieved.
  • the process of semi-waste pot refers to that the crude synthesis gas at 1300 ⁇ 1600 °C is only exchanged by the radiation waste pot at the outlet of the gasification chamber. After a certain amount of saturated steam is produced, the temperature is reduced to 700 ⁇ 900 °C, and then it is cooled in a water bath.
  • the water-to-gas ratio in syngas is comparable to the chilling process. With different operating conditions, the water-to-gas ratio is generally between 0.8 and 1.2, which can ensure that no steam or only a small amount of steam is added in the conversion section, which is a more efficient process flow for chemical production.
  • the mature process only includes the chilling process and the full waste pot process, and the semi-waste pot process is still in the research and development or trial operation stage.
  • Comprehensively starting the gasification device containing the waste pot, the slag plugging of the waste pot, the accumulation of ash, and the leakage of the heat exchange tube are the important reasons for the short operating cycle and poor stability of the device. Therefore, how to efficiently utilize the high-temperature sensible heat of the crude syngas while ensuring that the gasifier can operate stably for a long period of time remains an unsolved problem in the technical field.
  • the present invention provides a gasification furnace with radiant heat exchange and a gasification method with a long operating period and good stability.
  • the gasification furnace recovers the high-temperature sensible heat of syngas. At the same time, it can effectively solve the problem of slagging and ash accumulation in the waste pot process, and can run stably for a long period.
  • a gasification furnace with radiation heat exchange includes a shell and a furnace body provided in the shell.
  • the furnace body includes a gasification chamber, a radiation heat exchange chamber, and chilling arranged coaxially from top to bottom. room;
  • the gasification chamber includes a burner connection port at the top, a lower slag port with a swirl at the bottom, and a gasification reaction chamber located between the top and the bottom.
  • the gasification reaction chamber is provided with a water-cooled wall;
  • the wall surface of the radiation heat exchange chamber is a film-type water-cooled wall, and a spray device is arranged on the upper part of the inside of the film-type water-cooled wall, and the spray device includes a plurality of cooling nozzles arranged in a ring shape and layered; A plurality of heat exchange screens are arranged on the inner wall surface; a diversion exhaust tube is arranged at the lower part of the radiation heat exchange chamber, and the diversion exhaust tube has an inverted cone structure;
  • the chilling chamber is located below the diversion exhaust tube, and a chilling spray head is arranged on the top of the chilling chamber.
  • the inner diameter of the lower slag mouth is smaller than the inner diameter of the gasification reaction chamber, and the ratio of the inner diameter of the lower slag mouth to the inner diameter of the gasification reaction chamber is 1: 3 to 1: 8.
  • the inner diameter of the lower slag mouth is smaller than the inner diameter of the radiation heat exchange chamber, and the ratio of the inner diameter of the lower slag mouth to the inner diameter of the radiation heat exchange chamber is 1: 3 to 1: 8.
  • the lower slag mouth is provided with a swirl guide groove in the same direction as the air flow.
  • the included angle ⁇ between the shrinking slope of the diversion exhaust cylinder and the horizontal direction is 65-75 °.
  • the projection of the film-type water-cooled wall in the horizontal direction is circular or polygonal.
  • the heat exchange screen When the projection of the film-type water-cooled wall on a horizontal plane is circular, the heat exchange screen has a deflection angle ⁇ with respect to a radial direction of the film-type water-cooled wall;
  • the heat exchange screen When the projection of the film-type water-cooled wall on a horizontal plane is a polygon, the heat exchange screen has a deflection angle ⁇ with respect to a vertical line of the film-type water-cooled wall.
  • the range of the deflection angle ⁇ is 0-45 °.
  • the chilling spray head is arranged annularly on the inner wall of the chilling chamber.
  • a gas inlet water wall boiler water inlet N4 is provided on the casing corresponding to the lower part of the gasification chamber, and a gas wall water cooled steam outlet N3 is provided on the casing corresponding to the upper part of the gasification chamber;
  • the top of the casing is provided with a burner connection nozzle N1, and the bottom of the casing is provided with a gasifier slag discharge opening N2.
  • a membrane water-cooled wall boiler water inlet is provided on the casing and corresponding to the bottom of the radiation heat exchange chamber, and a membrane water-cooled wall steam and water outlet is provided on the casing and corresponding to the top of the radiation heat exchange chamber, and the shell
  • a side zone cooling water inlet is provided corresponding to the upper part of the radiation heat exchange chamber, and the side zone cooling water inlet is arranged in communication with the cooling nozzle.
  • a chilled water inlet is provided on the casing and corresponding to the top of the chilled chamber, and the chilled water inlet is disposed in communication with the chilled spray head.
  • a gasification method based on the gasification furnace includes the following steps:
  • step (a) the temperature of the coal gasification reaction is 1300 to 1600 ° C, and the temperature of the high-temperature crude synthesis gas after the reaction is 1300 to 1600 ° C.
  • step (d) the temperature of the crude syngas after the high-level thermal energy is recovered through the radiation heat exchange chamber is 700-900 ° C.
  • the gasification furnace with radiation heat exchange comprises a gasification chamber, a radiation heat exchange chamber and a chilling chamber arranged coaxially from top to bottom.
  • the top of the gasification chamber is a burner connection port.
  • Raw coal and pure oxygen are sprayed into the gasification chamber through the burner to perform a coal gasification reaction.
  • the crude synthesis gas and molten ash are swirled down to enter the lower slag port. Constrained by the special swirl structure of the lower slag mouth, the airflow and molten slag entering the radiant heat exchange chamber still maintain the swirling manifold, and the followability of the slag and airflow is enhanced, which greatly reduces the random diffusion of ash and slag to the radiant heat transfer.
  • the heat exchange screen on the inner wall of the radiant heat exchanger is deflected by a certain angle in the direction of the swirling flow, which not only increases the diameter of the slag passing, but also reduces the disturbance of the air flow on the inner edge of the heat exchange screen, and structurally reduces the risk of slagging and dust accumulation. .
  • the unreacted carbon and the generated CO 2 are still undergoing a Buddell reaction, and the CO reacts with the injected water to change the reaction, so that the effective gas in the crude syngas at the outlet of the radiant heat exchanger (CO + H 2 ) content increases by 1-2%, hydrogen-carbon ratio (H 2 / CO) increases by 0.1, and gasification performance is improved.
  • a set of annular and layered spray devices is provided inside the membrane water-cooled wall in the upper part of the radiation heat exchange chamber, and the low-temperature region (less than 900) close to the membrane water-cooled wall is formed by the spray of the medium. °C) and the core high temperature zone (above 900 °C) located in the center, to achieve the side zone cooling.
  • the edge zone cooling technology can effectively reduce the wall surface temperature of the top area of the radiation heat exchange chamber and ensure that the radiation heat exchange chamber can run for a long period of time. In the central area of the crude syngas, the temperature is still high, and the radiant heat transfer capability is strong, ensuring high radiant heat transfer efficiency.
  • a radiant heat exchange screen with a deflection angle is added to the inside of the membrane water-cooled wall of the radiant heat exchange chamber, which not only increases the heat exchange area of the radiant waste pot per unit height, but also does not cause a rough synthesis gas that swirls.
  • the eddy current is formed with the ash and slag on the innermost edge of the heat exchange screen, which ensures that the diameter of the slag is increased without increasing the size of the equipment, and the risk of slagging and ash accumulation is structurally reduced.
  • the present invention recovers the high-temperature sensible heat of the crude syngas in the radiation heat exchange chamber.
  • the temperature of the crude syngas before chilling is still higher than the condensation temperature of alkali metal oxides such as potassium and sodium, and salts thereof, and does not exist. Slag blocking caused by high alkali metal content.
  • the requirements for parameters such as sticky temperature characteristics and ash content of raw coal are relatively wide. Available raw materials include lignite, bituminous coal, anthracite, coal coke and petroleum coke, etc., which can realize the localization of raw coal.
  • the gasification furnace of the present invention recovers the high-temperature sensible heat of crude synthesis gas, improves the energy utilization efficiency, and can produce 4 to 12 MPa of saturated steam by one thousand standard cubic meters of effective gas (CO + H 2 ).
  • the water-to-gas ratio of the synthesis gas at the gasifier's outlet is equivalent to the gasification technology of the chilling process in the prior art, and does not increase the consumption in the downstream section.
  • the chilled water flow rate is reduced to 30% to 70% of the chilled process, the load in the flash section is reduced, the water circulation volume is correspondingly reduced, the overall economic benefit is increased, and the effective gas cost per unit volume is reduced by about 10%.
  • the gasification furnace according to the present invention fundamentally solves the problem of slagging and ash deposition in the process of radiative heat exchange, and ensures that the device achieves "stable and long-lasting".
  • FIG. 1 is a schematic structural diagram of a radiant heat exchange gasification furnace provided by Embodiment 1 of the present invention
  • FIG. 2 is a schematic structural diagram of a cross section of a straight tube portion of a radiation heat exchange chamber provided in Embodiment 1 of the present invention
  • Embodiment 3 is a schematic structural diagram of a radiant heat exchange gasification furnace provided by Embodiment 2 of the present invention.
  • FIG. 4 is a schematic structural diagram of a cross section of a straight tube portion of a radiation heat exchange chamber provided in Embodiment 2 of the present invention.
  • N1-burner connection nozzle N2-gasifier slag outlet, N3-gasifier water wall soda outlet, N4-gasifier water wall boiler water inlet, N5-membrane water wall soda outlet, N6-side zone Cooling water inlet, N7-membrane water wall boiler water inlet, N8-chilled water inlet, N9-synthetic gas outlet, N9'-synthetic gas and black water mixed discharge port, N10-gasifier black water discharge port.
  • This embodiment provides a gasification furnace with radiant heat transfer.
  • the structure is shown in FIG. 1.
  • the gasification furnace includes a shell 8 and a furnace body provided in the shell 8.
  • the furnace body includes a top to bottom structure.
  • a gasification chamber, a radiation heat exchange chamber 7 and a chilling chamber are coaxially arranged in this order.
  • the gasification chamber includes a burner connection port at the top, a lower slag port 4 with a swirl at the bottom, and a gasification reaction chamber 2 located between the top and the bottom.
  • the burner connection port and the gasification burner 1 connection, the gasification reaction chamber 2 is provided with a water-cooled wall 3;
  • the casing 8 is provided with a gas inlet water-walled boiler water inlet N4 corresponding to the lower part of the gasification chamber, and the casing 8 is provided with a corresponding
  • An upper part of the gasification chamber is provided with a water-cooled wall vapor-water outlet N3 of the gasification chamber;
  • a top of the casing 8 is provided with a burner connection nozzle N1.
  • Raw coal and pure oxygen are injected into the gasification chamber through a burner to perform a coal gasification reaction at 1300 to 1600 ° C. Constrained by the special swirl structure of the gasification burner 1, the reacted crude syngas and molten ash slag swirl.
  • the large-sized slag is thrown on the inner wall surface of the water-cooled wall 3 to form a protective slag layer.
  • the slag layer reaches a certain thickness, the thickness of the slag layer no longer increases, and the liquid slag layer on the inner wall surface does not cool down and enter Under the slag mouth.
  • the crude gas and some fine particles of ash also swirl out of the gasification reaction chamber 2 and enter the lower slag mouth.
  • the lower slag mouth is provided with a swirl guide groove in the same direction as the air flow.
  • the inner diameter of the lower slag mouth is smaller than the inner diameter of the gasification reaction chamber 2, and the ratio of the inner diameter of the lower slag mouth to the inner diameter of the gasification reaction chamber 2 is 1: 3 to 1: 8;
  • the inner diameter of the slag mouth is smaller than the inner diameter of the radiation heat exchange chamber 7, and the ratio of the inner diameter of the lower slag mouth to the inner diameter of the radiation heat exchange chamber 7 is 1: 3 to 1: 8.
  • the lower slag mouth 4 with swirl flow is the connection channel between the gasification reaction chamber 2 and the radiation heat exchange chamber 7, and the inner diameter of the lower slag mouth is much smaller than the gasification reaction chamber 2 located above it.
  • the inner diameter of the radiant heat exchange chamber 7 located below it the flow field of the high-temperature crude synthesis gas and molten slag in the gasifier is first contracted and then expanded, and the flow velocity at the contracted position is the fastest, at the lower slag mouth There is a swirl guide groove in the same direction as the airflow.
  • the device can avoid the rapid and random diffusion of the crude syngas in the radial direction after exiting the slag outlet, maintain the followability of the ash and gas flow in the crude syngas, and reduce the collision between the ash and slag and the inner wall of the radiation heat exchanger , Greatly reducing the tendency of ash and slagging after the crude synthesis gas and ash and slag enter the radiation heat exchange chamber 7.
  • the wall surface of the radiation heat exchange chamber 7 is a film-type water-cooled wall 6, and the projection of the film-type water-cooled wall 6 in a horizontal direction is circular.
  • a spraying device is provided on the inner upper part of the film-type water-cooled wall 6, and the spraying device includes a plurality of cooling spray heads 5 arranged in a ring shape and in layers.
  • the cooling nozzle 5 is used to spray the medium (the cooling medium in this embodiment is cooling water) to form a low-temperature region (less than 900 ° C.) close to the film-type water-cooled wall 6 and a core high-temperature region (higher than 900) in the center. °C), to achieve the side zone cooling.
  • a membrane water-cooled wall boiler water inlet N7 is provided on the casing 8 and corresponding to the bottom of the radiation heat exchange chamber 7, and a membrane water-cooled wall soda is provided on the casing 8 and corresponding to the top of the radiation heat exchange chamber 7.
  • the outlet N5 is provided with a side zone cooling water inlet N6 on the casing 8 corresponding to the upper part of the radiation heat exchange chamber 7, and the side zone cooling water inlet N6 is provided in communication with the cooling nozzle 5.
  • the edge zone cooling technology has the following characteristics: (1) the temperature of the surface of the membrane water-cooled wall 6 is low, and it will not directly contact the high-temperature crude syngas, which ensures that the equipment can run for a long period of time; (2) after cooling by the spray medium, the The ash and slag at the side of the syngas has changed from liquid to solid. Even if it comes into contact with the heat exchange surface, it will not form bonded slag. It may only adhere to some loose dry ash and fall off by vibration or co-current airflow.
  • a diversion exhaust tube 9 is provided at the lower part of the radiation heat exchange chamber 7, and the diversion exhaust tube 9 has an inverted cone structure; the included angle ⁇ between the contraction slope of the diversion exhaust tube 9 and the horizontal direction is 60 to 75 °, ⁇ is greater than the repose angle of the ash at this temperature. Under this condition, only a small amount of solid ash particles may adhere to the inner wall surface of the diversion exhaust cylinder 9. Driven by the airflow flowing in the same direction, the attached solid ash particles collide with the new solid ash particles in the airflow and fall off. Therefore, there are no working conditions in the diversion exhaust tube 9 that accumulate a large amount of solid ash and block the mouth of the tube and affect slag discharge.
  • a plurality of heat exchange screens 12 are provided on the inner wall surface of the film-type water-cooled wall 6.
  • the diameter of the tangent circle formed by the inner edge of the heat exchange screen 12 is defined as the diameter of the slag, that is, the diameter of the clear space through which the ash can pass without obstruction. Within this diameter, the ash in the molten state will not touch the radiation heat exchange chamber 7 Trim.
  • the preferred diameter of the slag passing should be 1.5 to 2 times the inner diameter of the lower slag opening.
  • the heat exchange screen 12 is deflected from the original radial direction perpendicular to the circular membrane water-cooled wall 6 to a certain direction ( ⁇ ).
  • ⁇ the projection of the film-type water-cooled wall 6 on a horizontal plane is circular, and the heat exchange screen 12 has a deflection angle ⁇ with respect to a radial direction of the film-type water-cooled wall 6; and the value of the deflection angle ⁇ The range is 0 to 45 °.
  • the deflection direction of the heat exchange screen 12 is consistent with the high-temperature crude synthesis gas and ash slag swirl direction, the deflection angle ⁇ is adjustable, and the angle control value should be adjusted according to different operating coal types and different operating conditions.
  • the total radiant heat exchange area remains basically unchanged, and the diameter of the slag passing is increased from d2 to d3, and the net area of crude synthesis gas and ash slag is further improved.
  • the inner edge of the heat exchange screen 12 is no longer perpendicular to the circumferential movement of the swirling coarse syngas, and it will not increase the turbulence at the boundary of the air flow, keeping the shape of the rough synthesis air flow substantially unchanged, reducing the fine ash slag particles and the heat exchange screen. 12 surface collision probability, reducing the tendency of dust accumulation.
  • the temperature of the crude synthesis gas is reduced from 1300 to 1600 ° C to 700 to 900 ° C.
  • the ash and slag have been completely converted from the molten state to the solid state, and by-products per thousand standard square effective gas (CO + H 2 ) can be produced as a by-product.
  • ⁇ 12MPa saturated steam 0.5 ⁇ 1.0t. After the steam is overheated by the heater, it can enter the steam pipe network of the corresponding level and be used as power steam.
  • the chilling chamber is located below the diversion exhaust tube 9.
  • a chilling chamber water bath 11 is provided in the lower part of the chilling chamber.
  • a plurality of chilling nozzles 10 are provided on the top of the chilling chamber.
  • the chilling shower head 10 is arranged in a ring shape.
  • a chilled water inlet N8 is provided on the casing 8 corresponding to the top of the chilling chamber, and the chilled water inlet N8 is arranged in communication with the chilling shower head 10.
  • a large amount of chilled water at the top of the chilling chamber is sprayed into the interior of the furnace through the chilling nozzle 10.
  • the crude syngas at about 700-900 ° C is thoroughly mixed with chilled water and quickly cooled down to 200-230 ° C. After the impact of the small water droplets, the crude syngas and ash and slag are fully mixed, and then the gas is separated by the gas-liquid separation effect.
  • the synthesis gas outlet N9 in the upper part of the cold room flows out of the gasifier and enters the downstream washing device.
  • the gasified black water passes through the water bath 11 of the chilling chamber and is then discharged from the black water discharge port N10 of the gasifier in the lower part of the chilling chamber and sent to the flash evaporation system to recover energy; the ash is discharged from the gasifier slag discharge port N2 provided at the bottom .
  • the high-temperature crude synthesis gas and ash and slag pass through the gasification reaction chamber 2, the lower slag port 4 with swirl flow, and the radiation heat exchange chamber 7 into the chilling chamber water bath 11 in sequence. There is a certain swirling effect in the chamber or channel, and the swirling direction remains the same.
  • the amount of chilled water in the semi-waste pot process of the present invention is about 30% to 70% of the amount of chilled water in the chilling process, and the energy saving effect is obvious.
  • This embodiment provides another gasification furnace with radiation heat exchange.
  • the structure is shown in FIG. 3, and includes a shell 8 and a furnace body disposed in the shell 8.
  • the furnace body includes a top-to-bottom A gasification chamber, a radiation heat exchange chamber 7 and a chilling chamber are coaxially arranged in this order.
  • the gasification chamber includes a burner connection port at the top, a lower slag port 4 with a swirl at the bottom, and a gasification reaction chamber 2 located between the top and the bottom.
  • the burner connection port and the gasification burner 1 connection, the gasification reaction chamber 2 is provided with a water-cooled wall 3;
  • the casing 8 is provided with a gas inlet water-walled boiler water inlet N4 corresponding to the lower part of the gasification chamber, and the casing 8 is provided with a corresponding
  • An upper part of the gasification chamber is provided with a water-cooled wall vapor-water outlet N3 of the gasification chamber;
  • a top of the casing 8 is provided with a burner connection nozzle N1.
  • Raw coal and pure oxygen are injected into the gasification chamber through a burner to perform a coal gasification reaction at 1300 to 1600 ° C. Constrained by the special swirl structure of the gasification burner 1, the reacted crude syngas and molten ash slag swirl.
  • the large-sized slag is thrown on the inner wall surface of the water-cooled wall 3 to form a protective slag layer.
  • the slag layer reaches a certain thickness, the thickness of the slag layer no longer increases, and the liquid slag layer on the inner wall surface does not cool down and enters Under the slag mouth.
  • the crude gas and some fine particles of ash also swirl out of the gasification reaction chamber 2 and enter the lower slag mouth.
  • the lower slag mouth is provided with a swirl guide groove in the same direction as the air flow.
  • the inner diameter d1 of the lower slag mouth is smaller than the inner diameter of the gasification reaction chamber 2, and the ratio of the inner diameter d1 of the lower slag mouth to the inner diameter of the gasification reaction chamber 2 is 1: 3 to 1: 8;
  • the inner diameter d1 of the lower slag mouth is smaller than the inner diameter of the radiation heat exchange chamber 7, and the ratio of the inner diameter d1 of the lower slag mouth to the inner diameter of the radiation heat exchange chamber 7 is 1: 3 to 1: 8.
  • the lower slag port 4 with swirl flow is the connection channel between the gasification reaction chamber 2 and the radiation heat exchange chamber 7, and the inner diameter d1 of the lower slag port is much smaller than the gasification reaction chamber located above it.
  • the flow field of the high-temperature crude syngas and molten slag in the gasifier is first contracted and then expanded, and the flow velocity at the contracted position is the fastest, and the lower slag There is a swirl guide groove in the mouth with the same direction as the airflow.
  • the device can avoid the rapid and random diffusion of the crude synthesis gas in the radial direction after exiting the slag outlet, maintain the followability of the ash and gas flow in the crude synthesis gas, and reduce the collision between the ash and slag and the inner wall of the radiation heat exchanger , Greatly reducing the tendency of ash and slagging after the crude synthesis gas and ash and slag enter the radiation heat exchange chamber 7.
  • the wall surface of the radiation heat exchange chamber 7 is a film-type water-cooled wall 6, and the projection of the film-type water-cooled wall 6 in the horizontal direction is a regular polygon.
  • the projection of the film-type water-cooled wall 6 in the horizontal direction is a regular octagon; an upper part of the inside of the film-type water-cooled wall 6 is provided with a spray device, and the spray device includes a plurality of annular and divided ⁇ Arranging of cooling nozzles 5.
  • the cooling nozzle 5 is used to spray the medium (the cooling medium in this embodiment is cooling water) to form a low-temperature region (less than 900 ° C.) close to the film-type water-cooled wall 6 and a core high-temperature region (higher than 900) in the center. °C), to achieve the side zone cooling.
  • a membrane water-cooled wall boiler water inlet N7 is provided on the casing 8 and corresponding to the bottom of the radiation heat exchange chamber 7, and a membrane water-cooled wall soda is provided on the casing 8 and corresponding to the top of the radiation heat exchange chamber 7.
  • the outlet N5 is provided with a side zone cooling water inlet N6 on the casing 8 corresponding to the upper part of the radiation heat exchange chamber 7, and the side zone cooling water inlet N6 is provided in communication with the cooling nozzle 5.
  • the edge zone cooling technology has the following characteristics: (1) the temperature of the surface of the membrane water-cooled wall 6 is low, and it will not directly contact the high-temperature crude syngas, which ensures that the equipment can run for a long period of time; (2) after cooling by the spray medium, the The ash and slag at the edge of the syngas has changed from liquid to solid. Even if it comes into contact with the heat exchange surface, it will not form bonded slag. It may only hang some loose dry ash and fall off by vibration or co-current airflow.
  • a diversion exhaust tube 9 is provided at the lower part of the radiation heat exchange chamber 7, and the diversion exhaust tube 9 has an inverted cone structure; the included angle ⁇ between the contraction slope of the diversion exhaust tube 9 and the horizontal direction is 60 to 75 °, ⁇ is greater than the repose angle of the ash at this temperature. Under this condition, only a small amount of solid ash particles may adhere to the inner wall surface of the diversion exhaust cylinder 9. Driven by the airflow flowing in the same direction, the attached solid ash particles collide with the new solid ash particles in the airflow and fall off. Therefore, there are no working conditions in the diversion exhaust tube 9 that accumulate a large amount of solid ash and block the mouth of the tube and affect slag discharge.
  • a plurality of heat exchange screens 12 are provided on the inner wall surface of the film-type water-cooled wall 6.
  • the diameter of the tangent circle formed by the inner edge of the heat exchange screen 12 is defined as the diameter of the slag, that is, the diameter of the clear space through which the ash can pass without obstruction. Within this diameter, the ash in the molten state will not touch the radiation heat exchange chamber 7 Trim.
  • the preferred diameter of the slag passing should be 1.5 to 2 times the inner diameter of the lower slag opening.
  • the heat exchange screen 12 is deflected by a certain angle ( ⁇ ) from the direction perpendicular to the regular polygonal film-type water-cooled wall 6 to the direction of the swirling flow.
  • ⁇ the projection of the film-type water-cooled wall 6 on a horizontal plane is a polygon
  • the heat exchange screen 12 has a deflection angle ⁇ with respect to a vertical line of the film-type water-cooled wall 6; and the value of the deflection angle ⁇ The range is 0 to 45 °.
  • the deflection direction of the heat exchange screen 12 is consistent with the high-temperature crude synthesis gas and ash slag swirl direction, the deflection angle ⁇ is adjustable, and the angle control value should be adjusted according to different operating coal types and different operating conditions.
  • the total radiant heat exchange area remains basically unchanged, and the diameter of the slag passing is increased from d2 to d3, and the net area of crude synthesis gas and ash slag is further improved.
  • the edges of the heat exchange screen 12 are no longer perpendicular to the circumferential movement of the swirling coarse syngas, and the turbulence at the boundary of the air flow will not be increased.
  • the shape of the rough synthesis air flow will be basically unchanged, and the fine slag particles and the heat exchange screen 12 will be reduced. The chance of collision on the surface reduces the tendency to deposit dust.
  • the temperature of the crude synthesis gas is reduced from 1300 to 1600 ° C to 700 to 900 ° C.
  • the ash and slag have been completely converted from the molten state to the solid state, and by-products per thousand standard square effective gas (CO + H 2 ) can be produced as a by-product.
  • ⁇ 12MPa saturated steam 0.5 ⁇ 1.0t. After the steam is overheated by the heater, it can enter the steam pipe network of the corresponding level and be used as power steam.
  • the chilling chamber is located below the diversion exhaust tube 9.
  • a chilling chamber water bath 11 is provided in the lower part of the chilling chamber.
  • a plurality of chilling nozzles 10 are provided on the top of the chilling chamber.
  • the chilling shower head 10 is arranged in a ring shape.
  • a chilled water inlet N8 is provided on the casing 8 corresponding to the top of the chilling chamber, and the chilled water inlet N8 is arranged in communication with the chilling shower head 10.
  • a large amount of chilled water at the top of the chilling chamber is sprayed into the interior of the furnace through the chilling nozzle 10.
  • the crude syngas at about 700-900 ° C is thoroughly mixed with chilled water and quickly cooled down to 200-230 ° C.
  • the gasification furnace of this embodiment does not have a gas-liquid separation space.
  • the small water droplets, the crude synthesis gas and the ash residue are fully mixed and then enter the chilling chamber water bath 11 and are discharged from the gasifier through the synthesis gas and black water mixing discharge port N9 ′ in the middle and lower part of the chilling chamber water bath 11.
  • a separate tank is separately set outside the gasification furnace.
  • the crude synthesis gas on the top of the separation tank enters the washing device, and the black water and ash residue at the bottom of the separation tank are sent to the flash evaporation system for recovery.
  • the gasification furnace described in this embodiment can effectively reduce the overall height.
  • the high-temperature crude synthesis gas and ash and slag pass through the gasification reaction chamber 2, the lower slag port 4 with swirl flow, and the radiation heat exchange chamber 7 into the chilling chamber water bath 11 in sequence.
  • the amount of chilled water in the semi-waste pot process of the present invention is about 30% to 70% of the amount of chilled water in the chilling process, and the energy saving effect is obvious.

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Abstract

一种带辐射换热的气化炉及气化方法，气化炉包括壳体（8）和设于壳体（8）内的炉体，炉体包括由上至下依次同轴设置的气化室、辐射换热室（7）和激冷室，辐射换热室（7）的壁面为膜式水冷壁（6），膜式水冷壁（6）的内侧上部设置喷射装置，膜式水冷壁（6）的内壁面设置换热屏（12），辐射换热室（7）的下部设置导流排气筒（9），激冷室位于导流排气筒（9）的下方。原料煤和纯氧喷射到气化反应室（2）内进行煤气化反应，反应产物经带旋流的下渣口（4）进入辐射换热室（7），换热屏（12）顺旋流方向偏转一定角度，降低了结渣和积灰的风险。

Description

一种带辐射换热的气化炉及气化方法 技术领域
本发明属于煤化工技术领域，具体涉及一种带辐射换热的气化炉及气化方法。
背景技术
进入二十一世纪以来，我国的煤化工进入高速发展阶段，包括固定床气化技术、流化床气化技术和气流床气化技术均得到了长足的发展，新技术、新工艺也如雨后春笋般不断涌现。经过工业装置的验证和市场的筛选，气流床气化技术成为煤制各种化学品的主流气化技术，该技术不仅在节能减排方面远优于其他气化技术，而且在装置大型化方面走在行业的前列，单台气化炉日处理煤量已经达到3000吨。
从粗合成气的能量回收和减温措施角度划分，气流床气化技术包括激冷流程和废锅流程。
激冷流程指1300～1600℃的粗合成气自气化室出口直接进入200～250℃的水浴内，将高温粗合成气快速冷却至低温。该流程的特点是装置稳定，操作简单，气化炉能够长周期运行，但是该气化流程没有充分利用粗合成气的高温显热，而直接将1300～1600℃的粗合成气激冷至220℃左右，高温显热转化成低温饱和蒸汽，能效指标偏低。此外，为保证气化炉运行平稳，工厂大多按照激冷水泵的最大能力运行，造成气化炉外排黑水量大大增加，使高温合成气中的能量更多的被带到闪蒸系统，产出大量含灰的低品位蒸汽。闪蒸系统中只有灰水预热和除氧器补水预热能够消耗部分蒸汽，其余部分蒸汽因含尘无法补入低压蒸汽管网，只能就地放空，造成工厂经济性下降。
废锅流程包括全废锅流程和半废锅流程。全废锅流程指1300～1600℃的粗合成气自气化室出口先后通过辐射废锅和对流废锅，在对流废锅出口温度降至约350℃，每千标方有效气(CO+H 2)可副产高温过热蒸汽0.7～0.9t，能效指 标最优。但是该流程合成气中水气比(水蒸气量/干气量)仅为0.2～0.3，更适用于IGCC联合发电，如果做化工产品还需要在变换装置向系统内补入大量蒸汽，尤其是制氢气产品，水气比需要增加至1.0左右，装置净副产的蒸汽量大打折扣，产出的经济效益无法弥补增加的装置投资。另外，现有的全废锅流程对原料煤煤质要求极其严苛，包括灰分含量、挥发份含量、灰熔点、黏温特性、硅铝比、钾钠含量等参数均需要通过多种煤的配煤稳定在一个很窄的范围内，无法实现原料煤的本地化。
半废锅流程指1300～1600℃的粗合成气自气化室出口仅通过辐射废锅换热，副产一定量的饱和蒸汽后降温至700～900℃，再进入水浴激冷，激冷后合成气中水气比与激冷流程相当。随着操作条件的不同，水气比一般介于0.8～1.2之间，可保证变换工段不补蒸汽或只补入少量蒸汽，是符合化工生产的更有效的工艺流程。
在国内已开车的气化装置中，成熟的工艺仅包括激冷流程和全废锅流程，半废锅流程尚处于研发或试运行阶段。综合已开车的含废锅的气化装置，废锅堵渣积灰、换热管泄露等原因是造成装置运行周期短、稳定性差的重要原因。因此，如何高效利用粗合成气的高温显热，同时保证气化炉能够长周期稳定运行依然是本技术领域尚未解决的难题。
发明内容
为了解决现有技术存在的上述问题，本发明提供了一种运行周期长、稳定性好的带辐射换热的气化炉及气化方法，所述气化炉在实现回收合成气高温显热的同时，有效解决废锅流程中结渣积灰的问题，能长周期稳定运行。
本发明所采用的技术方案为：
一种带辐射换热的气化炉，包括壳体和设于所述壳体内的炉体，所述炉体包括由上至下依次同轴设置的气化室、辐射换热室和激冷室；
所述气化室包括位于顶部的烧嘴连接口、位于底部的带旋流的下渣口、以及位于顶部和底部之间的气化反应室，所述气化反应室设有水冷壁；
所述辐射换热室的壁面为膜式水冷壁，所述膜式水冷壁的内侧上部设置喷射装置，所述喷射装置包括多个呈环形且分层布置的冷却喷头；所述膜式水冷壁的内壁面设置若干换热屏；所述辐射换热室的下部设置导流排气筒，所述导流排气筒为倒锥形结构；
所述激冷室位于所述导流排气筒的下方，所述激冷室的顶部设置激冷喷头。
所述下渣口的内径小于所述气化反应室的内径，且所述下渣口的内径与所述气化反应室的内径之比为1:3～1:8。
所述下渣口的内径小于所述辐射换热室的内径，且所述下渣口的内径与所述辐射换热室的内径之比为1:3～1:8。
所述下渣口内设置有与气流方向相同的旋流导向槽。
所述导流排气筒的收缩斜面与水平方向的夹角α为65～75°。
所述膜式水冷壁在水平方向上的投影为圆形或多边形。
所述膜式水冷壁在水平面上的投影为圆形时，所述换热屏相对于所述膜式水冷壁的径向具有偏转角度β；
所述膜式水冷壁在水平面上的投影为多边形时，所述换热屏相对于所述膜式水冷壁的边垂线具有偏转角度β。
所述偏转角度β的取值范围为0-45°。
所述激冷喷头呈环形布置于所述激冷室的内壁。
所述壳体上、对应所述气化室的下部设置气化室水冷壁锅炉水入口N4，所述壳体上、对应所述气化室的上部设置气化室水冷壁汽水出口N3；
所述壳体的顶部设置烧嘴连接管口N1，所述壳体的底部设置气化炉排渣口N2。
所述壳体上、对应所述辐射换热室的底部设置膜式水冷壁锅炉水入口，所述壳体上、对应所述辐射换热室的顶部设置膜式水冷壁汽水出口，所述壳体上、 对应所述辐射换热室的上部设置边区冷却水入口，所述边区冷却水入口与所述冷却喷头连通设置。
所述壳体上、对应所述激冷室的顶部设置激冷水入口，所述激冷水入口与所述激冷喷头连通设置。
一种基于所述气化炉的气化方法，包括如下步骤：
(a)原料煤和纯氧通过气化烧嘴喷射到气化反应室内进行煤气化反应，反应后的高温粗合成气和熔融态的灰渣旋流而下进入带旋流的下渣口；
(b)在所述带旋流的下渣口的旋流结构作用下，进入到辐射换热室的高温粗合成气和熔融态灰渣仍保持旋流流形；
(c)在辐射换热室内，高温粗合成气和熔融态灰渣的高位热能被膜式水冷壁和换热屏吸收，粗合成气温度降低，灰渣由熔融态转化为固态；
(d)经辐射换热室回收高位热能后的粗合成气和固态灰渣进入激冷室水浴内，粗合成气经快速增湿冷却，并与固态灰渣实现气固分离；粗合成气经洗涤后送出，固态灰渣由气化炉底部排出。
步骤(a)中，所述煤气化反应的温度为1300～1600℃，反应后的高温粗合成气的温度为1300～1600℃。
步骤(d)中，经辐射换热室回收高位热能后的粗合成气的温度为700～900℃。
本发明的有益效果为：
1、本发明所述的带辐射换热的气化炉，包括由上至下依次同轴设置的气化室、辐射换热室和激冷室。气化室的顶部为烧嘴连接口，原料煤和纯氧通过烧嘴喷射到气化室内进行煤气化反应，反应后的粗合成气和熔融态的灰渣旋流而下进入下渣口。受下渣口特殊旋流结构的约束，进入到辐射换热室的气流和熔融态灰渣仍然保持旋流流形，灰渣与气流的跟随性增强，大大降低灰渣随机扩散至辐射换热室内壁面的几率。同时，辐射换热器内壁的换热屏顺旋流方向偏 转一定角度，既增加了过渣通径，又减弱了换热屏内边缘对气流的扰动，从结构上降低了结渣积灰的风险。
2、在辐射换热室内，未反应完全的碳与生成的CO 2仍在进行布多尔反应，CO与喷入的水发生变换反应，使得辐射换热器出口处粗合成气中的有效气(CO+H 2)含量增加1-2％，氢碳比(H 2/CO)提高0.1，气化性能得到提升。
3、本发明通过在辐射换热室上部的膜式水冷壁内侧，设有一组环形且分层布置的喷射装置，通过介质的喷射，形成贴近所述膜式水冷壁的低温区(低于900℃)和位于中心的核心高温区(高于900℃)，实现边区冷却。所述边区冷却技术可有效降低辐射换热室顶部区域的壁面温度，保证辐射换热室能够长周期运行。在粗合成气的中心区域，温度仍为高温，辐射换热能力较强，确保高的辐射换热效率。
4、本发明在所述辐射换热室的膜式水冷壁内侧增加带偏转角度的辐射换热屏，既增加了单位高度辐射废锅的换热面积，又不会造成旋流的粗合成气和灰渣在换热屏最内侧边缘形成涡流，更保证在设备尺寸不增加的前提下加大了过渣直径，从结构上降低了结渣积灰的风险。
5、本发明在所述辐射换热室回收了粗合成气的高温显热，激冷前粗合成气的温度仍高于钾钠等碱金属氧化物及其盐类的凝华温度，不存在碱金属含量高造成的堵渣问题。且对原料煤黏温特性、灰分含量等参数的要求较宽泛，可使用的原料包括褐煤、烟煤、无烟煤、煤焦和石油焦等，能够实现原料煤的本地化。
6、本发明所述气化炉，回收了粗合成气的高温显热，提高了能量的利用效率，每千标方有效气(CO+H 2)可副产4～12MPa的饱和蒸汽0.5～1.0t，气化炉出口合成气的水气比与现有技术中的激冷流程气化技术相当，不增加下游工段的消耗。同时，激冷水流量降低为激冷流程的30％～70％，闪蒸工段的负荷降低，水循环量也相应降低，整体经济效益增加，单位体积有效气成本下降约10％。
7、本发明所述气化炉，从根本上解决了辐射换热过程中的结渣积灰问题，保障装置实现“安稳长满优”。
附图说明
为了更清楚地说明本发明实施例或现有技术中的技术方案，下面将对实施例或现有技术描述中所需要使用的附图作简单地介绍，显而易见地，下面描述中的附图仅仅是本发明的一些实施例，对于本领域普通技术人员来讲，在不付出创造性劳动的前提下，还可以根据这些附图获得其他的附图。
图1是本发明实施例1提供的一种带辐射换热气化炉的结构示意图；
图2是本发明实施例1提供的辐射换热室的直筒部分截面的结构示意图；
图3是本发明实施例2提供的一种带辐射换热气化炉的结构示意图；
图4是本发明实施例2提供的辐射换热室的直筒部分截面的结构示意图。
图中1-气化烧嘴，2-气化反应室，3-水冷壁，4-带旋流的下渣口，5-冷却喷头，6-膜式水冷壁，7-辐射换热室，8-壳体，9-导流排气筒，10-激冷喷头，11-激冷室水浴，12-换热屏；
N1-烧嘴连接管口，N2-气化炉排渣口，N3-气化室水冷壁汽水出口，N4-气化室水冷壁锅炉水入口，N5-膜式水冷壁汽水出口，N6-边区冷却水入口，N7-膜式水冷壁锅炉水入口，N8-激冷水入口，N9-合成气出口，N9’-合成气及黑水混合排放口，N10-气化炉黑水排放口。
具体实施方式
为使本发明的目的、技术方案和优点更加清楚，下面将对本发明的技术方案进行详细的描述。显然，所描述的实施例仅仅是本发明一部分实施例，而不是全部的实施例。基于本发明中的实施例，本领域普通技术人员在没有做出创造性劳动的前提下所得到的所有其它实施方式，都属于本发明所保护的范围。
实施例1
本实施例提供了一种带辐射换热的气化炉，其结构如图1所示，包括壳体8和设于所述壳体8内的炉体，所述炉体包括由上至下依次同轴设置的气化室、 辐射换热室7和激冷室。
所述气化室包括位于顶部的烧嘴连接口、位于底部的带旋流的下渣口4以及位于顶部和底部之间的气化反应室2，所述烧嘴连接口与气化烧嘴1连接，所述气化反应室2设有水冷壁3；所述壳体8上、对应所述气化室的下部设置气化室水冷壁锅炉水入口N4，所述壳体8上、对应所述气化室的上部设置气化室水冷壁汽水出口N3；所述壳体8的顶部设置烧嘴连接管口N1。原料煤和纯氧通过烧嘴喷射到气化室内在1300～1600℃进行煤气化反应，受气化烧嘴1特殊旋流结构的约束，反应后的粗合成气和熔融态的灰渣旋流而下，大颗粒的熔渣被甩到水冷壁3内壁面形成保护渣层，当渣层达到一定厚度时，渣层厚度不再增加，内壁面未被冷却的液渣层顺流而下进入到下渣口。而粗煤气和部分细颗粒灰渣也旋流出气化反应室2，进入到下渣口。
所述下渣口内设置有与气流方向相同的旋流导向槽。所述下渣口的内径小于所述气化反应室2的内径，且所述下渣口的内径与所述气化反应室2的内径之比为1:3～1:8；所述下渣口的内径小于所述辐射换热室7的内径，且所述下渣口的内径与所述辐射换热室7的内径之比为1:3～1:8。这样设置的理由在于：所述带旋流的下渣口4是气化反应室2和辐射换热室7之间的连接通道，下渣口的内径远小于位于其上方的气化反应室2的内径和位于其下方的辐射换热室7的内径，高温粗合成气及熔融灰渣在气化炉内的流场为先收缩后扩张，并且在收缩位置处的流速最快，在下渣口内设有与气流旋向相同的旋流导向槽，当高温粗合成气及熔融灰渣高速通过时，增强气流的旋流强度，加大气流周向运动速率，使得在不同操作条件下出下渣口粗合成气的流场在可控的范围内。所述装置可避免出下渣口后粗合成气在径向上的快速随机扩散，保持粗合成气中的灰渣与气流的跟随性，减少灰渣间及灰渣与辐射换热器内壁的碰撞，大大减弱粗合成气及灰渣进入辐射换热室7后的积灰结渣倾向。
所述辐射换热室7的壁面为膜式水冷壁6，所述膜式水冷壁6在水平方向上的投影为圆形。所述膜式水冷壁6的内侧上部设置喷射装置，所述喷射装置 包括多个呈环形且分层布置的冷却喷头5。利用所述冷却喷头5进行介质(本实施例喷射介质为冷却水)的喷射，形成贴近所述膜式水冷壁6的低温区(低于900℃)和位于中心的核心高温区(高于900℃)，实现边区冷却。所述壳体8上、对应所述辐射换热室7的底部设置膜式水冷壁锅炉水入口N7，所述壳体8上、对应所述辐射换热室7的顶部设置膜式水冷壁汽水出口N5，所述壳体8上、对应所述辐射换热室7的上部设置边区冷却水入口N6，所述边区冷却水入口N6与所述冷却喷头5连通设置。
所述边区冷却技术具有以下特点：(1)膜式水冷壁6表面的温度较低，不会直接与高温粗合成气接触，保障设备能够长周期运行；(2)经喷射介质冷却后，粗合成气边区处的灰渣已经由液态转变为固态，即使接触到换热表面也不会形成粘结渣，只可能附着一些疏松的干灰，经振打或同向气流的推动力而脱落；(3)中心高温区依然保持很强的辐射能力，换热效果与不增加边区冷却方案相当；(4)边区冷却方案仅影响气流边界处小颗粒固体的运动轨迹，对大颗粒和气流中心颗粒运动轨迹的影响很小，大大降低了熔融灰渣与换热表面触碰的几率。
所述辐射换热室7的下部设置导流排气筒9，所述导流排气筒9为倒锥形结构；所述导流排气筒9的收缩斜面与水平方向的夹角α为60～75°，α大于该温度下灰渣的安息角，在该条件下，只可能有少量的固态灰渣颗粒会附着在导流排气筒9的内壁面上。在同向流动的气流带动下，已附着的固态灰渣颗粒又与气流内新的固态灰渣颗粒相碰撞而脱落。因此，导流排气筒9内不存在积聚大量固态灰渣并堵塞筒口影响排渣的工况。
为增强辐射换热的效果，如图2所示，所述膜式水冷壁6的内壁面设置若干换热屏12。定义由换热屏12内侧边缘形成的切圆直径为过渣直径，即灰渣可无阻碍通过的净空间直径，在该直径范围内熔融态的灰渣不会触碰到辐射换热室7内件。优选的过渣直径应大于下渣口内径的1.5～2倍。
为保证气化炉外壳直径不增加而增大过渣直径，将换热屏12由原有垂直于 圆形膜式水冷壁6的径向方向向顺旋流方向偏转一定角度(β)。具体为：所述膜式水冷壁6在水平面上的投影为圆形，所述换热屏12相对于所述膜式水冷壁6的径向具有偏转角度β；所述偏转角度β的取值范围为0～45°。所述换热屏12的偏转方向与所述高温粗合成气及灰渣旋流方向一致，偏转角度β为可调节，角度控制值应根据不同操作煤种和不同操作条件而调整。换热屏12偏转一定角度后，总辐射换热面积基本保持不变，而过渣直径由d2增大至d3，粗合成气及灰渣流通的净面积进一步提升。此外，换热屏12内边缘不再与旋流粗合成气周向运动相垂直，不会增加气流边界位置的湍动，保持粗合成气流形基本不变，降低灰渣细颗粒与换热屏12表面的碰撞几率，减弱积灰倾向。
经过辐射换热后，粗合成气的温度由1300～1600℃降低至700～900℃，灰渣已经由熔融态全部转化为固态，每千标方有效气(CO+H 2)可副产4～12MPa的饱和蒸汽0.5～1.0t。该蒸汽经过热器过热后可进入对应等级的蒸汽管网作为动力蒸汽使用。
所述激冷室位于所述导流排气筒9的下方，所述激冷室的下部设置激冷室水浴11，所述激冷室的顶部设置多个激冷喷头10，多个所述激冷喷头10呈环形布置，所述壳体8上、对应所述激冷室的顶部设置激冷水入口N8，所述激冷水入口N8与所述激冷喷头10连通设置。
在激冷室顶部大量的激冷水通过所述激冷喷头10喷入炉膛内部。约700～900℃的粗合成气与激冷水充分混合后快速降温到200～230℃，撞击后的小水滴和粗合成气及灰渣充分混合后，再通过气液分离作用，合成气从激冷室上部的合成气出口N9流出气化炉，进入下游的洗涤装置。气化黑水经过激冷室水浴11后再从激冷室下部的气化炉黑水排放口N10排出，送至闪蒸系统回收能量；灰渣从底部设置的气化炉排渣口N2排出。高温粗合成气及灰渣依次经过气化反应室2、带旋流的下渣口4、辐射换热室7进入到激冷室水浴11内，所述高温粗合成气及灰渣在经过各腔室或通道时均存在一定的旋流作用，且旋流方向保持一致。经过核算，对于相同产气量的气化装置，本发明所述半废锅流 程的激冷水用量约为激冷流程激冷水用量的30％～70％，节能效果明显。
实施例2
本实施例提供了另一种带辐射换热的气化炉，其结构如图3所示，包括壳体8和设于所述壳体8内的炉体，所述炉体包括由上至下依次同轴设置的气化室、辐射换热室7和激冷室。
所述气化室包括位于顶部的烧嘴连接口、位于底部的带旋流的下渣口4以及位于顶部和底部之间的气化反应室2，所述烧嘴连接口与气化烧嘴1连接，所述气化反应室2设有水冷壁3；所述壳体8上、对应所述气化室的下部设置气化室水冷壁锅炉水入口N4，所述壳体8上、对应所述气化室的上部设置气化室水冷壁汽水出口N3；所述壳体8的顶部设置烧嘴连接管口N1。原料煤和纯氧通过烧嘴喷射到气化室内在1300～1600℃进行煤气化反应，受气化烧嘴1特殊旋流结构的约束，反应后的粗合成气和熔融态的灰渣旋流而下，大颗粒的熔渣被甩到水冷壁3内壁面形成保护渣层，当渣层达到一定厚度时，渣层厚度不再增加，内壁面未被冷却的液渣层顺流而下进入到下渣口。而粗煤气和部分细颗粒灰渣也旋流出气化反应室2，进入到下渣口。
所述下渣口内设置有与气流方向相同的旋流导向槽。所述下渣口的内径d1小于所述气化反应室2的内径，且所述下渣口的内径d1与所述气化反应室2的内径之比为1:3～1:8；所述下渣口的内径d1小于所述辐射换热室7的内径，且所述下渣口的内径d1与所述辐射换热室7的内径之比为1:3～1:8。这样设置的理由在于：所述带旋流的下渣口4是气化反应室2和辐射换热室7之间的连接通道，下渣口的内径d1远小于位于其上方的气化反应室2的内径和位于其下方的辐射换热室7的内径，高温粗合成气及熔融灰渣在气化炉内的流场为先收缩后扩张，并且在收缩位置处的流速最快，在下渣口内设有与气流旋向相同的旋流导向槽，当高温粗合成气及熔融灰渣高速通过时，增强气流的旋流强度，加大气流周向运动速率，使得在不同操作条件下出下渣口粗合成气的流场在可控的范围内。所述装置可避免出下渣口后粗合成气在径向上的快速随机扩散， 保持粗合成气中的灰渣与气流的跟随性，减少灰渣间及灰渣与辐射换热器内壁的碰撞，大大减弱粗合成气及灰渣进入辐射换热室7后的积灰结渣倾向。
所述辐射换热室7的壁面为膜式水冷壁6，所述膜式水冷壁6在水平方向上的投影为正多边形。优选地，本实施例中所述膜式水冷壁6在水平方向上的投影为正八边形；所述膜式水冷壁6的内侧上部设置喷射装置，所述喷射装置包括多个呈环形且分层布置的冷却喷头5。利用所述冷却喷头5进行介质(本实施例喷射介质为冷却水)的喷射，形成贴近所述膜式水冷壁6的低温区(低于900℃)和位于中心的核心高温区(高于900℃)，实现边区冷却。所述壳体8上、对应所述辐射换热室7的底部设置膜式水冷壁锅炉水入口N7，所述壳体8上、对应所述辐射换热室7的顶部设置膜式水冷壁汽水出口N5，所述壳体8上、对应所述辐射换热室7的上部设置边区冷却水入口N6，所述边区冷却水入口N6与所述冷却喷头5连通设置。
所述边区冷却技术具有以下特点：(1)膜式水冷壁6表面的温度较低，不会直接与高温粗合成气接触，保障设备能够长周期运行；(2)经喷射介质冷却后，粗合成气边区处的灰渣已经由液态转变为固态，即使接触到换热表面也不会形成粘结渣，只可能挂一些疏松的干灰，经振打或同向气流的推动力而脱落；(3)中心高温区依然保持很强的辐射能力，换热效果与不增加边区冷却方案相当；(4)边区冷却方案仅影响气流边界处小颗粒固体的运动轨迹，对大颗粒和气流中心颗粒运动轨迹的影响很小，大大降低了熔融灰渣与换热表面触碰的几率。
所述辐射换热室7的下部设置导流排气筒9，所述导流排气筒9为倒锥形结构；所述导流排气筒9的收缩斜面与水平方向的夹角α为60～75°，α大于该温度下灰渣的安息角，在该条件下，只可能有少量的固态灰渣颗粒会附着在导流排气筒9的内壁面上。在同向流动的气流带动下，已附着的固态灰渣颗粒又与气流内新的固态灰渣颗粒相碰撞而脱落。因此，导流排气筒9内不存在积聚大量固态灰渣并堵塞筒口影响排渣的工况。
为增强辐射换热的效果，如图4所示，所述膜式水冷壁6的内壁面设置若干换热屏12。定义由换热屏12内侧边缘形成的切圆直径为过渣直径，即灰渣可无阻碍通过的净空间直径，在该直径范围内熔融态的灰渣不会触碰到辐射换热室7内件。优选的过渣直径应大于下渣口内径的1.5～2倍。
为保证气化炉外壳直径不增加而增大过渣直径，将换热屏12由垂直于正多边形膜式水冷壁6的方向向顺旋流方向偏转一定角度(β)。具体为：所述膜式水冷壁6在水平面上的投影为多边形，所述换热屏12相对于所述膜式水冷壁6的边垂线具有偏转角度β；所述偏转角度β的取值范围为0～45°。所述换热屏12的偏转方向与所述高温粗合成气及灰渣旋流方向一致，偏转角度β为可调节，角度控制值应根据不同操作煤种和不同操作条件而调整。换热屏12偏转一定角度后，总辐射换热面积基本保持不变，而过渣直径由d2增大至d3，粗合成气及灰渣流通的净面积进一步提升。此外，换热屏12边缘不再与旋流粗合成气周向运动相垂直，不会增加气流边界位置的湍动，保持粗合成气流形基本不变，降低灰渣细颗粒与换热屏12表面的碰撞几率，减弱积灰倾向。
经过辐射换热后，粗合成气的温度由1300～1600℃降低至700～900℃，灰渣已经由熔融态全部转化为固态，每千标方有效气(CO+H 2)可副产4～12MPa的饱和蒸汽0.5～1.0t。该蒸汽经过热器过热后可进入对应等级的蒸汽管网作为动力蒸汽使用。
所述激冷室位于所述导流排气筒9的下方，所述激冷室的下部设置激冷室水浴11，所述激冷室的顶部设置多个激冷喷头10，多个所述激冷喷头10呈环形布置，所述壳体8上、对应所述激冷室的顶部设置激冷水入口N8，所述激冷水入口N8与所述激冷喷头10连通设置。
在激冷室顶部大量的激冷水通过所述激冷喷头10喷入炉膛内部。约700～900℃的粗合成气与激冷水充分混合后快速降温到200～230℃，相比于实施例1中的气化炉，本实施例气化炉不设置气液分离空间，撞击后的小水滴和粗合成气及灰渣充分混合后一并进入激冷室水浴11，并经激冷室水浴11中下部的合 成气及黑水混合排放口N9’排出气化炉。再在气化炉外单独设置一个分离罐，分离罐顶部的粗合成气进入洗涤装置，分离罐底部的黑水和灰渣送入闪蒸系统回收。本实施例所述气化炉相对于实施例1中的气化炉，可以有效降低整体高度。
高温粗合成气及灰渣依次经过气化反应室2、带旋流的下渣口4、辐射换热室7进入到激冷室水浴11内，所述高温粗合成气及灰渣在经过各腔室或通道时均存在一定的旋流作用，且旋流方向保持一致。经过核算，对于相同产气量的气化装置，本发明所述半废锅流程的激冷水用量约为激冷流程激冷水用量的30％～70％，节能效果明显。
以上所述，仅为本发明的具体实施方式，但本发明的保护范围并不局限于此，任何熟悉本技术领域的技术人员在本发明揭露的技术范围内，可轻易想到变化或替换，都应涵盖在本发明的保护范围之内。因此，本发明的保护范围应以所述权利要求的保护范围为准。

Claims (10)

  1. 一种带辐射换热的气化炉，其特征在于，包括壳体(8)和设于所述壳体(8)内的炉体，所述炉体包括由上至下依次同轴设置的气化室、辐射换热室(7)和激冷室；
    所述气化室包括位于顶部的烧嘴连接口、位于底部的带旋流的下渣口(4)、以及位于顶部和底部之间的气化反应室(2)，所述气化反应室(2)设有水冷壁(3)；
    所述辐射换热室(7)的壁面为膜式水冷壁(6)，所述膜式水冷壁(6)的内侧上部设置喷射装置，所述喷射装置包括多个呈环形且分层布置的冷却喷头(5)；所述膜式水冷壁(6)的内壁面设置若干换热屏(12)；所述辐射换热室(7)的下部设置导流排气筒(9)，所述导流排气筒(9)为倒锥形结构；
    所述激冷室位于所述导流排气筒(9)的下方，所述激冷室的顶部设置激冷喷头(10)。
  2. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述下渣口的内径小于所述气化反应室(2)的内径，且所述下渣口的内径与所述气化反应室(2)的内径之比为1:3～1:8。
  3. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述下渣口的内径小于所述辐射换热室(7)的内径，且所述下渣口的内径与所述辐射换热室(7)的内径之比为1:3～1:8。
  4. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述下渣口(4)内设置有与气流旋向相同的导向槽。
  5. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述导流排气筒(9)的收缩斜面与水平方向的夹角α为60～75°。
  6. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述膜式水冷壁(6)在水平方向上的投影为圆形或多边形。
  7. 根据权利要求6所述的带辐射换热的气化炉，其特征在于，所述膜式水冷壁(6)在水平面上的投影为圆形时，所述换热屏(12)相对于所述膜式水冷壁(6)的径向具有偏转角度β；
    所述膜式水冷壁(6)在水平面上的投影为多边形时，所述换热屏(12)相对于所述膜式水冷壁(6)的边垂线具有偏转角度β。
  8. 根据权利要求7所述的带辐射换热的气化炉，其特征在于，所述偏转角度β的取值范围为0-45°。
  9. 根据权利要求1所述的带辐射换热的气化炉，其特征在于，所述激冷喷头(10)呈环形布置于所述激冷室的内壁。
  10. 一种基于权利要求1-9任一项所述气化炉的气化方法，其特征在于，包括如下步骤：
    (a)原料煤和纯氧通过气化烧嘴(1)喷射到气化反应室(2)内进行煤气化反应，反应后的高温粗合成气和熔融态的灰渣旋流而下进入带旋流的下渣口(4)；
    (b)在所述带旋流的下渣口(4)的旋流结构作用下，进入到辐射换热室(7)的高温粗合成气和熔融态灰渣仍保持旋流流形；
    (c)在辐射换热室(7)内，高温粗合成气和熔融态灰渣的高位热能被膜式水冷壁(6)和换热屏(12)吸收，粗合成气温度降低，灰渣由熔融态转化为固态；
    (d)经辐射换热室(7)回收高位热能后的粗合成气和固态灰渣进入激冷室水浴(11)内，粗合成气经快速增湿冷却，并与固态灰渣实现气固分离；粗合成气经洗涤后送出，固态灰渣由气化炉底部排出。
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