CN110791326A - Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method - Google Patents
Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method Download PDFInfo
- Publication number
- CN110791326A CN110791326A CN201911150116.2A CN201911150116A CN110791326A CN 110791326 A CN110791326 A CN 110791326A CN 201911150116 A CN201911150116 A CN 201911150116A CN 110791326 A CN110791326 A CN 110791326A
- Authority
- CN
- China
- Prior art keywords
- gasification
- bed
- auxiliary
- gas
- furnace
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Images
Classifications
-
- 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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—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
- C10J3/72—Other features
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Gasification And Melting Of Waste (AREA)
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention provides a circulating fluidized bed gasification device with a gasification auxiliary bed and a gasification method, wherein the gasification device comprises: the gasification furnace (1) is provided with a fuel inlet, a gasifying agent inlet, a return gas inlet, a furnace gas outlet, a bottom slag outlet and a material returning port; the inlet of the gas-solid separator (2) is communicated with the furnace gas outlet of the gasification furnace (1); and the gasification auxiliary bed comprises a circulating material inlet, a gasifying agent inlet, a return coal gas outlet and a return carbon-containing material outlet, the circulating material inlet of the gasification auxiliary bed is communicated with the solid phase outlet of the gas-solid separator (2), the return coal gas outlet of the gasification auxiliary bed is communicated with the return coal gas inlet of the gasification furnace (1), and the return carbon-containing material outlet of the gasification auxiliary bed is communicated with the return port of the gasification furnace (1). According to the gasification apparatus and the gasification method of the present invention, the carbon conversion rate of the gasification apparatus can be improved.
Description
Technical Field
The invention relates to the technical field of fuel gasification, in particular to a circulating fluidized bed gasification device with a gasification auxiliary bed and a circulating fluidized bed gasification method with the gasification auxiliary bed.
Background
Coal gasification is one of core technologies of clean and efficient utilization technologies of coal, and is the basis for developing coal-based chemical products, coal-based clean fuels, industrial gas, poly-generation systems and other coal chemical process industries.
The existing coal gasification technology can be divided into the following steps according to the gas-solid flow form: fixed bed gasification technology, fluidized bed gasification technology and entrained flow bed gasification technology. The fixed bed coal gasification technology takes lump coal as a raw material, and the gasification furnace has obvious dry layer, pyrolysis layer, gasification layer and combustion layer, low slag discharging temperature and coal gas outlet temperature, and high system thermal efficiency. The entrained flow coal gasification technology takes coal powder with the particle size less than 100 mu m as a raw material, has high reaction temperature, adopts slag tapping, has high gasification strength and large single-furnace treatment scale, but generally adopts pure oxygen as a gasification agent due to high gasification temperature, has high oxygen consumption and high equipment investment and operation cost.
The fluidized bed coal gasification technology can utilize crushed coal with the particle size of 0-10 mm, a complex coal preparation system is not needed, and the coal preparation cost is low; the gasification strength is high and is generally 2-3 times of that of a fixed bed; air can be used as a gasifying agent; the outlet temperature of the crude gas is high, and the crude gas hardly contains tar and phenols. Compared with the traditional fluidized bed coal gasification technology, the circulating fluidized bed coal gasification technology developed in recent years has the characteristics of high circulation rate, higher gasification strength, more sufficient gas-solid mixing, more uniform reaction temperature and the like, has larger single-furnace gasification scale and stronger adaptability to coal types, but has higher carbon content in fly ash and needs to further improve the carbon conversion rate.
In the existing circulating fluidized bed coal gasification technology, the temperature of the lower part of a hearth of a gasification furnace is highest, the combustion share is the largest, but the carbon content of materials is low, and the particle concentration is high; and the reduction portion is gradually increased upwards along the height direction of the hearth, the temperature in the furnace is gradually reduced, the carbon content of the material is increased, and the particle concentration is reduced. In order to avoid slag bonding, the temperature of the lower part of the hearth is limited, so that the range of improving the overall temperature of the gasification furnace by improving the temperature of the lower part of the hearth is limited, and the effect of improving the gasification efficiency is limited. Although secondary air is introduced into a region with high carbon content of materials in the hearth through the classification of the gasifying agent, the temperature of the region can be increased, the particle concentration of the region is low, the introduced air or oxygen preferentially reacts with coal gas, the probability of reaction with carbon in solid materials is low, and the promotion effect of improving the carbon conversion rate of a system and the cold coal gas efficiency is not obvious enough. After gasification reaction of the gasification furnace, most of solid materials are collected by the cyclone separator and return to the hearth through the circulation loop; while the non-captured fine ash leaves the gasification reaction system. The carbon content of the solid material and the fine ash returned to the hearth is higher (the mass fraction of the carbon in the solid material returned to the hearth is 50-80%, and the mass fraction of the carbon in the fine ash is 30-50%).
In summary, in the conventional circulating fluidized bed coal gasification technology, the ash content of the lower part of the gasification furnace is the highest, and the gasification temperature is also the highest, and the temperature and the ash content of the gasification furnace are gradually reduced from the bottom to the top of the gasification furnace along the height direction. In order to avoid slag bonding, the temperature of the lower part of the hearth is not too high, and the temperature is limited, so that the range of increasing the overall temperature of the gasification furnace by increasing the temperature of the lower part of the hearth is limited. The temperature is limited at the upper part of the hearth which needs high temperature to promote the gasification reaction of carbon and carbon dioxide, so that the carbon conversion rate of the circulating fluidized bed gasification furnace is not high, the carbon content of fine powder ash is higher, and the application of the circulating fluidized bed gasification technology is not facilitated. Although the temperature distribution in the height direction of the hearth of the gasification furnace can be changed through the graded air distribution, the operation temperature of the gasification furnace is not limited by the temperature at the lower part of the hearth any more, oxygen or air introduced by the graded air distribution preferentially reacts with coal gas, the reaction probability with carbon in the region is very small, and the promotion effect on the gasification reaction performance of the system is not obvious enough. Although the fine ash discharged from the gasification furnace can be treated into high-temperature gas and ash by additionally building a high-temperature reaction device, an additional system needs to be built, so that the equipment investment and the operation cost are greatly increased, and the stable operation and the coal adaptability of the circulating fluidized bed gasification furnace can be influenced.
Disclosure of Invention
The object of the present invention is to overcome at least partially the disadvantages of the prior art and to provide a circulating fluidized bed gasification apparatus with an auxiliary gasification bed and a method for circulating fluidized bed gasification with an auxiliary gasification bed, which enable an increased carbon conversion of the gasification apparatus.
The invention also aims to provide a circulating fluidized bed gasification device with a gasification auxiliary bed and a circulating fluidized bed gasification method with the gasification auxiliary bed, so as to reduce the carbon content of fine ash.
The invention also aims to provide a circulating fluidized bed gasification device with a gasification auxiliary bed and a circulating fluidized bed gasification method with the gasification auxiliary bed, which improve the carbon conversion rate of a system, have low equipment investment and operation cost and do not reduce the coal gasification adaptability of the circulating fluidized bed.
To achieve one of the above objects or purposes, the technical solution of the present invention is as follows:
a circulating fluidized bed gasification apparatus with a gasification auxiliary bed, the gasification apparatus comprising:
the gasification furnace is provided with a fuel inlet, a gasification agent inlet, a return coal gas inlet, a furnace discharge coal gas outlet, a bottom slag outlet and a material return port;
the inlet of the gas-solid separator is communicated with the furnace gas outlet of the gasification furnace; and
the gasification auxiliary bed comprises a circulating material inlet, a gasification agent inlet, a return coal gas outlet and a return carbon-containing material outlet, the circulating material inlet of the gasification auxiliary bed is communicated with the solid phase outlet of the gas-solid separator, the return coal gas outlet of the gasification auxiliary bed is communicated with the return coal gas inlet of the gasification furnace, and the return carbon-containing material outlet of the gasification auxiliary bed is communicated with the return port of the gasification furnace.
According to a preferred embodiment of the invention, a primary material returning device is further arranged between the gas-solid separator and the gasification auxiliary bed, and the primary material returning device is respectively connected with the solid phase outlet of the gas-solid separator and the circulating material inlet of the gasification auxiliary bed.
According to a preferred embodiment of the invention, the gasification device further comprises a secondary material returning device, and the secondary material returning device is respectively connected with the return carbon-containing material outlet of the gasification auxiliary bed and the material returning port of the gasification furnace.
According to a preferred embodiment of the present invention, the lower portion of the gasification furnace has a shape that is tapered from top to bottom.
According to a preferred embodiment of the present invention, the height of the fuel inlet of the gasification furnace from the bottom of the gasification furnace is 1/2-1/4 of the total height of the gasification furnace.
According to a preferred embodiment of the invention, the gasification auxiliary bed is a fluidized bed reactor.
According to a preferred embodiment of the invention, the circulating material inlet and the return carbonaceous material outlet of the gasification auxiliary bed are respectively located on opposite sides of the side wall of the gasification auxiliary bed.
According to a preferred embodiment of the invention, the secondary material returning device is positioned at the bottom of the gasification auxiliary bed, and the secondary material returning device is combined with the gasification auxiliary bed, so that a return carbon-containing material outlet of the gasification auxiliary bed is directly connected with an inlet of the secondary material returning device.
According to a preferred embodiment of the invention, the gasification device further comprises an additional gas-solid separator and an additional material returning device, an inlet of the additional gas-solid separator is connected with a gas phase outlet of the gas-solid separator, a solid phase outlet of the additional gas-solid separator is connected with an inlet of the additional material returning device, and an outlet of the additional material returning device is connected with a circulating material inlet of the gasification auxiliary bed.
According to a preferred embodiment of the invention, the carbonaceous material inlet of the high-temperature gasification auxiliary bed is positioned in the dense-phase region of the high-temperature gasification auxiliary bed, and the primary material returning device is provided with a balance pipe communicated with the dilute-phase region of the high-temperature gasification auxiliary bed.
According to a preferred embodiment of the invention, a gasification agent inlet is arranged on the connecting pipeline connecting the additional material returning device and the auxiliary gasification bed.
According to a preferred embodiment of the present invention, the position of the return gas inlet of the gasification furnace is higher than the position of the return port of the gasification furnace.
According to a preferred embodiment of the present invention, the return gas inlet of the gasification furnace is provided at the middle upper portion of the gasification furnace.
According to a preferred embodiment of the invention, the primary material returning device is a mechanical device or a non-mechanical device; and/or the secondary material returning device is a mechanical device or a non-mechanical device.
According to a preferred embodiment of the invention, the gasification agent inlet of the gasification auxiliary bed is arranged at the bottom of the gasification auxiliary bed, and the return gas outlet of the gasification auxiliary bed is arranged at the top of the gasification auxiliary bed.
According to a preferred embodiment of the invention, the jet direction of the gasification agent entering the gasification agent inlet on the connecting duct is at an acute angle to the direction of movement of the material in the connecting duct.
According to a preferred embodiment of the invention, the gas-solid separator is a cyclone or an inertial separator and the additional gas-solid separator is a cyclone.
According to a preferred embodiment of the invention, the gasification auxiliary bed further comprises a slag discharge port, and the slag discharge port is arranged at the bottom of the gasification auxiliary bed.
According to another aspect of the present invention, there is provided a method of circulating fluidized bed gasification with a gasification auxiliary bed, wherein a gasification reaction occurs in the gasification auxiliary bed (3) using the circulating fluidized bed gasification apparatus with a gasification auxiliary bed as described in any one of the above embodiments.
According to a preferred embodiment of the present invention, the gasification method comprises:
a) introducing a first gasifying agent into the gasification furnace to perform partial combustion and gasification reactions with fed fuel and return carbon-containing materials returned from the gasification auxiliary bed to generate first coal gas, first carbon-containing materials and bottom slag;
b) the first carbon-containing material flies upwards under the carrying of the first coal gas and is heated by the return coal gas from the gasification auxiliary bed, carbon in the first carbon-containing material further generates gasification reaction with the first coal gas and the return coal gas to generate furnace-discharging coal gas, and the first carbon-containing material after the further reaction is converted into carbon-containing material and flows to the gas-solid separator under the carrying of the furnace-discharging coal gas;
c) after the carbonaceous material and the discharged coal gas are separated by the gas-solid separator, the discharged coal gas and the fly ash are discharged from a gas phase outlet of the gas-solid separator, and the separated circulating material returns to the gasification auxiliary bed;
d) the second gasifying agent and the circulating material are subjected to gasification reaction in the gasification auxiliary bed to generate return coal gas and return carbon-containing materials; and
e) the return coal gas and the return carbon-containing material are respectively returned to the gasification furnace, and the bottom slag is discharged from the gasification furnace.
According to a preferred embodiment of the present invention, the ratio of water vapor to coal in the gasification furnace is 0.2 to 0.6 by mass, and the ratio of oxygen to coal is 0.2 to 0.5m3/kg。
According to a preferred embodiment of the present invention, the ratio of air or oxygen to water vapor in the first gasifying agent is adjusted to control the temperature of the lower part of the gasification furnace to be 850-950 ℃.
According to a preferred embodiment of the invention, the fluidization velocity of the gasification auxiliary bed is between 0.5m/s and 2.5 m/s.
According to a preferred embodiment of the present invention, the temperature of the gasification auxiliary bed is controlled to be 50 to 300 ℃ higher than the temperature of the lower part of the gasification furnace.
According to a preferred embodiment of the invention, the first gasification agent is oxygen, air or water vapour, or a mixture of oxygen and water vapour, or a mixture of air and water vapour; and/or
The second gasifying agent is oxygen, air or water vapor, or a mixture of oxygen and water vapor, or a mixture of air and water vapor.
According to a preferred embodiment of the invention, the first gasification agent introduced into the gasification furnace is fed in two stages from different locations of the gasification furnace.
According to the distribution characteristics of carbon concentration in material circulation of the circulating fluidized bed coal gasification technology, the high-temperature gasification auxiliary bed is added on the circulation loop, the solid material with high carbon content is gasified at high temperature, the high-temperature solid material generated by high-temperature gasification is returned to the middle lower part of the hearth of the gasification furnace, and the high-temperature coal gas generated by high-temperature gasification is introduced to the middle upper part of the gasification furnace, so that the gasification reaction of the hearth is enhanced, the carbon conversion rate and the coal gas quality of the gasification furnace are improved, and the carbon content of fine ash is reduced.
The high-temperature gasification auxiliary bed is added on the circulating loop, so that the distribution rule of the temperature and the carbon content of the hearth of the conventional circulating fluidized bed is changed, a low-temperature partial combustion area is formed at the lower part of the hearth, and a gasification high-temperature area is formed at the middle upper part of the hearth. The distribution rule is beneficial to strengthening the gasification reaction of the gasification furnace, avoiding slag bonding at the lower part of the hearth and being beneficial to the stable operation of the gasification furnace.
Compared with the scheme of treating fine ash by establishing a set of high-temperature reaction device (molten state slag discharge), the method has the advantages of simpler flow, lower equipment investment and operation cost and no additional generation of three wastes; compared with the scheme of returning high-temperature flue gas or coal gas generated by burning or gasifying fine dust to the gasification furnace, the invention is an open material circulation loop, has no problem of dust accumulation, and effectively utilizes the sensible heat carried by the fine dust, thereby improving the carbon conversion rate of the system without reducing the adaptability of the coal gasified by the circulating fluidized bed.
Drawings
FIG. 1 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to an embodiment of the present invention;
FIG. 2 is a gasification process diagram of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to an embodiment of the present invention;
FIG. 3 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to another embodiment of the present invention; and
FIG. 4 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to yet another embodiment of the present invention.
Detailed Description
Exemplary embodiments of the present invention will hereinafter be described in detail with reference to the accompanying drawings, wherein like or similar reference numerals denote like or similar elements. Furthermore, in the following detailed description, for purposes of explanation, numerous specific details are set forth in order to provide a thorough understanding of the embodiments of the disclosure. It may be evident, however, that one or more embodiments may be practiced without these specific details. In other instances, well-known structures and devices are shown in schematic form in order to simplify the drawing.
Designers have found that the carbon conversion of the system can be increased by a regasification or combustion reaction. One possible idea is to utilize a high temperature reaction device to perform high temperature reaction treatment on all fine dust discharged by the system, so as to improve the carbon conversion rate of the system, introduce the fine dust into a hot air furnace for treatment, and return the generated hot flue gas to a circulating fluidized bed gasification furnace to participate in reaction and heat supplementation.
According to the general inventive concept, there is provided a circulating fluidized bed gasification apparatus with a gasification auxiliary bed, the gasification apparatus including: the gasification furnace is provided with a fuel inlet, a gasification agent inlet, a return coal gas inlet, a furnace discharge coal gas outlet, a bottom slag outlet and a material return port; the inlet of the gas-solid separator is communicated with the furnace gas outlet of the gasification furnace; and the gasification auxiliary bed comprises a circulating material inlet, a gasification agent inlet, a return coal gas outlet and a return carbon-containing material outlet, the circulating material inlet of the gasification auxiliary bed is communicated with the solid phase outlet of the gas-solid separator, the return coal gas outlet of the gasification auxiliary bed is communicated with the return coal gas inlet of the gasification furnace, and the return carbon-containing material outlet of the gasification auxiliary bed is communicated with the return port of the gasification furnace.
It should be noted that the arrangement of the gasification auxiliary bed (or high-temperature gasification auxiliary bed) of the invention is different from the arrangement of a high-temperature reaction device, the high-temperature gasification auxiliary bed of the invention is used as a part of the circulating fluidized bed gasification device and is used as the assistance of the gasification furnace, a set of high-temperature reaction system is not required to be built, and the construction cost and the operation cost are effectively controlled.
FIG. 1 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to an embodiment of the present invention. As shown in fig. 1, the circulating fluidized bed gasification device with the high-temperature gasification auxiliary bed comprises a gasification furnace 1, a gas-solid separator 2, a primary material returning device 4, a high-temperature gasification auxiliary bed 3 and a secondary material returning device 5 which are connected in sequence, wherein the secondary material returning device 5 is connected with the gasification furnace 1, and the high-temperature gasification auxiliary bed 3 is communicated with the middle lower part of the gasification furnace 1 through the secondary material returning device 5. Specifically, a fuel inlet, a gasifying agent inlet, a return coal gas inlet, a furnace gas discharging outlet, a bottom slag outlet and a material returning port are arranged on the gasification furnace 1, an inlet, a gas phase outlet and a solid phase outlet are arranged on the gas-solid separator 2, and the gasification auxiliary bed comprises a circulating material inlet, a gasifying agent inlet, a return coal gas outlet and a return carbon-containing material outlet. The primary material returning device 4 is arranged between the gas-solid separator 2 and the gasification auxiliary bed and comprises an inlet and an outlet, the inlet and the outlet of the primary material returning device 4 are respectively connected with the solid phase outlet of the gas-solid separator 2 and the circulating material inlet of the gasification auxiliary bed, the secondary material returning device 5 is arranged between the gasification auxiliary bed and the gasification furnace 1 and comprises an inlet and an outlet, and the inlet and the outlet of the secondary material returning device 5 are respectively connected with the return furnace carbon-containing material outlet of the gasification auxiliary bed and the return material port of the gasification furnace 1. The inlet of the gas-solid separator 2 is communicated with the furnace gas outlet of the gasification furnace 1, the circulating material inlet of the gasification auxiliary bed is communicated with the solid phase outlet of the gas-solid separator 2 through a primary material returning device 4, the return gas outlet of the gasification auxiliary bed is communicated with the return gas inlet of the gasification furnace 1, and the return carbon-containing material outlet of the gasification auxiliary bed is communicated with the return port of the gasification furnace 1 through a secondary material returning device 5.
In the embodiment of fig. 1, the lower part of the gasification furnace is in a shape that the section is reduced from top to bottom, the gasification agent inlet can be arranged at the bottom and/or the lower part of the gasification furnace, the height of the fuel inlet from the bottom of the gasification furnace is 1/2-1/4 of the total height of the gasification furnace, and the high-temperature gasification auxiliary bed 3 is a fluidized bed reactor. Alternatively, the primary and secondary material returning devices may be mechanical or non-mechanical devices.
Optionally, the circulating material inlet and the return carbon-containing material outlet of the high-temperature gasification auxiliary bed 3 are respectively located on two opposite sides of the side wall of the high-temperature gasification auxiliary bed 3. Therefore, the residence time of the solid materials in the high-temperature gasification auxiliary bed is prolonged, and the gasification efficiency in the high-temperature gasification auxiliary bed is improved.
In an alternative embodiment, the carbonaceous material inlet of the high-temperature gasification auxiliary bed 3 is positioned in the dense-phase region of the high-temperature gasification auxiliary bed 3, and the primary material returning device 4 is provided with a balance pipe communicated with the dilute-phase region of the high-temperature gasification auxiliary bed 3.
Advantageously, the position of the return gas inlet of the gasification furnace 1 should be higher than the position of the return port of the gasification furnace 1, and further advantageously, the return gas inlet of the gasification furnace 1 is disposed at the middle upper portion of the gasification furnace 1. And for the high-temperature gasification auxiliary bed, a gasification agent inlet of the gasification auxiliary bed is arranged at the bottom of the gasification auxiliary bed, and a return coal gas outlet of the gasification auxiliary bed is arranged at the top of the gasification auxiliary bed.
The invention also provides a gasification method of the circulating fluidized bed with the high-temperature gasification auxiliary bed, which adopts a gasification device of the circulating fluidized bed with the high-temperature gasification auxiliary bed, and comprises a gasification furnace 1, a gas-solid separator 2, a high-temperature gasification auxiliary bed 3 and a channel which are connected in sequence. As shown in fig. 2, the method comprises the following steps:
a) introducing a first gasifying agent A into the gasification furnace 1, the fed coal B and the high-temperature carbonaceous material E returned from the high-temperature gasification auxiliary bed 31Partial combustion and gasification reaction are carried out to generate first coal gas, first carbon-containing materials and bottom slag H;
b) the first carbon-containing material enters the middle upper part of the hearth of the gasification furnace under the carrying of the first coal gas and is heated by the high-temperature coal gas F from the high-temperature gasification auxiliary bed 3, and carbon in the first carbon-containing material, the first coal gas and CO in the high-temperature coal gas F2Further gasifying with steam to produce coal gas C, and converting the first carbon-containing material into carbon-containing material E0And flows to the gas-solid separator 2 under the carrying of the coal gas C;
c) carbon-containing materials E0And the coal gas C is separated by the gas-solid separator 2, the coal gas C and the fine dust D are discharged from a gas phase outlet, and the separated circulating material E2Returning to the high-temperature gasification auxiliary bed 3;
d) second gasifying agent G and circulating material E2The gasification reaction is carried out in the high-temperature gasification auxiliary bed 3 to generate high-temperature coal gas F and high-temperature carbon-containing material E1；
e) High-temperature coal gas F enters the middle upper part of the gasification furnace to react with the first carbon-containing material and the like, and the high-temperature carbon-containing material E1Then go back to gasificationThe furnace and the bottom slag H are discharged from the bottom of the gasification furnace.
In the above gasification method, the mass ratio of steam to coal in the gasification furnace 1 is 0.2 to 0.6kg/kg, and the oxygen-coal ratio is 0.2 to 0.5m3In terms of/kg. Advantageously, the temperature of the lower part of the gasification furnace 1 is controlled to be 850-950 ℃ by adjusting the ratio of air or oxygen to water vapor in the first gasification agent A. As mentioned above, the high temperature gasification auxiliary bed 3 is a fluidized bed reactor, the fluidization speed is 0.5 m/s-2.5 m/s, and the temperature of the high temperature gasification auxiliary bed 3 is controlled to be 50-300 ℃ higher than the temperature of the lower part of the gasification furnace. The purpose and the most fundamental idea for arranging the auxiliary bed to carry out high-temperature gasification are to control the temperature of the gasification auxiliary bed to be 50-300 ℃ higher than the temperature of the lower part of the gasification furnace.
According to an embodiment of the present invention, the first gasifying agent a may be oxygen, air or water vapor, or a mixture of oxygen and water vapor, or a mixture of air and water vapor, and the second gasifying agent G may be oxygen, air or water vapor, or a mixture of oxygen and water vapor, or a mixture of air and water vapor. Furthermore, the first gasification agent a introduced into the gasification furnace 1 can be fed in two stages from different locations of the gasification furnace 1.
The lower part of the gasification furnace is in a shape with a reduced section, and the section area is gradually reduced from top to bottom. A gasifying agent inlet is arranged at the bottom or the bottom and the lower part of the gasification furnace 1 and is used for introducing a gasifying agent into the circulating fluidized bed gasification device; the gasification furnace is provided with a fuel inlet for introducing gasification raw materials such as coal into the gasification furnace 1, and the height of the fuel inlet of the gasification furnace 1 from the bottom of the gasification furnace is 1/2-1/4 of the total height of the gasification furnace 1. A material returning port communicated with the secondary material returning device 5 is arranged at the middle lower part of the gasification furnace 1. The bottom of the gasification furnace 1 is provided with a slag discharge port for discharging slag generated in the gasification furnace. The bottom of the gasification furnace is the lowest part of the space formed by the wall surface of the gasification furnace, and the lower part of the gasification furnace is the wall surface of the gasification furnace close to the bottom of the gasification furnace and the space enclosed by the wall surface.
The bottom of the high-temperature gasification auxiliary bed 3 is provided with a gasification agent inlet, the top is provided with a return coal gas outlet, a communicating pipeline is arranged between the return coal gas outlet and the middle or middle upper part of the gasification furnace, and the coal gas generated by gasification reaction in the high-temperature gasification auxiliary bed enters the gasification furnace through the communicating pipeline. In an optional embodiment, the circulating material inlet and the return carbon-containing material outlet of the high-temperature gasification auxiliary bed 3 are positioned at two sides of the high-temperature gasification auxiliary bed 3, so that the residence time of the solid material in the high-temperature gasification auxiliary bed is prolonged, and the gasification efficiency in the high-temperature gasification auxiliary bed is improved.
In an alternative embodiment, the gasification raw material enters the gasifier from the fuel inlet of the gasifier 1, and is subjected to gasification reaction with the gasification agent added from the bottom and/or lower part of the gasifier to generate the carbonaceous material and coal gas. A large amount of coal gas carrying carbon-containing materials enter a gas-solid separator 2 through an upper outlet of the gasification furnace 1 to complete gas-solid separation, and captured particles are sent to a dense phase region at the middle lower part of a high-temperature gasification auxiliary bed 3 through a primary material returning device 4. The other part of the gasification agent is added into the system from the high-temperature gasification auxiliary bed 3, is mixed with the material from the primary material returning device 4 and carries out gasification reaction to generate high-temperature carbon-containing material and high-temperature coal gas, a return coal gas outlet is arranged at the upper part of the high-temperature gasification auxiliary bed 3, and the high-temperature coal gas leaves the high-temperature gasification auxiliary bed through the outlet, enters the middle part and/or the middle upper part of the gasification furnace 1 and participates in the gasification reaction process in the gasification furnace 1; the high-temperature carbon-containing materials in the high-temperature gasification auxiliary bed 3 return to the lower part of the gasification furnace 1 along with the secondary material returning device 5 and continue to participate in the gasification process in the gasification furnace. And qualified coal gas generated by gasification carries a small part of fine dust which is not captured by the gas-solid separator, and leaves the system through a gas phase outlet at the top of the gas-solid separator 2.
The high-temperature gasification auxiliary bed is added on the basis of the existing circulating fluidized bed coal gasification material circulating loop, and the circulating material separated by the separator is returned to the gasification furnace after being converted from low temperature to high temperature, so that the temperature of the middle upper part of the hearth of the gasification furnace which has high carbon content and mainly takes gasification endothermic reaction is greatly increased, the gasification strength is improved, and the carbon content of fine ash is effectively reduced; meanwhile, the lower part of the gasification furnace has high ash content but lower temperature, so that the lower part of the gasification furnace is effectively prevented from slagging, and the safe, stable and efficient operation of a gasification system is ensured.
The principle of the invention is as follows: by analyzing the temperature distribution, the carbon content distribution of solid particles, the particle concentration distribution and the reaction share distribution of the gasification furnace in the height direction of the circulating fluidized bed, a high-temperature gasification auxiliary bed is arranged on a circulating loop of the circulating fluidized bed, and the gasification reaction and the gasification agent of carbon are graded, so that the gasification reaction of the carbon-containing materials respectively occurs in the gasification furnace and the high-temperature gasification auxiliary bed in the circulating process. In the whole circulation process, the gasifying agent is divided into two parts, one part is introduced into the gasifying furnace to participate in conventional gasification reaction, and the other part is introduced into the high-temperature gasification auxiliary bed. In addition, the temperature of the solid material is increased through the gasification process in the high-temperature gasification auxiliary bed, and the high-temperature solid material returns to the middle lower part of the gasification furnace, so that a high-temperature gasification reaction zone is formed in the middle lower part area of the gasification furnace; high-temperature coal gas in the gasification auxiliary bed is introduced into the middle upper part of the gasification furnace, the reaction of carbon and carbon dioxide and the reaction of carbon and water vapor in the gasification furnace are enhanced, the carbon content and the carbon dioxide concentration at the upper part of the gasification furnace are reduced, the effective gas content is improved, and the problems that the temperature of the middle upper part area of the gasification furnace is low, the gasification reaction speed is low, and the carbon content of fine ash discharged out of a system is high in the existing circulating fluidized bed coal gasification technology are solved.
FIG. 3 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to another embodiment of the present invention. In contrast to the embodiment shown in FIG. 1, an additional gas-solid separator 6 is added after the gas-solid separator 2, and correspondingly, a material returning device 7 is added, wherein the material returning device 7 is communicated with the high-temperature gasification auxiliary bed 3. Specifically, an inlet of the additional gas-solid separator 6 is connected with a gas phase outlet of the gas-solid separator 2, a solid phase outlet of the additional gas-solid separator 6 is connected with an inlet of the additional material returning device, and an outlet of the additional material returning device is connected with a circulating material inlet of the gasification auxiliary bed. The gas-solid separator 2 can be a cyclone separator or an inertial separator (with a separation efficiency of 85% -95%), and the additional gas-solid separator 6 can be a cyclone dust collector (with a dust removal efficiency of 60% >, E%99%) and the return feeder 7 can be a non-mechanical return valve. The fine carbon-containing material J trapped by the additional gas-solid separator 6 is conveyed to the high-temperature gasification auxiliary bed 3 through a non-mechanical material return valve, a gasification agent inlet is arranged on a connecting pipeline from the non-mechanical material return valve to the high-temperature gasification auxiliary bed 3, and a third gasification agent I is added into the connecting pipeline by adopting jet flow. The included angle between the jet flow direction of the third gasifying agent I and the moving direction of the fine carbon-containing materials in the connecting pipeline is an acute angle, and the fine carbon-containing materials J are quickly mixed and reacted with the gasifying agent under the entrainment of the jet flow of the third gasifying agent I to generate high-temperature slag and coal gas. High-temperature slag and coal gas are introduced into a dense-phase region of a high-temperature gasification auxiliary bed 3 to further participate in the gasification reaction in the high-temperature gasification auxiliary bed, a slag discharge port is arranged at the bottom of the high-temperature gasification auxiliary bed 3, and coarse slag H is discharged2And (4) discharging the system. The third gasifying agent I is air or a mixture of oxygen and water vapor. Under the condition of ensuring that the materials collected by the two-stage gas-solid separator can normally return to the high-temperature gasification auxiliary bed 3, the two-stage gas-solid separator can improve the collection rate of fine dust and reduce carbon brought out by the fine dust, thereby further improving the carbon conversion rate of the system. Preferably, the fine carbon-containing material collected by the second-stage gas-solid separator and the gasifying agent are gasified at a higher temperature, and the highest temperature of the high-temperature slag entering the high-temperature gasification auxiliary bed can be higher than the flowing temperature of the coal ash and can be molten slag. The high-temperature slag is dispersed under the turbulent impact of the materials in the fluidized bed and exchanges heat with the materials in the fluidized bed. Coarse slag H2The fine slag is discharged from a slag discharge port at the bottom of the high-temperature gasification auxiliary bed, and the fine slag is accompanied with a high-temperature carbon-containing material E1And enters the gasification furnace 1. While increasing the gasification reaction rate of the fine carbonaceous material, ash agglomerates in the portion of the fine carbonaceous material are discharged from the system to reduce the ash content in the recycle system. This approach is particularly suitable for the gasification of coal having relatively poor gasification activity and low ash content.
FIG. 4 is a schematic view of a circulating fluidized bed gasification apparatus with a gasification auxiliary bed according to yet another embodiment of the present invention. The high-temperature gasification auxiliary bed 3 is combined with the secondary material returning device 5, the secondary material returning device 5 is positioned at the bottom of the high-temperature gasification auxiliary bed 3, so that a return furnace carbon-containing material outlet of the gasification auxiliary bed is directly connected with an inlet of the secondary material returning device 5, and the secondary material returning device 5 can be a non-mechanical material returning valve or a combined device consisting of a mechanical valve and a non-mechanical material returning valve. The second gasifying agent G is uniformly fed from the circumferential direction of the high-temperature gasification auxiliary bed, so that the upper part of the second gasifying agent G fed is a fluidized bed, and the bottom combined with the material returning device is a moving bed. Therefore, the gasification agent and the carbon-containing materials are fully mixed and quickly reacted, the temperature of the high-temperature gasification auxiliary bed is uniformly distributed, and the carbon-containing materials in the high-temperature gasification auxiliary bed are stably and controllably returned to the gasification furnace. The structural form effectively inhibits the carbon-containing materials from quickly leaving the high-temperature gasification auxiliary bed due to short circuit, is favorable for steam activation of the carbon-containing materials in a high-temperature environment, and further reduces the carbon content of the bottom slag of the gasification furnace and the carbon content of fine ash.
Furthermore, the first gasifying agent A introduced into the hearth of the gasification furnace can enter the gasification furnace in two stages, namely primary air and secondary air respectively, wherein the primary air is fed from the bottom of the gasification furnace and is mainly used for fluidization at the lower part of the gasification furnace and combustion reaction of bottom slag, and the proportion of the primary air is 40-70% of that of the first gasifying agent A; the secondary air and the material return port are at the same horizontal height, and the wind direction of the secondary air inclines downwards or upwards, and the included angle between the secondary air and the horizontal plane is 15-60 degrees. The proportion of the secondary air is 30 to 60 percent of that of the first gasifying agent A. The gasification agent introduced into the hearth of the gasification furnace is classified, so that the temperature of the lower part of the gasification furnace and the particle size distribution of bottom slag can be adjusted on the basis of meeting the normal circulation of the circulating fluidized bed, the lower part of the gasification furnace is in the safe reaction temperature range of combustion reaction or partial combustion reaction, and the problem of slag bonding caused by overtemperature on the lower part of the circulating fluidized bed gasification furnace is effectively solved.
According to the distribution characteristics of carbon concentration in material circulation of the circulating fluidized bed coal gasification technology, the high-temperature gasification auxiliary bed is added on the circulation loop, the solid material with high carbon content is gasified at high temperature, the high-temperature solid material generated by high-temperature gasification is returned to the middle lower part of the hearth of the gasification furnace, and the high-temperature coal gas generated by high-temperature gasification is introduced to the middle upper part of the gasification furnace, so that the gasification reaction of the hearth is enhanced, the carbon conversion rate and the coal gas quality of the gasification furnace are improved, and the carbon content of fine ash is reduced.
The high-temperature gasification auxiliary bed is added on the circulating loop, so that the distribution rule of the temperature and the carbon content of the hearth of the conventional circulating fluidized bed is changed, a low-temperature partial combustion area is formed at the lower part of the hearth, and a gasification high-temperature area is formed at the middle upper part of the hearth. The distribution rule is beneficial to strengthening the gasification reaction of the gasification furnace, avoiding slag bonding at the lower part of the hearth and being beneficial to the stable operation of the gasification furnace.
The method has simple flow, low equipment investment and operation cost, and no additional generation of three wastes; compared with the scheme of returning high-temperature flue gas or coal gas generated by burning or gasifying fine dust to the gasification furnace, the invention is an open material circulation loop, has no problem of dust accumulation, and effectively utilizes the sensible heat carried by the fine dust, thereby improving the carbon conversion rate of the system without reducing the adaptability of the coal gasified by the circulating fluidized bed.
Although embodiments of the present invention have been shown and described, it would be appreciated by those skilled in the art that changes may be made in these embodiments without departing from the principles and spirit of the invention. The scope of applicability of the present invention is defined by the appended claims and their equivalents.
List of reference numerals:
1 gasification furnace
2 gas-solid separator
3 high-temperature gasification auxiliary bed
4 one-stage material returning device
5 two-stage material returning device
6 additional gas-solid separator
7 material returning device
A first gasifying agent
Coal B
C gas
D fine ash
E0Carbonaceous material
E1High temperature carbonaceous material
E2Circulating material
F high temperature gas
G second gasifying agent
H bottom slag
H2Coarse slag
I third gasifying agent
J fine carbon-containing material.
Claims (17)
1. A circulating fluidized bed gasification apparatus with a gasification auxiliary bed, the gasification apparatus comprising:
the gasification furnace (1) is provided with a fuel inlet, a gasifying agent inlet, a return gas inlet, a furnace gas outlet, a bottom slag outlet and a material returning port;
the inlet of the gas-solid separator (2) is communicated with the furnace gas outlet of the gasification furnace (1); and
the gasification auxiliary bed (3) comprises a circulating material inlet, a gasification agent inlet, a return coal gas outlet and a return carbon-containing material outlet, the circulating material inlet of the gasification auxiliary bed is communicated with the solid phase outlet of the gas-solid separator (2), the return coal gas outlet of the gasification auxiliary bed is communicated with the return coal gas inlet of the gasification furnace (1), and the return carbon-containing material outlet of the gasification auxiliary bed is communicated with the return port of the gasification furnace (1).
2. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 1, wherein:
a primary material returning device (4) is also arranged between the gas-solid separator (2) and the gasification auxiliary bed, and the primary material returning device (4) is respectively connected with the solid phase outlet of the gas-solid separator (2) and the circulating material inlet of the gasification auxiliary bed.
3. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 2, wherein:
the gasification device further comprises a secondary material returning device (5), and the secondary material returning device (5) is respectively connected with a return carbon-containing material outlet of the gasification auxiliary bed and a material returning port of the gasification furnace (1).
4. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 1, wherein:
the lower part of the gasification furnace (1) has a shape which is reduced from top to bottom.
5. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 1, wherein:
the height of the fuel inlet of the gasification furnace (1) from the bottom of the gasification furnace (1) is 1/2-1/4 of the total height of the gasification furnace (1).
6. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 1, wherein:
the gasification auxiliary bed is a fluidized bed reactor.
7. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 1, wherein:
the circulating material inlet and the return carbon-containing material outlet of the gasification auxiliary bed are respectively positioned on two opposite sides of the side wall of the gasification auxiliary bed.
8. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed according to claim 3, wherein:
the secondary material returning device (5) is positioned at the bottom of the gasification auxiliary bed, and the secondary material returning device (5) is combined with the gasification auxiliary bed together, so that a return carbon-containing material outlet of the gasification auxiliary bed is directly connected with an inlet of the secondary material returning device (5).
9. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed according to claim 3, wherein:
the gasification device also comprises an additional gas-solid separator (6) and an additional material returning device, wherein the inlet of the additional gas-solid separator (6) is connected with the gas phase outlet of the gas-solid separator (2), the solid phase outlet of the additional gas-solid separator (6) is connected with the inlet of the additional material returning device, and the outlet of the additional material returning device is connected with the circulating material inlet of the gasification auxiliary bed.
10. The circulating fluidized bed gasification apparatus with an auxiliary gasification bed of claim 9, wherein:
a gasification agent inlet is arranged on a connecting pipeline connecting the additional material returning device and the gasification auxiliary bed.
11. A method of circulating fluidized bed gasification with an auxiliary gasification bed, using a circulating fluidized bed gasification apparatus with an auxiliary gasification bed according to any of claims 1 to 10, characterized in that the gasification reaction takes place in the auxiliary gasification bed (3).
12. The circulating fluidized bed gasification process with a gasification auxiliary bed of claim 11, wherein the gasification process comprises:
a) introducing a first gasifying agent (A) into the gasification furnace (1) to perform partial combustion and gasification reaction with fed fuel and return carbon-containing materials returned from the gasification auxiliary bed to generate first coal gas, first carbon-containing materials and bottom slag (H);
b) the first carbon-containing material is carried by the first coal gas to fly upwards and is heated by the return coal gas from the gasification auxiliary bed, the carbon in the first carbon-containing material further generates gasification reaction with the first coal gas and the return coal gas to generate furnace-discharging coal gas, and the first carbon-containing material after further reaction is converted into carbon-containing material (E)0) And flows to the gas-solid separator (2) under the carrying of the discharged gas;
c) carbon-containing Material (E)0) After the furnace-discharging coal gas is separated by the gas-solid separator (2), the furnace-discharging coal gas and the ash powder are discharged from a gas phase outlet of the gas-solid separator (2), and the separated circulating material (E)2) Returning to the gasification auxiliary bed;
d) second gasifying agent (G) and circulating material (E)2) Gasification reaction is carried out in the gasification auxiliary bed to generate return coal gas and return carbon-containing materials; and
e) the return coal gas and the return carbon-containing material are respectively returned to the gasification furnace, and the bottom slag (H) is discharged from the gasification furnace.
13. The circulating fluidized bed gasification process with an auxiliary gasification bed of claim 12, wherein:
the mass ratio of the water vapor to the coal in the gasification furnace (1) is 0.2-0.6, and the oxygen-coal ratio is 0.2-0.5 m3/kg。
14. The circulating fluidized bed gasification process with an auxiliary gasification bed of claim 12, wherein:
adjusting the ratio of air or oxygen to water vapor in the first gasifying agent (A), and controlling the temperature of the lower part of the gasification furnace (1) to be 850-950 ℃.
15. The circulating fluidized bed gasification process with an auxiliary gasification bed of claim 12, wherein:
the fluidization speed of the gasification auxiliary bed is 0.5-2.5 m/s.
16. The circulating fluidized bed gasification process with an auxiliary gasification bed of claim 12, wherein:
controlling the temperature of the gasification auxiliary bed to be 900-1300 ℃.
17. The circulating fluidized bed gasification process with an auxiliary gasification bed of claim 12, wherein:
the temperature of the gasification auxiliary bed is controlled to be 50-300 ℃ higher than the temperature of the lower part of the gasification furnace.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911150116.2A CN110791326B (en) | 2019-11-21 | 2019-11-21 | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911150116.2A CN110791326B (en) | 2019-11-21 | 2019-11-21 | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN110791326A true CN110791326A (en) | 2020-02-14 |
| CN110791326B CN110791326B (en) | 2021-10-12 |
Family
ID=69445780
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911150116.2A Active CN110791326B (en) | 2019-11-21 | 2019-11-21 | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN110791326B (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111996039A (en) * | 2020-08-26 | 2020-11-27 | 中国科学院工程热物理研究所 | Staged gasification method and apparatus |
| CN112210636A (en) * | 2020-10-09 | 2021-01-12 | 新疆八一钢铁股份有限公司 | Device for strengthening central gas flow of reduction furnace of Ou metallurgical furnace |
| CN112852498A (en) * | 2020-12-30 | 2021-05-28 | 中国科学院工程热物理研究所 | Fuel dealkalization device and method, circulating fluidized bed gasification device and method |
Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1999032583A1 (en) * | 1997-12-09 | 1999-07-01 | Danish Fluid Bed Technology Aps | Method and apparatus for gasification of solid carbonaceous material |
| JP2003176486A (en) * | 2001-12-10 | 2003-06-24 | Ebara Corp | Integrated circulating fluidized bed gasifying furnace |
| CN201574143U (en) * | 2009-11-20 | 2010-09-08 | 田原宇 | Grading gasification furnace of powdered coal circulating fluidized bed |
| CN102212399A (en) * | 2010-04-07 | 2011-10-12 | 中国科学院工程热物理研究所 | Thermal pyrolysis combination method and device |
| CN102277200A (en) * | 2011-07-05 | 2011-12-14 | 舒克孝 | Method for preparing coal gas by virtue of pulverized coal grading gasification |
| CN102936518A (en) * | 2012-11-16 | 2013-02-20 | 中国石油大学(华东) | Household garbage coupling fluidized bed grading pyrolysis gasification technology |
| JP2013189510A (en) * | 2012-03-13 | 2013-09-26 | Ihi Corp | Circulation type gasification furnace |
| CN103911179A (en) * | 2014-03-26 | 2014-07-09 | 安徽科达洁能股份有限公司 | Coal gasification method and device |
| CN104704088A (en) * | 2012-07-17 | 2015-06-10 | 派若尼耳有限公司 | Apparatus and methods for gasification |
| CN106554826A (en) * | 2015-09-30 | 2017-04-05 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash melting |
| CN107043641A (en) * | 2016-02-06 | 2017-08-15 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash loopback |
-
2019
- 2019-11-21 CN CN201911150116.2A patent/CN110791326B/en active Active
Patent Citations (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1999032583A1 (en) * | 1997-12-09 | 1999-07-01 | Danish Fluid Bed Technology Aps | Method and apparatus for gasification of solid carbonaceous material |
| JP2003176486A (en) * | 2001-12-10 | 2003-06-24 | Ebara Corp | Integrated circulating fluidized bed gasifying furnace |
| CN201574143U (en) * | 2009-11-20 | 2010-09-08 | 田原宇 | Grading gasification furnace of powdered coal circulating fluidized bed |
| CN102212399A (en) * | 2010-04-07 | 2011-10-12 | 中国科学院工程热物理研究所 | Thermal pyrolysis combination method and device |
| CN102277200A (en) * | 2011-07-05 | 2011-12-14 | 舒克孝 | Method for preparing coal gas by virtue of pulverized coal grading gasification |
| JP2013189510A (en) * | 2012-03-13 | 2013-09-26 | Ihi Corp | Circulation type gasification furnace |
| CN104704088A (en) * | 2012-07-17 | 2015-06-10 | 派若尼耳有限公司 | Apparatus and methods for gasification |
| CN102936518A (en) * | 2012-11-16 | 2013-02-20 | 中国石油大学(华东) | Household garbage coupling fluidized bed grading pyrolysis gasification technology |
| CN103911179A (en) * | 2014-03-26 | 2014-07-09 | 安徽科达洁能股份有限公司 | Coal gasification method and device |
| CN106554826A (en) * | 2015-09-30 | 2017-04-05 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash melting |
| CN107043641A (en) * | 2016-02-06 | 2017-08-15 | 中国科学院工程热物理研究所 | Circulation fluidized bed coal gasifying method and device with fine ash loopback |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111996039A (en) * | 2020-08-26 | 2020-11-27 | 中国科学院工程热物理研究所 | Staged gasification method and apparatus |
| CN111996039B (en) * | 2020-08-26 | 2021-08-24 | 中国科学院工程热物理研究所 | Staged gasification method and apparatus |
| CN112210636A (en) * | 2020-10-09 | 2021-01-12 | 新疆八一钢铁股份有限公司 | Device for strengthening central gas flow of reduction furnace of Ou metallurgical furnace |
| CN112210636B (en) * | 2020-10-09 | 2024-05-24 | 新疆八一钢铁股份有限公司 | Device for strengthening central gas flow of reduction furnace of European smelting furnace |
| CN112852498A (en) * | 2020-12-30 | 2021-05-28 | 中国科学院工程热物理研究所 | Fuel dealkalization device and method, circulating fluidized bed gasification device and method |
| CN112852498B (en) * | 2020-12-30 | 2022-03-04 | 中国科学院工程热物理研究所 | Fuel dealkalization device and method, circulating fluidized bed gasification device and method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN110791326B (en) | 2021-10-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101245264B (en) | Single-bed self-heating type thermal decomposition gasification combustion reactor and thermal decomposition gasification combustion method | |
| CN108753368B (en) | Circulating fluidized bed coal gasification system and method | |
| CN110791326B (en) | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method | |
| CN100577775C (en) | Coal gasification device of circulating fluidized bed and method for generating coal gas by using coal gasification device | |
| CN106554826B (en) | Circulating fluidized bed coal gasification method and device with fine ash fusion | |
| CN103911179B (en) | Coal gasification method and device | |
| CN107043641B (en) | Coal gasification method and device of circulating fluidized bed with fine ash return | |
| CN106221814B (en) | A kind of colm water cooling fireplace segmented couples gasification installation and gasification process | |
| CN105861066A (en) | Inferior coal segmented-coupling gasifying device and gasifying method | |
| CN111763535B (en) | Method and device for preparing fuel gas or synthesis gas by biomass fluidized bed gasification | |
| CN201241071Y (en) | Single-bed self-heating type thermal decomposition gasification combusting reactor | |
| CN106753582A (en) | Low-tar biomass gasifying system | |
| CN106675658A (en) | Device and method for high-flux circulating fluidized bed low-rank coal gasifying | |
| CN100363461C (en) | Method and device for preparing fuel gas from biomass/domestic garbage double bed type heat decomposition | |
| CN107118807B (en) | System and method for preparing reducing gas by lignite double-bed gasification | |
| CN104197323A (en) | Inner and outer circulation coupled device for separating carbon dioxide by burning coal-based chemical loopings | |
| CN201046952Y (en) | Coal gasification device of circulating fluidized bed | |
| CN209702674U (en) | A kind of gasification system | |
| CN208649244U (en) | A kind of circulation fluidized bed coal gasifying system | |
| CN110373230A (en) | A kind of method that fluidized gasification flying dust returns furnace gas | |
| CN110205164B (en) | Circulating fluidized bed gasification device and circulating fluidized bed gasification method | |
| CN109385308A (en) | A kind of the double bed electricity generation system and method for coal-fired coupling domestic garbage pyrolysis | |
| CN107760385B (en) | Coal gasification device combining fluidized bed and molten bed and method thereof | |
| CN114774169B (en) | Gasification device, gasification method, and thermochemical reaction device | |
| CN106336907A (en) | Device and process for cyclone pyrolysis high-throughput circulation gasification |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |