CN113265273B - Double fluidized bed coal gasification system and control method thereof - Google Patents
Double fluidized bed coal gasification system and control method thereof Download PDFInfo
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- CN113265273B CN113265273B CN202110545317.3A CN202110545317A CN113265273B CN 113265273 B CN113265273 B CN 113265273B CN 202110545317 A CN202110545317 A CN 202110545317A CN 113265273 B CN113265273 B CN 113265273B
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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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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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
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
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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
- C10J3/72—Other features
- C10J3/723—Controlling or regulating the gasification process
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Abstract
The disclosure relates to a dual fluidized bed coal gasification system and a control method thereof. A fluidized bed heat exchanger comprising: a housing, a first inlet duct, a first outlet duct, a second inlet duct, a second outlet duct, a particle fluidization component, and a particle screening component; the first inlet pipe, the first outlet pipe, the second inlet pipe and the second outlet pipe are all communicated with the shell; the first inlet pipe and the second inlet pipe are used for introducing solid particles into the shell; the particle fluidization component is used for fluidizing the solid particles; the particle screening component is used for screening first solid particles and second solid particles from fluidized solid particles, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles. The fluidized bed heat exchanger provided by the disclosure is applied to a double fluidized bed coal gasification system, the bridging phenomenon of the material returning vertical pipe can be prevented, and the operation stability of the gasification furnace and the combustion furnace is improved.
Description
Technical Field
The disclosure relates to the technical field of fluidized bed coal gasification, in particular to a double-fluidized bed coal gasification system and a control method thereof.
Background
The dual fluidized bed coal gasification system comprises two fluidized bed reactors: a gasification furnace and a combustion furnace. The high-temperature superheated steam introduced into the gasification furnace is fluidized gas and a gasifying agent, the air introduced into the combustion furnace is fluidized gas and a combustion improver, the pulverized coal enters the gasification furnace through the feeder, the pulverized coal is pyrolyzed at high temperature and simultaneously undergoes water gas and water vapor shift reaction with the steam to generate carbon monoxide, hydrogen, carbon dioxide and methane, unreacted carbon, inert bed material and coal ash enter the combustion furnace through the return feeder to be subjected to high-temperature combustion, the heated inert bed material and the heated coal ash enter the gasification furnace through the return feeder again, and heat is provided for the pyrolysis and gasification of the coal of the gasification furnace. The reaction temperature of the gasification furnace is about 800 ℃, and the reaction temperature of the combustion furnace is about 950 ℃. The heat required by gasification in the gasification furnace is provided by high-temperature circulating materials generated after coal in the combustion furnace is combusted, oxygen or air does not need to be introduced into the gasification furnace for combustion and heat release, an air separation device is omitted, and the effective gas component in the coal gas is high, the heat value of the coal gas is high, and the gasification furnace has good economic benefit.
Because the fluidized beds at the present stage all adopt fast beds, the material circulation rate is high, in order to meet the requirement of high material circulation rate, the cyclone efficiency is also required to be particularly high, and fine powder (comprising desulfurized limestone and ash in coal) can also be collected by cyclone, so that the proportion of fine powder (less than or equal to 100 mu m) in the fluidized beds is very high, and the proportion of fine powder can be continuously increased due to the continuous circulation of the material in a gasification furnace and a combustion furnace. When the content of fine powder in the circulating material gradually accumulates to exceed a certain proportion (more than or equal to 15 percent), the fine powder is accumulated on a certain cross section of the return material vertical pipe due to the existence of upward gas quantity in the return material vertical pipe, a fault phenomenon can occur, the cross-linking phenomenon can also be called as a bridging phenomenon, after the bridging phenomenon occurs, the return material is stopped, and the stable operation of a gasification furnace and a combustion furnace in a double fluidized bed coal gasification system is seriously influenced.
Disclosure of Invention
To solve the above technical problem or at least partially solve the above technical problem, the present disclosure provides a dual fluidized bed coal gasification system and a control method thereof.
The present disclosure provides a fluidized bed heat exchanger comprising: a housing, a first inlet duct, a first outlet duct, a second inlet duct, a second outlet duct, a particle fluidization component, and a particle screening component;
wherein the first inlet tube, the first outlet tube, the second inlet tube, and the second outlet tube all pass through the shell; the first inlet pipe and the second inlet pipe are used for introducing solid particles into the shell; the particle fluidization component is used for fluidizing the solid particles; the particle screening component is used for screening first solid particles and second solid particles from fluidized solid particles, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles.
Optionally, the first inlet pipe is located at the top of the shell, the first outlet pipe is located at the bottom of the shell, the second inlet pipe and the second outlet pipe are located at the side of the shell, and the second outlet pipe is closer to the top of the shell than the second inlet pipe;
The particle screening component comprises a third inlet pipe, wherein the third inlet pipe is positioned outside the shell and communicated with the first outlet pipe and is used for sending gas with preset flow rate into the shell.
Optionally, the particle fluidization component comprises a fourth inlet pipe and an air distribution plate; the air distribution plate is positioned in the shell and forms an air chamber with the bottom of the shell; the fourth inlet pipe is positioned outside the shell, is communicated with the air chamber and is used for feeding fluidizing gas to the air chamber; the first outlet pipe penetrates through the air distribution plate.
Optionally, the air inlets of the third inlet pipe and the fourth inlet pipe are both communicated with the same air supply pipe.
Optionally, a first air speed regulating and controlling valve is arranged on a pipeline of the third inlet pipe, and/or a second air speed regulating and controlling valve is arranged on a pipeline of the fourth inlet pipe.
Optionally, the particle sorting component comprises a fifth inlet pipe located outside the housing and communicating with the first outlet pipe for feeding oxygen to the first outlet pipe.
Optionally, the first inlet pipe extends to the inside of the shell, the discharge port of the first inlet pipe is closer to the bottom of the shell than the second outlet pipe, and the distance between the discharge port of the first inlet pipe and the feed port of the second outlet pipe in the extending direction of the first inlet pipe ranges from 200mm to 500 mm.
Optionally, the distance from the feed inlet of the second outlet pipe to the top of the housing is greater than or equal to 1 m.
The present disclosure provides a dual fluidized bed coal gasification system, comprising: the gasification furnace, the combustion furnace, the gasification furnace cyclone separator, the combustion furnace cyclone separator, the gasification furnace material returning device, the combustion furnace material returning device and the fluidized bed heat exchanger provided by the disclosure;
a feed inlet of a first inlet pipe of the fluidized bed heat exchanger is connected with a discharge outlet of the gasification furnace cyclone separator, and a feed inlet of the gasification furnace cyclone separator is connected with a circulating material outlet of the gasification furnace;
a discharge hole of a first outlet pipe of the fluidized bed heat exchanger is connected with a feed inlet of the gasification furnace material returning device, and a discharge hole of the gasification furnace material returning device is connected with a circulating material inlet of the gasification furnace;
a feed inlet of a second inlet pipe of the fluidized bed heat exchanger is connected with a discharge outlet of the combustion furnace cyclone separator, and a feed inlet of the combustion furnace cyclone separator is connected with a circulating material outlet of the combustion furnace;
and a discharge port of a second outlet pipe of the fluidized bed heat exchanger is connected with a feed port of the combustion furnace material returning device, and a discharge port of the combustion furnace material returning device is connected with a circulating material inlet of the combustion furnace.
The present disclosure also provides a control method of a dual fluidized bed coal gasification system, the control method including:
capturing solid particles from the gasification furnace by using a cyclone separator of the gasification furnace, and introducing the solid particles into the fluidized bed heat exchanger through a first inlet pipe of the fluidized bed heat exchanger;
capturing solid particles from the combustion furnace by using a combustion furnace cyclone separator, and introducing the solid particles into the fluidized bed heat exchanger through a second inlet pipe of the fluidized bed heat exchanger;
fluidizing solid particles introduced into the interior of a fluidized bed heat exchanger with a particle fluidizing component of the fluidized bed heat exchanger;
screening first solid particles and second solid particles from the fluidized solid particles by using a particle screening component of a fluidized bed heat exchanger, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles;
returning the first solid particles to the gasifier using a gasifier return;
returning the second solid particles to the furnace using a furnace return.
Compared with the prior art, the technical scheme provided by the embodiment of the disclosure has the following advantages:
according to the technical scheme provided by the embodiment of the disclosure, the fluidized bed heat exchanger with the coarse and fine solid particle screening function is designed, the fluidized bed heat exchanger can be additionally arranged in a double-fluidized bed coal gasification system, and solid particles (gasification furnace circulating material and combustion furnace circulating material) are fluidized by a particle fluidizing component in the operation process of the double-fluidized bed coal gasification system, so that the gasification furnace circulating material and the combustion furnace circulating material are mixed and exchange heat in the fluidized bed heat exchanger, and the heat exchange is more sufficient and uniform; and, the first solid particles (coarse solid particles) with larger particle size and the second solid particles (fine solid particles) with smaller particle size are screened from the fluidized solid particles through the particle screening component, the first solid particles are led out from the first outlet pipe, and the second solid particles are led out from the second outlet pipe, so that the coarse solid particles and the fine solid particles are separated in the fluidized bed heat exchanger and are respectively led out from different outlet pipes, the bridging phenomenon caused by the fact that the coarse solid particles and the fine solid particles exist in the material returning vertical pipe at the same time and the proportion of the fine solid particles is increased is effectively prevented, the problem of material returning failure is avoided, and the operation stability of the gasification furnace and the combustion furnace in the dual fluidized bed gasification system is improved.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.
In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.
FIG. 1 is a schematic structural diagram of a conventional dual fluidized bed coal gasification system;
FIG. 2 is a schematic structural diagram of a fluidized bed heat exchanger provided in an embodiment of the present disclosure;
fig. 3 is a schematic structural diagram of a dual fluidized bed coal gasification system according to an embodiment of the present disclosure.
Detailed Description
In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.
In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.
Fig. 1 is a schematic structural view of a conventional dual fluidized bed coal gasification system. As shown in fig. 1, a conventional dual fluidized bed coal gasification system includes a gasification furnace 1, a combustion furnace 2, a gasification furnace cyclone 3, a combustion furnace cyclone 4, a gasification furnace return feeder 5, and a combustion furnace return feeder 6. The concrete flow of material circulation is as follows: the material gets into gasifier cyclone 3 from the gasifier, the material that is caught by gasifier cyclone 3 gets into burning furnace returning charge ware 6 through the return pipe, it sends into burning furnace 2 to burn burning furnace returning charge ware 6 with the material, the material burns at burning furnace 2 high temperature, the material after the heating gets into burning furnace cyclone 4 from burning furnace 2, the material that is caught by burning furnace cyclone 4 gets into gasifier returning charge ware 5 through the return pipe, gasifier returning charge ware 5 returns the material to gasifier 1 in order to provide the heat for the pyrolysis and the gasification of the coal of gasifier. However, as the proportion of the fine materials in the materials is continuously increased and the amount of upward gas exists in the vertical return pipe 10, the fine materials are accumulated on a certain cross section of the vertical return pipe 10, a bridging phenomenon occurs, the material return is stopped, and the stable operation of the gasification furnace and the combustion furnace in the double fluidized beds is seriously influenced.
In order to solve the above problems, embodiments of the present disclosure provide a fluidized bed heat exchanger, and the method will be described below with reference to specific embodiments.
The embodiment of the disclosure provides a fluidized bed heat exchanger, which can be applied to a double fluidized bed coal gasification system, can be used as heat exchange equipment for circulating materials of a gasification furnace and circulating materials of a combustion furnace, and can separate the circulating materials of the gasification furnace returned to the gasification furnace and the circulating materials of the combustion furnace returned to the combustion furnace according to the particle size of the materials. The fluidized bed heat exchanger comprises: a housing, a first inlet duct, a first outlet duct, a second inlet duct, a second outlet duct, a particle fluidization component, and a particle screening component; the first inlet pipe, the first outlet pipe, the second inlet pipe and the second outlet pipe are all communicated with the shell; the first inlet pipe and the second inlet pipe are used for introducing solid particles into the shell; the particle fluidization component is used for fluidizing the solid particles; the particle screening component is used for screening first solid particles and second solid particles from fluidized solid particles, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles.
The fluidized bed heat exchanger provided by the embodiment of the disclosure can be additionally arranged in a double fluidized bed coal gasification system, and in the operation process of the double fluidized bed coal gasification system, solid particles (gasification furnace circulating material and combustion furnace circulating material) are fluidized by the particle fluidizing component, so that the gasification furnace circulating material and the combustion furnace circulating material are mixed and exchange heat in the fluidized bed heat exchanger, and the heat exchange is more sufficient and uniform; and, the first solid particles (coarse solid particles) with larger particle size and the second solid particles (fine solid particles) with smaller particle size are screened from the fluidized solid particles through the particle screening component, the first solid particles are led out from the first outlet pipe, and the second solid particles are led out from the second outlet pipe, so that the coarse solid particles and the fine solid particles are separated in the fluidized bed heat exchanger and are respectively led out from different outlet pipes, the bridging phenomenon caused by the fact that the coarse solid particles and the fine solid particles exist in the material returning vertical pipe at the same time and the proportion of the fine solid particles is increased is effectively prevented, the problem of material returning failure is avoided, and the operation stability of the gasification furnace and the combustion furnace in the dual fluidized bed gasification system is improved.
In some embodiments, the first inlet tube is located at the top of the shell, the first outlet tube is located at the bottom of the shell, the second inlet tube and the second outlet tube are located at the side of the shell, and the second outlet tube is closer to the top of the shell than the second inlet tube; the particle screening component comprises a third inlet pipe, the third inlet pipe is positioned outside the shell and communicated with the first outlet pipe, and the third inlet pipe is used for feeding gas with preset flow rate into the shell.
In some embodiments, the particle fluidization member includes a fourth inlet duct and a grid plate; the air distribution plate is positioned in the shell and forms an air chamber with the bottom of the shell; the fourth inlet pipe is positioned outside the shell, is communicated with the air chamber and is used for feeding fluidizing gas to the air chamber; the first outlet pipe penetrates through the air distribution plate.
Based on the above technical solution, in a specific embodiment of the present disclosure, fig. 2 is a schematic structural diagram of a fluidized bed heat exchanger provided in the embodiment of the present disclosure. As shown in fig. 2, the fluidized bed heat exchanger 7 includes: a shell 70, a first inlet pipe 71, a first outlet pipe 72, a second inlet pipe 73, a second outlet pipe 74, a third inlet pipe 75, a fourth inlet pipe 76, and a wind distribution plate 77; wherein the first inlet pipe 71 is positioned at the top of the shell 70, the first outlet pipe 72 is positioned at the bottom of the shell 70, the second inlet pipe 73 and the second outlet pipe 74 are positioned at the side of the shell 70, and the second outlet pipe 74 is closer to the top of the shell 70 than the second inlet pipe 73, i.e. the second inlet pipe 73 is positioned below the second outlet pipe 74 in fig. 2, the third inlet pipe 75 is positioned outside the shell 70 and is communicated with the first outlet pipe 72 for feeding gas with preset flow rate to the inside of the shell 70, the air distribution plate 77 is positioned inside the shell 70 and forms an air chamber 78 with the bottom of the shell 70; a fourth inlet duct 76 is located outside the housing 70 and communicates with the plenum 78 for feeding the fluidizing gas to the plenum 78, and the first outlet duct 72 extends through the air distribution plate 77.
In the above embodiment, the first inlet pipe 71 is used to introduce solid particles (i.e., gasifier cycle material) coming out of the gasifier into the inside of the housing 70, and the second inlet pipe 73 is used to introduce solid particles (i.e., furnace cycle material) coming out of the furnace into the inside of the housing 70. In practical use, the fluidized bed heat exchanger shown in fig. 2 is arranged vertically, with the top of the housing 70 on top and the bottom of the housing 70 on bottom; meanwhile, coarse bed material (inert bed material) is used in the gasification furnace and fine bed material (inert bed material) is used in the combustion furnace, and accordingly, the particle diameter of the gasification furnace circulation material introduced from the first inlet pipe 71 is larger than the particle diameter of the combustion furnace circulation material introduced from the second inlet pipe 73. Based on this, fluidizing gas, such as flue gas (which may be recycled flue gas of a dual fluidized bed coal gasification system), is fed into the plenum 78 through the fourth inlet pipe 76, and the fluidizing gas is uniformly blown into the interior of the housing 70 through the plenum 78, so that the gasifier cycle material and the burner cycle material entering the interior of the housing 70 are mixed for heat exchange. Considering that the weight of the particles with different particle sizes is usually different, i.e. the weight of the coarse particles is larger, so that the coarse particles need a larger flow rate of upward gas to float, the disclosed technical solution can separate the gasifier cycle material from the furnace cycle material by introducing gas with a preset flow rate from the bottom of the housing 70. After the gasification furnace circulating material and the combustion furnace circulating material are mixed and exchange heat, the flow velocity of gas introduced through the third inlet pipe 75 is set, so that the combustion furnace circulating material floats upwards, the gasification furnace circulating material sinks, further the gasification furnace circulating material (first solid particles) is led out from the first outlet pipe 72, and the combustion furnace circulating material (second solid particles) is led out from the second outlet pipe 74, so that the gasification furnace circulating material and the combustion furnace circulating material are separated, further the gasification furnace circulating material can be returned to the gasification furnace again when the fluidized bed heat exchanger is applied to a double fluidized bed coal gasification system, heat is provided for gasification reaction in the gasification furnace, meanwhile, the combustion furnace circulating material is returned to the combustion furnace again, and heat is absorbed by combustion in the combustion furnace. Furthermore, the present disclosure enables the gasifier cycle material after heat exchange to be rapidly drawn out from the first outlet pipe 72 and the burner cycle material after heat exchange to be rapidly drawn out from the second outlet pipe 74 by designing the first inlet pipe 71 to be located at the top of the housing 70, the first outlet pipe 72 to be located at the bottom of the housing 70, the second inlet pipe 73 and the second outlet pipe 74 to be located at the side of the housing 70, and the second outlet pipe 74 to be closer to the top of the housing 70 than the second inlet pipe 73.
In some embodiments, the fluidization gas is flue gas which is dedusted by a flue gas deduster and has the temperature of 900-1000 ℃. Alternatively, the gas with the predetermined flow rate may be the fluidizing gas. After heat exchange, the fluidizing gas and the gas at the predetermined flow rate can be led out from the gas outlet pipe 83 above the second outlet pipe 74 and discharged into the flue gas duct after the recirculated flue gas lead-out pipe.
In some embodiments, the first solid particles have a particle size of 300 μm or more and the second solid particles have a particle size of 300 μm or less, i.e., by setting the predetermined flow rate of the gas, the material having a particle size of 300 μm or more can be returned to the gasification furnace while the material having a particle size of 300 μm or less is returned to the combustion furnace.
Based on the technical scheme, in some embodiments, in the actual operation process of the dual fluidized bed coal gasification system, 0-8mm of coal enters the gasification furnace to generate gasification reaction with water vapor, meanwhile, the coal is cracked due to high-temperature pyrolysis and gasification, part of large particles are changed into small particles, bed materials in the gasification furnace and the reacted coal enter the fluidized bed heat exchanger, coal particles with the particle size larger than or equal to 300 microns can enter the gasification furnace again to perform gasification reaction, coal particles with the particle size smaller than 300 microns enter the combustion furnace to supplement fuel for combustion of the combustion furnace, and full utilization of the coal is achieved.
It should be noted that the structure of the fluidized bed heat exchanger shown in fig. 2 is only one possible embodiment of the present disclosure, and the fluidized bed heat exchanger is only required to realize heat exchange between the gasification furnace circulating material and the combustion furnace circulating material and separation of heat exchange between the gasification furnace circulating material and the combustion furnace circulating material, and the present disclosure does not limit other specific structures.
In some embodiments, the air inlet of the third inlet tube 75 and the air inlet of the fourth inlet tube 76 are both in communication with the same air supply tube 79. Thereby simultaneously supplying air to the plenum 78 and the first outlet duct 72.
In some embodiments, to achieve the preset flow rate and/or fluidization gas flow rate adjustment, a first gas flow rate adjustment valve 80 is provided in the conduit of the third inlet duct 75, and/or a second gas flow rate adjustment valve 81 is provided in the conduit of the fourth inlet duct 76. That is, in some embodiments, the pipeline of the third inlet pipe 75 is provided with a first air speed regulating valve 80; in some embodiments, the fourth inlet tube 76 is provided with a second air flow regulating valve 81; in some embodiments, a first air flow rate regulating valve 80 is provided in the conduit of the third inlet tube 75 and a second air flow rate regulating valve 81 is provided in the conduit of the fourth inlet tube 76. In this manner, the preset flow rate can be adjusted by adjusting the first air velocity adjusting valve 80, thereby adjusting the sizes of the first solid particles and the second solid particles. For example, increasing the preset flow rate increases the particle size of the first solid particles, i.e., the larger particle size first solid particles can be drawn out of the first outlet pipe 72, which reduces gasifier recycle material returned to the gasifier and increases furnace recycle material returned to the furnace. Conversely, decreasing the preset flow rate decreases the size of the first solid particles, i.e., smaller size first solid particles can be drawn from the first outlet pipe 72, which increases gasifier circulation material back to the gasifier and decreases furnace circulation material back to the furnace. Meanwhile, the amount of coal in the gasification furnace and the combustion furnace can be adjusted by adjusting the first air speed adjusting and controlling valve 80. Therefore, the proportion of gasification and heat supply can be adjusted by adjusting the first air speed adjusting and controlling valve 80 so as to adapt to gasification reaction under different working conditions. In addition, the flow rate of the fluidizing gas can be adjusted by adjusting the second gas velocity adjusting valve 81, so that the flow rate of solid particles in the shell is adjusted, and the adjustment of the heat exchange speed is realized.
In some embodiments, the particle screening component includes a fifth inlet duct 82, the fifth inlet duct 82 being located outside the housing 70 and communicating with the first outlet duct 72 for feeding oxygen to the first outlet duct. When coarse particle circulating materials in the gasification furnace are gradually reduced and fine particle circulating materials in the combustion furnace are gradually increased, oxygen can be introduced into a first outlet pipe 72 of the fluidized bed heat exchanger to replace part of gas with preset flow rate, the oxygen can be subjected to combustion reaction with carbon after being introduced, a high-temperature melting area is formed above the first outlet pipe 72, the fine particle circulating materials are melted and then bonded into large particles, and the large particles are led out through the first outlet pipe 72 and then enter the gasification furnace, so that the coarse particle circulating materials of the gasification furnace are increased, the fine particle circulating materials of the combustion furnace are reduced, and the stable operation of the gasification furnace and the combustion furnace is ensured.
In some embodiments, the first inlet pipe 71 extends to the inside of the shell 70, the discharge opening of the first inlet pipe 71 is closer to the bottom of the shell than the second outlet pipe 74, that is, the bottom end of the first inlet pipe 71 is lower than the second outlet pipe 74 in fig. 2, and the distance between the discharge opening of the first inlet pipe 71 and the feed opening of the second outlet pipe 74 in the extending direction (vertical direction in practical application) of the first inlet pipe 71 is 200mm to 500 mm. So, guarantee that the coarse grain circulation material of gasifier can not enter into the combustion furnace, avoid gasifier fuel and bed material not enough, and prevent that the bed material of coarse grain or coal from getting into the fluidization that influences combustion furnace behind the combustion furnace.
In some embodiments, the distance from the feed opening of the second outlet tube 74 to the top of the housing 70 is greater than or equal to 1 m. In this manner, a sufficient ash settling height is ensured so that the secondary solid particles are directed out of the secondary outlet pipe 74.
In some embodiments, the fluidized bed heat exchanger may also include a differential level gauge 84. Optionally, a differential level gauge 84 is located on the side of the housing 70 and includes an upper pressure port and a lower pressure port. Wherein the upper pressure introduction port is higher than the second outlet pipe 74.
Based on the foregoing technical solution, an embodiment of the present disclosure further provides a dual fluidized bed coal gasification system, and fig. 3 is a schematic structural diagram of the dual fluidized bed coal gasification system provided in the embodiment of the present disclosure. With reference to fig. 2 and 3, the dual fluidized bed coal gasification system comprises: the gasification furnace 1, the combustion furnace 2, the gasification furnace cyclone separator 3, the combustion furnace cyclone separator 4, the gasification furnace return feeder 5, the combustion furnace return feeder 6 and the fluidized bed heat exchanger 7 provided by the embodiment of the disclosure;
wherein, the feed inlet of the first inlet pipe 71 of the fluidized bed heat exchanger 7 is connected with the discharge outlet of the gasification furnace cyclone separator 3, and the feed inlet of the gasification furnace cyclone separator 3 is connected with the circulating material outlet of the gasification furnace 1;
the discharge hole of the first outlet pipe 72 of the fluidized bed heat exchanger 7 is connected with the feed inlet of the gasifier returning device 5, and the discharge hole of the gasifier returning device 5 is connected with the circulating material inlet of the gasifier 1;
The feed inlet of a second inlet pipe 73 of the fluidized bed heat exchanger 7 is connected with the discharge outlet of the combustion furnace cyclone separator 4, and the feed inlet of the combustion furnace cyclone separator 4 is connected with the circulating material outlet of the combustion furnace 2;
the discharge port of the second outlet pipe 74 of the fluidized bed heat exchanger 7 is connected with the feed port of the combustion furnace material returning device 6, and the discharge port of the combustion furnace material returning device 6 is connected with the circulating material inlet of the combustion furnace 2.
Based on the technical scheme, in a specific embodiment, the fuel A and the fluidized reaction gas E enter the fluidized bed 1 for reaction, the reacted gas carrying bed materials and carbon particles enters the gasifier cyclone separator 3, and the gas J enters the rear system for waste heat recovery, dust removal, purification and other processes for use by a user; the bed material and the carbon particles trapped by the gasifier cyclone 3 enter the fluidized bed heat exchanger 7 through the first flap valve 91, after the bed material and the carbon particles are heated by the combustion furnace circulating material trapped by the combustion furnace cyclone 4, the bed material and the coal particles with the particle size of more than or equal to 300 mu m enter the gasifier 1 again through the gasifier return feeder 5 to provide heat for the gasifier reaction, and the operation is repeated.
The coal and the combustion furnace circulating material with the particle size of 0-100 mu m which are guided through the second outlet pipe 74 are sent into the combustion furnace 2 through the combustion furnace return feeder 6 and have combustion reaction with the air F to heat the combustion furnace circulating material with the particle size of 0-100 mu m, then the flue gas carries the combustion furnace circulating material and the coal ash to enter the combustion furnace cyclone separator 4, and the flue gas passes through the high-temperature flue gas dust remover 8 and then is discharged into a chimney through a waste heat recovery device, a flue gas purification device and the like; the material captured by the cyclone separator 4 of the combustion furnace enters the fluidized bed heat exchanger 7 through the second flap valve 92 to heat the circulating material of the gasification furnace; the furnace circulation material enters through a second inlet pipe 73 of the fluidized bed heat exchanger 7 and exits through a second outlet pipe 74 of the fluidized bed heat exchanger 7.
In addition, in some embodiments, the gasification furnace may be supplemented with a coarse-particle bed material B, and when the carbon transferred from the gasification furnace fails to satisfy the combustion temperature after combustion in the combustion furnace, a supplementary fuel C, which is a fine-particle fuel, is added from the combustion furnace. Alternatively, fuel a may be screened to obtain fine particulate fuel as supplemental fuel C.
In the embodiment of the disclosure, the operation temperature of the gasification furnace is 700-750 ℃, and the temperature of the circulating material of the gasification furnace which is fed into the gasification furnace again from the fluidized bed heat exchanger through the return device 5 is 800-850 ℃. The operation temperature of the combustion furnace is 950-.
The dual fluidized bed coal gasification system provided by the embodiment of the disclosure comprises the fluidized bed heat exchanger provided by the embodiment of the disclosure, has the same functions and beneficial effects, and is not described again here.
The disclosure also provides a control method of the double fluidized bed coal gasification system, which comprises the following steps:
and 101, capturing solid particles coming out of the gasification furnace by using a cyclone separator of the gasification furnace, and introducing the solid particles into the fluidized bed heat exchanger through a first inlet pipe of the fluidized bed heat exchanger.
Step 102, capturing solid particles from the combustion furnace by using the cyclone separator of the combustion furnace, and introducing the solid particles into the fluidized bed heat exchanger through a second inlet pipe of the fluidized bed heat exchanger.
Step 103, fluidizing the solid particles introduced into the fluidized bed heat exchanger by using the particle fluidizing part of the fluidized bed heat exchanger.
104, screening first solid particles and second solid particles from the fluidized solid particles by using a particle screening component of the fluidized bed heat exchanger, leading the first solid particles out of a first outlet pipe, and leading the second solid particles out of a second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles;
and 105, returning the first solid particles to the gasification furnace by using a gasification furnace return feeder.
And 106, returning the second solid particles to the combustion furnace by using a combustion furnace return feeder.
The control method of the dual fluidized bed coal gasification system provided by the embodiment of the present disclosure is used for controlling material flow in the dual fluidized bed coal gasification system, and specific reference may be made to the above embodiment, which is not described herein again.
It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.
The previous description is only for the purpose of describing particular embodiments of the present disclosure, so as to enable those skilled in the art to understand or implement the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.
Claims (9)
1. A dual fluidized bed coal gasification system, comprising: the gasification furnace, the combustion furnace, the gasification furnace cyclone separator, the combustion furnace cyclone separator, the gasification furnace material returning device, the combustion furnace material returning device and the fluidized bed heat exchanger;
the fluidized bed heat exchanger includes: a housing, a first inlet duct, a first outlet duct, a second inlet duct, a second outlet duct, a particle fluidization component, and a particle screening component;
wherein the first inlet tube, the first outlet tube, the second inlet tube, and the second outlet tube all pass through the shell; the first inlet pipe and the second inlet pipe are used for introducing solid particles into the shell; the particle fluidization component is used for fluidizing the solid particles; the particle screening component is used for screening first solid particles and second solid particles from fluidized solid particles, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles;
A feed inlet of a first inlet pipe of the fluidized bed heat exchanger is connected with a discharge outlet of the gasification furnace cyclone separator, and a feed inlet of the gasification furnace cyclone separator is connected with a circulating material outlet of the gasification furnace;
a discharge hole of a first outlet pipe of the fluidized bed heat exchanger is connected with a feed inlet of the gasification furnace material returning device, and a discharge hole of the gasification furnace material returning device is connected with a circulating material inlet of the gasification furnace;
a feed inlet of a second inlet pipe of the fluidized bed heat exchanger is connected with a discharge outlet of the combustion furnace cyclone separator, and a feed inlet of the combustion furnace cyclone separator is connected with a circulating material outlet of the combustion furnace;
and a discharge port of a second outlet pipe of the fluidized bed heat exchanger is connected with a feed port of the combustion furnace material returning device, and a discharge port of the combustion furnace material returning device is connected with a circulating material inlet of the combustion furnace.
2. The dual fluidized bed coal gasification system of claim 1, wherein the first inlet pipe is located at the top of the housing, the first outlet pipe is located at the bottom of the housing, the second inlet pipe and the second outlet pipe are located at the side of the housing, and the second outlet pipe is closer to the top of the housing than the second inlet pipe;
The particle screening component comprises a third inlet pipe, wherein the third inlet pipe is positioned outside the shell and communicated with the first outlet pipe and is used for sending gas with preset flow rate into the shell.
3. The dual fluidized bed coal gasification system of claim 2, wherein the particle fluidization component comprises a fourth inlet pipe and a grid plate; the air distribution plate is positioned in the shell and forms an air chamber with the bottom of the shell; the fourth inlet pipe is positioned outside the shell, is communicated with the air chamber and is used for feeding fluidizing gas to the air chamber; the first outlet pipe penetrates through the air distribution plate.
4. The dual fluidized bed coal gasification system of claim 3, wherein the air inlet of the third inlet pipe and the air inlet of the fourth inlet pipe are both in communication with the same air supply pipe.
5. The dual fluidized bed coal gasification system according to claim 3, wherein the pipeline of the third inlet pipe is provided with a first air velocity regulating valve, and/or the pipeline of the fourth inlet pipe is provided with a second air velocity regulating valve.
6. The dual fluidized bed coal gasification system of claim 3, wherein the particle screening component comprises a fifth inlet pipe located outside the housing and in communication with the first outlet pipe for feeding oxygen to the first outlet pipe.
7. The dual fluidized bed coal gasification system according to claim 2, wherein the first inlet pipe extends to the inside of the shell, the discharge port of the first inlet pipe is closer to the bottom of the shell than the second outlet pipe, and the distance between the discharge port of the first inlet pipe and the feed port of the second outlet pipe in the extending direction of the first inlet pipe is 200mm to 500 mm.
8. The dual fluidized bed coal gasification system of claim 2, wherein the distance from the feed inlet of the second outlet pipe to the top of the housing is greater than or equal to 1 m.
9. A control method of a dual fluidized bed coal gasification system according to claim 1, characterized by comprising:
capturing solid particles from the gasification furnace by using a cyclone separator of the gasification furnace, and introducing the solid particles into the fluidized bed heat exchanger through a first inlet pipe of the fluidized bed heat exchanger;
capturing solid particles from the combustion furnace by using a combustion furnace cyclone separator, and introducing the solid particles into the fluidized bed heat exchanger through a second inlet pipe of the fluidized bed heat exchanger;
fluidizing solid particles introduced into the interior of a fluidized bed heat exchanger with a particle fluidizing component of the fluidized bed heat exchanger;
Screening first solid particles and second solid particles from the fluidized solid particles by using a particle screening component of a fluidized bed heat exchanger, leading the first solid particles out of the first outlet pipe, and leading the second solid particles out of the second outlet pipe, wherein the particle size of the first solid particles is larger than that of the second solid particles;
returning the first solid particles to the gasifier using a gasifier return;
returning the second solid particles to the furnace using a furnace return.
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| CN103756731B (en) * | 2014-01-03 | 2015-11-11 | 东南大学 | A kind of reciprocating cycle double fluidized bed solid fuel gasification device and method |
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