CN115772426A - Circulating fluidized bed device with byproduct coke powder and operation method thereof - Google Patents
Circulating fluidized bed device with byproduct coke powder and operation method thereof Download PDFInfo
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- CN115772426A CN115772426A CN202211558978.0A CN202211558978A CN115772426A CN 115772426 A CN115772426 A CN 115772426A CN 202211558978 A CN202211558978 A CN 202211558978A CN 115772426 A CN115772426 A CN 115772426A
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Abstract
The invention provides a circulating fluidized bed device for by-producing coke powder and an operation method thereof, wherein the circulating fluidized bed device comprises a circulating fluidized bed boiler, a separation unit, a cooling unit and a waste heat recovery unit; the circulating fluidized bed boiler comprises a main combustion chamber, a pyrolysis chamber, an auxiliary combustion chamber and a burnout chamber which are sequentially arranged from bottom to top; the main combustion chamber and the pyrolysis chamber are respectively and independently provided with a raw material inlet; the burnout chamber is connected with the separation unit; the pyrolysis chamber is connected with the cooling unit; the separation unit, the waste heat recovery unit and the cooling unit are sequentially in circulating connection; the operation method is based on the improvement of the device structure, the raw coal in the pyrolysis chamber is directly subjected to fluidized pyrolysis by using high-temperature flue gas generated by combustion of the main combustion chamber, the use requirement is met, high-value coke powder is produced as a byproduct, and in addition, the purposes of energy conservation and consumption reduction are achieved by matching the separation unit, the cooling unit and the waste heat recovery unit, so that the device has better economic benefit.
Description
Technical Field
The invention belongs to the technical field of coal chemical pyrolysis, and particularly relates to a circulating fluidized bed device for by-producing coke powder and an operation method thereof.
Background
With the increasing greenhouse effect, new energy power generation becomes the key point of research. However, the installed scale of new energy power generation such as wind power generation and solar power generation is still small, and the large power demand cannot be met temporarily, so that thermal power generation is still the current mainstream. The thermal power generation is mainly based on coal-fired power generation, the capacity ratio of a coal-fired machine assembling machine exceeds eighty percent, and NO discharged by coal-fired flue gas x 、SO 2 And Hg bring great harm to human health and ecological environment. Under the condition that the contradiction between coal burning and environmental protection is increasingly prominent, the circulating fluidized bed boiler becomes a first-selected novel combustion technology with high efficiency and low pollution.
However, it is not economical to grind raw coal and directly feed the ground coal into a circulating fluidized bed boiler for combustion. CN105062570A discloses a combined circulating fluidized bed gasification device and a method thereof, comprising a pyrolysis chamber, a gasification chamber and a cyclone separator which are connected in sequence; the pyrolysis chamber is respectively provided with a raw material inlet, a pyrolysis gas outlet and a semicoke outlet, and the pyrolysis gas outlet is arranged above the semicoke outlet; the gasification chamber is respectively provided with a primary air inlet, a pyrolysis gas inlet and a semicoke inlet, the pyrolysis gas outlet is connected with the pyrolysis gas inlet, and the semicoke outlet is connected with the semicoke inlet through an overflow pipe; the cyclone separator is provided with a gas outlet.
CN104962302A discloses a pyrolysis process and device of high temperature mixture in circulating fluidized bed boiler combustion chamber, including circulating fluidized bed boiler combustion chamber and the fluidized bed pyrolysis reactor who is equipped with pyrolysis coal slope pipe interface, the plenum upper end slope in the circulating fluidized bed boiler combustion chamber is provided with circulating fluidized bed distribution plate, set up the high temperature mixture export on the furnace wall side of the cone section district of fluidized bed distribution plate top of circulating fluidized bed boiler combustion chamber, the high temperature mixture export is connected to fluidized bed pyrolysis reactor on the side of reaction chamber bottom through high temperature mixture slope pipe, fluidized bed pyrolysis reactor's annular pyrolysis semicoke storehouse is connected to in the circulating fluidized bed boiler combustion chamber through pyrolysis semicoke slope pipe.
CN105754621A discloses a coal pyrolysis reactor-circulating fluidized bed combined system and a method for treating coal by using the same, the combined system comprises a coal pyrolysis reactor and a circulating fluidized bed which are independent and do not interfere with each other, and the existing conveying system of the circulating fluidized bed is used to realize the heat delivery of semicoke, ensure the combustion of semicoke and reduce the cost of coal topping process.
In the method, the fluidized bed boiler and the pyrolyzer are combined, the generated semicoke is fed into the fluidized bed boiler, and the energy utilization rate of a power generation system is improved to a certain extent, so that the economy is improved.
In summary, how to provide a method that is efficient and energy-saving and can further improve the economy of a circulating fluidized bed device is a technical problem to be solved at present.
Disclosure of Invention
Aiming at the problems in the prior art, the invention aims to provide a circulating fluidized bed device for by-producing coke powder and an operation method thereof.
In order to achieve the purpose, the invention adopts the following technical scheme:
in a first aspect, the invention provides a circulating fluidized bed device for byproduct coke powder, which comprises a circulating fluidized bed boiler, a separation unit, a cooling unit and a waste heat recovery unit;
the circulating fluidized bed boiler comprises a main combustion chamber, a pyrolysis chamber, an auxiliary combustion chamber and a burnout chamber which are sequentially arranged from bottom to top; a gas distribution plate is arranged between the main combustion chamber and the pyrolysis chamber; the main combustion chamber and the pyrolysis chamber are respectively and independently provided with a raw material inlet;
the burnout chamber is connected with the separation unit;
the pyrolysis chamber is connected with the cooling unit;
the separation unit, the waste heat recovery unit and the cooling unit are sequentially in circulating connection.
The invention adds the pyrolysis chamber between the main combustion chamber and the auxiliary combustion chamber in the circulating fluidized bed boiler, and the raw materials are respectively introduced into the main combustion chamber and the pyrolysis chamber, so that the circulating fluidized bed boiler can produce high-value coke powder as a byproduct while meeting the use requirement, and meanwhile, the purposes of energy saving and consumption reduction are achieved by matching the separation unit, the cooling unit and the waste heat recovery unit, and the invention has better economic benefit.
The following technical solutions are preferred technical solutions of the present invention, but not limited to the technical solutions provided by the present invention, and technical objects and advantageous effects of the present invention can be better achieved and achieved by the following technical solutions.
As a preferred technical solution of the present invention, the circulating fluidized bed apparatus further includes a crushing unit, and the crushing unit is independently connected to the main combustion chamber and the pyrolysis chamber, respectively.
As a preferred technical solution of the present invention, the separation unit is further connected to the primary combustion chamber.
As the preferable technical scheme of the invention, the sidewall of the burnout chamber is provided with a deoxygenated water inlet.
As the preferable technical scheme of the invention, the top of the burnout chamber is provided with a steam outlet.
In a second aspect, the present invention provides a method for operating the circulating fluidized bed apparatus of the first aspect, the method comprising the steps of:
raw coal is respectively fed into a main combustion chamber and a pyrolysis chamber of a circulating fluidized bed boiler, smoke generated by combustion in the main combustion chamber enters the pyrolysis chamber, fluidized pyrolysis is carried out on the raw coal in the pyrolysis chamber, and coke powder obtained by pyrolysis enters a cooling unit for fluidized cooling; the flue gas generated by pyrolysis enters an auxiliary combustion chamber for combustion, then enters a burnout chamber, the burned flue gas enters a separation unit, and the solid obtained by separation is circulated back to the main combustion chamber; the flue gas obtained by separation enters a waste heat recovery unit, enters a cooling unit to carry out fluidized cooling on the coke powder after heat release, and then returns to the separation unit to realize cyclic utilization.
Aiming at the uneconomic property that the fluidized bed boiler only burns raw coal, the arrangement of the pyrolysis chamber can lead high-temperature smoke generated by the combustion of the main combustion chamber to directly carry out fluidized pyrolysis on the raw coal in the pyrolysis chamber, and the byproduct of high-value coke powder can be used in the industries of metallurgy, glass, ceramics and the like. While the fluidization conditions help to feed the produced coke powder to the cooling unit. In addition, high-temperature flue gas generated by combustion can enter a cooling unit for fluidizing and cooling coke powder through further combustion and separation and waste heat recovery, so that cyclic utilization is realized, the energy is saved and the consumption is reduced in the whole process, and the industrial production is facilitated.
As a preferred technical scheme of the invention, the raw coal is crushed before being fed into the main combustion chamber and the pyrolysis chamber.
Preferably, the particle size of the crushed raw coal is < 6mm, for example 1mm, 1.5mm, 2mm, 2.5mm, 3mm, 3.5mm, 4mm, 4.5mm, 5mm, 5.5mm or 5.8mm, but is not limited to the recited values, and other values not recited in the numerical range are also applicable.
In the invention, the particle size of the raw coal has a great influence on the quality of the coke powder. If the particle size range is too wide, the fluidization state of the pulverized coal in the boiler is influenced, and the quality of the coke powder product is further influenced.
In a preferred embodiment of the present invention, the temperature of the main combustion chamber is 850 to 1050 ℃, for example 850 ℃, 900 ℃, 950 ℃, 1000 ℃ or 1050 ℃, but is not limited to the above-mentioned values, and other values not shown in the above-mentioned range are also applicable.
Preferably, the pressure in the primary combustion chamber is 3 to 14kPa, such as 3kPa, 6kPa, 8kPa, 10kPa, 12kPa, or 14kPa, but is not limited to the recited values, and other values not recited in the range of values are equally applicable.
Preferably, the temperature of the pyrolysis chamber is 630 to 680 ℃, such as 630 ℃, 635 ℃, 640 ℃, 645 ℃, 650 ℃, 655 ℃, 660 ℃, 665 ℃, 670 ℃, 675 ℃ or 680 ℃, but is not limited to the recited values, and other values not recited in the range of values are equally applicable.
Preferably, the pressure in the pyrolysis chamber is in the range of-0.05 kPa to 3kPa, such as-0.05 kPa, 0kPa, 0.5kPa, 1.0kPa, 1.5kPa, 2.0kPa, 2.5kPa, 3.0kP, or the like, but is not limited to the recited values, and other values not recited in this range of values are equally applicable.
As a preferable embodiment of the present invention, the mass of the raw coal in the main combustion chamber is 0.2 times or more, for example, 0.2 times, 0.3 times, 0.6 times, 0.7 times, 0.8 times, 0.9 times, 1.0 times, 1.1 times, 1.2 times, 1.3 times, 1.4 times, or 2 times the mass of the raw coal in the pyrolysis chamber, but the present invention is not limited to the above-mentioned values, and other values not shown in the above-mentioned value range are also applicable.
In the invention, the quality of the raw coal in the main combustion chamber can be adjusted according to production requirements, but the raw coal cannot be too low, otherwise, the raw coal in the pyrolysis chamber cannot be completely pyrolyzed, waste is caused, and the running economy of the whole device is poor.
As a preferable technical scheme of the invention, deoxygenated water is also introduced into the burnout chamber to generate steam.
In the present invention, the generated steam can be used for power generation or as a driving force for other production devices in the plant.
Compared with the prior art, the invention has the following beneficial effects:
the circulating fluidized bed device is characterized in that a pyrolysis chamber is additionally arranged between a main combustion chamber and an auxiliary combustion chamber in the circulating fluidized bed boiler, raw materials are respectively introduced into the main combustion chamber and the pyrolysis chamber, high-temperature flue gas generated by combustion in the main combustion chamber is used for directly fluidizing and pyrolyzing raw coal in the pyrolysis chamber, so that the circulating fluidized bed boiler meets the use requirement of steam production or power generation and simultaneously generates high-value coking powder as a byproduct, and the purposes of energy conservation and consumption reduction are achieved by matching with a separation unit, a cooling unit and a waste heat recovery unit, so that the circulating fluidized bed boiler has better economic benefit.
Drawings
Fig. 1 is a flow chart showing the operation of a circulating fluidized bed apparatus for by-producing coke powder according to application example 1 of the present invention.
The method comprises the following steps of 1-circulating fluidized bed boiler, 11-main combustion chamber, 12-pyrolysis chamber, 13-auxiliary combustion chamber, 14-burnout chamber, 2-separation unit, 3-cooling unit, 4-waste heat recovery unit and 5-crushing unit.
Detailed Description
In order to better explain the present invention and to facilitate the understanding of the technical solutions of the present invention, the present invention is further described in detail below. However, the following examples are only simple examples of the present invention and do not represent or limit the scope of the present invention, which is defined by the claims.
The following are typical but non-limiting examples of the invention:
example 1:
the embodiment provides a circulating fluidized bed device for byproduct coke powder, which comprises a circulating fluidized bed boiler 1, a separation unit 2, a cooling unit 3 and a waste heat recovery unit 4;
the circulating fluidized bed boiler 1 comprises a main combustion chamber 11, a pyrolysis chamber 12, an auxiliary combustion chamber 13 and a burnout chamber 14 which are sequentially arranged from bottom to top; the main combustion chamber 11 and the pyrolysis chamber 12 are respectively and independently provided with a raw material inlet;
the burnout chamber 14 is connected to the separation unit 2;
the pyrolysis chamber 12 is connected to the cooling unit 3;
the separation unit 2, the waste heat recovery unit 4 and the cooling unit 3 are sequentially in circulation connection.
The circulating fluidized bed apparatus further includes a crushing unit 5, and the crushing unit 5 is independently connected to the main combustion chamber 11 and the pyrolysis chamber 12, respectively.
The separation unit 2 is also connected to the main combustion chamber 11.
The lateral wall of burnout chamber 14 is provided with the deoxidization water entry, and the top is provided with the steam outlet.
Example 2:
the embodiment provides a circulating fluidized bed device for byproduct coke powder, which comprises a circulating fluidized bed boiler 1, a separation unit 2, a cooling unit 3 and a waste heat recovery unit 4;
the circulating fluidized bed boiler 1 comprises a main combustion chamber 11, a pyrolysis chamber 12, an auxiliary combustion chamber 13 and a burnout chamber 14 which are sequentially arranged from bottom to top; the main combustion chamber 11 and the pyrolysis chamber 12 are respectively and independently provided with a raw material inlet;
the burnout chamber 14 is connected to the separation unit 2;
the pyrolysis chamber 12 is connected with the cooling unit 3;
the separation unit 2, the waste heat recovery unit 4 and the cooling unit 3 are sequentially in circulation connection.
The separation unit 2 is also connected to the primary combustion chamber 11.
The lateral wall of burnout chamber 14 is provided with the deoxidization water entry, and the top is provided with the steam outlet.
Application example 1:
the present application example provides an operation method of a circulating fluidized bed device with byproduct coke powder, the circulating fluidized bed device is the circulating fluidized bed device in example 1, an operation flow chart of the circulating fluidized bed device is shown in fig. 1, and the operation method includes the following steps:
crushing raw coal, and controlling the particle size to be 4-5 mm; feeding 100t of crushed raw coal into a main combustion chamber 11 of a circulating fluidized bed boiler 1, and feeding 500t of crushed raw coal into a pyrolysis chamber 12 of the circulating fluidized bed boiler 1; burning the raw coal in the main combustion chamber 11 at 900 ℃ and 3-13 kPa, feeding the generated flue gas into a pyrolysis chamber 12, performing fluidized pyrolysis on the raw coal in the pyrolysis chamber 12 at the pyrolysis temperature of 650 ℃ and the pyrolysis pressure of-0.05-3 kPa, and feeding the coke powder obtained by pyrolysis into a cooling unit 3 for fluidized cooling to obtain a coke powder product of 250 t; the flue gas generated by pyrolysis enters an auxiliary combustion chamber 13 for combustion, the combustion temperature is 850 ℃, and the combustion pressure is-0.05 kPa; then the steam enters a burnout chamber 14, deoxygenated water is introduced into the burnout chamber 14 at the same time, the combustion temperature is 900 ℃, the combustion pressure is-0.05 kPa, and 1354t of the generated steam is used for power generation; the flue gas after burning out enters a separation unit 2, and the solid obtained by separation is circulated back to the main combustion chamber 11; the flue gas obtained by separation enters a waste heat recovery unit 4 for heat recovery, the flue gas after waste heat recovery enters a cooling unit 3 for fluidized cooling of coke powder, and then the flue gas returns to the separation unit 2 for cyclic utilization.
Application example 2:
the application example provides an operation method of a circulating fluidized bed device with byproduct coke powder, the circulating fluidized bed device is the circulating fluidized bed device in the embodiment 1, and the operation method comprises the following steps:
crushing raw coal, and controlling the particle size to be 4-5 mm; feeding 200t of crushed raw coal into a main combustion chamber 11 of the circulating fluidized bed boiler 1, and feeding 200t of crushed raw coal into a pyrolysis chamber 12 of the circulating fluidized bed boiler 1; burning the raw coal in the main combustion chamber 11 at 900 ℃ and 3-13 kPa, feeding the generated flue gas into a pyrolysis chamber 12, performing fluidized pyrolysis on the raw coal in the pyrolysis chamber 12 at the pyrolysis temperature of 650 ℃ and the pyrolysis pressure of-0.05-3 kPa, and feeding the coke powder obtained by pyrolysis into a cooling unit 3 for fluidized cooling to obtain 100t coke powder products; the flue gas generated by pyrolysis enters an auxiliary combustion chamber 13 for combustion, the combustion temperature is 850 ℃, and the combustion pressure is-0.05 kPa; then the mixture enters a burnout chamber 14, and simultaneously deoxygenated water is introduced into the burnout chamber 14, the combustion temperature is 900 ℃, the combustion pressure is-0.05 kPa, and steam 1724t can be generated for power generation; the flue gas after being burnt out enters a separation unit 2, and the solid obtained by separation is circulated back to the main combustion chamber 11; the flue gas obtained by separation enters a waste heat recovery unit 4 for heat recovery, the flue gas after waste heat recovery enters a cooling unit 3 for fluidized cooling of coke powder, and then the flue gas returns to the separation unit 2 for cyclic utilization.
Application example 3:
the application example provides an operation method of a circulating fluidized bed device with byproduct coke powder, the circulating fluidized bed device is the circulating fluidized bed device in the embodiment 1, and the operation method comprises the following steps:
crushing raw coal, and controlling the particle size to be 4-5 mm; feeding 300t of crushed raw coal into a main combustion chamber 11 of the circulating fluidized bed boiler 1, and feeding 200t of crushed raw coal into a pyrolysis chamber 12 of the circulating fluidized bed boiler 1; burning the raw coal in the main combustion chamber 11 at 900 ℃ and 3-13 kPa, feeding the generated flue gas into a pyrolysis chamber 12, performing fluidized pyrolysis on the raw coal in the pyrolysis chamber 12 at the pyrolysis temperature of 650 ℃ and the pyrolysis pressure of-0.05-3 kPa, and feeding the coke powder obtained by pyrolysis into a cooling unit 3 for fluidized cooling to obtain 100t coke powder products; the flue gas generated by pyrolysis enters the auxiliary combustion chamber 13 for combustion, the combustion temperature is 850 ℃, and the combustion pressure is-0.05 kPa; then the mixture enters a burnout chamber 14, deoxygenated water is introduced into the burnout chamber 14 at the same time, the combustion temperature is 900 ℃, the combustion pressure is-0.05 kPa, and 2464t of steam can be generated for power generation; the flue gas after being burnt out enters a separation unit 2, and the solid obtained by separation is circulated back to the main combustion chamber 11; the flue gas obtained by separation enters a waste heat recovery unit 4 for heat recovery, and the flue gas subjected to waste heat recovery enters a cooling unit 3 for fluidized cooling of coke powder and then returns to the separation unit 2 for recycling.
Comparative example application example 1:
this comparative application example provides a method for operating a circulating fluidized bed apparatus by-producing coke powder, the circulating fluidized bed apparatus is the circulating fluidized bed apparatus in example 1, and the operating method is different from the method in application only in that: the particle size of the crushed raw coal is controlled to be 0-10 mm.
When the coal powder is operated under the condition, the wide particle size range influences the fluidization state of the coal powder in the boiler, and further causes the quality reduction of the coke powder product.
The present invention is illustrated in detail by the examples given above, but the present invention is not limited to the details given above, which means that the present invention is not limited to the details given above. It will be apparent to those skilled in the art that any modifications to the present invention, equivalents thereof, additions of additional operations, selection of specific ways, etc., are within the scope and disclosure of the present invention.
Claims (10)
1. The circulating fluidized bed device with the byproduct of the coke powder is characterized by comprising a circulating fluidized bed boiler, a separation unit, a cooling unit and a waste heat recovery unit;
the circulating fluidized bed boiler comprises a main combustion chamber, a pyrolysis chamber, an auxiliary combustion chamber and a burnout chamber which are sequentially arranged from bottom to top; a gas distribution plate is arranged between the main combustion chamber and the pyrolysis chamber; the main combustion chamber and the pyrolysis chamber are respectively and independently provided with a raw material inlet;
the burnout chamber is connected with the separation unit;
the pyrolysis chamber is connected with the cooling unit;
the separation unit, the waste heat recovery unit and the cooling unit are sequentially in circulating connection.
2. The circulating fluidized bed apparatus of claim 1, further comprising a breaking unit independently connected to the primary combustion chamber and the pyrolysis chamber, respectively.
3. The circulating fluidized bed apparatus of claim 1 or 2, wherein the separation unit is further connected to the primary combustion chamber.
4. The circulating fluidized bed apparatus of any one of claims 1 to 3, wherein a sidewall of the burnout chamber is provided with an inlet for deoxygenated water.
5. The circulating fluidized bed apparatus of any one of claims 1 to 4, wherein the top of the burnout chamber is provided with a steam outlet.
6. A method of operating a circulating fluidized bed apparatus according to any one of claims 1 to 5, characterized in that the method of operating comprises the steps of:
raw coal is respectively fed into a main combustion chamber and a pyrolysis chamber of a circulating fluidized bed boiler, smoke generated by combustion in the main combustion chamber enters the pyrolysis chamber, fluidized pyrolysis is carried out on the raw coal in the pyrolysis chamber, and coke powder obtained by pyrolysis enters a cooling unit for fluidized cooling; the flue gas generated by pyrolysis enters an auxiliary combustion chamber for combustion and then enters a burnout chamber, the flue gas after burnout enters a separation unit, and the solid obtained by separation is circulated back to the main combustion chamber; the flue gas obtained by separation enters a waste heat recovery unit, enters a cooling unit to carry out fluidized cooling on the coke powder after heat release, and then returns to the separation unit to realize cyclic utilization.
7. The operating method according to claim 6, characterized in that the raw coal is crushed before being fed into the primary combustion chamber and the pyrolysis chamber;
preferably, the particle size of the crushed raw coal is less than 6mm.
8. The operating method according to claim 6 or 7, characterized in that the temperature of the main combustion chamber is 850 to 1050 ℃;
preferably, the pressure of the main combustion chamber is 3-14 kPa;
preferably, the temperature of the pyrolysis chamber is 630 to 680 ℃;
preferably, the pressure of the pyrolysis chamber is-0.05 to 3kPa.
9. The operating method according to any one of claims 6 to 8, characterized in that the mass of the raw coal in the main combustion chamber is more than 0.2 times the mass of the raw coal in the pyrolysis chamber.
10. An operating method according to any one of claims 6 to 9, characterized in that deoxygenated water is also fed into the burnout chamber to produce steam.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211558978.0A CN115772426A (en) | 2022-12-06 | 2022-12-06 | Circulating fluidized bed device with byproduct coke powder and operation method thereof |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202211558978.0A CN115772426A (en) | 2022-12-06 | 2022-12-06 | Circulating fluidized bed device with byproduct coke powder and operation method thereof |
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| CN115772426A true CN115772426A (en) | 2023-03-10 |
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