CN111996039B - Staged gasification method and apparatus - Google Patents
Staged gasification method and apparatus Download PDFInfo
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- CN111996039B CN111996039B CN202010874259.4A CN202010874259A CN111996039B CN 111996039 B CN111996039 B CN 111996039B CN 202010874259 A CN202010874259 A CN 202010874259A CN 111996039 B CN111996039 B CN 111996039B
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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
- C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
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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
Abstract
A staged gasification method and apparatus, the staged gasification method includes introducing fuel B and first gasification agent A into the first-class gasification unit to take place gasification reaction, produce gas-solid mixture C and bottom slag K; gas-solid mixture C is subjected to gas-solid separation to form primary coal gas E and hot semicoke D; feeding the hot semicoke D and a second gasifying agent F into a first reactor to react to generate a mixture G; and the mixture G and the primary coal gas E enter a heat exchange reactor to complete heat exchange reaction, so that solid bottom slag L and final coal gas H are generated, and graded gasification is completed. The invention fully utilizes the sensible heat of the product of the high-temperature reactor to promote the cracking of the tar and the conversion of carbon in the primary gas and improve the gasification performance of the system.
Description
Technical Field
The invention relates to the technical field of gasification, in particular to a gasification device and a gasification method for a carbon-containing raw material, and particularly relates to a staged gasification method and a staged gasification device.
Background
The coal gasification technology is an important component of clean coal technology, is one of main ways for efficiently and cleanly utilizing coal, and has become a core technology of numerous modern energy and chemical systems. The fluidized bed gasification can realize good back mixing and contact between the gasification agent and the fuel, wide-screen crushed coal particles can be used as the fuel, and the adaptability of the coal type is strong; however, fluidized bed gasification is limited by the fluidization of the particles and can generally only be operated below 1000 ℃, and the gasification reaction rate is low, resulting in low carbon conversion. The entrained flow coal gasification process has the advantages of high reaction temperature, high gasification strength, high production capacity and high carbon conversion rate, is the main development direction of the existing coal gasification technology, but has the problems of small particle size of coal powder entering a furnace, high preparation cost, large limitation on coal types and the like. In order to solve the defects of the gasification process, a staged gasification process is provided: the advantages of different reactors and gasification processes are combined, the coal gasification reaction process is controlled in a grading manner, the fuel preparation cost is reduced, the average reaction temperature of the system is increased, and efficient gasification is realized.
The prior staged gasification technology has the following limitations in the practical application process:
(1) for example, the first coal gas flow and the second coal gas flow are formed by separating the products generated by the reaction of the first-stage gasification unit, and then the first coal gas flow and the second coal gas flow are respectively sent to the second-stage gasification unit for staged reaction, which is beneficial to improving the gasification efficiency.
(2) The gas content and the solid content in the first gas flow and the second gas flow are important for the rapid formation of a high-temperature reaction zone in the secondary gasification unit and the carbon conversion rate of the system, and no regulation and control measures for the gas content and the solid content are provided in the prior art.
(3) In the prior entrained flow bed technology, measures of chilling high-temperature slag by cold coal gas, chilling water or cooling slag by a waste heat boiler are adopted, but the problems of tar and carbon residue contained in primary coal gas in staged gasification cannot be solved, high-temperature sensible heat cannot be effectively utilized, and the problems of complex system and wastewater generation also exist.
Disclosure of Invention
In view of the above, one of the main objectives of the present invention is to provide a staged gasification method and apparatus, so as to at least partially solve at least one of the above technical problems.
In order to achieve the above object, as one aspect of the present invention, there is provided a staged gasification method, comprising:
introducing the fuel B and a first gasifying agent A into a primary gasification unit to perform gasification reaction to generate a gas-solid mixture C and bottom slag K;
gas-solid mixture C is subjected to gas-solid separation to form primary coal gas E and hot semicoke D;
feeding the hot semicoke D and a second gasifying agent F into a first reactor to react to generate a mixture G;
and the mixture G and the primary coal gas E enter a heat exchange reactor to complete heat exchange reaction, so that solid bottom slag L and final coal gas H are generated, and graded gasification is completed.
As another aspect of the present invention, there is also provided a staged gasification apparatus, comprising:
the primary gasification unit is provided with a fuel inlet, a first gasification agent inlet, a bottom slag outlet and a gas-solid mixture outlet;
the separation unit comprises a separation unit inlet, a gas outlet and a solid outlet, and the separation unit inlet is communicated with the gas-solid mixture outlet;
the first reactor comprises a hot semicoke inlet, a second gasifying agent inlet and a first reactor outlet, and the hot semicoke inlet is communicated with the solid outlet; and
the heat exchange reactor is provided with a first heat exchange reactor inlet, a second heat exchange reactor inlet and a heat exchange reactor outlet, the first heat exchange reactor inlet is communicated with the first reactor outlet, and the second heat exchange reactor inlet is communicated with the gas outlet; the heat exchange reactor outlet comprises a heat exchange reactor bottom slag outlet and a final coal gas outlet.
Based on the technical scheme, compared with the prior art, the staged gasification method and the staged gasification device have at least one of the following advantages:
(1) the mass of the solid in the hot semicoke accounts for 70-95% of the mass of the solid in the gas-solid mixture and the mass of the gas accounts for 5-20% of the mass of the gas in the gas-solid mixture by regulating and controlling the outlet velocity of the hot semicoke of the separation unit and the velocity of the second gasifying agent F, so that the incompletely reacted carbon carried by the gas-solid mixture generated by the primary gasifying unit can intensively react with the second gasifying agent to promote the conversion of the carbon; the hot semicoke contains gas, which is beneficial to conveying the hot semicoke and realizing rapid reaction with a secondary gasification agent to form a high-temperature area; the gas volume ratio is less than 20 percent so as to reduce the proportion of the second-stage gasifying agent and the combustible gas in the gas-solid mixture for oxidation reaction and improve the reaction proportion of the second-stage gasifying agent and carbon, thereby improving the gasification performance of the system;
(2) the primary coal gas formed after separation of the separation unit enters a heat exchange reactor as a cooling medium, and does not need an additional chilling medium besides realizing tar cracking and carbon conversion by utilizing the sensible heat of a high-temperature mixture, thereby effectively reducing the complexity of the system and reducing the wastewater discharge;
(3) according to the composition of the second gasifying agent, the temperature of the high-temperature reactor and the proportion of the gas mass of the primary gas to the gas mass of the gas-solid mixture, the primary gas is firstly fed into the heat exchanger for heat exchange and temperature reduction before being fed into the heat exchange reactor, so that the temperature in the heat exchange reactor is increased as much as possible while solid-state slag discharge is ensured, the sensible heat of a product generated by the high-temperature reactor is fully utilized to promote the tar cracking and carbon conversion of the primary gas, and the gasification performance of the system is improved.
Drawings
FIG. 1 is a schematic diagram of an apparatus configuration for use in a staged gasification process in an exemplary embodiment of the invention;
FIG. 2 is a schematic view of the structure of an apparatus for use in the staged gasification process in example 1 of the present invention;
FIG. 3 is a schematic view of the structure of an apparatus used in the staged gasification method according to example 2 of the present invention.
Detailed Description
In order that the objects, technical solutions and advantages of the present invention will become more apparent, the present invention will be further described in detail with reference to the accompanying drawings in conjunction with the following specific embodiments.
The invention discloses a staged gasification method, which comprises the following steps:
introducing the fuel B and a first gasifying agent A into a primary gasification unit to perform gasification reaction to generate a gas-solid mixture C and bottom slag K;
gas-solid mixture C is subjected to gas-solid separation to form primary coal gas E and hot semicoke D;
feeding the hot semicoke D and a second gasifying agent F into a first reactor to react to generate a mixture G;
and the mixture G and the primary coal gas E enter a heat exchange reactor to complete heat exchange reaction, so that solid bottom slag L and final coal gas H are generated, and graded gasification is completed.
In some embodiments of the invention, the heat exchange reaction occurs with a tar cracking reaction and a carbon conversion reaction.
In some embodiments of the invention, the mass of solids carried in the hot semicoke D is between 70% and 95% of the mass of solids in the gas-solid mixture C.
In some embodiments of the invention, the mass of gas contained in the hot semicoke D is not more than 20% of the mass of gas in the gas-solid mixture C.
In some embodiments of the invention, the reaction temperature T1 of the hot semicoke D and the second gasifying agent F is in the range of T2< T1< T2+500 ℃; where t2 is the fuel ash softening temperature.
In some embodiments of the present invention, the raw gas E enters the first heat exchanger for heat exchange and temperature reduction before entering the heat exchange reactor.
In some embodiments of the invention, the outlet temperature T2 of the heat exchange reactor is 50-200 ℃ lower than T2.
In some embodiments of the invention, the staged gasification process further comprises waste heat recovery of the final gas H.
The invention also discloses a staged gasification device, comprising:
the primary gasification unit is provided with a fuel inlet, a first gasification agent inlet, a bottom slag outlet and a gas-solid mixture outlet;
the separation unit comprises a separation unit inlet, a gas outlet and a solid outlet, and the separation unit inlet is communicated with the gas-solid mixture outlet;
the first reactor comprises a hot semicoke inlet, a second gasifying agent inlet and a first reactor outlet, and the hot semicoke inlet is communicated with the solid outlet; and
the heat exchange reactor is provided with a first heat exchange reactor inlet, a second heat exchange reactor inlet and a heat exchange reactor outlet, the first heat exchange reactor inlet is communicated with the first reactor outlet, and the second heat exchange reactor inlet is communicated with the gas outlet; the heat exchange reactor outlet comprises a heat exchange reactor bottom slag outlet and a final coal gas outlet.
In some embodiments of the invention, the first reactor and the heat exchange reactor are of a unitary construction.
In one exemplary embodiment, the staged gasification process of the present invention employs an apparatus as shown in FIG. 1, comprising the steps of:
a) introducing a fuel B (taking coal as an example) and a first gasifying agent A into a primary gasification unit 1 to carry out gasification reaction to generate a gas-solid mixture C and bottom slag K;
b) the gas-solid mixture C is subjected to gas-solid separation through the separation unit 2 to form primary coal gas E and hot semicoke D;
c) feeding the hot semicoke D and a second gasifying agent F into a high-temperature reactor 31, and reacting to generate a high-temperature mixture G (a mixture of high-temperature gas, high-temperature ash and high-temperature liquid molten slag);
d) the high-temperature mixture G enters the heat exchange reactor 32, and the primary coal gas E enters the heat exchange reactor 32 to exchange heat with the high-temperature mixture G; meanwhile, hydrocarbon such as tar contained in the primary gas E is cracked at high temperature, and carbon contained in the primary gas E generates C + CO2→CO、C+H2O→CO+H2And the like; finally, generating solid bottom slag L and final gas H;
the mass of the solid carried in the hot semicoke D is 70-95% of that of the solid in the gas-solid mixture C, so that incompletely reacted carbon carried by the gas-solid mixture C generated by the primary gasification unit 1 intensively reacts with the second gasification agent F to promote the conversion of carbon;
wherein, the mass ratio of the gas contained in the hot semicoke D to the gas in the gas-solid mixture C is not higher than 20 percent, for example, 5 to 20 percent. On one hand, the hot semicoke D contains gas which is beneficial to conveying the hot semicoke and realizes quick reaction with the secondary gasifying agent F (combustible gas contained in the gas can quickly generate combustion reaction with the gasifying agent) to form a high-temperature zone, and on the other hand, the gas volume ratio is less than 20 percent to reduce the combustible gas (CH) in the secondary gasifying agent F and the gas-solid mixture C4、CO、H2Etc.) to improve the reaction ratio of the secondary gasifying agent F and carbon, thereby improving the gasification performance of the system.
Wherein the reaction temperature T1 of the hot semicoke D and the second gasifying agent F in the step c) is in the range of T2< T1< T2+500 ℃ (T2 is the softening temperature of fuel ash), and the carbon in the hot semicoke D is promoted to be fully converted in a shorter time through high-temperature reaction.
Wherein, the first gasifying agent A is air or oxygen or a mixture of air, oxygen and water vapor or both.
Wherein, the second gasifying agent F is air or oxygen or a mixture of air, oxygen and water vapor or both.
The technical solution of the present invention is further illustrated by the following specific embodiments in conjunction with the accompanying drawings. It should be noted that the following specific examples are given by way of illustration only and the scope of the present invention is not limited thereto.
Example 1
Fig. 2 is a schematic structural diagram of an apparatus used in the staged gasification method of the present embodiment, and the method of the present embodiment includes the following steps:
a) introducing a fuel B (taking coal as an example) and a first gasifying agent A into the primary gasification unit 1 through a fuel inlet and a first gasifying agent inlet respectively to carry out gasification reaction to generate a gas-solid mixture C and bottom slag K; wherein the bottom slag K is discharged from a bottom slag outlet, and the gas-solid mixture C enters the separation unit 2 from a gas-solid mixture outlet from a separation unit inlet.
b) The gas-solid mixture C is subjected to gas-solid separation through the separation unit 2 to form primary coal gas E and hot semicoke D;
c) respectively feeding the hot semicoke D and the second gasifying agent F into a high-temperature reactor 31 (namely a first reactor) from a hot semicoke inlet and a second gasifying agent inlet, and reacting to generate a high-temperature mixture G (a mixture of high-temperature gas, high-temperature ash and high-temperature liquid slag);
d) the high-temperature mixture G enters the heat exchange reactor 32 from the first inlet of the heat exchange reactor, and the primary coal gas E enters the heat exchange reactor 32 from the second inlet of the heat exchange reactor to exchange heat with the high-temperature mixture G; meanwhile, hydrocarbon such as tar contained in the primary gas E is cracked at high temperature, and carbon contained in the primary gas E generates C + CO2→CO、C+H2O→CO+H2And the like; finally generating solid bottom slag L and final gas H. Solid bottom slag L is discharged from a bottom slag outlet of the heat exchange reactor, and final gas H is discharged from a final gas outlet.
The second gasification agent F is used as a conveying medium and mixed with the hot semicoke D and then enters the high-temperature reactor 31, wherein the inlet speed of the separation unit 2 is 19-30 m/s, the outlet speed of the primary coal gas E is 10-30 m/s, and the outlet speed of the hot semicoke D is 5-20 m/sThe speed of the second gasifying agent F is 5-25 m/s, the speed of the second gasifying agent F after being mixed with the hot semicoke D is 10-25 m/s, the ratio of the mass of the solid carried in the hot semicoke D to the mass of the solid in the gas-solid mixture C can be adjusted between 70-95% by adjusting the speed of the second gasifying agent F, and the ratio of the mass of the gas contained in the hot semicoke D to the mass of the gas in the gas-solid mixture C can be adjusted within 20% (the speed of the second gasifying agent F is increased, the ratio of the mass of the gas in the hot semicoke D to the mass of the solid in the gas-solid mixture C is decreased), so that the combustible gas (CH) in the second gasifying agent F and the gas-solid mixture C is reduced as much as possible4、CO、H2Etc.) in the high-temperature reactor, a high-temperature zone in which the hot semicoke D can be melted is rapidly formed at the same time as the oxidation reaction occurs.
Wherein the reaction temperature T1 of the hot semicoke D and the second gasifying agent F in the step c) is in the range of T2< T1< T2+500 ℃ (T2 is the softening temperature of fuel ash), and the carbon in the hot semicoke D is promoted to be fully converted in a shorter time through high-temperature reaction.
Wherein the first gasifying agent A is a mixture of air and water vapor.
Wherein the second gasifying agent F is a mixture of air and water vapor.
According to the composition of the second gasifying agent F, the temperature of the high-temperature reactor 31 and the proportion of the gas mass of the primary coal gas E to the gas mass of the gas-solid mixture C, the primary coal gas E enters the first heat exchanger 41 for heat exchange and temperature reduction before entering the heat exchange reactor 32, so that the outlet temperature T2 of the heat exchange reactor 32 is 50-200 ℃ lower than that of T2, the temperature in the heat exchange reactor 32 is increased as much as possible while solid-state slag discharge is ensured, and the cracking of tar in the primary coal gas E at high temperature and the C + CO containing carbon in the primary coal gas E are promoted2→CO、C+H2O→CO+H2And (4) reacting.
Wherein, the final gas H is subjected to waste heat recovery through a second heat exchanger 42, and the heat exchanger 42 can be an air preheater or a steam superheater, a waste heat boiler, and the like.
Example 2
Fig. 3 is a schematic structural view of an apparatus used in the staged gasification method of the present embodiment. The method of this example differs from example 1 in that:
the second gasifying agent F is a mixture of pure oxygen and water vapor.
Because the gasifying agent is a mixture of pure oxygen and steam, the sensible heat of the high-temperature mixture G generated in the high-temperature reactor 31 is small at a certain temperature, so that the primary gas E directly enters the heat exchange reactor 32 to be mixed with the high-temperature mixture G to complete heat exchange and reaction without heat exchange and temperature reduction, and the solid slag discharge of the heat exchange reactor 32 can be realized.
The first reactor and the heat exchange reactor are of an integrated structure, namely, the first reactor outlet of the first reactor is directly communicated with the first inlet of the heat exchange reactor.
The above-mentioned embodiments are intended to illustrate the objects, technical solutions and advantages of the present invention in further detail, and it should be understood that the above-mentioned embodiments are only exemplary embodiments of the present invention and are not intended to limit the present invention, and any modifications, equivalents, improvements and the like made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (9)
1. A staged gasification process, comprising:
introducing the fuel B and a first gasifying agent A into a primary gasification unit to perform gasification reaction to generate a gas-solid mixture C and bottom slag K;
gas-solid mixture C is subjected to gas-solid separation to form primary coal gas E and hot semicoke D;
feeding the hot semicoke D and a second gasifying agent F into a first reactor to react to generate a mixture G, wherein the mixture G is a mixture of high-temperature gas, high-temperature ash and high-temperature liquid slag;
and (3) enabling the mixture G and the primary coal gas E to enter a heat exchange reactor to complete a heat exchange reaction, generating solid bottom slag L and final coal gas H, and completing staged gasification, wherein the primary coal gas E is used for cooling the mixture G, and cracking and carbon conversion of hydrocarbons such as tar contained in the primary coal gas E.
2. The staged gasification process of claim 1,
the mass of the solid carried in the hot semicoke D is 70-95% of that in the gas-solid mixture C.
3. The staged gasification process of claim 1,
the mass of the gas contained in the hot semicoke D is not higher than 20% of the mass of the gas in the gas-solid mixture C.
4. The staged gasification process of claim 1,
the reaction temperature T1 of the hot semicoke D and the second gasifying agent F is in the range of T2< T1< T2+500 ℃; where t2 is the fuel ash softening temperature.
5. The staged gasification process of claim 1,
and the primary coal gas E enters a first heat exchanger for heat exchange and temperature reduction before entering a heat exchange reactor.
6. The staged gasification process of claim 1,
the outlet temperature T2 of the heat exchange reactor is 50-200 ℃ lower than that of T2.
7. The staged gasification process of claim 1,
the grading gasification method also comprises the step of recovering waste heat of the final gas H.
8. A staged gasification apparatus comprising:
the primary gasification unit is provided with a fuel inlet, a first gasification agent inlet, a bottom slag outlet and a gas-solid mixture outlet;
the separation unit comprises a separation unit inlet, a gas outlet and a solid outlet, and the separation unit inlet is communicated with the gas-solid mixture outlet;
the first reactor comprises a hot semicoke inlet, a second gasifying agent inlet and a first reactor outlet, and the hot semicoke inlet is communicated with the solid outlet; and
the heat exchange reactor is provided with a first heat exchange reactor inlet, a second heat exchange reactor inlet and a heat exchange reactor outlet, the first heat exchange reactor inlet is communicated with the first reactor outlet, and the second heat exchange reactor inlet is communicated with the gas outlet; the heat exchange reactor outlet comprises a heat exchange reactor bottom slag outlet and a final coal gas outlet.
9. The staged gasification device of claim 8,
the first reactor and the heat exchange reactor are of an integrated structure.
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| CN110791326A (en) * | 2019-11-21 | 2020-02-14 | 中国科学院工程热物理研究所 | Circulating fluidized bed gasification device with auxiliary gasification bed and gasification method |
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| CN107880938A (en) * | 2016-09-30 | 2018-04-06 | 中国科学院工程热物理研究所 | Pre-heated classification gasification method and device |
| CN110551529A (en) * | 2019-09-03 | 2019-12-10 | 中国科学院工程热物理研究所 | Gasification fly ash recycling treatment and heat energy recycling system and method |
| CN110591761A (en) * | 2019-09-12 | 2019-12-20 | 浙江大学 | Coal fluidized bed partial gasification co-production device and process |
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