CN110951506B - Gasification furnace and gasification method thereof - Google Patents
Gasification furnace and gasification method thereof Download PDFInfo
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- CN110951506B CN110951506B CN201911257450.8A CN201911257450A CN110951506B CN 110951506 B CN110951506 B CN 110951506B CN 201911257450 A CN201911257450 A CN 201911257450A CN 110951506 B CN110951506 B CN 110951506B
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- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
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Abstract
The invention relates to the technical field of coal gasification, and provides a gasification furnace and a gasification method thereof. The gasification furnace comprises a primary reaction chamber, a secondary reaction chamber and a chilling chamber, wherein a first contraction section is arranged at the bottom of the primary reaction chamber, and an expansion section is arranged at the top of the secondary reaction chamber. The gasification method comprises the following steps: injecting the material and the oxidant into a primary reaction chamber by a burner, wherein the gas flow rate in the primary reaction chamber is 0.6-1.2m/s, and the retention time is 3-6 s; the flow speed of the mixed gas passing through the first contraction section is 8-12 m/s; the gas velocity in the secondary reaction chamber is 3-8m/s, and the retention time is 0.2-0.8 s; and the mixed gas generated by the secondary reaction enters the chilling chamber. This application divide into primary reaction room and secondary reaction room with the combustion chamber, sets up first shrink section in the bottom of primary reaction room, prevents that material and oxidant from escaping, and the reinforcing back mixing state improves the conversion rate of carbon, sets up the expansion section at secondary reaction room and avoids the gas reflux, increases the intensity of secondary reaction, improves the content of effective gas.
Description
Technical Field
The invention relates to the technical field of coal gasification, in particular to a gasification furnace and a gasification method thereof.
Background
At present, the coal water slurry gasification technology and the pulverized coal gasification technology are two mainstream entrained flow bed gasification technologies, wherein the coal water slurry or the pulverized coal is gasified with an oxidant to generate synthesis gas containing CO and H2, and then the synthesis gas is subjected to purification, transformation, synthesis and other processes to generate high-value-added chemicals such as methanol, ethylene glycol, urea and the like. The reactor is a core device of gasification reaction, and is commonly provided with a full mixed flow reactor and a plug flow reactor, wherein the full mixed flow reactor refers to a reactor in which media with different residence times are mixed and then react, and the plug flow reactor refers to a reactor in which the media enter and exit simultaneously and the residence times are the same.
Generally, the gasification furnace is considered as a full mixed flow reactor, and in the actual operation process, the carbon conversion rate of the gasification furnace is not ideal, because part of coal dust is not reacted in time and escapes out of a combustion chamber of the gasification furnace along with synthesis gas; the synthesis gas at the outlet of the gasification furnace also contains a small amount of oxygen, namely the oxygen also escapes; this indicates that the back-mixing effect is not good when the gasifier combustion chamber is used as a full-mixing flow reactor.
The top-mounted single-burner gasification furnaces such as the Texaco furnace, the space furnace, the Jinhua furnace and the like can be divided into a jet zone, a reflux zone and a pipe flow zone according to a zone model of a combustion chamber fluid flow process; the shell furnace, the four-burner gasifier and the like are side multi-burner gasifiers and can be divided into a jet area, an impact expansion flow area, a reflux area, a pipe flow area and other areas. The chemical reaction in the gasifier can be divided into a primary reaction and a secondary reaction, wherein the main product of the primary reaction is CO2、CH4Etc. the main products of the secondary reaction are CO and H2And the like. The reaction in the tubular flow region is mainly the secondary reaction, and the other region is mainly the primary reaction. In the existing entrained-flow gasifier technology, the composition of effective gas components is about 80-90%, the content of effective gas is low, and the generated carbon dioxide gas is about 10-20%, so that a large amount of greenhouse gas is brought to the environment.
Therefore, it is an important direction for the development of gasification technology to avoid the secondary reaction of the short-residence, unreacted coal dust and oxygen escaping from the furnace combustion chamber and the enhanced tubular flow region, thereby improving the carbon conversion rate and the available gas content.
Disclosure of Invention
In order to solve the above technical problems or at least partially solve the above technical problems, the present invention provides a gasification furnace and a gasification method thereof.
The gasification furnace comprises a primary reaction chamber, a secondary reaction chamber and a chilling chamber which are sequentially communicated from top to bottom, wherein a burner is connected onto the primary reaction chamber, a gas outlet is formed in the chilling chamber, a first contraction section is arranged at the bottom of the primary reaction chamber, the caliber of the first contraction section is gradually reduced from top to bottom, an expansion section communicated with the first contraction section is arranged at the top of the secondary reaction chamber, and the caliber of the expansion section is gradually increased from top to bottom.
Optionally, the expansion section is in a truncated cone shape, and an included angle between the inner wall of the expansion section and the center line of the secondary reaction chamber is less than or equal to 15 °.
Optionally, a second contraction section communicated with the chilling chamber is arranged at the bottom of the secondary reaction chamber, and the caliber of the second contraction section is gradually reduced from top to bottom.
Optionally, a first heat insulation layer is arranged on the inner wall of the primary reaction chamber, a second heat insulation layer is arranged on the inner wall of the secondary reaction chamber, and the first heat insulation layer and the second heat insulation layer both comprise refractory bricks or water-cooled walls.
Optionally, the periphery of the primary reaction chamber is provided with a plurality of first high-temperature thermocouples for measuring temperature, and the first high-temperature thermocouples are uniformly distributed in the middle and at the bottom of the primary reaction chamber or the first high-temperature thermocouples are uniformly distributed in the upper portion, the middle portion and at the bottom of the primary reaction chamber.
Optionally, the periphery of the secondary reaction chamber is provided with a plurality of second high-temperature thermocouples for measuring temperature, and the second high-temperature thermocouples are uniformly distributed in the middle and at the bottom of the secondary reaction chamber or the second high-temperature thermocouples are uniformly distributed in the upper portion, the middle portion and the bottom of the secondary reaction chamber.
Optionally, the ratio of the height to the diameter of the primary reaction chamber is 1.3-2.4, and the ratio of the height to the diameter of the secondary reaction chamber is 3-5.
Optionally, the diameter of the secondary reaction chamber is smaller than the diameter of the primary reaction chamber.
The application also provides a gasification method for executing the gasification furnace, which comprises the following steps:
injecting a material and an oxidant into the primary reaction chamber by a burner, wherein the flow rate of mixed gas generated by burning the material in the primary reaction chamber is 0.6-1.2m/s, and the retention time is 3-6 s;
accelerating the mixed gas and the molten slag through the first contraction section to enable the flow speed of the mixed gas passing through the first contraction section to be 8-12 m/s;
the mixed gas drives the slag to enter the expansion section for deceleration, so that the speed of the mixed gas entering the secondary reaction chamber is 3-8m/s, the retention time of the mixed gas in the secondary reaction chamber is 0.2-0.8s, and the diameter of the secondary reaction chamber is smaller than that of the primary reaction chamber;
and mixed gas generated by the secondary reaction chamber enters the chilling chamber through the second contraction section and is discharged through the gas outlet.
Optionally, the velocity of the mixed gas generated by the secondary reaction chamber flowing out through the second contraction section is 6-14 m/s.
Compared with the prior art, the technical scheme provided by the embodiment of the application has the following advantages:
this application divide into primary reaction room and secondary reaction room with the combustion chamber, sets up first shrink section in the bottom of primary reaction room, prevents that material and oxidant from escaping, and the reinforcing back mixing state improves the conversion rate of carbon, sets up the expansion section at secondary reaction room and avoids the gas reflux, increases the intensity of secondary reaction, improves the content of effective gas.
Drawings
FIG. 1 is a schematic view of a burner tip of a gasifier in one embodiment of the present invention;
FIG. 2 is a schematic view of a combustion chamber of a gasifier in one embodiment of the present invention;
FIG. 3 is a schematic diagram of the arrangement of a first high temperature thermocouple and a second high temperature thermocouple in one embodiment of the present invention;
FIG. 4 is a schematic view of a waterwall in both the first and second insulation layers in an embodiment of the present invention;
FIG. 5 is a schematic view of a burner of a gasification furnace disposed at a side of a primary reaction chamber in one embodiment of the present invention;
FIG. 6 is a schematic view of a gasification furnace with burners on its side surface, with a first high temperature thermocouple and a second high temperature thermocouple, according to an embodiment of the present invention;
FIG. 7 is a schematic view showing burners of a gasification furnace disposed on the top and side surfaces of a primary reaction chamber in one embodiment of the present invention.
Reference numerals:
1. a primary reaction chamber; 2. a secondary reaction chamber; 3. burning a nozzle; 4. a first outlet; 41. a second inlet; 5. a second outlet; 6. a quench chamber; 7. a down pipe; 8. water bath; 9. a riser pipe; 10. a gas outlet; 11. a slag outlet; 12. a first insulating layer; 13. a first constriction section; 14. an expansion section; 15. a second constriction section; 16. a first high temperature thermocouple; 17. a second high temperature thermocouple; 18. a second insulating layer.
Detailed Description
In order that the above objects, features and advantages of the present invention can be more clearly understood, the present invention will be further described in detail with reference to the accompanying drawings and examples. It is to be understood that the embodiments described are only a few embodiments of the present invention, and not all embodiments. The specific embodiments described herein are merely illustrative of the invention and are not to be construed as limiting the invention. All other embodiments, which can be derived by a person skilled in the art from the described embodiments of the invention, are within the scope of the invention.
With reference to fig. 1 to 7, the gasifier provided in the embodiment of the present application includes a primary reaction chamber 1, a secondary reaction chamber 2, and a chilling chamber 6, which are sequentially communicated from top to bottom, the primary reaction chamber 1 is connected with a burner 3, and a material and an oxidant enter the primary reaction chamber 1 through the burner 3 to be combusted. Wherein, the material comprises coal water slurry, pulverized coal or residual oil and the like, and the oxidant comprises oxygen and water vapor. The primary reaction chamber 1 mainly generates a primary reaction, specifically a combustion reaction, to generate CO2And CH4Mainly mixed gas. The burner 3 can be arranged on the top or the side of the primary reaction chamber 1 and is designed according to actual requirements. The chilling chamber 6 is provided with a gas outlet 10, and gas entering the chilling chamber 6 is cooled by the chilling chamber 6, discharged through the gas outlet 10 and enters the subsequent working procedure. The bottom of primary reaction chamber 1 is equipped with first constriction section 13, and the bore of first constriction section 13 reduces from top to bottom gradually, and the top of secondary reaction chamber 2 is equipped with the expansion section 14 with first constriction section 13 intercommunication, and the bore of expansion section 14 increases from top to bottom gradually.
This application divide into primary reaction chamber 1 and secondary reaction chamber 2 with the combustion chamber, and wherein, primary reaction chamber 1 is as the complete mixing flow reactor, and secondary reaction chamber 2 is as the plug flow reactor, sets up first contraction section 13 in primary reaction chamber 1's bottom, can prevent effectively that material and oxidant from escaping, and the reinforcing back mixing state improves the conversion ratio of carbon, sets up expansion section 14 in secondary reaction chamber and avoids the gas backward flow, increases the intensity of secondary reaction, improves the content of effective gas. Wherein, the primary reaction chamber 1 is cylindrical, and the ratio of the height to the diameter is 1.3-2.4. The secondary reaction chamber 2 is cylindrical, the ratio of the height to the diameter is 3-5, and the diameter of the secondary reaction chamber 2 is smaller than that of the primary reaction chamber 1, so that the phenomenon of back mixing in the secondary reaction chamber 2 is avoided.
The reaction temperature of the primary reaction chamber 1 is 1250-.
Further optimally, as shown in fig. 1, the expansion section 14 is in a truncated cone shape, and an included angle α between the inner wall of the expansion section 14 and the center line of the secondary reaction chamber 2 is less than or equal to 15 °, so that a backflow phenomenon is prevented, and a plug flow in the secondary reaction chamber 2 is ensured.
Referring to fig. 1 and 2, a second contraction section 15 communicated with the chilling chamber 6 is arranged at the bottom of the secondary reaction chamber 2, and the caliber of the second contraction section 15 is gradually reduced from top to bottom. For increasing the flow rate of the mixed gas entering the quench chamber 6. The chilling chamber 6 mainly comprises a down pipe 7, a water bath 8, an ascending pipe 9 and the like, wherein the bottom end of the down pipe 7 is inserted into the water bath 8, so that mixed gas and molten slag generated by the secondary reaction chamber enter the water bath 8, and the molten slag is precipitated in the water bath 8 and discharged through a slag outlet 11 arranged at the bottom of the chilling chamber 6. And the top of the ascending pipe 9 sprays chilled water for cooling the high-temperature mixed gas, wherein the chilled water is cooling water with lower temperature.
Referring to fig. 2, 4 and 7, a first heat insulation layer 12 is disposed on the inner wall of the primary reaction chamber 1, a second heat insulation layer 18 is disposed on the inner wall of the secondary reaction chamber 2, and both the first heat insulation layer 12 and the second heat insulation layer 18 include refractory bricks or water-cooled walls. In order to protect the first heat insulation layer 12 and the second heat insulation layer 18, the slag adhering to the inner walls of the primary reaction chamber 1 and the secondary reaction chamber 2 cannot be too thin, wherein the flow rate of the gas in the primary reaction chamber 1 and the secondary reaction chamber 2 should meet the flow rate requirement, and the phenomenon that the slag adhering is too thin due to too large flow rate is avoided.
In some embodiments, as shown in fig. 3 and 6 in combination, the outer circumference of the primary reaction chamber 1 is provided with a plurality of first high temperature thermocouples 16 for measuring temperature. Specifically, the first high temperature thermocouples 16 are uniformly distributed at the middle and bottom of the primary reaction chamber 1 or the first high temperature thermocouples 16 are uniformly distributed at the upper, middle and bottom of the primary reaction chamber 1. The outer circumference of the secondary reaction chamber 2 is provided with a plurality of second high temperature thermocouples 17 for measuring temperature. Specifically, the second high temperature thermocouples 17 are uniformly distributed at the middle and bottom of the secondary reaction chamber 2 or the second high temperature thermocouples 17 are uniformly distributed at the upper, middle and bottom of the secondary reaction chamber 2. The temperatures of different positions of the primary reaction chamber 1 and the secondary reaction chamber 2 can be detected by the first high temperature thermocouple 16 and the second high temperature thermocouple 17, respectively. Meanwhile, the using states of the primary reaction chamber 1 and the burner 3 can be judged according to the temperature difference of each position of the primary reaction chamber 1.
The present application also provides a gasification method of performing a gasification furnace, comprising the steps of:
step one, injecting a material and an oxidant into a primary reaction chamber 1 by a burner 3, wherein the flow velocity of the generated mixed gas in the primary reaction chamber 1 is 0.6-1.2m/s, and the retention time is 3-6 s.
Specifically, a first inlet communicated with the burner 3 is arranged on the primary reaction chamber 1, and a head is arranged at the top of the primary reaction chamber 1, and the head is preferably elliptical or semicircular. The volume and height-diameter ratio of the primary reaction chamber 1 are matched with the spraying range and angle of the burner 3, and the requirements of the retention time of the gas in the primary reaction chamber 1 and the gas flow rate are met. The residence time is too short and the reaction is incomplete; the retention time is too long, the volume of the gasification furnace is increased, and the manufacturing cost of the equipment is high. Therefore, the volume of the primary reaction chamber 1 is defined by the aspect ratio of the primary reaction chamber 1 and the flow rate and residence time of the gas in the primary reaction chamber 1, and the reaction in the primary reaction chamber 1 at the volume is more sufficient.
When the height of the primary reaction chamber 1 is too low, the coal dust and the oxidant which do not react in time can easily escape out of the primary reaction chamber 1; when the height of the gasification furnace is too high, the diameter of the gasification furnace is too small and the gas flow rate is too large under the condition of the same volume. In addition, the diameter size of the gasification furnace determines the size of the reflux zone and the amount of reflux to a certain extent, and in order to meet the requirement, the ratio of the height to the diameter of the primary reaction chamber 1 is 1.3-2.4. The primary reaction chamber 1 with the volume and the high warp ratio can prevent the coal dust and the oxidant from escaping from the primary reaction chamber 1, enhance the back mixing state, fully react and improve the conversion rate of carbon.
And step two, accelerating the mixed gas generated by the material and the oxidant and the molten slag through the first contraction section 13, so that the flow speed of the mixed gas passing through the first contraction section 13 is 8-12 m/s.
Specifically, the first outlet 4 is provided at the bottom of the first constriction section 13, the size of the first outlet 4 is determined according to the flow rate of the mixed gas generated by the reaction in the primary reaction chamber 1, and the flow rate of the gas is increased by the first constriction section 13. The smaller the first outlet 4 of the primary reaction chamber 1 is, the more beneficial the situation that the coal powder and the oxidant which are not reacted in time are prevented from escaping out of the primary reaction chamber 1 is; however, the first outlet 4 is too small, and the gas flow rate will be larger under the same load, which results in the first outlet 4 being seriously washed and reducing the service life of the equipment. In general, the optimal velocity of the mixed gas flowing out through the first outlet 4 is 8-12m/s, so the first outlet 4 is designed to meet the requirement, the coal powder and the oxidant are ensured to be fully reacted, and the carbon conversion rate is improved.
And step three, the mixed gas drives the slag to enter the expansion section 14 for speed reduction, so that the speed of the mixed gas entering the secondary reaction chamber 2 is 3-8m/s, the retention time of the mixed gas in the secondary reaction chamber 2 is 0.2-0.8s, and the diameter of the secondary reaction chamber 2 is smaller than that of the primary reaction chamber 1.
Specifically, the top end of the expanding section 14 is provided with a second inlet 41 communicated with the first outlet 4 of the first contracting section 13, the mixed gas and the molten slag generated by the primary reaction chamber 1 further enter the secondary reaction chamber 2, and the flow rate of the gas entering the secondary reaction chamber 2 can be increased by arranging the expanding section 14.
The volume and height/diameter ratio of the secondary reaction chamber 2 are determined by the residence time of the gas in the secondary reaction chamber 2. The residence time is too short and the reaction is incomplete; too long retention time, increased volume of the gasification furnace and equipmentThe manufacturing cost is high. The residence time requirement of the mixed gas in the secondary reaction chamber 2 is 0.2-0.8 seconds, the flow rate of the mixed gas entering the secondary reaction chamber 2 through the expansion section 14 is 3-8m/s, the reaction in the secondary reaction chamber 2 is more sufficient under the condition, and therefore, the volume of the secondary reaction chamber 2 can meet the design requirement. And in order to prevent the material from generating backflow in the secondary reaction chamber 2 and forming a back mixing phenomenon, the diameter of the secondary reaction chamber 2 is required not to be too large, and specifically, the ratio of the height to the diameter of the secondary reaction chamber is 3-5. The secondary reaction chamber 2 with the volume and the high warp ratio can effectively avoid the back mixing phenomenon, increase the reaction strength and improve the content of effective gas. Wherein, the reaction in the secondary reaction chamber 2 mainly takes place the secondary reaction, mainly the carbohydrate reaction, the inverse transformation, the methane conversion and the like, and the generated mixed gas comprises CO and H2And the like.
Step four, the mixed gas generated in the secondary reaction chamber 2 enters the chilling chamber 6 through the second contraction section 15 and is discharged through the gas outlet 10.
Specifically, the bottom of the secondary reaction chamber 2 is provided with a second outlet 5 communicated with a chilling chamber 6, and mixed gas and molten slag generated through secondary reaction enter the chilling chamber 6 from the second outlet 5. Further optimally, the size of the second outlet 5 of the secondary reaction chamber 2 is determined by the gas flow rate. In order to ensure that the high-temperature gas of the second outlet 5 can be fully mixed with the chilling water in the chilling chamber 6 and exchange heat, the gas flow rate needs to be within a reasonable range. The gas flow velocity is too high, the contact time of high-temperature gas and chilling water is too short, and the gas temperature is higher after heat exchange; the gas flow rate is too low, and molten slag carried by gas is easy to cool into large solid slag, which is not favorable for the stable operation of the system.
Therefore, the second contraction section 15 communicated with the chilling chamber 6 is arranged at the bottom of the secondary reaction chamber 2, and the flow rate of the gas passing through the second outlet 5 is increased by arranging the second contraction section 15, so that the flow rate of the mixed gas flowing out through the second contraction section 15 is 6-14m/s, and the design size of the second outlet 5 is required to meet the flow rate requirement.
Adopt split type design with the combustion chamber, use in different kinds of gasifiers and carry out the experiment, specific service conditions are as follows:
the first embodiment is as follows:
the method is applied to a top-placed single-burner 3 gasification furnace, and is combined with the drawings of fig. 1, fig. 2 and fig. 3, the coal feeding amount (dry basis) is designed to be 1000t/d, the pressure is 4.0MPa, and the first heat-insulating layer 12 is made of refractory bricks. The top of the gasification furnace is provided with a three-channel burner 3, and channels (from inside to outside) of the burner 3 are respectively central oxygen, coal water slurry and annular space oxygen, wherein the central oxygen accounts for about 20 percent of the total oxygen. The primary reaction chamber 1 is a full mixing flow reactor, and the height H of the primary reaction chamber 11Is 4m and has a diameter phi12.134m, height to diameter ratio of 1.87 and volume of 15m3. The secondary reaction chamber 2 is a plug flow reactor with a height H2Is 3m and has a diameter phi20.91m, height to diameter ratio of 3.29, alpha of 15 DEG, and volume of 2.4m3。
As shown in fig. 3, eight first high temperature thermocouples 16 are arranged on the periphery of the primary reaction chamber 1, every four first high temperature thermocouples 16 are on the same plane, and a pair of first high temperature thermocouples 16 on the upper and lower planes are on the same vertical plane; the angle of two adjacent first high-temperature thermocouples 16 in the same plane is 90 degrees; the upper four first high temperature thermocouples 16 at 1/2 of the primary reaction chamber 1 have a temperature of about 1300 c, which is an operation reference temperature of the gasification furnace and is required to be about 50 c higher than the ash melting point temperature (T3) of coal; the lower four first high temperature thermocouples 16 are at the bottom end of the straight cylinder of the primary reaction chamber 1 and have a temperature relatively higher than that of the upper four first high temperature thermocouples 16 by 50-100 deg.
The condition of the burner 3 can be judged by eight first high-temperature thermocouples 16. If the temperature of the upper four first high-temperature thermocouples 16 is normal, the temperature of the lower four first high-temperature thermocouples 16 is basically the same as or lower than that of the upper four first high-temperature thermocouples 16, which indicates that the speed at the outlet of the burner 3 is too high. And under the condition of stabilizing the furnace temperature, properly reducing the flow of the coal water slurry or the oxygen. If the temperatures of the lower four first high-temperature thermocouples 16 are normal, the temperatures of the upper four first high-temperature thermocouples 16 are basically the same as or lower than the temperatures of the lower four first high-temperature thermocouples 16, which indicates that the flow rate at the outlet of the burner 3 is too low, possibly due to the wear of the head of the burner 3. If the temperatures of the upper and lower pairs or two pairs of first high-temperature thermocouples 16 on the same vertical plane are abnormal at the same time, the burner 3 is indicated to have a bias flow phenomenon, and the vehicle should be stopped in time.
As shown in fig. 3, three second high temperature thermocouples 17 are disposed on the outer periphery of the secondary reaction chamber 2 and located at the upper, middle and lower parts of the secondary reactor, respectively, the temperatures of the three second high temperature thermocouples 17 decrease from top to bottom, and the second heat insulating layer 18 is made of refractory bricks. Compared with a single-burner 3 gasification furnace with the same grade, the gasification furnace with the design mode has the advantages that the volume is reduced by about 28 percent, the carbon conversion rate is improved by 2 percent, and the effective gas content is improved by 12 percent.
Example two:
the method is applied to a top-placed single-burner 3 gasification furnace, as shown in figure 4, the coal feeding amount (dry basis) is 1500t/d, the pressure is 4.0MPa, and the first heat-insulating layer 12 adopts a water-cooled wall; the top is provided with two channels of burners 3, and the channels (from inside to outside) of the burners 3 are respectively oxygen and pulverized coal. The primary reaction chamber 1 is a full mixing flow reactor with a height H1Is 4m and has a diameter phi12.7m, height to diameter ratio of 1.48, and volume of 25m3. The secondary reaction chamber 2 is a plug flow reactor with a height H2Is 3.5m and has a diameter phi20.96m, height-to-diameter ratio of 3.64, alpha of 15 DEG, and volume of 3m3The second heat-insulating layer 18 is a water-cooled wall.
The primary reaction chamber 1 is provided with eight first high-temperature thermocouples 16, every four first high-temperature thermocouples 16 are on the same plane, and a pair of first high-temperature thermocouples 16 on the upper plane and the lower plane are on the same vertical plane; the angle of two adjacent first high-temperature thermocouples 16 in the same plane is 90 degrees; the upper four first high temperature thermocouples 16 are at 1/2 of the primary reaction chamber 1 and the lower four first high temperature thermocouples 16 are at the bottom end of the straight cylinder of the primary reaction chamber 1. The secondary reaction chamber 2 is provided with three second high-temperature thermocouples 17 which are respectively positioned at the upper part, the middle part and the lower part, and the temperatures of the three second high-temperature thermocouples 17 are sequentially reduced from top to bottom. Compared with a single-burner 3 gasification furnace with the same grade, the gasification furnace with the design mode has the advantages that the volume is reduced by about 21 percent, the carbon conversion rate is improved by 1.5 percent, and the effective gas content is improved by 5 percent.
Example three:
the method is applied to a lateral multi-burner 3 gasification furnace, and is combined with the graph shown in fig. 5 and fig. 6, the coal feeding amount (dry basis) is 1500t/d, the pressure is 6.5MPa, and the first heat-insulating layer 12 is made of refractory bricks; the side part is provided with four three-channel burners 3, and the channels (from inside to outside) of the burners 3 are respectively central oxygen, coal water slurry and annular space oxygen, wherein the central oxygen accounts for about 18 percent of the total oxygen. The primary reaction chamber 1 is a full mixed flow reactor with high H1Is 5m, phi12.4m, height-to-diameter ratio of 2.08 and volume of 24m3(ii) a The secondary reaction chamber 2 is a plug flow reactor, the second heat-insulating layer 18 is made of refractory bricks, and the high H of the secondary reaction chamber 22Is 3.5m and has a diameter phi20.96m, height-to-diameter ratio of 3.64, alpha of 15 DEG, and volume of 3m3。
As shown in fig. 6, nine first high temperature thermocouples 16 are arranged on the periphery of the primary reaction chamber 1, every three first high temperature thermocouples 16 are on the same plane, and the first high temperature thermocouples 16 on the upper, middle and lower planes are in one-to-one correspondence in the vertical direction; the angle between two adjacent first high-temperature thermocouples 16 in the same plane is 120 degrees; the upper three first high-temperature thermocouples 16 are positioned at the top of the primary reaction chamber 1 and are positioned at the upper parts of the four burners 3; the middle three first high-temperature thermocouples 16 are positioned in the middle of the primary reaction chamber 1 and positioned at the lower parts of the four burners 3; the lower three first high temperature thermocouples 16 are at the bottom of the primary reaction chamber 1. Similarly, the conditions of the primary reaction chamber 1 and the burner 3 can be judged by the middle and lower six first high-temperature thermocouples 16.
If the temperatures of the three first high-temperature thermocouples 16 in the middle part are normal, the temperatures of the three first high-temperature thermocouples 16 in the lower part are the same as or lower than the temperatures of the three first high-temperature thermocouples 16 in the middle part, which indicates that the speed at the outlet of the burner 3 is too high, and the flow of the coal water slurry or the oxygen is properly reduced under the condition of stabilizing the furnace temperature; if the temperatures of the lower three first high-temperature thermocouples 16 are normal, the temperatures of the middle three first high-temperature thermocouples 16 are basically the same as or lower than the temperatures of the lower three first high-temperature thermocouples 16, which indicates that the flow rate at the outlet of the burner 3 is too low, possibly because the head of the burner 3 is worn; if the temperatures of the middle and next pairs of first high-temperature thermocouples 16 on the same vertical plane are abnormal at the same time, the burner 3 is indicated to have a bias flow phenomenon, and the vehicle should be stopped in time.
Since the upper three first high temperature thermocouples 16 are in the complicated impingement expansion flow and recirculation zones, the temperature variation is large and only used as an observation furnace temperature. The secondary reaction chamber 2 is provided with three second high-temperature thermocouples 17 which are respectively positioned at the upper part, the middle part and the lower part, and the temperatures of the three second high-temperature thermocouples 17 are sequentially reduced from top to bottom. Compared with a four-burner 3 gasification furnace with the same grade, the gasification furnace with the design mode has the advantages that the volume is reduced by about 33%, the carbon conversion rate is improved by 1.5%, and the effective gas content is improved by 11%.
Example four:
the method is applied to a top/side multi-burner 3 gasification furnace, and the coal feeding amount (dry basis) is 1500t/d, the pressure is 4.0MPa, wherein the pulverized coal is 500t/d, and the coal water slurry is 1000 t/d; the top of the burner is a pulverized coal burner 3, the burner 3 adopts a two-channel structure, and oxygen and pulverized coal are respectively arranged from inside to outside; the side parts of the four coal water slurry burners 3 are provided with three channel structures, the burners 3 are respectively provided with central oxygen, coal water slurry and annular space oxygen from inside to outside, wherein the central oxygen accounts for about 18 percent of the total oxygen.
As shown in fig. 7, the primary reaction chamber 1 is a total mixing flow reactor, and the first heat-insulating layer 12 is made of refractory bricks; high H1Is 5m and has a diameter phi12.4m, height-to-diameter ratio of 2.08 and volume of 24m3. The secondary reaction chamber 2 is a plug flow reactor, the second heat insulation layer 18 adopts a water-cooled wall, endothermic reaction is mainly carried out in the plug flow reactor, and the higher the temperature is, the more favorable the reaction is carried out in the positive direction; the temperature of the secondary reaction chamber 2 can be more effectively adjusted by adjusting the flow rate or the outlet temperature of the water in the water-cooling wall. Height H of the secondary reaction chamber 22Is 3.5m, phi20.96m, height-to-diameter ratio of 3.64, alpha of 15 DEG, and volume of 3m3。
Nine first high-temperature thermocouples 16 are arranged on the periphery of the primary reaction chamber 1, every three first high-temperature thermocouples 16 are on the same plane, and the first high-temperature thermocouples 16 on the upper plane, the middle plane and the lower plane are in one-to-one correspondence in the vertical direction; the angle of two adjacent first high-temperature thermocouples 16 in the same plane is 120 degrees; the upper three first high-temperature thermocouples 16 are positioned at the top of the primary reaction chamber 1 and are positioned at the upper parts of the four burners 3; the middle three first high-temperature thermocouples 16 are positioned in the middle of the primary reaction chamber 1 and positioned at the lower parts of the four burners 3; the lower three first high temperature thermocouples 16 are at the bottom of the primary reaction chamber 1. The secondary reaction chamber 2 is provided with three second high-temperature thermocouples 17 which are respectively positioned at an upper part, a middle part and a lower part, and the temperatures of the three second high-temperature thermocouples 17 are sequentially reduced from top to bottom. Compared with a top/side multi-burner 3 gasification furnace with the same grade, the gasification furnace with the design mode has the advantages that the volume is reduced by about 27%, the carbon conversion rate is improved by 1.5%, and the effective gas content is improved by 9%.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention, but not to limit it; although the present invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some technical features may be equivalently replaced; and such modifications or substitutions do not depart from the spirit and scope of the corresponding technical solutions of the embodiments of the present invention.
Claims (6)
1. The gasification method of the gasification furnace is characterized in that the gasification furnace comprises a primary reaction chamber, a secondary reaction chamber and a chilling chamber which are sequentially communicated from top to bottom, a burner is connected onto the primary reaction chamber, a gas outlet is arranged on the chilling chamber, a first contraction section is arranged at the bottom of the primary reaction chamber, the caliber of the first contraction section is gradually reduced from top to bottom, an expansion section communicated with the first contraction section is arranged at the top of the secondary reaction chamber, the caliber of the expansion section is gradually increased from top to bottom,
the expansion section is in a truncated cone shape, and the included angle between the inner wall of the expansion section and the central line of the secondary reaction chamber is less than or equal to 15 degrees;
the ratio of the height to the diameter of the primary reaction chamber is 1.3-2.4, so that the flow velocity of the mixed gas generated in the primary reaction chamber is 0.6-1.2m/s, the residence time is 3-6s, the flow velocity of the mixed gas passing through the first contraction section is 8-12m/s, the ratio of the height to the diameter of the secondary reaction chamber is 3-5, the speed of the mixed gas entering the secondary reaction chamber is 3-8m/s, and the residence time of the mixed gas in the secondary reaction chamber is 0.2-0.8 s;
the diameter of the secondary reaction chamber is smaller than that of the primary reaction chamber;
the reaction temperature in the secondary reaction chamber is lower than that in the primary reaction chamber;
the gasification method of the gasification furnace comprises the following steps:
injecting a material and an oxidant into the primary reaction chamber by a burner, wherein the flow rate of mixed gas generated by burning the material in the primary reaction chamber is 0.6-1.2m/s, and the retention time is 3-6 s;
accelerating the mixed gas and the molten slag through the first contraction section to enable the flow speed of the mixed gas passing through the first contraction section to be 8-12 m/s;
the mixed gas drives the slag to enter the expansion section for deceleration, so that the speed of the mixed gas entering the secondary reaction chamber is 3-8m/s, and the retention time of the mixed gas in the secondary reaction chamber is 0.2-0.8 s;
and mixed gas generated by the secondary reaction chamber enters the chilling chamber through the second contraction section and is discharged through the gas outlet.
2. The gasification method of a gasification furnace according to claim 1, wherein a second contraction section is provided at the bottom of the secondary reaction chamber and communicates with the quench chamber, and the diameter of the second contraction section is gradually reduced from top to bottom.
3. The gasification method of a gasification furnace according to claim 1, wherein a first heat insulating layer is provided on an inner wall of the primary reaction chamber, a second heat insulating layer is provided on an inner wall of the secondary reaction chamber, and each of the first heat insulating layer and the second heat insulating layer comprises a refractory brick or a water-cooled wall.
4. The gasification method of a gasification furnace according to claim 1, wherein a plurality of first high temperature thermocouples for measuring temperature are provided at the periphery of the primary reaction chamber, and the first high temperature thermocouples are uniformly distributed at the middle and bottom of the primary reaction chamber or the first high temperature thermocouples are uniformly distributed at the upper, middle and bottom of the primary reaction chamber.
5. The gasification method of a gasification furnace according to claim 1, wherein a plurality of second high temperature thermocouples for measuring temperature are provided at the outer periphery of the secondary reaction chamber, and the second high temperature thermocouples are uniformly distributed at the middle and bottom of the secondary reaction chamber or the second high temperature thermocouples are uniformly distributed at the upper, middle and bottom of the secondary reaction chamber.
6. The gasification method of a gasification furnace according to claim 1, wherein the mixed gas generated in the secondary reaction chamber flows out through the second constriction section at a velocity of 6 to 14 m/s.
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