CN216998304U - Fine coal hydrogenation grading gasification furnace - Google Patents
Fine coal hydrogenation grading gasification furnace Download PDFInfo
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- CN216998304U CN216998304U CN202220407258.3U CN202220407258U CN216998304U CN 216998304 U CN216998304 U CN 216998304U CN 202220407258 U CN202220407258 U CN 202220407258U CN 216998304 U CN216998304 U CN 216998304U
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Abstract
The utility model discloses a pulverized coal hydrogenation graded gasification furnace, which comprises a furnace body, wherein the interior of the furnace body is sequentially divided into a first reaction chamber, a chilling regulation chamber, a second reaction chamber and a semicoke cooling chamber from top to bottom; a pulverized coal nozzle, a first hydrogen nozzle and a first oxygen nozzle are arranged at the top of the first reaction chamber; at least one coal powder spray nozzle is arranged on the side wall of the chilling regulation and control chamber; a synthetic gas outlet is arranged on the side wall of the chilling control chamber above the pulverized coal spray nozzle; at least one second hydrogen nozzle and at least one second oxygen nozzle are arranged on the side wall of the second reaction chamber; the bottom of the semicoke cooling chamber is provided with a slag discharge port. The utility model has the advantages that the structure is simple, the implementation is easy, the continuous cracking reaction of the aromatic hydrocarbon oil product can be rapidly cut off, the yield of the whole oil product is improved, the influence on the carbon conversion rate of coal can be avoided, and the whole economy and operability are improved; obtaining effective synthesis gas and simultaneously improving the carbon conversion rate of the coal powder.
Description
The technical field is as follows:
the utility model relates to a gasification furnace, in particular to a pulverized coal hydrogenation graded gasification furnace.
Background art:
the top of the existing gasification furnace is provided with a combined nozzle, high-temperature and high-pressure hydrogen, oxygen and coal powder simultaneously enter the gasification furnace through the nozzle, firstly the high-temperature hydrogen and the oxygen generate oxygen-poor combustion reaction to obtain higher-temperature hydrogen with the temperature of more than 1000 ℃, then the hydrogen and the coal powder contact and then coal hydrogenation pyrolysis reaction (namely hydrogenation gasification) occurs, and the hydrogenation gasification refers to a process that carbon-containing compounds and the hydrogen react under the conditions of medium temperature (700 plus one of 1000 ℃) and high pressure (5-10MPa) to generate crude gas rich in methane, high value-added aromatic hydrocarbon oil and high-heat value semicoke. The existing gasification furnace is designed with a reaction section, semicoke and synthesis gas produced after reaction in the reaction section downwards enter a semicoke collection section of the gasification furnace to carry out gas-solid separation, the produced synthesis gas is discharged out of the gasification furnace from the middle upper part of the gasification furnace, firstly passes through a cyclone separator, the synthesis gas after preliminary purification is subjected to heat energy recovery through a waste heat boiler, and the low-temperature synthesis gas after heat energy recovery enters a crude gas filter to be purified again and then is sent to an oil product recovery section. High-temperature semicoke produced by the gasification furnace enters the semicoke cooler for cooling through a coke discharge pipe at the bottom of the gasification furnace under the action of gravity, and the cooled semicoke is depressurized through a semicoke locking hopper system and then is delivered.
As the main products of the hydro-gasification are methane and aromatic oil products, the main products and the auxiliary products can be preferentially selected according to factors such as market price, cost and the like, and the best benefit is created for enterprises. However, since the hydro-gasification is in a hydrogen-rich environment, the synthetic gas rich in the aromatic hydrocarbon oil product produced in the reaction section of the gasification furnace is in a high-temperature state during the transportation process, so the aromatic hydrocarbon oil product in the synthetic gas can continuously generate chain scission reaction with hydrogen at high temperature, thereby reducing the yield of the oil product. If the continuous cracking reaction of the aromatic oil is to be cut off quickly, the chilling operation is required to be carried out quickly, and the temperature of the aromatic oil is reduced to below 750 ℃. At present, the rapid chilling operation is mainly to rapidly cool by using chilling gas, wherein the chilling gas is purified gas from a methanol synthesis device, if the rapid cooling needs to consume a large amount of purified gas, meanwhile, the carbon conversion rate of coal in a gasification furnace is influenced to a certain extent after the cooling, and the overall economy and operability are reduced.
The utility model has the following contents:
the utility model aims to provide a pulverized coal hydrogenation graded gasification furnace which is simple in structure and can improve the overall oil yield.
The utility model is implemented by the following technical scheme: a pulverized coal hydrogenation graded gasification furnace comprises a furnace body, wherein the interior of the furnace body is sequentially divided into a first reaction chamber, a chilling regulation chamber, a second reaction chamber and a semicoke cooling chamber from top to bottom; a pulverized coal nozzle, a first hydrogen nozzle and a first oxygen nozzle are arranged at the top of the first reaction chamber; at least one coal powder spray nozzle is arranged on the side wall of the chilling regulation chamber; a synthetic gas outlet is formed in the side wall of the chilling control chamber above the pulverized coal spray nozzle; at least one second hydrogen nozzle and at least one second oxygen nozzle are arranged on the side wall of the second reaction chamber; and a slag discharge port is arranged at the bottom of the semicoke cooling chamber.
Furthermore, a funnel-shaped material guide plate is fixedly arranged at the lower part of the first reaction chamber; the pulverized coal nozzle is positioned on the outer side of the material guide plate.
Further, the inner diameter of the second reaction chamber is smaller than the inner diameters of the chilling control chamber and the semicoke cooling chamber.
Furthermore, a water-cooled wall is wrapped outside the semicoke cooling chamber, a water inlet of the water-cooled wall is communicated with a water outlet of the steam drum, and a water outlet of the water-cooled wall is communicated with a water inlet of the steam drum.
The utility model has the advantages that: 1. the utility model has simple structure and easy realization, and can rapidly cut off the continuous cracking reaction of the aromatic hydrocarbon oil product by arranging the chilling regulation chamber and then introducing the coal powder into the chilling regulation chamber to chill the synthetic gas so as to improve the yield of the whole oil product, avoid the influence on the carbon conversion rate of the coal and improve the whole economy and operability; 2. through setting up the second reaction chamber can be effectual to quench the buggy and the semicoke that do not react completely in the regulation and control room and carry out comprehensive gasification reaction, further obtain effectual synthetic gas, promote the carbon conversion rate of buggy simultaneously.
Description of the drawings:
in order to more clearly illustrate the embodiments of the present invention or the technical solutions in the prior art, the drawings used in the description of the embodiments or the prior art will be briefly described below, it is obvious that the drawings in the following description are only some embodiments of the present invention, and for those skilled in the art, other drawings can be obtained according to the drawings without creative efforts.
Fig. 1 is a schematic view of the overall structure of the present invention.
The device comprises a furnace body 1, a first reaction chamber 11, a chilling regulation and control chamber 12, a synthetic gas outlet 121, a second reaction chamber 13, a semicoke cooling chamber 14, a slag discharge port 141, a coal powder nozzle 2, a first hydrogen nozzle 3, a first oxygen nozzle 4, a coal powder spray nozzle 5, a second hydrogen nozzle 6, a second oxygen nozzle 7, a material guide plate 8, a water-cooled wall 9 and a steam pocket 10.
The specific implementation mode is as follows:
as shown in figure 1, the pulverized coal hydrogenation graded gasification furnace comprises a furnace body 1, wherein the interior of the furnace body 1 is sequentially divided into a first reaction chamber 11, a chilling regulation chamber 12, a second reaction chamber 13 and a semicoke cooling chamber 14 from top to bottom; a pulverized coal nozzle 2, a first hydrogen nozzle 3 and a first oxygen nozzle 4 are arranged at the top of the first reaction chamber 11; two pulverized coal nozzles 5 are arranged on the side wall of the chilling regulation and control chamber 12; a synthetic gas outlet 121 is arranged on the side wall of the chilling regulation and control chamber 12 above the pulverized coal nozzle 5; two second hydrogen nozzles 6 and two second oxygen nozzles 7 are arranged on the side wall of the second reaction chamber 13; a slag discharge port 141 is provided at the bottom of the semicoke cooling chamber 14.
A funnel-shaped material guide plate 8 is fixedly arranged at the lower part of the first reaction chamber 11; the pulverized coal nozzle 5 is positioned at the outer side of the material guide plate 8; the inner diameter of the second reaction chamber 13 is smaller than the inner diameters of the chilling regulation chamber 12 and the semicoke cooling chamber 14, so that the descending synthesis gas, the semicoke and the coal powder are favorable for gas-solid separation, and the synthesis gas can better extend from the inner wall of the furnace body 1 to the synthesis gas outlet 121; the method is beneficial to the concentration of semicoke/coal dust, and can generate more effective impact with high-temperature hydrogen, so that the reaction is more sufficient, and the carbon conversion rate is improved; the inner diameter of the semicoke cooling chamber 14 is enlarged for the purpose of fully heat exchange of the semicoke, so that the effective heat exchange area is increased, and heat energy recovery is carried out; the outer side of the semicoke cooling chamber 14 is wrapped with a water-cooled wall 9, the water inlet of the water-cooled wall 9 is communicated with the water outlet of the steam drum 10, and the water outlet of the water-cooled wall 9 is communicated with the water inlet of the steam drum 10.
The working principle is as follows: high-temperature and high-pressure hydrogen, oxygen and coal powder simultaneously enter a first reaction chamber 11 in a furnace body 1 through a first hydrogen nozzle 3, a first oxygen nozzle 4 and a coal powder nozzle 2, the high-temperature hydrogen and the oxygen are subjected to oxygen-deficient combustion reaction to obtain higher-temperature hydrogen with the temperature of more than 1000 ℃, and the hydrogen pyrolysis reaction of the coal is carried out after the first reaction chamber 11 is contacted with the coal powder. The produced synthesis gas and the semicoke move downwards to a chilling regulation chamber 12 for chilling, the coal powder sprayed by a coal powder spray nozzle 5 in the chilling regulation chamber 12 is used as a cooling medium, and when the coal powder is contacted with the high-temperature synthesis gas and the semicoke, partial cracking reaction can be carried out on the coal powder, so that the effective components of the product are improved.
The incompletely reacted coal dust and semicoke enter the second reaction chamber 13 under the self weight, high-temperature hydrogen gas and oxygen gas which are discharged from the second hydrogen nozzle 6 and the second oxygen nozzle 7 of the second reaction chamber 13 are subjected to oxygen-deficient combustion reaction to obtain higher-temperature hydrogen gas with the temperature of more than 1000 ℃, the hydrogen gas is reacted with the coal dust in the second reaction chamber 13 to perform comprehensive gasification reaction, effective synthetic gas is further obtained, the carbon conversion rate of the coal dust is improved, the produced synthetic gas ascends to the chilling regulation chamber 12 to be chilled and cooled, and the synthetic gas is mixed with the synthetic gas from the first reaction chamber 11, discharged from the synthetic gas outlet 121 and enters a subsequent oil recovery unit. The synthesis gas in the first reaction chamber 11 and the synthesis gas in the second reaction chamber 13 are chilled in the chilling regulation chamber 12, so that the continuous cracking reaction of the aromatic oil product can be rapidly cut off, the yield of the whole oil product is improved, the influence on the carbon conversion rate of coal can be avoided, and the whole economy and operability are improved.
The semicoke which is completely reacted in the second reaction chamber 13 enters the semicoke cooling chamber 14 to exchange heat with cooling water in the water-cooled wall 9, the cooled semicoke is discharged from the slag discharge port 141, steam and water after heat exchange enter the steam drum 10 to be subjected to steam-water separation, steam is discharged, and water is continuously used; the utility model has simple structure and easy realization.
The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the utility model, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.
Claims (4)
1. A pulverized coal hydrogenation graded gasification furnace is characterized by comprising a furnace body, wherein the interior of the furnace body is sequentially divided into a first reaction chamber, a chilling regulation chamber, a second reaction chamber and a semicoke cooling chamber from top to bottom; a pulverized coal nozzle, a first hydrogen nozzle and a first oxygen nozzle are arranged at the top of the first reaction chamber; at least one coal powder spray nozzle is arranged on the side wall of the chilling regulation chamber; a synthetic gas outlet is formed in the side wall of the chilling control chamber above the pulverized coal spray nozzle; at least one second hydrogen nozzle and at least one second oxygen nozzle are arranged on the side wall of the second reaction chamber; and a slag discharge port is arranged at the bottom of the semicoke cooling chamber.
2. The pulverized coal hydrogenation graded gasifier as claimed in claim 1, wherein a funnel-shaped material guide plate is fixedly arranged at the lower part of the first reaction chamber; the pulverized coal nozzle is positioned on the outer side of the material guide plate.
3. The pulverized coal hydrogenation graded gasification furnace according to claim 1, wherein the inner diameter of the second reaction chamber is smaller than the inner diameters of the quench control chamber and the semicoke cooling chamber.
4. The pulverized coal hydrogenation graded gasification furnace as claimed in claim 1, wherein a water-cooled wall is wrapped outside the semicoke cooling chamber, a water inlet of the water-cooled wall is communicated with a water outlet of the steam drum, and a water outlet of the water-cooled wall is communicated with a water inlet of the steam drum.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220407258.3U CN216998304U (en) | 2022-02-25 | 2022-02-25 | Fine coal hydrogenation grading gasification furnace |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202220407258.3U CN216998304U (en) | 2022-02-25 | 2022-02-25 | Fine coal hydrogenation grading gasification furnace |
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| Publication Number | Publication Date |
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| CN216998304U true CN216998304U (en) | 2022-07-19 |
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| CN202220407258.3U Active CN216998304U (en) | 2022-02-25 | 2022-02-25 | Fine coal hydrogenation grading gasification furnace |
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- 2022-02-25 CN CN202220407258.3U patent/CN216998304U/en active Active
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