CN215924866U - Reaction separation integrated gasification furnace - Google Patents
Reaction separation integrated gasification furnace Download PDFInfo
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- CN215924866U CN215924866U CN202121799098.3U CN202121799098U CN215924866U CN 215924866 U CN215924866 U CN 215924866U CN 202121799098 U CN202121799098 U CN 202121799098U CN 215924866 U CN215924866 U CN 215924866U
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Abstract
The utility model discloses a reaction and separation integrated gasification furnace, belonging to coal gasification equipment, aiming at solving the technical problems of simultaneously finishing gasification reaction and temperature reduction and dust removal of coal gas in the gasification furnace, preventing the blockage of a synthesis gas pipeline and reducing the construction and maintenance cost of the equipment, and adopting the technical scheme that: the gasification furnace comprises a furnace shell, wherein a reaction chamber is arranged at the position, close to the upper part, in the middle of the furnace shell, and a chilling chamber is arranged at the position, close to the lower part, in the middle of the furnace shell; the upper end of the reaction chamber is provided with a burner, the lower end of the reaction chamber is provided with a slag hole, a down pipe is arranged below the slag hole, the upper part of the down pipe is provided with a chilling ring, and the lower part of the down pipe is provided with a cooling water atomizer; the outer part of the down pipe is sleeved with a gas collecting pipe, an expansion pipe is arranged below the gas collecting pipe, and the expansion pipe is positioned above the chilling chamber; and a Venturi tube is arranged at one side of the expansion tube and communicated with the expansion tube.
Description
Technical Field
The utility model relates to coal gasification equipment, in particular to a reaction and separation integrated gasification furnace.
Background
At present, a pressurized gasification device generally comprises a gasification furnace and a gas washing device, wherein the gasification furnace is a device for performing gasification reaction between coal and an oxidant and performing primary washing and temperature reduction on the coal gas, and the gas washing device is used for further removing coal ash in the coal gas to obtain clean synthesis gas. Because the gasification furnace and the gas washing device are connected through a pipeline in the prior art, the synthesis gas containing coal ash can be slowly attached to the pipe wall in the process of conveying the synthesis gas pipeline between the gasification furnace and the gas washing device, the problems of dust accumulation and resistance increase of the pipeline exist after long-term operation, and the gasification furnace can be forced to stop in severe cases. In addition, due to the arrangement of the independent gas washing device, the construction cost and the maintenance difficulty of the device are increased.
Therefore, how to simultaneously complete gasification reaction and temperature reduction and dust removal of coal gas in a gasification furnace, prevent the blockage of a synthesis gas pipeline and reduce the equipment construction and maintenance cost is a problem to be solved urgently at present.
Disclosure of Invention
The technical task of the utility model is to provide a reaction and separation integrated gasification furnace, which solves the problems of simultaneously completing gasification reaction and temperature reduction and dust removal of coal gas in the gasification furnace, preventing the blockage of a synthesis gas pipeline and reducing the equipment construction and maintenance cost.
The technical task of the utility model is realized in the following way, the reaction and separation integrated gasification furnace comprises a furnace shell, wherein a reaction chamber is arranged at the upper position of the middle part in the furnace shell, and a chilling chamber is arranged at the lower position of the middle part in the furnace shell;
the upper end of the reaction chamber is provided with a burner, the lower end of the reaction chamber is provided with a slag hole, a down pipe is arranged below the slag hole, the upper part of the down pipe is provided with a chilling ring, and the lower part of the down pipe is provided with a cooling water atomizer; the outer part of the down pipe is sleeved with a gas collecting pipe, an expansion pipe is arranged below the gas collecting pipe, and the expansion pipe is positioned above the chilling chamber; and a Venturi tube is arranged at one side of the expansion tube and communicated with the expansion tube.
Preferably, an annular gap is arranged between the downcomer and the chilling ring, the width of the annular gap is 5-10mm, and uniform distribution of water films of the downcomer is guaranteed.
Preferably, the cooling water atomizer comprises an inner ring and an outer ring, a plurality of inner spray holes are uniformly distributed on the inner ring, a plurality of outer spray holes are uniformly distributed on the outer ring, and the outer spray holes and the inner spray holes are concentrically arranged.
Preferably, the inner spray holes are obliquely arranged upwards by 60 degrees, and the aperture of the inner spray holes is 2-6 mm;
the outer spray holes are obliquely arranged upwards by 60 degrees; the aperture of the outer spray hole 16 is 4-10 mm.
Preferably, the chilling chamber is provided with a liquid level meter, and the upper liquid level limit of the liquid level meter is 6-7m higher than the lower end of the expansion pipe.
Preferably, the diameter of the enlarged pipe is 1.5-2 times of the diameter of the descending pipe, so as to reduce the flow velocity of the raw synthesis gas, prevent the flow velocity of the raw synthesis gas from being too high, and carry slag and excessive chilling water to the Venturi pipe to cause blockage of the Venturi pipe.
Preferably, the gas inlet end of the gas collecting pipe is positioned in the middle of the furnace shell and above the chilling chamber, and the gas outlet end of the gas collecting pipe is positioned on the side wall of one side of the furnace shell and below the reaction chamber.
Preferably, the venturi tube is positioned on the inner side wall of the furnace shell, and the lower edge of the downcomer is lower than the lower edge of the inlet of the venturi tube, so that the synthesis gas is prevented from entraining ash and directly entering the venturi tube.
Preferably, a rotational flow baffle is arranged at the outlet of the Venturi tube, so that the synthesis gas flowing out of the Venturi tube rotates upwards along the wall of the cyclone chamber, and gas-liquid-solid separation is realized through centrifugal force; the sectional area of the opening of the rotational flow baffle is determined according to the flow velocity of gas at the outlet of the Venturi tube, and the flow velocity of the gas at the outlet of the Venturi tube is 10-30 m/s.
Preferably, the inner wall of the Venturi tube is provided with a wear-resistant coating, and the wear-resistant coating is tungsten carbide or chromium carbide.
The reaction separation integrated gasification furnace has the following advantages:
the gasification reaction and the temperature reduction and dust removal of coal gas are simultaneously completed in the gasification furnace, so that the content of synthetic gas dust out of the gasification furnace is less than 10mg/L, a coal gas washing device is not required to be independently arranged, and the gasification furnace has the advantages of preventing the blockage of a synthetic gas pipeline and reducing the construction and maintenance cost of equipment;
an annular gap is formed between the chilling ring and the downcomer to ensure that the water film of the downcomer is uniformly distributed;
(III) the diameter of the expansion pipe is 1.5-2 times of that of the descending pipe so as to reduce the flow velocity of the crude synthesis gas and prevent the flow velocity of the crude synthesis gas from being too high, and slag and excessive chilling water are carried to the Venturi pipe to cause the blockage of the Venturi pipe;
(IV) the lower edge of the downcomer is lower than the lower edge of the inlet of the Venturi tube, so that the synthesis gas is prevented from carrying ash slag and directly entering the Venturi tube;
and (V) in order to ensure that the coal gas and the water are fully wetted and cooled, the pipe diameter of the Venturi pipe needs to meet the requirement that the flow velocity in the pipe is 60-100m/s, and because the flow velocity cannot be directly measured, the wetting effect is ensured by monitoring the pressure difference of the Venturi pipe (namely the pressure difference P1 between the descending pipe and the chilling chamber) during normal operation.
Therefore, the utility model has the characteristics of reasonable design, simple structure, easy processing, small volume, convenient use, multiple purposes and the like, thereby having good popularization and use values.
Drawings
The utility model is further described below with reference to the accompanying drawings.
FIG. 1 is a schematic structural view of a gasification furnace;
FIG. 2 is a schematic structural view of a venturi tube;
FIG. 3 is a schematic view of a cooling water atomizer;
fig. 4 is a view from a-a in fig. 3.
In the figure: 1. the device comprises a burner 2, a furnace shell 3, a slag hole 4, a chilling ring 5, a gas collecting pipe 6, a downcomer 7, a cooling water atomizer 8, a Venturi tube 9, a water wall coil pipe 10, a chilling chamber 11, an expansion pipe 12, a reaction chamber 13, an inner ring 14, an outer ring 15, inner spray holes 16, outer spray holes 17, a rotational flow baffle 18, a wear-resistant coating 19 and a liquid level meter.
Detailed Description
A reaction/separation integrated gasification furnace according to the present invention will be described in detail below with reference to the drawings and specific examples.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description. And are not intended to indicate or imply that the referenced device or element must have a particular orientation, be constructed and operated in a particular orientation, and are therefore not to be considered limiting of the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
Example (b):
as shown in the attached figure 1, the gasification furnace comprises a furnace shell 2, a reaction chamber 12 is arranged at the upper position of the middle part in the furnace shell 2, and the reaction chamber 12 consists of a water wall coil pipe 9; a chilling chamber 10 is arranged at the position below the middle part in the furnace shell 2, and a slag discharging system is arranged at the lower end of the chilling chamber 10 and is positioned at the lower end of the furnace shell 2; the burner 1 has been seted up to furnace shell 2 upper end, and burner 1 is located 12 upper ends departments of reaction chamber, and slag notch 3 has been seted up to 12 lower extremes of reaction chamber, and quench ring 4 is installed to slag notch 3 department, and downtake 6 is installed to quench ring 4 below, is equipped with an annular gap between downtake 6 and the quench ring 4, and the annular gap width is 7mm, guarantees that the downtake water film distributes evenly. The gas collecting pipe 5 is sleeved outside the descending pipe 6, the gas collecting pipe 5 and the descending pipe 6 are arranged concentrically, the gas inlet end of the gas collecting pipe 5 is located in the middle of the furnace shell 2 and above the chilling chamber 10, and the gas outlet end of the gas collecting pipe 5 is located on the side wall of one side of the furnace shell 2 and below the reaction chamber 12.
The lower end of the downcomer 6 is provided with a cooling water atomizer 7, as shown in fig. 3 and 4, the cooling water atomizer 7 comprises an inner ring 13 and an outer ring 14, 90 inner spray holes 15 which are obliquely arranged upwards at 60 degrees are uniformly distributed on the inner ring 13, and 90 outer spray holes 16 which are obliquely arranged upwards at 60 degrees are uniformly distributed on the outer ring 14; the inner spray hole 15 has a diameter of 4mm, the outer spray hole 16 has a diameter of 7mm, and the outer spray hole 16 and the inner spray hole 15 are concentrically arranged. An expansion pipe 11 is arranged below the descending pipe 6, the expansion pipe 11 is positioned above the chilling chamber 10, a Venturi pipe 8 is arranged at one side of the expansion pipe 11, the Venturi pipe 8 is communicated with the expansion pipe 11, and the Venturi pipe 8 is arranged at the inner side wall of the furnace shell 2; the diameter of the enlarged pipe 11 is 1.8 times of that of the downcomer 6 so as to reduce the flow velocity of the crude synthesis gas and prevent the flow velocity of the crude synthesis gas from being too high, and slag and excessive chilling water are carried to the Venturi tube 8 to cause the blockage of the Venturi tube 8; the lower edge of the downcomer 6 is lower than the lower edge of the inlet of the venturi 8, so that the synthesis gas is prevented from carrying ash and slag and directly entering the venturi 8.
As shown in the attached figure 2, a rotational flow baffle 17 is arranged at the outlet of the venturi tube 8, so that the synthesis gas flowing out of the venturi tube 8 rotates upwards along the wall of the cyclone chamber, and gas-liquid-solid separation is realized through centrifugal force; the sectional area of the opening of the rotational flow baffle 17 is determined according to the flow velocity of the gas at the outlet of the Venturi tube 8, and the flow velocity of the gas at the outlet of the Venturi tube 8 is 20 m/s. Because the velocity of flow of the synthesis gas in the venturi tube 8 is relatively fast, the inner wall of the venturi tube 8 is provided with the wear-resistant coating 18, and the wear-resistant coating 18 adopts tungsten carbide or chromium carbide.
The working process of the utility model is as follows:
s1, enabling pulverized coal and oxygen to enter the gasification chamber 12 through the burner 1 for gasification reaction, and enabling high-temperature crude synthesis gas and liquid ash generated in the gasification chamber 12 to flow downwards to pass through the slag hole 3;
s2, chilling the liquid ash by chilling water to form solid ash, dropping the solid ash into a chilling chamber 10 water bath, and then entering a slag discharging system; the crude synthesis gas continuously flows downwards after being cooled by chilling water sprayed from the chilling ring 4; wherein, one part of chilling water is heated and vaporized by the crude synthesis gas into steam which enters the crude synthesis gas, and the other part of chilling water flows downwards along the inner wall of the downcomer 6 to form a layer of protective water film;
s3, the crude synthesis gas continuously flows downwards along the downcomer 6 to the cooling water atomizer 7, desalted water forms micro mist under the atomization action of the high-pressure inert gas, and the micro mist is fully contacted with the crude synthesis gas, so that the crude synthesis gas is rapidly cooled;
s4, enabling the crude synthesis gas to pass through the cooling water atomizer 7 and then enter the expansion pipe 11, and enabling the crude synthesis gas to carry chilling water from the expansion pipe 11 and enter the Venturi pipe 8;
s5, rapidly raising the flow speed of the crude synthesis gas in the Venturi tube 8 and atomizing chilling water carried in the crude synthesis gas, wherein dust in the crude synthesis gas is wetted and wrapped by the chilling water to form water mist; wherein, the water mist containing ash is thrown to the inner wall of the chilling chamber 10 and flows downwards into a water bath, and flows to a black water flash evaporation system through a black water pipeline;
s6, enabling the crude synthesis gas and the water mist containing ash to flow out of the Venturi tube 8 and tangentially enter the chilling chamber 10 to form rotational flow airflow; wherein, in order to prevent coal gas from entering the chilling chamber 10 from the bottom of the down pipe 6 in series and ensure that the crude synthesis gas enters the chilling chamber 10 tangentially, the liquid level of the chilling chamber 10 is higher than the liquid level in the expanding pipe 11 normally, and the water sealing effect is ensured by the liquid level difference between the chilling chamber 10 and the expanding pipe 11; a liquid level meter 19 is arranged on the chilling chamber 10, the upper limit of the liquid level L1 of the liquid level meter 19 is 6-7m higher than the lower end of the expansion pipe 11, a pressure difference meter P1 is arranged to monitor the pressure difference between the interior of the downcomer 6 and the chilling chamber 10, and the pressure difference is controlled to be not more than 55KPa in normal state; the liquid level L1 of the liquid level meter of the chilling chamber 10 is controlled according to the pressure difference P1 between the descending pipe 6 and the chilling chamber 10 and the flow rate of the synthetic gas in the descending pipe 6, and the formula is as follows:
L1＝a+P1/0.98+K；
wherein a is the distance (m) between the lower edge of the enlarged pipe 11 and the lower limit of the liquid level meter; k is a compensation coefficient, and the ratio of the value of K to the load of the gasification furnace is 1: 50.
s7, the purified synthesis gas enters the gas collecting pipe 5 along the gap between the Venturi tube 8 and the inner wall of the furnace shell 2 in a swirling manner, and then is discharged from the furnace along the gas collecting pipe 5 to enter the next working section.
In the embodiment, high-pressure inert gas is introduced into the inner ring 13, desalted water is introduced into the outer ring 14, and the desalted water is rapidly impacted and atomized by the high-pressure inert gas to form tiny water drops for rapidly cooling the crude synthesis gas, so that the Venturi tube 8 is prevented from being damaged due to overtemperature; meanwhile, the outer wall of the Venturi tube 8 is provided with a temperature measuring device T2, the flow rate of desalted water of the cooling water atomizer 7 is adjusted according to the change of the temperature measuring device T2, the temperature measuring device T2 rises to improve the flow rate of desalted water, otherwise, the flow rate of desalted water is reduced, and the flow rate of desalted water is not less than 20m at the lowest3H, in order to ensure the atomization effect of the cooling water atomizer 7, the high-pressure inert gas flow rate F1 is controlled in proportion to the desalted water flow rate F2, and the formula is as follows:
f1 ═ a proportionality coefficient F2;
wherein, the ratio of the proportionality coefficient to the furnace pressure of the gasification furnace is 1: 2; the high pressure inert gas is nitrogen or carbon dioxide.
Finally, it should be noted that: the above embodiments are only used to illustrate the technical solution of the present invention, and not to limit the same; while the utility model has been described in detail and with reference to the foregoing embodiments, it will be understood by those skilled in the art that: the technical solutions described in the foregoing embodiments may still be modified, or some or all of the technical features may be equivalently replaced; and the modifications or the substitutions do not make the essence of the corresponding technical solutions depart from the scope of the technical solutions of the embodiments of the present invention.
Claims (10)
1. A reaction and separation integrated gasification furnace is characterized by comprising a furnace shell, wherein a reaction chamber is arranged at the position, close to the upper part, in the middle of the furnace shell, and a chilling chamber is arranged at the position, close to the lower part, in the middle of the furnace shell;
the upper end of the reaction chamber is provided with a burner, the lower end of the reaction chamber is provided with a slag hole, a down pipe is arranged below the slag hole, the upper part of the down pipe is provided with a chilling ring, and the lower part of the down pipe is provided with a cooling water atomizer; the outer part of the down pipe is sleeved with a gas collecting pipe, an expansion pipe is arranged below the gas collecting pipe, and the expansion pipe is positioned above the chilling chamber; and a Venturi tube is arranged at one side of the expansion tube and communicated with the expansion tube.
2. The reaction and separation integrated gasification furnace according to claim 1, wherein an annular gap is formed between the downcomer and the quench ring, and the width of the annular gap is 5-10 mm.
3. The reaction and separation integrated gasification furnace according to claim 1, wherein the cooling water atomizer comprises an inner ring and an outer ring, a plurality of inner spray holes are uniformly distributed on the inner ring, a plurality of outer spray holes are uniformly distributed on the outer ring, and the outer spray holes and the inner spray holes are concentrically arranged.
4. The reaction and separation integrated gasification furnace according to claim 3, wherein the inner nozzle is obliquely arranged upward by 60 degrees, and the aperture of the inner nozzle is 2-6 mm;
the outer spray holes are obliquely arranged upwards by 60 degrees; the aperture of the outer spray hole (16) is 4-10 mm.
5. The reaction and separation integrated gasification furnace according to claim 1, wherein the chilling chamber is provided with a liquid level meter, and the upper liquid level limit of the liquid level meter is 6-7m higher than the lower end of the expansion pipe.
6. The reaction separation integrated gasification furnace according to claim 1, wherein the diameter of the enlarged pipe is 1.5 to 2 times the diameter of the downcomer.
7. The reaction-separation integrated gasification furnace according to claim 1, wherein the gas inlet end of the gas collecting pipe is located at the middle position of the furnace shell and above the chilling chamber, and the gas outlet end of the gas collecting pipe is located at one side wall of the furnace shell and below the reaction chamber.
8. The reaction and separation integrated gasification furnace according to claim 1, wherein the venturi tube is located at an inner side wall of the furnace shell, and a lower edge of the downcomer is lower than a lower edge of an inlet of the venturi tube.
9. The reaction and separation integrated gasification furnace according to claim 8, wherein a cyclone baffle is installed at the outlet of the venturi tube; the sectional area of the opening of the rotational flow baffle is determined according to the flow velocity of gas at the outlet of the Venturi tube, and the flow velocity of the gas at the outlet of the Venturi tube is 10-30 m/s.
10. The reaction and separation integrated gasification furnace according to claim 9, wherein a wear-resistant coating is provided on the inner wall of the venturi tube, and the wear-resistant coating is tungsten carbide or chromium carbide.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121799098.3U CN215924866U (en) | 2021-08-03 | 2021-08-03 | Reaction separation integrated gasification furnace |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202121799098.3U CN215924866U (en) | 2021-08-03 | 2021-08-03 | Reaction separation integrated gasification furnace |
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| Publication Number | Publication Date |
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| CN215924866U true CN215924866U (en) | 2022-03-01 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202121799098.3U Active CN215924866U (en) | 2021-08-03 | 2021-08-03 | Reaction separation integrated gasification furnace |
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| CN (1) | CN215924866U (en) |
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2021
- 2021-08-03 CN CN202121799098.3U patent/CN215924866U/en active Active
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