CN107537266B - Dust removal system and dust removal method for pyrolysis gas - Google Patents
Dust removal system and dust removal method for pyrolysis gas Download PDFInfo
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Abstract
The invention provides a dust removal system and a dust removal method for pyrolysis gas. The system comprises a fast pyrolysis furnace, a high-temperature chilling dust remover, a coarse dust remover, a fine dust remover, a heat recovery device, a gas-liquid separator, an oil-water separator and a circulating booster pump. The high-temperature chilling dust remover is respectively connected with the fast pyrolysis furnace and the coarse dust remover, the fine dust remover is respectively connected with the coarse dust remover and the heat recovery device, the gas-liquid separator is respectively connected with the heat recovery device and the oil-water separator, and the circulating booster pump is respectively connected with the high-temperature chilling dust remover, the heat recovery device and the oil-water separator. The invention can solve the problems of operation stability and safety of the high-temperature pyrolysis gas dust separation system, reduce the cost of the high-temperature pyrolysis gas purification system and reasonably utilize the heat of the high-temperature pyrolysis gas.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry, and particularly relates to a dust removal system and a dust removal method for pyrolysis gas.
Background
The coal pyrolysis upgrading technology can be classified into low-temperature (500-600 ℃) pyrolysis and medium-temperature (600-800 ℃) pyrolysis according to pyrolysis temperature; according to different heat supply mediums, the pyrolysis quality improvement technology can be divided into a gas phase heat carrier pyrolysis technology, a solid phase heat carrier pyrolysis technology and a special heat accumulating pyrolysis technology. In the pyrolysis process, the temperature of the gas outlet reaches 800 ℃ or even higher, a certain amount of tar, a great amount of dust and a great amount of heat are carried, and higher difficulty is brought to subsequent gas purification and tar recovery. The gas dust is separated under a certain temperature condition, so that on one hand, the difficulty of gas dust removal is reduced, and on the other hand, the recovery rate of tar is improved; therefore, the dust removal efficiency and the operation stability directly affect the economic benefit of the system.
At present, two main methods exist for dust separation of pyrolysis gas, namely, a gas chilling process is adopted, high-temperature gas is directly sprayed with water for cooling, and then three-phase separation is carried out on oil-water dust after cooling; and secondly, the gas is directly separated at high temperature through high-temperature gas-solid separation equipment.
The gas chilling process is used in mature coking industry and vertical furnace coking technology, and is mainly characterized in that ammonia water generated in the coking or pyrolysis process is directly contacted with pyrolysis gas in a chilling tower through a circulating pump at 78 ℃ for heat exchange, the temperature of the pyrolysis gas is reduced to 83 ℃, a mixture of tar, ammonia water and gas enters a gas-liquid separator, the heat exchange temperature of separated raw gas is reduced to 45 ℃ through the upper section of a primary cooler and circulating water, the raw gas enters the lower section through a riser and is cooled to 22 ℃ through refrigerating water, and the raw gas is pressurized through a gas blower. The method is suitable for a fixed bed with relatively larger raw coal particle size and a moving bed pyrolysis technology with longer residence time, and is characterized in that the dust content is lower, and if the method is adopted, the subsequent oil-water-dust separation difficulty is higher and the problem of blockage is more likely to occur, so that the system operation period is influenced; the high-temperature gas has higher temperature, carries a large amount of heat, has low heat utilization efficiency by adopting direct cooling, and generates a large amount of sewage.
The other method is that the coal gas is directly subjected to dust separation under the high-temperature condition, and is relatively more applied in the middle-temperature pyrolysis process, so that the problem that the oil-water dust separation is difficult is mainly solved, but in the middle-temperature pyrolysis process, the temperature of a coal gas outlet reaches 800 ℃ or higher, high-temperature equipment is directly utilized for dust separation, the equipment cost is higher, and the allowable stress of equipment materials is greatly reduced, so that the operation safety of a system is reduced; under the high temperature condition, the tar in the coal gas is easy to generate secondary cracking reaction, the yield of the tar is reduced, the coking rate of the tar is increased, and the stable operation of dust removal equipment is seriously influenced.
Disclosure of Invention
Aiming at the defects of the prior art, the invention provides a dust removal system and a dust removal method for pyrolysis gas, which can solve the problems of operation stability and safety of a pyrolysis gas dust separation system, reduce the cost of the pyrolysis gas purification system and reasonably utilize the heat of pyrolysis gas.
The dust removing system for high-temperature pyrolysis gas provided by the invention comprises:
the rapid pyrolysis furnace is provided with a pyrolysis material inlet, a semicoke outlet and a pyrolysis gas outlet;
the high-temperature chilling dust remover is sequentially provided with an inertial dust settling area, a spray dust suppression area and a temperature regulation area along the gas flowing direction, wherein the inertial dust settling area, the spray dust suppression area and the temperature regulation area are separated by an inner partition plate, a pyrolysis gas inlet is arranged on the inertial dust settling area, a gas outlet is arranged in the temperature regulation area, spray nozzles are arranged in the inertial dust settling area, the spray dust suppression area and the temperature regulation area, and a chilled water inlet is arranged on the spray nozzles; the high-temperature chilling dust remover is also provided with a first dust outlet; the high-temperature pyrolysis gas inlet is connected with the high-temperature pyrolysis gas outlet of the fast pyrolysis furnace;
the coarse dust removing device is provided with a gas inlet, a coarse dust removing gas outlet and a second dust outlet, and the gas inlet is connected with the gas outlet of the high-temperature chilling dust remover;
the fine dust removal device is provided with a coarse dust removal gas inlet, a dust removal gas outlet and a third dust outlet; the coarse dust-removing gas inlet is connected with a coarse dust-removing gas outlet of the coarse dust-removing device;
the heat recovery device is provided with a dust-removing gas inlet, a desalted water inlet, a flushing water inlet, a gas-liquid mixture outlet, a steam outlet and a wastewater outlet, wherein the dust-removing gas inlet is connected with the dust-removing gas outlet of the fine dust-removing device;
the gas-liquid separator is provided with a gas-liquid mixture inlet, a clean gas outlet and an oil-water mixture outlet, and the gas-liquid mixture inlet is connected with the gas-liquid mixture outlet of the heat recovery device;
the oil-water separator is provided with an oil-water mixture inlet, a water outlet and a tar outlet, and the oil-water mixture inlet is connected with the oil-water mixture outlet of the gas-liquid separator;
the circulating booster pump is provided with a water inlet and a pressurized water outlet, the water inlet is connected with the water outlet of the oil-water separator, and the pressurized water outlet is respectively connected with the chilled water inlet of the high-temperature chilled dust remover and the flushing water inlet of the heat recovery device.
In some embodiments of the invention, the diameter of the gas flow passage inside the high temperature chilled dust collector is 5-8 times the diameter of the pyrolysis gas inlet.
In some embodiments of the invention, the high temperature chilled dust collector is square or circular in shape.
In some embodiments of the invention, the water outlet of the inertial dust area nozzle is perpendicular to the direction of gas flow.
In some embodiments of the invention, the water outlet of the spray dust suppression zone nozzle is parallel to the direction of gas flow.
In some embodiments of the invention, the water outlet of the temperature adjustment zone showerhead is perpendicular to the direction of gas flow.
The method for removing dust from pyrolysis gas by using the dust removal system provided by the invention comprises the following steps:
the pyrolysis material is sent into the fast pyrolysis furnace for pyrolysis, and semicoke and high-temperature pyrolysis gas are obtained;
feeding the pyrolysis gas into the high-temperature chilled dust remover, and adopting chilled water to remove dust and cool to obtain coal gas;
feeding the gas into the coarse dust removal device for coarse dust removal to obtain coarse dust removal gas;
feeding the coarse dust-removing gas into the fine dust-removing device for fine dust removal to obtain dust-removing gas;
feeding the dust-removed gas into a heat recovery device to exchange heat with desalted water, wherein water vapor and tar in the dust-removed gas are condensed, and the desalted water is heated to obtain a gas-liquid mixture and vapor;
sending the gas-liquid mixture into the gas-liquid separator for separation to obtain an oil-water mixture and clean gas;
sending the oil-water mixture into the oil-water separator for separation to obtain tar and water;
after being pressurized by the circulating booster pump, the water is respectively used as chilling water to be sent into the mist high-temperature chilling dust remover and is used as flushing water to be sent into the heat recovery device.
In some embodiments of the invention, the chilled water is used in an amount of 1/8 to 1/7 of the mass flow of the pyrolysis gas.
In some embodiments of the invention, the temperature of the gas exiting the high temperature chilled dust collector is 380 ℃ to 550 ℃.
In some embodiments of the invention, the amount of chilled water injected by the inertial dust fall zone is 1/6-1/5 of the total chilled water amount, the amount of chilled water injected by the spray dust suppression zone is 3/5-2/3 of the total chilled water amount, and the amount of chilled water injected by the temperature adjustment zone is 1/6-1/5 of the total chilled water amount.
The invention avoids the safety risk caused by equipment coking and equipment material allowable stress reduction of conventional high-temperature dust separation, and avoids the problem of difficult oil-water-dust three-phase separation in the conventional chilling mode, thereby being capable of solving the stability and safety of lignite pyrolysis gas-dust separation operation.
The invention recovers sensible heat and latent heat, has high utilization efficiency and small water circulation, only needs to supplement part of chilling water in the initial stage, and generates water by pyrolysis in the normal operation process, thereby having high efficiency, energy conservation and environmental protection.
In addition, the volume of the increase of the steam quantity generated by the water sprayed into the high-temperature chilling dust remover is lower than the working condition volume caused by temperature reduction, so that the treatment capacity of dust removing equipment can be reduced, and the equipment material selection grade is reduced due to the temperature reduction, so that the operation cost of the system is low.
Additional aspects and advantages of the invention will be set forth in part in the description which follows, and in part will be obvious from the description, or may be learned by practice of the invention.
Drawings
Fig. 1 is a schematic structural diagram of a dust removal system for pyrolysis gas according to an embodiment of the present invention.
FIG. 2 is a schematic diagram of a high temperature chilled dust collector in an embodiment of the invention.
Fig. 3 is a process flow diagram of pyrolysis gas dust removal in an embodiment of the invention.
Detailed Description
The following detailed description of specific embodiments of the invention is provided in connection with the accompanying drawings and examples in order to provide a better understanding of the aspects of the invention and advantages thereof. However, the following description of specific embodiments and examples is for illustrative purposes only and is not intended to be limiting of the invention.
It should be noted that the directions or positional relationships indicated by the terms "upper", "lower", "left", "right" and the like in the present invention are directions or positional relationships based on those shown in the drawings, and are merely for convenience of description of the present invention, and do not require that the present invention must be constructed and operated in a specific direction, and thus should not be construed as limiting the present invention. Furthermore, the terms "first," "second," "third," and the like in this disclosure are used for descriptive purposes only and are not to be construed as indicating or implying a relative importance or implying a number of such features, whereby a feature defining "first," "second," "third," or the like, may explicitly or implicitly include one or more such features.
Fig. 1 shows a dust removal system for pyrolysis gas according to the present invention, comprising: raw material bin 1, fast pyrolysis furnace 2, high temperature chilling dust remover 3, coarse dust collector 4, fine dust collector 5, heat recovery device 6, gas-liquid separator 7, oil-water separator 8 and circulation booster pump 9.
The raw stock bin 1 is provided with a raw stock inlet 101 and a raw stock outlet 102.
The fast pyrolysis furnace 2 is provided with a pyrolysis material inlet 201, a semicoke outlet 202 and a pyrolysis gas outlet 203, wherein the pyrolysis material inlet 201 is connected with the raw material outlet 102 of the raw material bin 1.
The high-temperature chilled dust remover 3 is provided with a high-temperature pyrolysis gas inlet 301, a chilled water inlet 302, a coal gas outlet 303 and a first dust outlet 304, wherein the high-temperature pyrolysis gas inlet 301 is connected with the high-temperature pyrolysis gas outlet 203 of the rapid pyrolysis furnace 2.
The coarse dust collector 4 is provided with a gas inlet 401, a coarse dust-collecting gas outlet 402 and a second dust outlet 403, and the gas inlet 401 is connected with the gas outlet 303 of the high-temperature chilled dust collector 3.
The fine dust removal device 5 is provided with a coarse dust removal gas inlet 501, a dust removal gas outlet 502 and a third dust outlet 503, and the coarse dust removal gas inlet 501 is connected with the coarse dust removal gas outlet 402 of the coarse dust removal device 4.
The heat recovery device 6 is provided with a dust-removing gas inlet 601, a desalted water inlet 602, a flushing water inlet 603, a gas-liquid mixture outlet 604 and a steam outlet 605, and the dust-removing gas inlet 601 is connected with the dust-removing gas outlet 502 of the fine dust-removing device 5.
The gas-liquid separator 7 is provided with a gas-liquid mixture inlet 701, an oil-water mixture outlet 702 and a clean gas outlet 703, and the gas-liquid mixture inlet 701 is connected to the gas-liquid mixture outlet 604 of the heat recovery device 6.
The oil-water separator 8 is provided with an oil-water mixture inlet 801, a tar outlet 802 and a water outlet 803, and the oil-water mixture inlet 801 is connected with the oil-water mixture outlet 702 of the gas-liquid separator 7.
The circulation booster pump 9 is provided with a water inlet 901 and a pressurized water outlet 902, the water inlet 901 is connected with the water outlet 803 of the oil-water separator 8, and the pressurized water outlet 902 is respectively connected with the chilled water inlet 302 of the high-temperature chilled dust collector 3 and the flushing water inlet 603 of the heat recovery device 6.
The raw material bin 1 is not necessarily required to achieve the object of the present invention, and may be increased or decreased according to actual needs.
The high temperature chilled dust collector 3 is a core device of the invention, the structure of which is shown in fig. 2, and other devices of the invention are common devices in the art, and the structure is not repeated here.
As shown in fig. 2, along the direction of gas flow (first from bottom to top, then from top to bottom, and finally from bottom to top, see the opening of the inner partition 307, 305 in fig. 2 is an equipment body), the high-temperature chilled dust remover 3 is sequentially provided with an inertial dust settling zone a, a spray dust suppression zone b and a temperature regulation zone c, the inertial dust settling zone a, the spray dust suppression zone b and the temperature regulation zone c are separated by the inner partition 307, the inertial dust settling zone a is provided with a pyrolysis gas inlet 301, the temperature regulation zone b is provided with a gas outlet 303, the inertial dust settling zone a, the spray dust suppression zone b and the temperature regulation zone c are all provided with spray heads 306, and the spray heads 306 are provided with an excitation water inlet 302 (the direction indicated by an arrow in the figure is the spraying direction of excitation water).
The pyrolysis gas enters the high-temperature chilling dust remover 3 device body 305 through the pyrolysis gas inlet 301, is settled in the inertial dust settling zone a, and partial chilled water is sprayed from the gas inlet pipeline in an annular direction or at the side part of the high-temperature chilling dust remover 3 body perpendicular to the direction of the gas flow through the spray head 306 (namely, the water outlet of the spray head 306 of the inertial dust settling zone a is perpendicular to the direction of the gas flow), so that dust carried in the gas flow impacts the inner partition 307, and the dust removing and gasification reaction window effect of the inertial dust settling zone a is realized. In the spraying dust suppression zone b, part of the chilled water is sprayed through the spray head 306, the water spraying amount is controlled, the spraying point is arranged in the area with downward air flow, the spraying direction of the water mist and the air flow direction are the same (namely, the water outlet of the spray head 306 of the spraying dust suppression zone b is parallel to the air flow direction), the air flow field is not changed, the state of accelerating falling of dust in the area is kept, and the effect of dust suppression and cooling is achieved. In the temperature adjustment zone c, chilled water is injected in a direction perpendicular to the gas flow (i.e., the water outlet of the nozzle 306 of the temperature adjustment zone c is perpendicular to the gas flow direction), and the gas temperature is further adjusted to meet the operation requirements of the subsequent devices and is discharged through the gas outlet 303.
The shape of the high temperature chilled dust collector 3 is not used as a limitation, and in a preferred embodiment of the present invention, the shape of the high temperature chilled dust collector 3 is square or circular.
In order to fully utilize the self gravity of dust particles and further realize partial sedimentation, in the preferred embodiment of the invention, the diameter of the air flow channel inside the high-temperature chilled dust collector 3 is 5-8 times that of the pyrolysis gas inlet 301.
The pyrolysis gas contains a certain amount of CH 4 And carry a large amount of dust, and through the chilled water sprayed in a grading way, certain methane steam conversion reaction and high activity can occurThe dust can also generate water gas reaction, so that the effective component H in the gas is improved 2 The CO content while also consuming part of the pyrolysis water that has been produced.
And by adding a certain amount of chilled water, the partial pressure of tar steam in pyrolysis gas is reduced, which is beneficial to reducing secondary reaction of tar.
In addition, the staged chilling is adopted, so that the rapid pyrolysis furnace 2 has a certain dust suppression effect on the pyrolysis gas outlet 203.
The volume of the increase of the steam quantity generated by the water sprayed into the high-temperature chilling dust remover 3 is lower than the working condition volume caused by temperature reduction, so that the treatment capacity of dust removing equipment can be reduced, and the equipment material selection grade is reduced due to the temperature reduction, so that the running cost of the system is low.
As shown in fig. 3, the method for removing dust from high-temperature pyrolysis gas provided by the invention comprises the following steps:
and (3) delivering the pyrolysis material into a fast pyrolysis furnace 2 for pyrolysis to obtain semicoke and high-temperature pyrolysis gas. The carbocoal was collected and used for other purposes.
Sending the pyrolysis gas into a high-temperature chilled dust remover 3, and removing dust and cooling by chilled water to obtain coal gas.
The gas is sent into a coarse dust removing device 4 for coarse dust removal, and coarse dust removing gas is obtained.
And sending the coarse dust-removing gas into a fine dust-removing device 5 for fine dust removal to obtain dust-removing gas.
The dedusted gas is sent to a heat recovery device 6 to exchange heat with desalted water, water vapor and tar in the dedusted gas are condensed, and the desalted water is heated to obtain a gas-liquid mixture and vapor.
Feeding the gas-liquid mixture into a gas-liquid separator 7 for separation to obtain an oil-water mixture and clean gas;
the oil-water mixture is sent into an oil-water separator 8 for separation, and tar and water are obtained.
After being pressurized by the circulating booster pump 9, the water is respectively sent into the high-temperature chilled dust remover 3 as chilled water and is sent into the heat recovery device 6 as flushing water.
The high-temperature chilling dust remover 3 primarily removes dust, and the dust removal efficiency is 40% -50%. Under the action of the quenching water, the temperature of the pyrolysis gas is rapidly reduced, and the consumption of the quenching water is adjusted according to the set temperature after the pyrolysis gas is quenched. When the fast pyrolysis furnace 2 exists, the high-temperature chilling dust remover 3 is installed nearby the outlet of the fast pyrolysis furnace 2, so that the tar contained in the high-temperature pyrolysis gas can be guaranteed to be rapidly cooled, the secondary pyrolysis reaction of the tar under the high-temperature condition is reduced, and the coking phenomenon of a high-temperature section is reduced or even avoided. The consumption of chilled water accounts for about 1/8-1/7 of the mass flow of the high-temperature pyrolysis gas, the temperature of the high-temperature pyrolysis gas is reduced to 380-550 ℃ through chilled water, the temperature is ensured to be higher than the dew point of tar, the partial pressure of water vapor in the gas is increased due to the addition and gasification of part of water, the partial pressure of tar is reduced, and the coagulation adhesion condition of tar in subsequent treatment equipment is avoided; and at the temperature, compared with the material of the subsequent treatment equipment before chilling, the material of the subsequent treatment equipment can reduce the cost to a certain extent and improve the use safety. After the high-temperature pyrolysis gas is cooled to a set temperature in the high-temperature chilled dust remover 3, the gas with dust content of 25-80 g per cubic meter enters the coarse dust removing device 4 and the fine dust removing device 5 to remove dust in the gas, and the gas with dust content of 25-50 mg per cubic meter is formed. The dedusted coal gas enters a heat recovery device 6, and the desalted water at the temperature of 25-40 ℃ is utilized to exchange heat with the coal gas in countercurrent and indirectly, so that the water vapor and tar in the coal gas are condensed, and medium-pressure superheated steam is generated, thereby meeting the system recycling requirement or heat supply requirement. The condensed tar and condensed water are separated from coal gas in a gas-liquid separator 7, the coal gas is further purified, the tar and the condensed water are separated in an oil-water separator 8, the tar is taken as a product to enter a post-working section (specific process is not repeated here), part of the condensed water is pressurized by a circulating booster pump 9 and then is sent into a high-temperature chilling dust remover 3 in a grading manner, the other part of the condensed water is pressurized and then is used as flushing water, the generated residual pyrolysis water is sent into a sewage treatment unit (specific process is not repeated here), the residual pyrolysis water is generated in the pyrolysis process and accounts for about 6% -10% of raw coal, and the chilling water of the pressurizing chilling dust remover 3 is supplemented by the outside when the device is used for the first time.
In the preferred embodiment of the invention, the amount of the chilled water sprayed by the inertia dust fall area a of the high-temperature chilled dust remover 3 is 1/6-1/5 of the total chilled water amount, the amount of the chilled water sprayed by the spraying dust suppression area b is 3/5-2/3 of the total chilled water amount, and the amount of the chilled water sprayed by the temperature regulation area c is 1/6-1/5 of the total chilled water amount. The temperature of pyrolysis gas in different areas is controlled by controlling the injection amount of the quenching water so as to achieve corresponding effects. In the inertial dust settling zone a, the temperature in the zone is maintained at a relatively high temperature of about 800-850 ℃, the partial pressure of water vapor is properly increased, a methane vapor conversion and water gas reaction window is provided, and the hydrogen and carbon monoxide components in the gas are increased. In the spray dust suppression zone b, the temperature of the pyrolysis gas is rapidly reduced to 500-550 ℃, and in the downstream process of the gas flow, the total volume flow of the gas is reduced by 1/4 along with the reduction of the temperature, and the flow speed is reduced so as to be beneficial to the sedimentation of dust. In the temperature regulating zone c, the temperature of the gas outlet 303 needs to be controlled at 380-550 ℃.
The invention will now be described with reference to specific examples. The values of the process conditions taken in the examples below are exemplary and can be obtained in the ranges indicated in the foregoing summary, and for process parameters not specifically identified, reference may be made to conventional techniques. The detection methods used in the examples below are all conventional in the industry.
Example 1
In this embodiment, the system shown in fig. 1 is used to remove dust from pyrolysis gas, the diameter of the air flow channel inside the high-temperature chilled dust remover 3 is 5 times that of the pyrolysis gas inlet 301, the appearance of the high-temperature chilled dust remover 3 is square, the water outlet of the nozzle 306 in the inertial dust fall area a is perpendicular to the direction of gas flow, the water outlet of the nozzle 306 in the spray dust suppression area b is parallel to the direction of gas flow, and the water outlet of the nozzle 306 in the temperature regulation area c is perpendicular to the direction of gas flow. The specific process flow is as follows:
the pulverized coal enters the fast pyrolysis furnace 2 from the raw material feeding bin 1 to be pyrolyzed in a downlink pyrolysis mode, and the grain size of the raw material is smaller than 3mm. The temperature of the pyrolysis gas generated after pyrolysis in the fast pyrolysis furnace 2 is 900 ℃, and the dust content is 120g/Nm 3 The tar content is 80-150g/Nm 3 。
Sending the pyrolysis gas into a high-temperature chilled dust remover 3, and removing dust and cooling by chilled water to obtain coal gas. The total consumption of the chilled water is 1/8 of the mass flow of the pyrolysis gas, the amount of the chilled water sprayed by the inertia dust fall area a is 1/6 of the total chilled water, the amount of the chilled water sprayed by the spraying dust suppression area b is 2/3 of the total chilled water, and the amount of the chilled water sprayed by the temperature regulation area c is 1/6 of the total chilled water. The temperature of the obtained gas is 450-510 ℃.
The gas is sent into a coarse dust removing device 4 for coarse dust removal, and coarse dust removing gas is obtained.
And sending the coarse dust-removing gas into a fine dust-removing device 5 for fine dust removal to obtain dust-removing gas. Dust content of the dust-removed gas is 25mg/Nm 3 The following is given.
The dedusted gas is sent to a heat recovery device 6 to exchange heat with desalted water, water vapor and tar in the dedusted gas are condensed, and the desalted water is heated to obtain a gas-liquid mixture and vapor. The temperature of the gas-liquid mixture is 70-82 ℃, the temperature of the steam is 400 ℃, and the pressure is 3.8Mpa.
The gas-liquid mixture is sent into a gas-liquid separator 7 for separation, and an oil-water mixture and clean gas are obtained.
The oil-water mixture is sent into an oil-water separator 8 for separation, and tar and water are obtained.
After being pressurized by the circulating booster pump 9, the water is respectively sent into the high-temperature chilled dust remover 3 as chilled water and is sent into the heat recovery device 6 as flushing water.
Example 2
In this embodiment, the system shown in fig. 1 is used to remove dust from pyrolysis gas, the diameter of the air flow channel inside the high-temperature chilled dust remover 3 is 8 times that of the pyrolysis gas inlet 301, the appearance of the high-temperature chilled dust remover 3 is circular, the water outlet of the nozzle 306 in the inertial dust fall area a is perpendicular to the direction of gas flow, the water outlet of the nozzle 306 in the spray dust suppression area b is parallel to the direction of gas flow, and the water outlet of the nozzle 306 in the temperature regulation area c is perpendicular to the direction of gas flow. The specific process flow is as follows:
the pulverized coal enters the fast pyrolysis furnace 2 from the raw material feeding bin 1 to be pyrolyzed in a downlink pyrolysis mode, and the grain size of the raw material is smaller than 6mm. Quick speedThe temperature of the pyrolysis gas generated after pyrolysis in the pyrolysis furnace 2 is 850 ℃, and the dust content is 100g/Nm 3 Tar content of 50-100g/Nm 3 。
Sending the pyrolysis gas into a high-temperature chilled dust remover 3, and removing dust and cooling by chilled water to obtain coal gas. The total consumption of the chilled water is 1/7 of the mass flow of the pyrolysis gas, the amount of the chilled water sprayed by the inertia dust fall area a is 1/5 of the total chilled water, the amount of the chilled water sprayed by the spraying dust suppression area b is 3/5 of the total chilled water, and the amount of the chilled water sprayed by the temperature regulation area c is 1/5 of the total chilled water. The temperature of the obtained gas is 380-450 ℃.
The gas is sent into a coarse dust removing device 4 for coarse dust removal, and coarse dust removing gas is obtained.
And sending the coarse dust-removing gas into a fine dust-removing device 5 for fine dust removal to obtain dust-removing gas. Dust content of the dust-removed gas is 20mg/Nm 3 The following is given.
The dedusted gas is sent to a heat recovery device 6 to exchange heat with desalted water, water vapor and tar in the dedusted gas are condensed, and the desalted water is heated to obtain a gas-liquid mixture and vapor. The temperature of the gas-liquid mixture is 70-82 ℃, the temperature of the steam is 201 ℃, and the pressure is 1.6Mpa.
The gas-liquid mixture is sent into a gas-liquid separator 7 for separation, and an oil-water mixture and clean gas are obtained.
The oil-water mixture is sent into an oil-water separator 8 for separation, and tar and water are obtained.
After being pressurized by the circulating booster pump 9, the water is respectively sent into the high-temperature chilled dust remover 3 as chilled water and is sent into the heat recovery device 6 as flushing water.
According to the embodiment, the safety risk caused by equipment coking and equipment material allowable stress reduction of conventional high-temperature dust separation is avoided, and the problem that the subsequent oil-water-dust three-phase separation is difficult in a conventional chilling mode is avoided, so that the stability and safety of the operation of separating the lignite pyrolysis gas dust can be solved.
The invention recovers sensible heat and latent heat, has high utilization efficiency and small water circulation, only needs to supplement part of chilling water in the initial stage, and generates water by pyrolysis in the normal operation process, thereby having high efficiency, energy conservation and environmental protection.
It is apparent that the above examples are only illustrative of the present invention and are not limiting of the embodiments. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. And obvious variations or modifications thereof are contemplated as falling within the scope of the present invention.
Claims (8)
1. A dust removal system for pyrolysis gas, comprising:
the rapid pyrolysis furnace is provided with a pyrolysis material inlet, a semicoke outlet and a pyrolysis gas outlet;
the high-temperature chilling dust remover is sequentially provided with an inertial dust settling area, a spray dust suppression area and a temperature regulation area along the gas flowing direction, wherein the inertial dust settling area, the spray dust suppression area and the temperature regulation area are separated by an inner partition plate, a pyrolysis gas inlet is arranged on the inertial dust settling area, a gas outlet is arranged in the temperature regulation area, spray nozzles are arranged in the inertial dust settling area, the spray dust suppression area and the temperature regulation area, and a chilled water inlet is arranged on the spray nozzles; the high-temperature chilling dust remover is also provided with a first dust outlet; the high-temperature pyrolysis gas inlet is connected with the high-temperature pyrolysis gas outlet of the fast pyrolysis furnace;
the coarse dust removing device is provided with a gas inlet, a coarse dust removing gas outlet and a second dust outlet, and the gas inlet is connected with the gas outlet of the high-temperature chilling dust remover;
the fine dust removal device is provided with a coarse dust removal gas inlet, a dust removal gas outlet and a third dust outlet; the coarse dust-removing gas inlet is connected with a coarse dust-removing gas outlet of the coarse dust-removing device;
the heat recovery device is provided with a dust-removing gas inlet, a desalted water inlet, a flushing water inlet, a gas-liquid mixture outlet, a steam outlet and a wastewater outlet, wherein the dust-removing gas inlet is connected with the dust-removing gas outlet of the fine dust-removing device;
the gas-liquid separator is provided with a gas-liquid mixture inlet, a clean gas outlet and an oil-water mixture outlet, and the gas-liquid mixture inlet is connected with the gas-liquid mixture outlet of the heat recovery device;
the oil-water separator is provided with an oil-water mixture inlet, a water outlet and a tar outlet, and the oil-water mixture inlet is connected with the oil-water mixture outlet of the gas-liquid separator;
the circulating booster pump is provided with a water inlet and a pressurized water outlet, the water inlet is connected with the water outlet of the oil-water separator, and the pressurized water outlet is respectively connected with the chilled water inlet of the high-temperature chilled dust remover and the flushing water inlet of the heat recovery device;
the diameter of the air flow channel in the high-temperature chilling dust remover is 5-8 times of the diameter of the pyrolysis gas inlet;
the appearance of the high-temperature chilling dust remover is square or round.
2. The dust removal system of claim 1, wherein the water outlet of the inertial dust area nozzle is perpendicular to the direction of gas flow.
3. The dust removal system of claim 1, wherein the water outlet of the spray dust suppression zone nozzle is parallel to the direction of gas flow.
4. The dust removal system of claim 1, wherein the water outlet of the temperature conditioning zone nozzle is perpendicular to the direction of gas flow.
5. A method of dedusting pyrolysis gas using the dedusting system of any of claims 1-4, comprising the steps of:
the pyrolysis material is sent into the fast pyrolysis furnace for pyrolysis, and semicoke and high-temperature pyrolysis gas are obtained;
feeding the pyrolysis gas into the high-temperature chilled dust remover, and adopting chilled water to remove dust and cool to obtain coal gas;
feeding the gas into the coarse dust removal device for coarse dust removal to obtain coarse dust removal gas;
feeding the coarse dust-removing gas into the fine dust-removing device for fine dust removal to obtain dust-removing gas;
feeding the dust-removed gas into a heat recovery device to exchange heat with desalted water, wherein water vapor and tar in the dust-removed gas are condensed, and the desalted water is heated to obtain a gas-liquid mixture and vapor;
sending the gas-liquid mixture into the gas-liquid separator for separation to obtain an oil-water mixture and clean gas;
sending the oil-water mixture into the oil-water separator for separation to obtain tar and water;
after being pressurized by the circulating booster pump, the water is respectively used as chilling water to be sent into the high-temperature chilling dust remover and is used as flushing water to be sent into the heat recovery device.
6. The method of claim 5, wherein the chilled water is used in an amount of 1/8 to 1/7 of the mass flow of the pyrolysis gas.
7. The method of claim 5, wherein the temperature of the gas exiting the high temperature chilled dust collector is 380 ℃ to 550 ℃.
8. The method of claim 5, wherein the amount of chilled water injected by the inertial dust suppression zone is 1/6-1/5 of the total amount of chilled water, the amount of chilled water injected by the spray dust suppression zone is 3/5-2/3 of the total amount of chilled water, and the amount of chilled water injected by the temperature adjustment zone is 1/6-1/5 of the total amount of chilled water.
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