Gasification device for anthracite or coke

Abstract

The utility model provides a gasification device for anthracite or coke. The gasification device comprises a gasification furnace, the dust removal and heat recovery assembly comprises a medium-pressure waste heat boiler, a dust removal filtering device and a heat recovery assembly; dust-containing gas at an outlet of the gasification furnace enters a medium-pressure waste heat boiler so as to carry out heat exchange and cooling on the dust-containing gas; the medium-pressure waste heat boiler outputs the cooled dust-containing coal gas to a dust removal filtering device, so that the dust-containing coal gas is filtered and subjected to dust removal, and coal gas is output; the heat recovery assembly comprises a waste heat recoverer communicated with the dust removal filtering device through a washing piece, and the waste heat recoverer recovers heat in the coal gas and outputs raw coal gas and coal gas water; and a gas water flash evaporation system. The efficient dust removal filtering device is additionally arranged at the dusty gas outlet of the medium-pressure waste heat boiler, so that the built gasification device is transformed, the stable operation of the gas water flash evaporation system is improved, and the overall operation and input cost is reduced while the operation cycle of the gasification device is prolonged.

Description

Technical Field

[0001] This application relates to the technical field of gas production, and particularly to a gasification device for anthracite or coke. Background Art

[0002] In a system for gasifying anthracite or coke to produce gas, it includes a Saiding furnace, a medium-pressure waste heat boiler, a waste heat recovery device, and a gas-water flash evaporation system. Currently, after the gas at the outlet of the Saiding furnace passes through a cyclone separator, it enters the medium-pressure waste heat boiler. According to the actual on-site operation situation, in addition to the clogging condition of the medium-pressure waste heat boiler, the downstream high-pressure flash gas carries a serious amount of dust, resulting in serious clogging of the true flash gas condenser. The true flash cannot reach the designed vacuum degree, the ammonia-nitrogen in the wastewater exceeds the standard, and the coal dust in the clarifying tank is difficult to settle, and a large amount of flocculant needs to be added.

[0003] According to the upcoming gasification device to be built, a dust removal and filtration device can be set at the gas outlet of the Saiding furnace to filter the dusty gas at the outlet of the gasification furnace, so that the gas output by the dust removal and filtration device contains almost no dust. However, during the transformation of the already built gasification device, due to layout limitations and pipeline stress reasons, it is impossible to install an efficient dust removal and filtration device between the gas outlet of the Saiding furnace and the medium-pressure waste heat boiler. Summary of the Utility Model

[0004] This application aims to solve at least one of the technical problems in the related art to some extent. For this reason, the purpose of this application is to propose a gasification device for anthracite or coke. By adding an efficient dust removal and filtration device at the dusty gas outlet of the medium-pressure waste heat boiler, the stable operation of the gas-water flash evaporation system is improved, while the operation cycle of the gasification device is increased, and the overall operation and investment costs are reduced.

[0005] To achieve the above object, a gasification device for anthracite or coke proposed by this application includes:

[0006] A gasification furnace for gasifying anthracite or coke;

[0007] A dust removal and heat recovery assembly, which includes a medium-pressure waste heat boiler, a dust removal and filtration device, and a heat recovery assembly; the dusty gas at the outlet of the gasification furnace enters the medium-pressure waste heat boiler to exchange heat and cool down the dusty gas; the medium-pressure waste heat boiler outputs the cooled dusty gas to the dust removal and filtration device to filter and remove dust from the dusty gas and output gas; the heat recovery assembly includes a waste heat recovery device connected to the dust removal and filtration device through a washing member, and the waste heat recovery device recovers the heat in the gas and outputs crude gas and gas water; and

[0008] The coal gas water flashing system includes a medium-pressure flash vessel, a vacuum flash assembly, and a waste water filter; the medium-pressure flash vessel and the vacuum flash assembly respectively remove the coal gas in the coal gas water; the waste water filter is connected to the vacuum flash assembly and is used for filtering the waste water output by the vacuum flash assembly.

[0009] In some embodiments, the dust removal and filtration device includes a filtration assembly and a liquid seal; the filtration assembly includes a filter and a pressure-variable lock hopper arranged in sequence from upstream to downstream; the dust-containing coal gas output by the medium-pressure waste heat boiler is passed through the filter to remove the pulverized coal therein; the pulverized coal is introduced into the pressure-variable lock hopper, and after pressure relief, it is input downstream; the coal gas output by the filter enters the waste heat recovery device; the liquid seal is connected in parallel with the filter, and when the filter is blocked or the pressure difference becomes larger, the dust-containing coal gas output by the medium-pressure waste heat boiler enters the waste heat recovery device after passing through the liquid seal.

[0010] In some embodiments, the filter includes a plurality of filter element members extending in the vertical direction, and the air inlet of the filter is located at the bottom of the filter element members.

[0011] In some embodiments, the filtration assembly further includes an anti-blowing assembly arranged at the top of the filter to blow the coal dust on the surface of the filter into the pressure-variable lock hopper.

[0012] In some embodiments, the anti-blowing assembly includes a purging member, which is arranged corresponding to each filter element member and is located at the top of the filter element member.

[0013] In some embodiments, the filtration assembly further includes a cold ash machine; its inlet is connected to the pressure-variable lock hopper to cool the pulverized coal to normal temperature.

[0014] In some embodiments, the air inlet of the washing member is connected to the filter, its liquid inlet is connected to the coal gas water, and at the same time, the liquid outlet of the washing member is connected to the waste heat recovery device.

[0015] In some embodiments, a circulating water pump is arranged between the liquid inlets of the waste heat recovery device and the washing member.

[0016] In some embodiments, the air inlet of the purging member is connected to medium-pressure superheated steam at a temperature of 450 °C to purge the coal dust on the surface of the filter with the medium-pressure superheated steam.

[0017] In some embodiments, the waste water filter includes a waste water filter with a transfer pump arranged on the pipeline; the waste water filter is communicated with the vacuum flash assembly to treat the waste water.

[0018] Additional aspects and advantages of the present application will be given in part in the following description, become apparent in part from the following description, or be understood through the practice of the present application. Description of the Drawings

[0019] The above and / or additional aspects and advantages of the present application will become apparent and be readily understood from the following description of embodiments in conjunction with the accompanying drawings, where:

[0020] Figure 1 is a partial structural schematic diagram of a system for producing coal gas in the related art;

[0021] Figure 2 is a structural schematic diagram of a coal gas water flash evaporation system in the related art;

[0022] Figure 3 is a partial structural schematic diagram of a gasification device for anthracite or coke according to an embodiment of the present application;

[0023] Figure 4 is a structural schematic diagram of a dust removal and filtration device according to an embodiment of the present application;

[0024] Figure 5 is a structural schematic diagram of a dust removal and filtration device according to an embodiment of the present application;

[0025] Figure 6 is a structural schematic diagram of a coal gas water flash evaporation system according to an embodiment of the present application;

[0026] In the figure, 1, coal bunker; 2, coal lock; 3, gasification furnace; 4, cyclone separator; 5, medium-pressure waste heat boiler; 6, Venturi scrubber; 7, waste heat recovery device; 8, circulating water pump; 9, medium-pressure flash evaporator; 10, vacuum flash evaporator; 11, clarification tank; 12, plate and frame filter press; 13, gasification water buffer tank; 14, waste water filter element; 15, vacuum flash evaporation condenser; 16, vacuum flash evaporation separator; 17, gas-liquid separator.

[0027] 101, coal bunker; 20, coal lock; 30, gasification furnace; 40, dust removal and filtration device; 401, filter; 402, variable pressure lock hopper; 403, liquid seal member; 404, backflush assembly; 405, cold ash machine; 50, medium-pressure waste heat boiler; 60, scrubbing member; 70, waste heat recovery device; 80, circulating water pump; 90, medium-pressure flash evaporator; 100, vacuum flash evaporator; 110, vacuum flash evaporation condenser; 120, vacuum flash evaporation separator; 130, waste water filter; 140, gas-liquid separator. Detailed implementation manners

[0028] Embodiments of the present application will be described in detail below. Examples of the embodiments are shown in the accompanying drawings, where like or similar reference numerals denote like or similar elements or elements having like or similar functions throughout. The embodiments described below by referring to the drawings are exemplary and are only used to explain the present application and should not be construed as a limitation of the present application. On the contrary, the embodiments of the present application include all changes, modifications, and equivalents that fall within the spirit and scope of the appended claims.

[0029] Referring to Figure 1 - Figure 2 , in the related art, a system for producing coal gas by coal gasification is proposed, which includes a Saiding furnace (gasifier 3), a medium-pressure waste heat boiler 5, a waste heat recovery device 7, and a coal gas water flash evaporation system. The raw coal is pulverized coal. The raw coal enters the coal bin 1, and then enters the gasifier 3 through the coal lock 2 for pressurized gasification. The dust content of the dusty coal gas output from the gasifier 3 is 5-6 g / Nm 3 . The dusty coal gas enters the downstream cyclone separator 4 for dust removal and oil removal treatment. The cyclone separator 4 separates the pulverized coal and the coal gas in the dusty coal gas. However, the coal gas output from the cyclone separator 4 still contains a large amount of dust powder and enters the medium-pressure waste heat boiler 5. At this time, the normal temperature of the coal gas entering the medium-pressure waste heat boiler 5 is 500-550°C; while the coal gas enters the medium-pressure waste heat boiler 5, medium-pressure boiler feed water is introduced into the medium-pressure waste heat boiler 5. The medium-pressure boiler feed water and the coal gas exchange heat in the medium-pressure waste heat boiler 5, reducing the coal gas from 500-550°C to 300-330°C and outputting it. At the same time, the medium-pressure boiler feed water absorbs the heat of the coal gas to generate medium-pressure superheated steam. However, the upper tube sheet of the medium-pressure waste heat boiler 5 is prone to dust accumulation during operation. A dust removal and filtration device can be set at the gas outlet of the Saiding furnace to filter the dusty coal gas at the outlet of the gasifier 3, so that the coal gas output from the dust removal and filtration device contains almost no dust. However, during the transformation of the existing gasification device, due to layout limitations and pipeline stress, it is impossible to install an efficient dust removal and filtration device between the gas outlet of the Saiding furnace and the medium-pressure waste heat boiler 5.

[0030] The coal gas at 300-330°C passes through the Venturi scrubber 6, and high-pressure coal gas water is used to spray the coal gas. The coal gas and the coal gas water are jointly introduced into the waste heat recovery device 7 through the Venturi scrubber 6. In the waste heat recovery device 7, low-pressure boiler feed water is used to exchange heat with the coal gas. The heat-exchanged coal gas is separated by a gas-liquid separator 17 connected to the waste heat recovery device 7 to obtain crude coal gas and coal gas water; the crude coal gas is transported downstream, and the coal gas water separated by the gas-liquid separator 17 flows back to the waste heat recovery device 7; at the same time, the heat-exchanged low-pressure boiler feed water generates low-pressure steam and releases it to the outside.

[0031] Meanwhile, it should be noted that part of the gas water in the waste heat recovery device 7 is sent to the gas water flash evaporation system for treatment, and part of the supernatant liquid is utilized by setting a circulating water pump 8 between the waste heat recovery device 7 and the liquid inlet of the washing component and introducing it into the Venturi scrubber 6 to cool the newly introduced gas and remove dust and oil from the gas. However, the dust content in the circulating gas water is relatively large, resulting in serious wear of the pipelines and valves, and the circulation volume of the circulating water pump 8 is 200 m 3 / h, with a relatively large circulation volume.

[0032] In the related art, the gas water flash evaporation system includes a medium-pressure flash evaporator 9, a vacuum flash evaporator 10, a clarification tank 11, a plate and frame filter press 12, a gasification water buffer tank 13, a waste water filter component 14, etc.; that is, the gas water entering the gas water flash evaporation system passes through the high flash gas generated by the medium-pressure flash evaporator 9 and is transported to the downstream in sequence; the gas water output by the medium-pressure flash evaporator 9 then passes through the vacuum flash evaporator 10, and the true flash gas generated by the vacuum flash evaporator 10 passes through a vacuum flash condenser 15 and a vacuum flash separator 16 in sequence to obtain vacuum flash gas, and the vacuum degrees of the vacuum flash evaporator 10, the vacuum flash condenser 15, and the vacuum flash separator 16 are maintained by a vacuum pump. The gas water output by the vacuum flash evaporator 10 enters the clarification tank 11, and a flocculant is added to the clarification tank 11 to precipitate the dust coal in the gas water; after the gas water stays in the clarification tank 11 for a sufficient length of time, the liquid in the clarification tank 11 is output to the gasification water buffer tank 13, and the liquid in the gasification water buffer tank 13 is output to the waste water filter component 14 for filtration treatment; the slurry in the clarification tank 11 is fed into the plate and frame filter press 12 for pressure filtration, the formed filter cake is transported out, and the filtrate is returned to the clarification tank 11.

[0033] In the related art, the dust content in the dust-containing gas discharged from the bottom of the waste heat recovery device 7 is large and the dust floats in the water, resulting in a relatively large amount of dust in the gas phase during the flash evaporation process of the water entering the medium-pressure flash gas, and the flash gas cannot be efficiently utilized; the top of the vacuum flash evaporator 10 contains dust, resulting in dust accumulation in the vacuum flash condenser 15, poor heat exchange effect, ineffective guarantee of the vacuum pump inlet pressure, ineffective removal of ammonia nitrogen in the waste water at the bottom of the vacuum flash evaporator 10, high ammonia nitrogen content in the discharged waste water, and great difficulty in sewage treatment.

[0034] Therefore, during the transformation process of the existing gasification device in the related art, due to layout limitations and pipeline stress, it is impossible to install an efficient dust removal and filtration device between the gas outlet of the Saiding furnace and the medium-pressure waste heat boiler 5. The dust content in the dust-containing gas discharged from the bottom of the waste heat recovery device 7 is large and the dust floats in the water, resulting in a relatively large amount of dust in the gas phase during the flash evaporation process of the water entering the medium-pressure flash gas, and the flash gas cannot be efficiently utilized; the top of the vacuum flash evaporator 10 contains dust, resulting in dust accumulation in the vacuum flash condenser 15, poor heat exchange effect, ineffective guarantee of the vacuum pump inlet pressure, ineffective removal of ammonia nitrogen in the waste water at the bottom of the vacuum flash evaporator 10, high ammonia nitrogen content in the discharged waste water, and great difficulty in sewage treatment.

[0035] To achieve the above object, a gasification device for anthracite or coke proposed in this application includes: a gasification furnace 30, a dust removal and heat recovery component, and a coal gas water flash evaporation system; wherein the gasification furnace 30 is used for gasifying anthracite or coke. For example, the gasification furnace 30 is a Saiding furnace. In this embodiment, the raw coal is anthracite or coke. The anthracite or coke enters the coal bunker 101, and then enters the gasification furnace 30 through the coal lock 20 for pressurized gasification. This process is the same as the gasification process of raw coal in the related art and will not be elaborated here.

[0036] Particularly, the dust removal and heat recovery component includes a medium-pressure waste heat boiler 50, a dust removal and filtration device 40, and a heat recovery component. The dust removal and filtration device 40 is located downstream of the medium-pressure waste heat boiler 50 and is used for filtering the dust-containing coal gas output by the medium-pressure waste heat boiler 50. That is, the dust-containing coal gas output by the gasification furnace 30 enters the medium-pressure waste heat boiler 50 for heat exchange and cooling. In the medium-pressure waste heat boiler 50, medium-pressure boiler feed water is introduced to recover the heat in the dust-containing coal gas and generate medium-pressure superheated steam. Then, the medium-pressure waste heat boiler 50 outputs the cooled dust-containing coal gas, and this dust-containing coal gas enters the dust removal and filtration device 40 downstream of the medium-pressure waste heat boiler 50 for filtration treatment as Figure 3 shown. The dust removal and filtration device 40 includes a filtration component; the filtration component includes a filter 401 and a pressure-variable lock hopper 402 arranged in sequence from upstream to downstream. The dust-containing coal gas output by the medium-pressure waste heat boiler 50 is de-dusted of its pulverized coal through the filter 401; the pulverized coal is introduced into the pressure-variable lock hopper 402, depressurized, and then input downstream; the coal gas output by the filter 401 enters the waste heat recovery device 70. In other words, as Figure 4 shown, the gas inlet of the filter 401 is connected to the dust-containing coal gas outlet of the medium-pressure waste heat boiler 50. The dust-containing coal gas output by the medium-pressure waste heat boiler 50 is de-dusted of its pulverized coal through the filter 401. The pulverized coal outlet of the filter 401 is connected to the inlet of the pressure-variable lock hopper 402, and the pulverized coal is introduced into the pressure-variable lock hopper 402, depressurized, and then input downstream. After the dust-containing coal gas is de-dusted of its pulverized coal through the filter 401, the filtration efficiency of the filter element of the filter 401 can reach more than 99.5%. After the coal gas exits the filter 401, the dust content of the coal gas is lower than 30mg / Nm 3 and can be regarded as almost dust-free, which will reduce the dust-carrying amount of the coal gas water flash evaporation system and reduce the blockage of heat exchangers, etc., and can greatly improve the operation cycle and operation stability of the gasification device.

[0037] In addition, the dust removal and filtration device 40 in this application further includes a liquid seal member 403. The liquid seal member 403 is connected in parallel with the filter 401 and is arranged between the medium-pressure waste heat boiler 50 and the waste heat recovery device 70. That is, under certain working conditions, the dust-containing gas output by the medium-pressure waste heat boiler 50 enters the waste heat recovery device 70 after passing through the liquid seal member 403. For example, when the operating differential pressure of the filtration assembly reaches the set value, after the filter 401 is blocked or the differential pressure becomes larger, the dust-containing gas output by the medium-pressure waste heat boiler 50 can break through the liquid seal member 403 at the outlet of the medium-pressure waste heat boiler 50 to the downstream, so as to avoid the gasifier 30 from being pressurized and stopped.

[0038] The heat recovery assembly includes a waste heat recovery device 70 connected to the filter 401 through a washing member 60; the waste heat recovery device 70 recovers the heat in the gas and outputs raw gas and gas water. In other words, as Figure 3 shown, the dust-containing gas output by the gasifier 30 enters the medium-pressure waste heat boiler 50. At the same time, medium-pressure boiler feed water is introduced into the medium-pressure waste heat boiler 50. The medium-pressure boiler feed water and the dust-containing gas exchange heat in the medium-pressure waste heat boiler 50, reducing the temperature of the dust-containing gas from 500 - 550 °C to 300 - 330 °C, and at the same time generating medium-pressure superheated steam; the 300 - 330 °C dust-containing gas enters the filter 401 again for dust removal and purification to obtain gas. The gas first passes through the washing member 60. For example, the washing member 60 can be a Venturi scrubber. When the gas passes through the Venturi scrubber, high-pressure gas water is used to spray-wash the gas, and the gas and the gas water are jointly introduced into the waste heat recovery device 70 through the Venturi scrubber for gas cleaning and heat recovery as Figure 6 shown. In the waste heat recovery device 70, the waste heat is exchanged between the low-pressure boiler feed water and the gas. After heat exchange, the gas passes through a gas-liquid separator 140 for gas-liquid separation to obtain raw gas; the low-pressure boiler feed water after heat exchange generates low-pressure steam; the gas water separated by the gas-liquid separator 140 can be sent to the gas water flash evaporation system.

[0039] The gas water flash evaporation system in this application includes a medium-pressure flash evaporator 90, a vacuum flash evaporation assembly, and a waste water filtering member; the medium-pressure flash evaporator 90 and the vacuum flash evaporation assembly respectively remove the gas in the gas water; the waste water filtering member is connected to the vacuum flash evaporation assembly and is used for filtering the coal dust entrained in the waste water output by the vacuum flash evaporation assembly.

[0040] Therefore, this application improves the stable operation of the gas water flash evaporation system by adding an efficient dust removal and filtration device 40 at the dust-containing gas outlet of the medium-pressure waste heat boiler 50. While increasing the operation cycle of the gasification device, the overall operation and investment costs are reduced. Among them, only the cost saved by the flash steam per year can reach 1.8 million: the calculation method is 6 / 4 x 8000 x 150, and the cost saved in waste water treatment is 400,000, and the calculation method is 20 * 2.5 * 8000.

[0041] In some embodiments, the filter 401 includes multiple groups of filter elements extending in the vertical direction, and the air inlet of the filter 401 is located at the bottom of the filter elements.

[0042] For example, the filter 401 is a high-efficiency filter 401 that includes multiple groups of filter elements extending in the vertical direction, and each group of filter elements includes multiple filter elements; the air inlet of the filter 401 is located at the bottom of the filter elements, the pulverized coal outlet of the filter 401 is located below the filter elements, and the gas outlet of the filter 401 is located at the top of the filter elements; the inlet of the pressure-variable lock hopper 402 is connected to the pulverized coal outlet of the filter 401; the dust content of the dusty gas at the outlet of the medium-pressure waste heat boiler 50 is filtered to 10 mg / Nm 3 or less; the filtered pulverized coal is high-pressure dry coal dust, which is depressurized after passing through the pressure-variable lock hopper 402 and then input downstream after being reduced to atmospheric pressure.

[0043] In some embodiments, the filtration assembly further includes a backwashing assembly 404 disposed on the top of the filter 401 to blow the coal dust on the surface of the filter 401 into the pressure-variable lock hopper 402.

[0044] Among them, the filtration assembly further includes a backwashing assembly 404 disposed on the top of the filter 401. It can be known that during the filtration process of the filter 401, the pressure difference will gradually increase. The backwashing assembly 404 is disposed on the top of the filter 401 and can be backwashed according to the actual operating conditions to blow the fine pulverized coal on the surface of the filter 401 into the pressure-variable lock hopper 402 for storage. For example Figure 5 The backwashing assembly 404 shown includes a purging member, which is provided in one-to-one correspondence with the filter elements and is located on the top of the filter elements; under the set working conditions, the backwashing assembly 404 performs timed backwashing.

[0045] In some embodiments, a differential pressure detection alarm may be provided at the inlet and outlet of the filter 401. According to the operating conditions, when the differential pressure of the filter 401 increases, medium-pressure superheated steam at a temperature of 450 °C is introduced into the inlet of the purging member to purge the coal dust on the surface of the filter 401 with the medium-pressure superheated steam. By using medium-pressure superheated steam, the dust coal filtered by the filter element of the filter 401 is flushed into the pressure-variable lock hopper 402 for storage, restoring the filtering function of the filter 401 and saving the investment cost of the system. Among them, when the temperature of the medium-pressure superheated steam is relatively low, such as medium-pressure superheated steam at 300 °C, it is easy to contain liquid water and block the filter. When the differential pressure of the filter 401 increases to the point where the filtering function cannot be restored by backwashing with medium-pressure superheated steam, to prevent serious accidents caused by the pressure buildup in the gasifier 30, at this time, the gas passes through the liquid seal member 403 and enters the downstream. The liquid seal height of the liquid seal member 403 is matched with the maximum differential pressure of the filter 401. During normal operation, the differential pressure of the filter element of the filter 401 is about 3 - 5 kPa, and the maximum differential pressure shall not be greater than 10 kPa. The liquid seal height of the liquid seal member 403 is 1.5 m. When the differential pressure of the filter 401 increases to 15 kPa, the gas will break through the liquid seal member 403 and enter the downstream scrubbing member. After the control room plans to stop the vehicle according to the actual operating conditions, the filter 401 is overhauled, and the filter element of the filter 401 is taken out for flushing or replacement.

[0046] In some embodiments, the filtration assembly further includes a cold ash machine 405; its inlet is connected to the pressure-variable lock hopper 402 to cool the pulverized coal to room temperature.

[0047] Among them, the filtration assembly further includes a cold ash machine 405 as Figure 5 shown, the inlet of the cold ash machine 405 is connected to the pressure-variable lock hopper 402. After the pressure-variable lock hopper 402 is depressurized to atmospheric pressure, the pulverized coal enters the cold ash machine 405 and is cooled to room temperature and then pneumatically conveyed to downstream users. In some embodiments, program-controlled valves are provided between the lock hopper and the filter 401 and between the lock hopper and the cold ash machine 405. The fine ash filtered by the filter 401 enters the pressure-variable lock hopper 402. When the material level in the pressure-variable lock hopper 402 reaches the high material level, the program-controlled valve between the pressure-variable lock hopper 402 and the filter 401 is closed, and the lock hopper starts to depressurize from 4.0 MPa(g) until it reaches atmospheric pressure; then the program-controlled valve between the pressure-variable lock hopper 402 and the cold ash machine 405 is opened, and the fine ash in the lock hopper is discharged into the cold ash machine 405. After the coal ash is cooled, it is sent to the boiler for use. After the fine ash in the lock hopper is completely discharged, the program-controlled valve between the lock hopper and the cold ash machine 405 is closed, and the lock hopper is pressurized with high-pressure steam. After being pressurized to 4.0 MPa(g), the program-controlled valve between the lock hopper and the filter 401 is opened to start the next cycle.

[0048] Therefore, the working principle of the dust removal and filtration device 40 applicable to anthracite or coke gasification in this embodiment is as follows:

[0049] After the dusty coal gas at the outlet of the gasifier passes through the medium-pressure waste heat boiler 50, the temperature drops to ~300°C; the dusty coal gas is introduced into the filter 401, and the dusty coal gas is filtered from 5 - 6 g / Nm 3 to 10 mg / Nm 3 or less; the pulverized coal filtered from the dusty coal gas is introduced into the pressure swing lock hopper 402, depressurized to atmospheric pressure, and then enters the cold ash machine 405 to be cooled to room temperature, and then pneumatically conveyed to downstream users. The coal gas filtered by the filter 401 is introduced into the waste heat recovery device 70. As the filter 401 operates, the operating pressure difference of the filter 401 gradually increases. The backwashing assembly 404 provided at the top of the filter 401 can perform backwashing regularly according to the actual operating conditions, and blow the fine pulverized coal on the surface of the filter 401 into the pressure swing lock hopper 402 for storage; when the operating pressure difference of the filter element reaches the set value, the dusty coal gas output from the gasifier 30 can break through the liquid seal member 403 at the outlet of the gasifier 30 to downstream to avoid the gasifier 30 from being pressurized and shut down.

[0050] In some embodiments, the gas inlet of the scrubber 60 is connected to the filter 401, the liquid inlet of the scrubber 60 is introduced with coal gas water, and the liquid outlet of the scrubber 60 is connected to the waste heat recovery device 70.

[0051] Among them, the gas inlet of the scrubber 60 is connected to the filter 401 to introduce the coal gas with a dust content of 10 mg / Nm 3 or less after being purified by the filter 401 into the scrubber 60; the liquid inlet of the scrubber 60 is introduced with coal gas water to further wash and dedust the coal gas; the liquid outlet of the scrubber 60 is connected to the waste heat recovery device 70, so that the coal gas and the coal gas water are simultaneously introduced into the waste heat recovery device 70; at the same time, low-pressure boiler feed water is introduced into the waste heat recovery device 70 to realize the recovery of crude coal gas and the heat exchange of the coal gas.

[0052] In some embodiments, a circulating water pump 80 is provided between the liquid inlets of the waste heat recovery device 70 and the scrubber 60.

[0053] In this embodiment, a circulating water pump 80 is provided between the liquid inlets of the waste heat recovery device 70 and the scrubber 60 as Figure 3 shown, and the coal gas water in the waste heat recovery device 70 is reused to be introduced into the scrubber 60 to cool the newly introduced coal gas and remove dust from the coal gas; in the related art, due to the use of a cyclone separator to separate the dusty coal gas after gasification, the circulating coal gas water contains dust, resulting in serious wear of the pipeline and valves, and the circulating volume of the circulating water pump 80 is 200 m 3 / h, with a relatively large circulating volume; however, in this embodiment, the circulating coal gas water contains almost no coal dust, so that the circulating volume of the circulating water pump 80 is reduced to 60 m 3 / h while extending the service life of the pipeline and valves.

[0054] In some embodiments, the wastewater filtering member includes a wastewater filter 130 provided with a delivery pump on a pipeline; the wastewater filter 130 is communicated with a vacuum flashing assembly for treating wastewater.

[0055] In this embodiment, after the coal gas water enters the coal gas water flashing system, the coal gas in the coal gas water is removed through the medium-pressure flash evaporator 90 and the vacuum flashing assembly respectively. The vacuum flashing assembly includes a vacuum flash evaporator 100, a vacuum flash condenser 110, and a vacuum flash separator 120 for sending the vacuum flash steam to sulfur recovery. This is a conventional setting in the art and will not be elaborated here. However, in this embodiment, the wastewater output from the vacuum flash evaporator 100 directly enters the wastewater filtering member. The wastewater filtering member includes a wastewater filter 130 provided with a delivery pump on a pipeline, which can directly filter and treat the wastewater.

[0056] In summary, for the transformation of the anthracite or coke gasification device in this application, after adding a dust removal and filtration device 40 downstream of the medium-pressure waste heat boiler 50, the flashing effect can be effectively improved, and the efficient utilization of the flash steam can be improved. Among them, the operating cost of the transformed gasification device is reduced: the utilization rate of the by-product medium-pressure flash steam saves 2.2 million yuan in operating costs; after adding the filter 401, the estimated equipment costs of the pressure-changing lock hopper 402, the cold ash machine 405, the water seal tank, etc. are about 3.5 million yuan; the payback period is about 1.6 years, and the on-site blockage condition will be greatly optimized, and the heat exchange effect is improved.

[0057] It should be noted that in the description of this application, the terms "first", "second", etc. are only used for descriptive purposes and cannot be understood as indicating or implying relative importance. In addition, in the description of this application, unless otherwise specified, the meaning of "a plurality" is two or more.

[0058] Any process or method description shown in the flowchart or described in other ways herein can be understood as representing a module, segment, or part of code including one or more executable instructions for implementing a specific logical function or process. The scope of the preferred embodiments of this application includes additional implementations, where the functions can be executed in a substantially simultaneous manner or in a reverse order according to the involved functions, rather than in the order shown or discussed. This should be understood by those skilled in the technical field to which the embodiments of this application belong.

[0059] In the description of this specification, the description with reference to the terms "one embodiment", "some embodiments", "example", "specific example", or "some examples", etc. means that the specific features, structures, materials, or characteristics described in connection with the embodiment or example are included in at least one embodiment or example of this application. In this specification, the schematic representations of the above terms do not necessarily refer to the same embodiment or example. Moreover, the specific features, structures, materials, or characteristics described can be combined in a suitable manner in any one or more embodiments or examples.

[0060] Although the embodiments of the present application have been shown and described above, it can be understood that the above embodiments are exemplary and should not be construed as limiting the present application. Those of ordinary skill in the art can make changes, modifications, substitutions, and variations to the above embodiments within the scope of the present application.

Claims

1. A gasification device for anthracite or coke, characterized in that: include: A gasifier for gasifying anthracite or coke; A dust removal and heat recovery component, comprising a medium-pressure waste heat boiler, a dust removal and filtering device, and a heat recovery component; the dust-containing coal gas at the outlet of the gasifier enters the medium-pressure waste heat boiler to heat exchange and cool the dust-containing coal gas; the medium-pressure waste heat boiler outputs the cooled dust-containing coal gas to the dust removal and filtering device to filter and remove dust from the dust-containing coal gas and output the coal gas; the heat recovery component comprises a waste heat recovery device connected to the dust removal and filtering device through a washing unit, the waste heat recovery device recovers heat in the coal gas and outputs raw coal gas and coal gas water; and A coal gas water flash evaporation system comprises a medium-pressure flash evaporator, a vacuum flash evaporation component and a wastewater filter; the medium-pressure flash evaporator and the vacuum flash evaporation component respectively remove coal gas from coal gas water; the wastewater filter is connected to the vacuum flash evaporation component and is used to filter the wastewater output by the vacuum flash evaporation component.

2. The anthracite or coke gasification device according to claim 1, characterized in that: The dust removal and filtering device includes a filter assembly and a liquid seal; the filter assembly includes a filter and a transformer lock bucket arranged in sequence upstream and downstream; the dust-containing coal gas output by the medium-pressure waste heat boiler passes through the filter to remove the coal powder therein; the coal powder is passed into the transformer lock bucket to release the pressure and then input downstream; the coal gas output by the filter enters the waste heat recovery device; the liquid seal is connected in parallel with the filter, and when the filter is blocked or the pressure difference becomes large, the dust-containing coal gas output by the medium-pressure waste heat boiler passes through the liquid seal and enters the waste heat recovery device.

3. The anthracite or coke gasification device according to claim 2, characterized in that: The filter comprises a plurality of filter core members extending in a vertical direction, and the air inlet of the filter is located at the bottom of the filter core members.

4. The anthracite or coke gasification device according to claim 3, characterized in that: The filter assembly also includes a back-blowing assembly arranged on the top of the filter to blow the coal dust on the surface of the filter into the variable pressure lock bucket.

5. The anthracite or coke gasification device according to claim 4, characterized in that: The backflush assembly includes a purge component, which is arranged in one-to-one correspondence with the filter element and is located on the top of the filter element.

6. The anthracite or coke gasification device according to claim 4, characterized in that: The filter assembly also includes an ash cooler; the inlet of the cooler is connected to the voltage-changing lock bucket to cool the coal powder to room temperature.

7. The anthracite or coke gasification device according to any one of claims 1 to 6, characterized in that: The air inlet of the washing component is connected to a filter, and the gas water is introduced into the liquid inlet of the washing component; meanwhile, the liquid outlet of the washing component is connected to a waste heat recovery device.

8. The anthracite or coke gasification device according to claim 7, characterized in that: A circulating water pump is arranged between the waste heat recovery device and the liquid inlet of the washing component.

9. The anthracite or coke gasification device according to claim 5, characterized in that: Medium-pressure superheated steam with a temperature of 450° C. is introduced into the air inlet of the purge member to purge the coal dust on the surface of the filter with the medium-pressure superheated steam.

10. The anthracite or coke gasification device according to claim 6, characterized in that: The wastewater filter element comprises a wastewater filter provided with a delivery pump on a pipeline; the wastewater filter is connected to the vacuum flash evaporation component to process the wastewater.

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