WO2022105328A1 - 碎煤加压气化煤气水分离及回用系统及方法 - Google Patents

碎煤加压气化煤气水分离及回用系统及方法 Download PDF

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Publication number
WO2022105328A1
WO2022105328A1 PCT/CN2021/113367 CN2021113367W WO2022105328A1 WO 2022105328 A1 WO2022105328 A1 WO 2022105328A1 CN 2021113367 W CN2021113367 W CN 2021113367W WO 2022105328 A1 WO2022105328 A1 WO 2022105328A1
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water
gas
vacuum
pressure
gas water
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PCT/CN2021/113367
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English (en)
French (fr)
Inventor
左永飞
李小红
施福富
范辉
周恩利
刘丰力
韩鑫凤
袁辉峰
刘利利
李树枫
李叶珺
徐景亮
赵宇宏
王红林
车丽玮
张海峰
郭彦江
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赛鼎工程有限公司
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Publication of WO2022105328A1 publication Critical patent/WO2022105328A1/zh

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F9/00—Multistage treatment of water, waste water or sewage
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/12—Treatment of sludge; Devices therefor by de-watering, drying or thickening
    • C02F11/121—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering
    • C02F11/122—Treatment of sludge; Devices therefor by de-watering, drying or thickening by mechanical de-watering using filter presses
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/02—Treatment of water, waste water, or sewage by heating
    • C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
    • C02F1/06—Flash evaporation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/20—Treatment of water, waste water, or sewage by degassing, i.e. liberation of dissolved gases
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/40—Devices for separating or removing fatty or oily substances or similar floating material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2301/00—General aspects of water treatment
    • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F3/00—Biological treatment of water, waste water, or sewage

Definitions

  • the invention relates to the technical field of gas separation and reuse, in particular to a system and method for water separation and reuse of crushed coal pressurized gasification gas.
  • the crude gas produced by the pressurized gasification of crushed coal contains a large amount of water vapor, dust and carbonized by-products, such as tar, light oil, naphthalene, phenol, fatty acid, dissolved gas and inorganic salts, etc., and the temperature is also high . Therefore, it needs to be cooled and washed to reduce the temperature and remove harmful substances in the raw gas. During the washing and cooling process of the crude gas, these impurity components enter the water to form gas water with multiple components in the three states of gas, liquid and solid. The content of various ingredients is also not the same. Gas water cannot be directly treated by conventional biochemical, filtration, reverse osmosis and other methods. Oil, dust, phenol, ammonia, etc. must be separated and recovered. On the one hand, valuable substances in wastewater are recovered, which can produce certain Economic benefits; on the other hand, the wastewater can meet the influent requirements of general wastewater treatment methods, and then be discharged after biochemical treatment to meet the national discharge standards.
  • the flashed gas water enters the lower tar separator to separate the gas water and tar by using the density difference, and the dusty tar with a density greater than water is discharged from the bottom, which can be used as a product or returned to the gasifier for gasification again; density Light oil and gas water smaller than water overflow from the upper part of the tar separator into the gas water buffer tank, part of the gas water is sent back to the gasification cycle by the high pressure pump, and the excess gas water enters the light oil separator.
  • the light oil separator is equipped with coke and TPI plate components. On the one hand, impurities are filtered, and on the other hand, the oil droplets are condensed and float on the water surface to form an oil layer.
  • the light oil is led out through the upper overflow weir and sent to the oil storage tank.
  • the water enters the water chamber after passing through the TPI plate, and is then drawn out through the overflow weir.
  • the water is pumped into the dual-media filter for further dust removal and then sent to the phenol and ammonia recovery device.
  • the purpose is to remove the dust, oil and The dissolved gas is separated, most of the water is used for recycling, and a small part of the water is further deoiled, ammonia distilled, and dephenolized, and then the water quality is de-biochemically treated to meet the biochemical requirements.
  • the existing gas water treatment system aggregates different types of gas water from different equipment for gas water separation and recovery. There are multiple separators and buffers in the device process, which not only causes the entire gas water separation and recovery. The system occupies a large area, high investment, high operating cost, long process and many equipments, which make many pollutant discharge points and easily cause serious environmental pollution.
  • the present invention provides a system and method for separating and reusing crushed coal pressurized gasification gas water.
  • the technical scheme adopted in the present invention is: a system for separating and reusing crushed coal pressurized gasification gas water, which comprises a medium pressure flasher, a first vacuum flasher, a settling tank, a gas water tank, Deacidification tower, first vacuum flash separator, ammonia distillation tower, second vacuum flasher, second vacuum flash separator, third vacuum flash separator, flocculant tank, filter press, filtrate tank, several Water pump and pipeline, wherein: the first water inlet of the medium pressure flasher is connected with the transformation high temperature condensate pipeline, the second water inlet of the medium pressure flasher is connected with the gasification dust-containing gasification water pipeline, the medium pressure flasher The water outlet of the evaporator is connected with the first water inlet of the first vacuum flasher through the pipeline, the second water inlet of the first vacuum flasher is connected with the low-pressure gasification gas water pipeline, and the third water inlet of the first vacuum flasher is connected with the water pipeline.
  • the low-pressure start-up gas water pipeline is connected, the water outlet of the first vacuum flasher is connected to the water inlet of the sedimentation tank through the pipeline and the water pump, and the water outlet of the sedimentation tank is connected to the water inlet of the filter press through the pipeline and the water pump.
  • the water outlet of the filtrate tank is connected with the water inlet of the filtrate tank through the pipeline, the water outlet of the filtrate tank is connected with the water inlet of the sedimentation tank through the pipeline and the water pump, and the water inlet of the sedimentation tank is also connected with the outlet of the flocculant tank through the pipeline.
  • the gas water outlet of the settling tank is connected with the gas water inlet of the gas water tank through the pipeline, and the gas water outlet of the gas water tank is connected with the gas water biochemical treatment equipment and the gas water reuse equipment through the pipeline and the water pump.
  • the top of the gas water tank is sealed with the inert gas pipeline; the air outlet of the medium pressure flasher is connected to the air inlet of the deacidification tower through the pipeline, and the water inlet of the second vacuum flasher is connected to the transformation low temperature condensate pipeline.
  • the water outlet of the second vacuum flasher is connected to the first water inlet of the deacidification tower through a pipeline and a water pump, and the water outlet of the deacidification tower is connected to the water inlet of the ammonia distillation tower through a pipeline and a water pump, and the water outlet of the ammonia distillation tower It is connected with the crude gas washing equipment; the air outlet of the first vacuum flasher is connected to the air inlet of the first vacuum flash separator through a pipeline, and the air outlet of the first vacuum flash separator is connected to the third vacuum flasher through a pipeline.
  • the air inlet of the steam separator is connected, the water outlet of the first vacuum flash separator is connected to the second water inlet of the deacidification tower through a pipeline and a water pump; the air outlet of the second vacuum flasher is connected to the second vacuum through a pipeline
  • the air inlet of the flash separator is connected, the air outlet of the second vacuum flash separator is connected to the air inlet of the third vacuum flash separator through a pipeline, and the water outlet of the second vacuum flash separator is connected through a pipeline It is connected with the second water inlet of the deacidification tower, and the water outlet of the third vacuum flash separator is connected with the second water inlet of the deacidification tower through a pipeline.
  • the crushed coal pressurized gasification gas water separation and reuse system further includes an oil collecting float and an oil tank, the oil collecting float is arranged inside the gas water tank, and the bottom of the oil collecting float is connected to the oil tank through a hose.
  • a cooling water jacket is provided outside the gas water tank and the breathing gas discharge pipeline at the top of the settling tank.
  • a method for separating and reusing crushed coal pressurized gasification gas water comprising the following steps: S1, transforming high temperature condensate and gasification dust-containing gasification water after degassing by a medium pressure flasher, and degassing them with gasification low pressure gas water and gas
  • S1 transforming high temperature condensate and gasification dust-containing gasification water after degassing by a medium pressure flasher, and degassing them with gasification low pressure gas water and gas
  • the coal gas and water of the melting car enter the first vacuum flasher together and the dissolved gas is deeply removed in the first vacuum flasher;
  • S2 the gas water after the dissolved gas is mixed with the flocculant from the flocculant tank and then sent to the settling tank;
  • S3 the solid material settled at the bottom of the settling tank is dehydrated by the filter press to make mud cake, the filtrate generated by the pressure filtration and dehydration enters the filtrate tank and returns to the settling tank, and the gas water in the upper part of
  • a part of the gas water in the water tank is used as the washing water for the gasification of low-pressure gas water and is reused by the gas water reuse equipment, and the remaining gas water goes to the gas water biochemical treatment equipment;
  • the bottom of the acid tower is sprayed into the deacidification tower as the heat source of the deacidification tower, and the acid gas in the flash gas is removed from the deacidification tower at the same time; S5, the low temperature condensate is transformed into and de-dissolved in the second vacuum flasher, and the dissolved gas is removed.
  • the latter gas water is then sent to the deacidification tower for deacidification; S6, the condensate formed by the flashing of the first vacuum flasher and the second vacuum flasher enters the first vacuum flasher and the second vacuum flasher respectively. After the vacuum flash separation, it continues to enter the third vacuum flash separator for vacuum flash separation, and the condensed liquid condensed through the first vacuum flash separator, the second vacuum flash separator and the third vacuum flash separator From the top of the deacidification tower, it is sent to the deacidification tower for deacidification; S7, the deacidification gas desulfurization recovery equipment obtained from the deacidification of the deacidification tower, the gas water after the deacidification of the deacidification tower enters the ammonia distillation tower, and the ammonia distillation tower The gas water after steaming ammonia is used as washing water for the recycling of crude gas washing equipment, and the ammonia water/liquid ammonia produced in the ammonia steaming tower is recycled and reused.
  • the transformed high-temperature condensate is gas water with a dust content of not more than 2000 mg/L, a temperature of 150-190 ° C, and a pressure of 3.0-7.0 MPa;
  • the gasified dust-containing gasified water is the dust-containing water Gas water with a temperature of 180-200°C and a pressure of 3.0-7.0MPa not more than 3000mg/L;
  • the transformation low temperature condensate is a dust content less than 50mg/L, a temperature of 40-80°C, and a pressure of 3.0-5.0 MPa gas water;
  • the low-pressure gasification gas water is gas water with a dust content of less than 100 mg/L, a temperature of 60-80 °C, and a pressure of 0.5-0.7 MPa;
  • the low-pressure start-up gas water is a gas water with a dust content of less than 200 mg /L gas water with temperature of 60-80°C and pressure of 0.5-0.7MPa.
  • the flash temperature of the medium-pressure flash evaporator is 140-160° C. and the pressure is 0.4-0.5 MPa.
  • the flash temperature of the first vacuum flasher is 80-86° C. and the vacuum degree is 50-60 kPa.
  • the added amount of the flocculant is 1 ton of coal gas water and 3-5 g of the flocculant.
  • inert gas is continuously introduced into the top of the settling tank and the gas water tank.
  • the beneficial effects of the present invention are as follows: 1.
  • gas water of different classifications such as high temperature condensate, gasification dust-containing gasification water, low temperature condensate, gasification low pressure gas water and gasification start-up gas water.
  • gas water of different classifications such as high temperature condensate, gasification dust-containing gasification water, low temperature condensate, gasification low pressure gas water and gasification start-up gas water.
  • the whole system of the present invention has simple equipment, safe and stable operation, and can effectively reduce the cost of gas water treatment.
  • FIG. 1 is a schematic diagram of the system composition of the present invention.
  • FIG. 2 is a schematic diagram of the connection relationship between the present invention and the gasification unit, the washing unit and the transformation unit.
  • the crushed coal pressurized gasification gas-water separation and reuse system in this embodiment includes a medium-pressure flasher 1, a first vacuum flasher 2, a settling tank 3, a gas-water tank 4, a dehydrator Acid tower 5, first vacuum flash separator 6, ammonia distillation tower 7, second vacuum flasher 8, second vacuum flash separator 9, third vacuum flash separator 10, flocculant tank 11, filter press Machine 12, filtrate tank 13, several water pumps and pipelines, wherein: the first water inlet of the medium pressure flasher 1 is connected with the pipeline for converting high temperature condensate, and the second water inlet of the medium pressure flasher 1 is connected to the gasification
  • the dust gasification water pipeline is connected, the water outlet of the medium pressure flasher 1 is connected to the first water inlet of the first vacuum flasher 2 through the pipeline, and the second water inlet of the first vacuum flasher 2 is connected to the low pressure gasification gas water pipeline Connection, the third water inlet of the first vacuum flasher 2 is connected with the low-pressure start-up gas water pipeline, the water outlet of the
  • the water inlet of the filter press 12 is connected to the water inlet of the filter press 12 through the pipeline and the water pump, the water outlet of the filter press 12 is connected to the water inlet of the filtrate tank 13 through the pipeline, and the water outlet of the filtrate tank 13 is connected to the sedimentation tank 3 through the pipeline and the water pump.
  • the water inlet is connected, the water inlet of the sedimentation tank 3 is also connected with the discharge port of the flocculant tank 11 through the pipeline, the gas water outlet of the sedimentation tank 3 is connected with the gas water inlet of the gas water tank 4 through the pipeline, and the gas water tank 4
  • the gas water outlet is connected with the gas water biochemical treatment equipment (coal lock gas washing equipment and driving gas washing equipment) and the gas water recycling equipment through pipelines and water pumps, and the top of the settling tank 3 and the gas water tank 4 is connected with the inert gas pipe.
  • the air outlet of the medium pressure flasher 1 is connected with the air inlet of the deacidification tower 5 through the pipeline
  • the water inlet of the second vacuum flasher 8 is connected with the shift low temperature condensate pipeline
  • the second vacuum flasher 8 The water outlet is connected with the first water inlet of the deacidification tower 5 through the pipeline and the water pump
  • the water outlet of the deacidification tower 5 is connected with the water inlet of the ammonia distillation tower 7 through the pipeline and the water pump
  • the water outlet of the ammonia distillation tower 7 is connected with the water inlet of the ammonia distillation tower 7.
  • the crude gas washing equipment is connected; the air outlet of the first vacuum flasher 2 is connected to the air inlet of the first vacuum flash separator 6 through a pipeline, and the air outlet of the first vacuum flash separator 6 is connected to the third vacuum flasher 6 through a pipeline.
  • the air inlet of the vacuum flash separator 10 is connected, and the water outlet of the first vacuum flash separator 6 is connected with the second water inlet of the deacidification tower 5 through pipelines and a water pump; the air outlet of the second vacuum flasher 8 is connected by The pipeline is connected to the air inlet of the second vacuum flash separator 9, the air outlet of the second vacuum flash separator 9 is connected to the air inlet of the third vacuum flash separator 10 through the pipeline, and the second vacuum flash separator 9
  • the water outlet of the steam separator 9 is connected to the second water inlet of the deacidification tower 5 through a pipeline, and the water outlet of the third vacuum flash separator 10 is connected to the second water inlet of the deacidification tower 5 through a pipeline.
  • a gasification unit, a washing unit and a transformation unit are connected before the pressurized coal gasification gas water separation and reuse system according to the embodiment of the present invention.
  • the crushed coal raw material is added to the crushed coal pressurized gasifier through the coal hopper for pressurized gasification to generate gasified crude gas.
  • the gasified crude gas is dedusted by the cyclone separator before reaching the waste heat boiler, and the waste heat boiler recovers the gas After the heat in the medium is removed, the gas will continue to be dedusted in three stages by the Venturi washing equipment and the crude gas washing equipment, and then sent to the conversion equipment, precooler, intermediate and final cooling equipment and ammonia washing tower in the conversion unit.
  • the crushed coal is any one of anthracite, coke or semi-coke.
  • the precooler produces a high-temperature condensate that is transformed.
  • the intermediate and final cooling equipment and the ammonia washing tower produce shifted cryogenic condensate.
  • the Venturi scrubber produces gasified dust-laden gasified water.
  • Coal lock gas scrubbing equipment produces low pressure gasification gas water.
  • the driving gas washing equipment produces low pressure driving gas water.
  • the crushed coal pressurized gasification gas-water separation and reuse system further includes an oil-collecting float 14 and an oil tank 15, the oil-collecting float 14 is arranged inside the gas-water tank 4, and the bottom of the oil-collecting float 14 passes through a hose. Connected with the oil tank 15, the height of the oil collecting float 14 can change with the liquid level in the gas water tank 4, and the light oil floating on the upper part of the gas water tank 4 can enter the oil collecting float 14 and be collected into the oil tank 15 through a hose, The collection of light oil is achieved.
  • a cooling water jacket 16 is provided outside the breathing gas discharge pipes at the top of the gas water tank 4 and the settling tank 3 .
  • the cooling water jacket 16 can cool the breathing gas discharged from the breathing gas discharge pipe at the top of the gas water tank 4 and the settling tank 3, so that the condensable odor can be condensed and flow back to the equipment, so as to avoid VOCs or odor from the gas water.
  • Tank 4 and settling tank 3 discharge.
  • the embodiment of the present invention also provides a method for separating and reusing the pressurized gasification gas of crushed coal. It is realized by a gas-water separation and reuse system, which specifically includes the following steps.
  • the flashing temperature of the medium pressure flasher 1 is 140-160° C. and the pressure is 0.4-0.5 MPa.
  • the flashing temperature of the first vacuum flasher 2 is 80-86° C., and the vacuum degree is 50-60 kPa.
  • the added amount of the flocculant is 1 ton of coal gas water and 3-5 g of the flocculant.
  • the solid material settled at the bottom of the settling tank 3 is dehydrated by the filter press 12 to make mud cake, and the filtrate generated by the pressure filtration and dehydration enters the filtrate tank 13 and returns to the settling tank 3 again, and the gas water at the top of the settling tank 3 sends Into the gas water tank 4, a part of the gas water in the gas water tank 4 is used as the washing water for gasification of low-pressure gas water for the gas water reuse equipment (coal lock gas washing equipment and driving gas washing equipment), and the remaining gas water goes to Gas water biochemical treatment equipment.
  • the flash steam flashed from the medium pressure flasher 1 is sprayed into the deacidification column 5 from the bottom of the deacidification column 5 as the heat source of the deacidification column 5, and the acid gas in the flash steam is removed from the deacidification column 5 at the same time.
  • the transformed low-temperature condensate enters and is de-dissolved in the second vacuum flasher 8, and the gas water after the de-dissolved gas is removed is sent to the deacidification tower 5 for deacidification.
  • the condensate formed by the flashing of the first vacuum flasher 2 and the second vacuum flasher 8 respectively enters the first vacuum flasher 6 and the second vacuum flasher 9 for vacuum flash separation, and then continues to enter the first vacuum flasher 6 and the second vacuum flasher 9 respectively.
  • the three vacuum flash separators 10 carry out vacuum flash separation, and the condensed liquid condensed through the first vacuum flash separator 6, the second vacuum flash separator 9 and the third vacuum flash separator 10 is removed from the deacidification tower 5. The top is sent to deacidification tower 5 for deacidification.
  • the deacidification gas desulfurization recovery equipment obtained by the deacidification of the deacidification tower 5 the gas water after the deacidification of the deacidification tower 5 enters the ammonia distillation tower 7, and the gas water after the ammonia distillation in the ammonia distillation tower 7 is used as washing water as The crude gas washing equipment is reused, and the ammonia water/liquid ammonia produced in the ammonia distillation tower 7 is recycled and reused.
  • the transformed high-temperature condensate is gas water with a dust content of not more than 2000 mg/L, a temperature of 150-190 °C, and a pressure of 3.0-7.0 MPa; 3000mg/L gas water with a temperature of 180-200°C and a pressure of 3.0-7.0MPa;
  • the transformation low temperature condensate is one with a dust content of less than 50mg/L, a temperature of 40-80°C and a pressure of 3.0-5.0MPa Gas water;
  • the low-pressure gasification gas water is gas water with a dust content of less than 100 mg/L, a temperature of 60-80 °C, and a pressure of 0.5-0.7 MPa;
  • the low-pressure start-up gas water is a gas water with a dust content of less than 200 mg/L , Gas water with temperature of 60-80°C and pressure of 0.5-0.7MPa.
  • inert gas is continuously introduced into the top of the settling tank 3 and the gas water tank 4, so that the interior of the settling tank 3 and the gas water tank 4 always maintains a slight positive pressure (0.2-0.5 kPa) greater than 0.2 kPa.
  • the crushed coal in this embodiment is Jincheng anthracite with a water content of 5%.
  • the coal sample is crushed and sieved to obtain a coal sample with a particle size of 5-50 mm, which is loaded into a crushed coal pressurized gasifier for crushed coal pressurized gasification , the gasification pressure is 4.0MPa, and the gasification temperature is 1250°C.
  • the crude gas produced by gasification is divided into high temperature gas water and low temperature gas water according to the dust content, temperature and pressure in the water during washing. Temperature and pressure are divided into high temperature condensate and gasification dust-containing gasification water, low temperature gas water is divided into low temperature condensate conversion, low pressure gasification gas water and low pressure driving gas water according to dust content, temperature and pressure.
  • the above coal samples are processed by the gasification unit, washing unit and conversion unit, and the dust content of the transformed high-temperature condensate is 1900 mg/L, the temperature is 150 °C, and the pressure is 4 MPa, and the dust content of the gasification dust-containing gasification water is 2800 mg/L, temperature of 189°C, and pressure of 4.0 MPa.
  • the dust content of the transformed low-temperature condensate is 45mg/L, the temperature is 67.5°C, and the pressure is 3.75MPa.
  • the dust content of the low-pressure gasification gas water is 90mg/L, the temperature is 70°C, and the pressure is 0.5MPa.
  • the dust content is 180mg/L, the temperature is 65°C, and the pressure is 0.65MPa.
  • the transformed high-temperature condensate and gasification dust-containing gasification water are first degassed by the medium pressure flasher 1, and then enter the first vacuum flasher 2 together with the gasification low pressure gas water and the gasification start-up gas water to remove the dissolved gas in depth.
  • the flashing temperature of the flasher 1 is 144°C
  • the pressure is 0.4MPa
  • the flashing temperature of the first vacuum flasher 2 is 84.8°C
  • the vacuum degree is 50kPa
  • the gas water after de-dissolved gas is added according to 1 ton of gas water
  • the proportion of 3g flocculant is added into the flocculant and mixed and then sent to the settling tank 3.
  • the solid material settled at the bottom of the settling tank 3 is dehydrated by the filter press 12 to make a mud cake with a water content of 22%, and the filtrate enters the filtrate tank 13. Then return to the settling tank 3, and the gas water in the upper part of the settling tank 3 is sent to the gas water tank 4 as the washing water of the gasification low-pressure gas water, which is reused for the coal lock gas washing equipment and the driving gas washing equipment, and the biochemical treatment of the remaining degassing water. equipment.
  • the flash steam flashed from the medium pressure flasher 1 is injected from the bottom of the deacidification tower 5 as a heat source of the deacidification tower 5, and the acid gas in the flash steam is removed at the same time.
  • the low temperature condensate is transformed into and de-dissolved gas in the second vacuum flasher 8, and the gas water after the dissolved gas is removed is sent to the deacidification tower 5 for deacidification; the first vacuum flasher 2 and the second vacuum flasher 8
  • the condensate formed by flashing enters the first vacuum flash separator 6 and the second vacuum flash separator 9 respectively for vacuum flash separation, and then continues to enter the third vacuum flash separator 10 for vacuum flash separation.
  • a vacuum flash separator 6, the second vacuum flash separator 9 and the condensed liquid of the third vacuum flash separator 10 are sent into the deacidification tower 5 from the top of the deacidification tower 5 for deacidification; the deacidification tower 5
  • the operating pressure of the entire gas-water separation and reuse process is a micro-positive pressure operation greater than 0.2kPa.
  • the top of the settling tank 3 and the gas-water tank 4 is continuously supplied with an inert gas as a protective gas to ensure that the system pressure is greater than 0.2kPa micro-positive pressure , so that VOCs and odors in the system can be collected in a centralized manner, by-product steam from incineration or RTO.
  • the function of continuously feeding inert gas into the sedimentation tank 3 and the gas water tank 4 to seal their tops is mainly to prevent the negative pressure of the sedimentation tank 3 and the gas water tank 4 from inhaling air from their breathing valves to keep the tank slightly positive.
  • the normal pressure setting value of the sealing valve should be 0.2kPa, and the intersection with the set pressure of the breathing valve, single exhalation valve or control valve should be avoided to generate unnecessary inert gas circulation and high operating costs.
  • the pressure gasification of anthracite crushed coal in the embodiment of the present invention utilizes the characteristics of low oil content, low COD content and low dust content in the gas water.
  • anthracite is used for pressurized gasification. Since anthracite has low water content, generally the total water content is below 10%, the volatile matter is less than 10%, the carbon content is high, the coal ash melting point is high, and the ash content is high.
  • the true density is generally 1.4-1.8g/cm 3 , the mineral content of anthracite is high, and the true density is 1.8-1.9g/cm 3 .
  • the thermal stability of anthracite is high, and it is not easy to powder into the gasifier. The amount of coal dust brought out of the gasifier is small, and the density difference between the coal dust particles and the gas water is about large, so the coal dust is easier to separate, and the residence time of the dusty gas water separator can be shortened.
  • the water quality requirements for entering the biochemical treatment equipment are generally COD less than or equal to 3500mg/L, pH between 8.0-9.0, oil content less than or equal to 50mg/L, and BOD not more than 1100mg/L.
  • the current gas water effluent and reuse indicators are shown in Table 3. The oil content of the gas water removed from the biochemical treatment equipment is high, and it needs to be oxidized before entering the biochemical treatment to reduce the COD content.
  • the ammonia content and COD content of the gas water going to the biochemical treatment equipment and the gas water for reuse of the gas water are far less than those obtained by the current gas water separation and recovery system and method. gas water.
  • the crushed coal in this example is Jincheng anthracite with a water content of 6%.
  • the coal sample is crushed and sieved to obtain a coal sample with a particle size of 5-50 mm, which is loaded into the crushed coal pressurized gasifier for crushed coal pressurized gasification , the gasification pressure is 5.0MPa, and the gasification temperature is 1250°C.
  • the crude gas produced by gasification is divided into high temperature gas water and low temperature gas water according to the dust content, temperature and pressure in the water during washing. Temperature and pressure are divided into high temperature condensate and gasification dust-containing gasification water, low temperature gas water is divided into low temperature condensate conversion, low pressure gasification gas water and low pressure driving gas water according to dust content, temperature and pressure.
  • the dust content of the transformed high-temperature condensate obtained from the above coal samples processed by the gasification unit, the washing unit and the transformation unit is 1800 mg/L, the temperature is 158 °C, and the pressure is 5 MPa, and the dust content of the gasification dust-containing gasification water is 1985mg/L, temperature 196°C, pressure 5.0MPa.
  • the dust content of the transformed low-temperature condensate is 48mg/L, the temperature is 70.5°C, and the pressure is 4.75MPa.
  • the dust content of the low-pressure gasification gas water is 98mg/L, the temperature is 72°C, and the pressure is 0.6MPa.
  • the dust content of water was 180 mg/L, the temperature was 75°C, and the pressure was 0.55 MPa.
  • the high-temperature condensate of the transformation and the gasification dust-containing gasification water are first degassed by the medium pressure flasher 1, and then enter the first vacuum flasher 2 together with the gasification low pressure gas water and the gasification start-up gas water to remove the dissolved gas in depth.
  • the flash temperature of the evaporator 1 is 148°C
  • the pressure is 0.5MPa
  • the flash temperature of the first vacuum flasher 2 is 86°C
  • the vacuum degree is 60kPa
  • the gas water after the de-dissolved gas is added with 4.5 ton of gas water according to 1 ton.
  • the proportion of g flocculant is added into the flocculant and mixed and then sent to the settling tank 3.
  • the solid material settled at the bottom of the settling tank 3 is dehydrated by the filter press 12 to make a mud cake with a water content of 28%, and the filtrate enters the filtrate tank 13. Then return to the settling tank 3, and the gas water in the upper part of the settling tank 3 is sent to the gas water tank 4 as the washing water of the gasification low-pressure gas water, which is reused for the coal lock gas washing equipment and the driving gas washing equipment, and the remaining degas water biochemical treatment equipment. .
  • the flash steam flashed from the medium pressure flasher 1 is injected from the bottom of the deacidification tower 5 as a heat source of the deacidification tower 5, and the acid gas in the flash steam is removed at the same time.
  • the low temperature condensate is transformed into and de-dissolved gas in the second vacuum flasher 8, and the gas water after the dissolved gas is removed is sent to the deacidification tower 5 for deacidification; the first vacuum flasher 2 and the second vacuum flasher 8
  • the condensate formed by flashing enters the first vacuum flash separator 6 and the second vacuum flash separator 9 respectively for vacuum flash separation, and then continues to enter the third vacuum flash separator 10 for vacuum flash separation.
  • a vacuum flash separator 6, the second vacuum flash separator 9 and the condensed liquid of the third vacuum flash separator 10 are sent into the deacidification tower 5 from the top of the deacidification tower 5 for deacidification; the deacidification tower 5
  • the operating pressure of the entire gas-water separation and reuse process is operated with a slight positive pressure greater than 0.2kPa.
  • the top of the sedimentation tank 3 and the gas-water tank 4 is continuously supplied with an inert gas as a protective gas to ensure that the system pressure is greater than 0.2kPa.
  • the slight positive pressure operation, the system Middle VOCs and odors can be collected in a centralized manner, by-product steam from incineration or RTO.
  • the function of continuously feeding inert gas into the sedimentation tank 3 and the gas water tank 4 to seal their tops is mainly to prevent the negative pressure of the sedimentation tank 3 and the gas water tank 4 from inhaling air from their breathing valves to keep the tank slightly positive.
  • the normal pressure setting value of the sealing valve should be 0.2kPa, and the intersection with the set pressure of the breathing valve, single exhalation valve or control valve should be avoided, resulting in unnecessary inert gas circulation and high operating costs.
  • the crushed coal in this example is Yangquan anthracite with a water content of 8%.
  • the coal sample is crushed and sieved to obtain a coal sample with a particle size of 5-50 mm, which is loaded into the crushed coal pressurized gasifier for crushed coal pressurized gasification , the gasification pressure is 7.0MPa, and the gasification temperature is 1350°C.
  • the crude gas produced by gasification is divided into high temperature gas water and low temperature gas water according to the dust content, temperature and pressure in the water during washing, and the high temperature gas water is based on the dust content.
  • temperature and pressure are divided into transformation of high temperature condensate and gasification of dust-containing gasification water
  • low temperature gas water is divided into transformation of low temperature condensate
  • low pressure gasification gas water and low pressure driving gas water according to dust content, temperature and pressure.
  • Different types of gas water are separated and reused separately. The whole process of separation and reuse of gas water is maintained at a slight positive pressure of more than 0.2kPa and protected by inert gas to ensure that VOCs and odors in the system can be centrally treated.
  • the dust content of the transformed high-temperature condensate obtained from the above-mentioned coal samples processed by the gasification unit, the washing unit and the transformation unit is 1785 mg/L, the temperature is 170 °C, and the pressure is 7 MPa, and the dust content of the gasification dust-containing gasification water is 1650 mg/L, temperature of 197°C, and pressure of 7.0 MPa.
  • the dust content of the transformed low-temperature condensate is 35mg/L, the temperature is 67.5°C, and the pressure is 3.75MP.
  • the dust content of the low-pressure gasification gas water is 65mg/L, the temperature is 70°C, and the pressure is 0.5MPa.
  • the dust content of water was 150 mg/L, the temperature was 60°C, and the pressure was 0.5 MPa.
  • the high-temperature condensate of the transformation and the gasification dust-containing gasification water are first degassed by the medium pressure flasher 1, and then enter the first vacuum flasher 2 together with the gasification low pressure gas water and the gasification start-up gas water to remove the dissolved gas in depth.
  • the flash temperature of the evaporator 1 is 144°C
  • the pressure is 0.4MPa
  • the flash temperature of the first vacuum flasher 2 is 84.8°C
  • the vacuum degree is 50kPa
  • the gas water after de-dissolved gas is added with 4.8 ton of gas water according to 1 ton of gas water.
  • the proportion of g flocculant is added into the flocculant and mixed and then sent to the settling tank 3.
  • the solid material settled at the bottom of the settling tank 3 is dehydrated by the filter press 12 to make a mud cake with a water content of 28%, and the filtrate enters the filtrate tank 13. Then return to the settling tank 3, and the gas water in the upper part of the settling tank 3 is sent to the gas water tank 4 as the washing water of the gasification low-pressure gas water, which is reused for the coal lock gas washing equipment and the driving gas washing equipment, and the remaining degas water biochemical treatment equipment. .
  • the flash steam flashed from the medium pressure flasher 1 is injected from the bottom of the deacidification tower 5 as a heat source of the deacidification tower 5, and the acid gas in the flash steam is removed at the same time.
  • the low temperature condensate is transformed into and de-dissolved gas in the second vacuum flasher 8, and the gas water after the dissolved gas is removed is sent to the deacidification tower 5 for deacidification; the first vacuum flasher 2 and the second vacuum flasher 8
  • the condensate formed by flashing enters the first vacuum flash separator 6 and the second vacuum flash separator 9 respectively for vacuum flash separation, and then continues to enter the third vacuum flash separator 10 for vacuum flash separation.
  • a vacuum flash separator 6, the second vacuum flash separator 9 and the condensed liquid of the third vacuum flash separator 10 are sent into the deacidification tower 5 from the top of the deacidification tower 5 for deacidification; the deacidification tower 5
  • the operating pressure of the entire gas-water separation and reuse process is operated with a slight positive pressure greater than 0.2kPa.
  • the top of the sedimentation tank 3 and the gas-water tank 4 is continuously supplied with an inert gas as a protective gas to ensure that the system pressure is greater than 0.2kPa.
  • the slight positive pressure operation, the system Middle VOCs and odors can be collected in a centralized manner, by-product steam from incineration or RTO.
  • the crushed coal in this example is semi-coke with a water content of 8%.
  • the coal sample is crushed and sieved to obtain a coal sample with a particle size of 5-50 mm, which is loaded into a crushed coal pressurized gasifier for crushed coal pressurized gasification , the gasification pressure is 3MPa, and the gasification temperature is 1250°C.
  • the crude gas produced by gasification is divided into high temperature gas water and low temperature gas water according to the dust content, temperature and pressure in the water during washing. Temperature and pressure are divided into high temperature condensate and gasification dust-containing gasification water, low temperature gas water is divided into low temperature condensate conversion, low pressure gasification gas water and low pressure driving gas water according to dust content, temperature and pressure.
  • the dust content of the transformed high-temperature condensate obtained by the above-mentioned coal samples processed by the gasification unit, the washing unit and the transformation unit is 980 mg/L, the temperature is 155 °C, and the pressure is 3 MPa, and the dust content of the gasification dust-containing gasification water is 1250 mg/L, temperature of 185°C, and pressure of 3.0 MPa.
  • the dust content of the transformed low-temperature condensate is 30mg/L, the temperature is 66°C, and the pressure is 3MPa.
  • the dust content of the low-pressure gasification gas water is 65mg/L, the temperature is 75°C, and the pressure is 0.5MPa.
  • the dust content is 120mg/L, the temperature is 60°C, and the pressure is 0.5MPa.
  • the high-temperature condensate of the transformation and the gasification dust-containing gasification water are first degassed by the medium pressure flasher 1, and then enter the first vacuum flasher 2 together with the gasification low pressure gas water and the gasification start-up gas water to remove the dissolved gas in depth.
  • the flash temperature of the evaporator 1 is 142°C
  • the pressure is 0.4MPa
  • the flash temperature of the first vacuum flasher 2 is 82°C
  • the vacuum degree is 50kPa
  • the gas water after the de-dissolved gas is added 3g according to 1 ton of gas water
  • the proportion of the flocculant is added to the flocculant and mixed and then sent to the settling tank 3.
  • the solid material settled at the bottom of the settling tank 3 is dehydrated by the filter press 12 to make a mud cake with a water content of 23%, and the filtrate enters the filtrate tank 13.
  • the gas water in the upper part of the settling tank 3 is sent to the gas water tank 4 as the washing water for gasification of low-pressure gas water, which is reused for the coal lock gas washing equipment and the driving gas washing equipment, and the remaining gas water is removed from the biochemical treatment equipment.
  • the flash steam flashed from the medium pressure flasher 1 is injected from the bottom of the deacidification tower 5 as a heat source of the deacidification tower 5, and the acid gas in the flash steam is removed at the same time.
  • the low temperature condensate is transformed into and de-dissolved gas in the second vacuum flasher 8, and the gas water after the dissolved gas is removed is sent to the deacidification tower 5 for deacidification; the first vacuum flasher 2 and the second vacuum flasher 8
  • the condensate formed by flashing enters the first vacuum flash separator 6 and the second vacuum flash separator 9 respectively for vacuum flash separation, and then continues to enter the third vacuum flash separator 10 for vacuum flash separation.
  • a vacuum flash separator 6, the second vacuum flash separator 9 and the condensed liquid of the third vacuum flash separator 10 are sent into the deacidification tower 5 from the top of the deacidification tower 5 for deacidification; the deacidification tower 5
  • the operating pressure of the entire gas-water separation and reuse process is operated with a slight positive pressure greater than 0.2kPa.
  • the top of the sedimentation tank 3 and the gas-water tank 4 is continuously supplied with an inert gas as a protective gas to ensure that the system pressure is greater than 0.2kPa.
  • the slight positive pressure operation, the system Middle VOCs and odors can be collected in a centralized manner, by-product steam from incineration or RTO.
  • Settling tank 3 and gas water tank 4 continue to pass inert gas to seal their tops to prevent negative pressure in sedimentation tank 3 and gas water tank 4 and inhale air from their breathing valves to maintain a slight positive pressure in the tank , the normal pressure of the sealing valve is set to 0.4kPa, and the intersection with the set pressure of the breathing valve and the single exhalation valve or the control valve should be avoided, resulting in unnecessary inert gas circulation and high operating costs.
  • the crushed coal in this embodiment is coke with a water content of 5%.
  • the coal sample is crushed and sieved to obtain a coal sample with a particle size of 5-50 mm, which is loaded into a crushed coal pressurized gasifier for crushed coal pressurized gasification.
  • the gasification pressure is 3MPa, and the gasification temperature is 1250°C.
  • the crude gas produced by gasification is divided into high temperature gas water and low temperature gas water according to the dust content, temperature and pressure in the water during washing. And pressure is divided into high temperature condensate transformation and gasification dust-containing gasification water, low temperature gas water is divided into transformation low temperature condensate, low pressure gasification gas water and low pressure driving gas water according to dust content, temperature and pressure.
  • Different types of gas water are separated and reused separately. The whole process of separation and reuse of gas water is maintained at a slight positive pressure of more than 0.2kPa and protected by inert gas to ensure that VOCs and odors in the system can be centrally treated.
  • the dust content of the transformed high-temperature condensate obtained after the above coal samples are processed by the gasification unit, the washing unit and the transformation unit is 1200 mg/L, the temperature is 165 °C, and the pressure is 3 MPa, and the dust content of the gasification dust-containing gasification water is 1800 mg/L, temperature of 185°C, and pressure of 3.0 MPa.
  • the dust content of the transformed low-temperature condensate is 46mg/L, the temperature is 66°C, and the pressure is 3.0MPa.
  • the dust content of the low-pressure gasification gas water is 84mg/L, the temperature is 75°C, and the pressure is 0.5MPa.
  • the dust content of water was 150 mg/L, the temperature was 78°C, and the pressure was 0.7 MPa.
  • the high-temperature condensate of the transformation and the gasification dust-containing gasification water are first degassed by the medium pressure flasher 1, and then enter the first vacuum flasher 2 together with the gasification low pressure gas water and the gasification start-up gas water to remove the dissolved gas in depth.
  • the flash temperature of the evaporator 1 is 142°C
  • the pressure is 0.4MPa
  • the flash temperature of the first vacuum flasher 2 is 82°C
  • the vacuum degree is 50kPa
  • the gas water after the de-dissolved gas is added 3g according to 1 ton of gas water
  • the proportion of flocculant is added to the flocculant and mixed and then sent to the sedimentation tank 3.
  • the solid material settled at the bottom of the sedimentation tank 3 is dehydrated by the filter press 12 to make a mud cake with a water content of 22%, and the filtrate enters the filtrate tank 13.
  • the gas water in the upper part of the settling tank 3 is sent to the gas water tank 4 as the washing water for gasification of low-pressure gas water, which is reused for the coal lock gas washing equipment and the driving gas washing equipment, and the remaining gas water is removed from the biochemical treatment equipment.
  • the flash steam flashed from the medium pressure flasher 1 is injected from the bottom of the deacidification tower 5 as a heat source of the deacidification tower 5, and the acid gas in the flash steam is removed at the same time.
  • the low temperature condensate is transformed into and de-dissolved gas in the second vacuum flasher 8, and the gas water after the dissolved gas is removed is sent to the deacidification tower 5 for deacidification; the first vacuum flasher 2 and the second vacuum flasher 8
  • the condensate formed by flashing enters the first vacuum flash separator 6 and the second vacuum flash separator 9 respectively for vacuum flash separation, and then continues to enter the third vacuum flash separator 10 for vacuum flash separation.
  • a vacuum flash separator 6, the second vacuum flash separator 9 and the condensed liquid of the third vacuum flash separator 10 are sent into the deacidification tower 5 from the top of the deacidification tower 5 for deacidification; the deacidification tower 5
  • the operating pressure of the entire gas-water separation and reuse process is operated with a slight positive pressure greater than 0.2kPa.
  • the top of the sedimentation tank 3 and the gas-water tank 4 is continuously supplied with an inert gas as a protective gas to ensure that the system pressure is greater than 0.2kPa.
  • the slight positive pressure operation, the system Middle VOCs and odors can be collected in a centralized manner, by-product steam from incineration or RTO.
  • Settling tank 3 and gas water tank 4 continue to pass inert gas to seal their tops to prevent negative pressure in sedimentation tank 3 and gas water tank 4 and inhale air from their breathing valves to maintain a slight positive pressure in the tank , the normal pressure of the sealing valve is set to 0.5kPa, and the intersection with the set pressure of the breathing valve and the single exhalation valve or the control valve should be avoided, resulting in unnecessary inert gas circulation and high operating costs.

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Abstract

本发明提供一种碎煤加压气化煤气水分离及回用系统及方法，属于煤气分离和回用领域。本发明将不同分类的煤气水分别进行分离和回用，不仅使得整个系统占地面积小，投资低、运行成本低，且处理流程短、设备少，污染物排放点少，不易造成环境污染。通过设置中压闪蒸器、真空闪蒸器、真空闪蒸分离器和蒸氨塔等设备，并设置沉降槽和煤气水罐顶部与惰性气体管路密封连接，使整个系统及分离回用过程保持大于0.2kPa的微正压操作，从而能保证系统中排出的VOCs和臭气能集中处理。

Description

碎煤加压气化煤气水分离及回用系统及方法 技术领域
本发明涉及煤气分离和回用技术领域，尤其涉及一种碎煤加压气化煤气水分离及回用系统及方法。
 背景技术
碎煤加压气化产生的粗煤气中含有大量的水蒸气、粉尘和碳化的副产物，例如焦油、轻油、萘、酚、脂肪酸、溶解的气体和无机盐类等，而且温度也较高。因此，需要对其进行冷却和洗涤，以降低温度和除去粗煤气中的有害物质。在粗煤气的洗涤和冷却过程中，这些杂质成分便进入水中，形成了有气、液、固三态存在的多种成分的煤气水，煤气水成分较为复杂，而且随着煤种的不同，各种成分的含量也不尽相同。煤气水用常规的生化、过滤、反渗透等方法不能直接处理，必须先将其中的油、尘、酚、氨等进行分离和回收，一方面回收了废水中的有价值物质，可产生一定的经济效益；另一方面也使废水能够满足一般废水处理方法的进水要求后，经过生化处理达到国家排放标准后排放。
《现代煤化工技术手册》中简述了目前最为经典的煤气水分离与回收流程，这也是目前碎煤加压气化技术中普遍使用的流程，具体是将压力为3.0-6.0MPa的气化煤气水和变换冷却煤气水分别送入煤气水分离系统后，首先被冷却到90℃，然后进入煤气水膨胀器闪蒸膨胀到常压，将煤气水中溶解的CO 2 、NH 3 及部分水蒸气等气体闪蒸分离。经闪蒸后的煤气水进入下部的焦油分离器利用密度差进行煤气水与焦油的分离，密度大于水的含尘焦油从底部排出，可作为产品也可返回气化炉再次进行气化；密度小于水的轻油与煤气水从焦油分离器上部溢流进入煤气水缓冲槽，一部分煤气水经高压泵送回气化循环使用，多余的煤气水进入轻油分离器。在轻油分离器中装有焦碳和TPI板组件，一方面过滤杂质，一方面使油滴凝聚后上浮于水面形成油层，轻油通过上部的溢流堰引出送入油储槽，下部的水经过TPI板后进入水室，再经过溢流堰引出，经缓冲槽后用泵送入双介质过滤器进一步除尘后送往酚、氨回收装置，其目的就是将煤气水中的尘、油和溶解的气进行分离，大部分水作为循环使用，小部分水进一步脱油、蒸氨、脱酚后满足生化要求的水质去生化处理。
但是随着煤气技术的发展，逐步向着大型化、节能环保、高效稳定的方向发展，目前常规使用的碎煤加压气化技术煤气水分离和回收流程不能满足现代要求，主要体现在：1、现有的煤气水处理系统对来自于不同设备的不同类型的煤气水汇总到一起进行煤气水分离和回收，在装置流程中设置有多台分离器和缓冲器，不仅造成整个煤气水分离和回收系统占地面积大，投资高，运行成本高，而且流程长，设备多，使得污染物排放点多，容易造成严重的环境污染。
2、现有的煤气水分离和回收系统中会用到多台缓冲器和分离器等，这些设备采用常压操作，容易造成排放的VOCs(Volatile Organic Compounds，挥发性有机物)、臭气等无法收集后集中处理，使得现场环境恶劣。
 技术问题
为解决上述技术问题，本发明提供一种碎煤加压气化煤气水分离及回用系统及方法。
 技术解决方案
为解决上述技术问题，本发明采用的技术方案是：一种碎煤加压气化煤气水分离及回用系统，其包括中压闪蒸器、第一真空闪蒸器、沉降槽、煤气水罐、脱酸塔、第一真空闪蒸分离器、蒸氨塔、第二真空闪蒸器、第二真空闪蒸分离器、第三真空闪蒸分离器、絮凝剂罐、压滤机、滤液罐、若干水泵和管路，其中：所述中压闪蒸器的第一进水口与变换高温冷凝液管路连接，中压闪蒸器的第二进水口与气化含尘气化水管路连接，中压闪蒸器的出水口通过管路与第一真空闪蒸器的第一进水口连接，第一真空闪蒸器的第二进水口与低压气化煤气水管路连接，第一真空闪蒸器的第三进水口与低压开车煤气水管路连接，第一真空闪蒸器的出水口通过管路和水泵与沉降槽的进水口连接，沉降槽的出水口通过管路和水泵与压滤机的进水口连接，压滤机的出水口通过管路与滤液罐的进水口连接，滤液罐的出水口通过管路和水泵与沉降槽的进水口连接，沉降槽的进水口还通过管路与絮凝剂罐的出料口连接，沉降槽的煤气水出口通过管路与煤气水罐的煤气水进口连接，煤气水罐的煤气水出口通过管路和水泵与煤气水生化处理设备和煤气水回用设备连接，所述沉降槽和煤气水罐顶部与惰性气体管路密封连接；中压闪蒸器的出气口通过管路与脱酸塔的进气口连接，第二真空闪蒸器的进水口与变换低温冷凝液管路连接，第二真空闪蒸器的出水口通过管路和水泵与脱酸塔的第一进水口连接，脱酸塔的出水口通过管路和水泵与蒸氨塔的进水口连接，蒸氨塔的出水口与粗煤气洗涤设备连接；第一真空闪蒸器的出气口通过管路与第一真空闪蒸分离器的进气口连接，第一真空闪蒸分离器的出气口通过管路与第三真空闪蒸分离器的进气口连接，第一真空闪蒸分离器的出水口通过管路和水泵与脱酸塔的第二进水口连接；第二真空闪蒸器的出气口通过管路与第二真空闪蒸分离器的进气口连接，第二真空闪蒸分离器的出气口通过管路与第三真空闪蒸分离器的进气口连接，第二真空闪蒸分离器的出水口通过管路与脱酸塔的第二进水口连接，第三真空闪蒸分离器的出水口通过管路与脱酸塔的第二进水口连接。
可选地，碎煤加压气化煤气水分离及回用系统还包括集油浮子和油罐，所述集油浮子设于煤气水罐内部，集油浮子底部通过软管与油罐连接。
可选地，所述煤气水罐和沉降槽顶部的呼吸气排出管道外设有冷却水套管。
一种碎煤加压气化煤气水分离及回用方法，其包括如下步骤：S1，变换高温冷凝液和气化含尘气化水经中压闪蒸器脱气后，与气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器并在第一真空闪蒸器中深度脱出溶解气；S2，脱溶解气后的煤气水与来自于絮凝剂罐的絮凝剂混合后送入沉降槽；S3，沉降在沉降槽底部的固体物料经压滤机压滤脱水制成泥饼，压滤脱水生成的滤液进入滤液罐中并再返回沉降槽，沉降槽上部的煤气水送入煤气水罐，煤气水罐中的一部分煤气水作为气化低压煤气水的洗涤水为煤气水回用设备回用，剩余的煤气水去煤气水生化处理设备；S4，中压闪蒸器闪蒸出的闪蒸气从脱酸塔底部喷入脱酸塔作为脱酸塔的热源，同时脱酸塔脱出闪蒸气中的酸性气；S5，变换低温冷凝液进入并在第二真空闪蒸器中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔中脱酸性气；S6，第一真空闪蒸器和第二真空闪蒸器闪蒸形成的冷凝液分别进入第一真空闪蒸分离器和第二真空闪蒸分离器进行真空闪蒸分离后，继续进入第三真空闪蒸分离器进行真空闪蒸分离，经过第一真空闪蒸分离器、第二真空闪蒸分离器和第三真空闪蒸分离器冷凝的冷凝液从脱酸塔塔顶送入脱酸塔中脱酸；S7，脱酸塔脱酸得到的脱酸气去硫回收设备，脱酸塔脱酸后的煤气水进入蒸氨塔，在蒸氨塔中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔中产生的氨水/液氨回收再利用。
可选地，所述变换高温冷凝液为含尘量不大于2000mg/L、温度为150-190℃、压力为3.0-7.0MPa的煤气水；所述气化含尘气化水为含尘量不大于3000mg/L、温度为180-200℃、压力为3.0-7.0MPa的煤气水；所述变换低温冷凝液为含尘量小于50mg/L、温度为40-80℃、压力为3.0-5.0MPa的煤气水；所述低压气化煤气水为含尘量小于100mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水；所述低压开车煤气水为含尘量小于200mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水。
可选地，所述中压闪蒸器的闪蒸温度为140-160℃、压力为0.4-0.5MPa。
可选地，所述第一真空闪蒸器的闪蒸温度为80-86℃、真空度为50-60kPa。
可选地，所述絮凝剂的加入量为1吨煤气水加入3-5g絮凝剂。
可选地，所述沉降槽和煤气水罐顶部持续通入惰性气体。
 有益效果
本发明的有益效果是：1、通过将变换高温冷凝液、气化含尘气化水、变换低温冷凝液、气化低压煤气水和气化开车煤气水这几种不同分类的煤气水分别进行处理来实现煤气水的分离和回用，使整个流程所用设备少，不仅使得整个系统占地面积小，投资低、运行成本低，而且处理流程短、设备少，使得污染物排放点少，不易造成环境污染，具有节能环保、高效稳定的优点。
2、通过设置中压闪蒸器、真空闪蒸器、真空闪蒸分离器和蒸氨塔等设备，并设置沉降槽和煤气水罐顶部与惰性气体管路密封连接，使得整个系统及分离回用过程保持大于0.2kPa的微正压操作，从而能够保证系统中排出的VOCs和臭气能够集中处理，使现场环境友好。
3、本发明整个系统设备简单，运行安全稳定，能有效降低煤气水处理的成本。
实践证明，与目前的煤气水分离及回用系统相比，本发明的系统及方法投资减少了50％，运行费用节约了50％。
 附图说明
图1是本发明的系统组成示意图。
图2是本发明与气化单元、洗涤单元和变换单元的连接关系示意图。
 本发明的实施方式
下面将结合附图和实施例对本发明作进一步地详细描述。
如图1所示，本实施例中的碎煤加压气化煤气水分离及回用系统，其包括中压闪蒸器1、第一真空闪蒸器2、沉降槽3、煤气水罐4、脱酸塔5、第一真空闪蒸分离器6、蒸氨塔7、第二真空闪蒸器8、第二真空闪蒸分离器9、第三真空闪蒸分离器10、絮凝剂罐11、压滤机12、滤液罐13、若干水泵和管路，其中：所述中压闪蒸器1的第一进水口与变换高温冷凝液管路连接，中压闪蒸器1的第二进水口与气化含尘气化水管路连接，中压闪蒸器1的出水口通过管路与第一真空闪蒸器2的第一进水口连接，第一真空闪蒸器2的第二进水口与低压气化煤气水管路连接，第一真空闪蒸器2的第三进水口与低压开车煤气水管路连接，第一真空闪蒸器2的出水口通过管路和水泵与沉降槽3的进水口连接，沉降槽3的出水口通过管路和水泵与压滤机12的进水口连接，压滤机12的出水口通过管路与滤液罐13的进水口连接，滤液罐13的出水口通过管路和水泵与沉降槽3的进水口连接，沉降槽3的进水口还通过管路与絮凝剂罐11的出料口连接，沉降槽3的煤气水出口通过管路与煤气水罐4的煤气水进口连接，煤气水罐4的煤气水出口通过管路和水泵与煤气水生化处理设备(煤锁气洗涤设备和开车煤气洗涤设备)和煤气水回用设备连接，所述沉降槽3和煤气水罐4顶部与惰性气体管路密封连接；中压闪蒸器1的出气口通过管路与脱酸塔5的进气口连接，第二真空闪蒸器8的进水口与变换低温冷凝液管路连接，第二真空闪蒸器8的出水口通过管路和水泵与脱酸塔5的第一进水口连接，脱酸塔5的出水口通过管路和水泵与蒸氨塔7的进水口连接，蒸氨塔7的出水口与粗煤气洗涤设备连接；第一真空闪蒸器2的出气口通过管路与第一真空闪蒸分离器6的进气口连接，第一真空闪蒸分离器6的出气口通过管路与第三真空闪蒸分离器10的进气口连接，第一真空闪蒸分离器6的出水口通过管路和水泵与脱酸塔5的第二进水口连接；第二真空闪蒸器8的出气口通过管路与第二真空闪蒸分离器9的进气口连接，第二真空闪蒸分离器9的出气口通过管路与第三真空闪蒸分离器10的进气口连接，第二真空闪蒸分离器9的出水口通过管路与脱酸塔5的第二进水口连接，第三真空闪蒸分离器10的出水口通过管路与脱酸塔5的第二进水口连接。
如图2所示，本发明实施例所述的碎煤加压气化煤气水分离及回用系统之前连接有气化单元、洗涤单元和变换单元。具体地，碎煤原料经过加煤锁斗加入碎煤加压气化炉中进行加压气化产生气化粗煤气，气化粗煤气经过旋风分离器进行除尘后到达废热锅炉，废热锅炉回收煤气中的热量后，继续由文丘里洗涤设备和粗煤气洗涤设备对煤气进行三级除尘后送入变换单元中的变换设备、预冷器、中间、终冷设备和洗氨塔。碎煤加压气化炉中的一部分煤气进入煤锁气洗涤设备，另一部分还进入开车煤气洗涤设备。所述碎煤为无烟煤、焦炭或半焦中的任意一种。其中，预冷器产生变换高温冷凝液。中间、终冷设备和洗氨塔产生变换低温冷凝液。文丘里洗涤设备产生气化含尘气化水。煤锁气洗涤设备产生低压气化煤气水。开车煤气洗涤设备产生低压开车煤气水。
可选地，碎煤加压气化煤气水分离及回用系统还包括集油浮子14和油罐15，所述集油浮子14设于煤气水罐4内部，集油浮子14底部通过软管与油罐15连接，集油浮子14的高度可随煤气水罐4内液位变化，浮于煤气水罐4上部的轻油可以进入集油浮子14并通过软管收集至油罐15中，实现了轻油的收集。
可选地，所述煤气水罐4和沉降槽3顶部的呼吸气排出管道外设有冷却水套管16。冷却水套管16可以对从煤气水罐4和沉降槽3顶部的呼吸气排出管道排出的呼吸气进行冷却，使易凝臭气冷凝后自流回设备，从而避免VOCs或臭气等从煤气水罐4和沉降槽3中排出。
本发明实施例还提供了一种碎煤加压气化煤气水分离及回用方法，该碎煤加压气化煤气水分离及回用方法可以采用图1所示的碎煤加压气化煤气水分离及回用系统来实现，具体包括如下步骤。
S1，变换高温冷凝液和气化含尘气化水经中压闪蒸器1脱气后，与气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2并在第一真空闪蒸器2中深度脱出溶解气。
可选地，所述中压闪蒸器1的闪蒸温度为140-160℃、压力为0.4-0.5MPa。所述第一真空闪蒸器2的闪蒸温度为80-86℃、真空度为50-60kPa。
S2，脱溶解气后的煤气水与来自于絮凝剂罐11的絮凝剂混合后送入沉降槽3。
可选地，所述絮凝剂的加入量为1吨煤气水加入3-5g絮凝剂。
S3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成泥饼，压滤脱水生成的滤液进入滤液罐13中并再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4，煤气水罐4中的一部分煤气水作为气化低压煤气水的洗涤水为煤气水回用设备(煤锁气洗涤设备和开车煤气洗涤设备)回用，剩余的煤气水去煤气水生化处理设备。
S4，中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入脱酸塔5作为脱酸塔5的热源，同时脱酸塔5脱出闪蒸气中的酸性气。
S5，变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气。
S6，第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸。
S7，脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
其中，所述变换高温冷凝液为含尘量不大于2000mg/L、温度为150-190℃、压力为3.0-7.0MPa的煤气水；所述气化含尘气化水为含尘量不大于3000mg/L、温度为180-200℃、压力为3.0-7.0MPa的煤气水；所述变换低温冷凝液为含尘量小于50mg/L、温度为40-80℃、压力为3.0-5.0MPa的煤气水；所述低压气化煤气水为含尘量小于100mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水；所述低压开车煤气水为含尘量小于200mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水。
可选地，所述沉降槽3和煤气水罐4顶部持续通入惰性气体，以使沉降槽3和煤气水罐4内部始终保持大于0.2kPa的微正压(0.2-0.5kPa)。
下面以几个例子对本发明实施例提供的方法进行举例说明。
实施例1。
本实施例中的碎煤为含水5％的晋城无烟煤，煤样经过破碎、筛分后获得粒径为5-50mm煤样，装入碎煤加压气化炉中进行碎煤加压气化，气化压力为4.0MPa，气化温度1250℃，气化产生的粗煤气在洗涤时依据水中含尘量、温度以及压力分为高温煤气水和低温煤气水，高温煤气水依据含尘量、温度以及压力分为变换高温冷凝液和气化含尘气化水，低温煤气水依据含尘量、温度以及压力分为变换低温冷凝液、低压气化煤气水和低压开车煤气水。不同分类的煤气水分别分离回用，整个煤气水的分离回用过程保持大于0.2kPa的微正压操作并采用惰性气体保护，以保证系统中VOCs和臭气能够集中处理。
上述煤样经过气化单元、洗涤单元和变换单元处理得到的变换高温冷凝液的含尘量为1900mg/L、温度为150℃、压力为4MPa，气化含尘气化水的含尘量为2800mg/L、温度为189℃、压力为4.0MPa。变换低温冷凝液的含尘量为45mg/L、温度为67.5℃、压力为3.75MPa，低压气化煤气水的含尘量为90mg/L、温度为70℃、压力0.5MPa，低压开车煤气水的含尘量为180mg/L、温度为65℃、压力为0.65MPa。
其中，高温煤气水和低温煤气水的主要污染物特性数据分别见表1和表2。
Figure 105550dest_path_image002
。
其中，变换高温冷凝液和气化含尘气化水先经中压闪蒸器1脱气后与气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2深度脱出溶解气，所述中压闪蒸器1的闪蒸温度为144℃，压力为0.4MPa，所述第一真空闪蒸器2的闪蒸温度为84.8℃，真空度为50kPa；脱溶解气后的煤气水按照1吨煤气水添加3g絮凝剂的比例加入絮凝剂混合后送入沉降槽3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成含水量为22％的泥饼，滤液进入滤液罐13中再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4作为气化低压煤气水的洗涤水为煤锁气洗涤设备和开车煤气洗涤设备回用，剩余的去煤气水的生化处理设备。中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入作为脱酸塔5热源，同时脱出闪蒸气中的酸性气。变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气；第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸；脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
整个煤气水分离及回用过程的操作压力为大于0.2kPa的微正压操作，沉降槽3和煤气水罐4顶部持续通入设置惰性气体作为保护气，保证系统压力为大于0.2kPa微正压，使系统中VOCs和臭气等能够集中收集焚烧或RTO副产蒸汽。沉降槽3和煤气水罐4持续通入惰性气体对它们顶部进行密封的作用主要是为了防止沉降槽3和煤气水罐4出现负压而从它们的呼吸阀吸入空气，以保持罐内微正压，密封阀正常压力设定值宜为0.2kPa，并应避免与呼吸阀和单呼阀或控制阀等设定压力交集，以产生不必要的惰性气循环和运行费用高。
本发明实施例采用无烟煤碎煤加压气化是利用煤气水中油含量少，COD含量低，尘含量低的特点。本实施例中采用无烟煤进行加压气化，由于无烟煤水份低，一般全水含量在10％以下，挥发分小于10％，碳含量高，煤灰熔点高，灰含量高。真密度一般为1.4-1.8g/cm 3 ，无烟煤中矿物质含量高，真密度更是达到1.8-1.9g/cm 3，再加上无烟煤的热稳定性高，进入气化炉内不易于粉化，带出气化炉的煤尘量小、煤尘颗粒与煤气水密度差约大，所以煤尘更容易分离，可以缩短含尘煤气水分离器的停留时间。
目前进入生化处理设备的水质要求，一般是COD小于等于3500mg/L，pH在8.0-9.0之间，油含量小于等于50mg/L，BOD不大于1100mg/L。目前的煤气水出水和回用指标见表3，去生化处理设备的煤气水中的油含量高，在入生化前还需要进行氧化处理，降低COD含量。
Figure dest_path_image003
。
通过本发明实施例提供的方法处理后，去往生化处理设备的煤气水和进行煤气水回用的煤气水中，氨含量、COD含量等远小于通过目前煤气水分离和回收系统及方法处理得到的煤气水。
实施例2。
本实施例中的碎煤为含水6％的晋城无烟煤，煤样经过破碎、筛分后获得粒径为5-50mm煤样，装入碎煤加压气化炉中进行碎煤加压气化，气化压力为5.0MPa，气化温度1250℃，气化产生的粗煤气在洗涤时依据水中含尘量、温度以及压力分为高温煤气水和低温煤气水，高温煤气水依据含尘量、温度以及压力分为变换高温冷凝液和气化含尘气化水，低温煤气水依据含尘量、温度以及压力分为变换低温冷凝液、低压气化煤气水和低压开车煤气水。不同分类的煤气水分别分离回用，整个煤气水的分离回用过程保持大于0.2kPa的微正压操作并采用惰性气体保护，保证系统中VOCs和臭气能够集中处理。
上述煤样经过气化单元、洗涤单元和变换单元处理得到的变换高温冷凝液的含尘量为1800mg/L、温度为158℃、压力为5MPa，气化含尘气化水的含尘量为1985mg/L、温度为196℃、压力5.0MPa。变换低温冷凝液的含尘量为48mg/L、温度为70.5℃，压力为4.75MPa，低压气化煤气水的含尘量为98mg/L、温度为72℃、压力为0.6MPa，低压开车煤气水的含尘量为180mg/L、温度为75℃、压力0.55MPa。
其中，变换高温冷凝液和气化含尘气化水先经中压闪蒸器1脱气后和气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2深度脱出溶解气，所述中压闪蒸器1的闪蒸温度为148℃，压力为0.5MPa，所述第一真空闪蒸器2的闪蒸温度为86℃，真空度为60kPa；脱溶解气后的煤气水按照1吨煤气水添加4.5g絮凝剂的比例加入絮凝剂混合后送入沉降槽3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成含水量为28％的泥饼，滤液进入滤液罐13中再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4作为气化低压煤气水的洗涤水为煤锁气洗涤设备和开车煤气洗涤设备回用，剩余的去煤气水生化处理设备。中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入作为脱酸塔5热源，同时脱出闪蒸气中的酸性气。变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气；第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸；脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
整个煤气水分离回用过程的操作压力大于0.2kPa的微正压操作，沉降槽3和煤气水罐4顶部持续通入设置惰性气体作为保护气，保证系统压力大于0.2kPa微正压操作，系统中VOCs和臭气等能够集中收集焚烧或RTO副产蒸汽。沉降槽3和煤气水罐4持续通入惰性气体对它们顶部进行密封的作用主要是为了防止沉降槽3和煤气水罐4出现负压而从它们的呼吸阀吸入空气，以保持罐内微正压，密封阀正常压力设定值宜为0.2kPa，并应避免与呼吸阀和单呼阀或控制阀等设定压力交集，产生不必要的惰性气循环和运行费用高。
实施例3。
本实施例中的碎煤为含水8％的阳泉无烟煤，煤样经过破碎、筛分后获得粒径为5-50mm煤样，装入碎煤加压气化炉中进行碎煤加压气化，气化压力为7.0MPa，气化温度为1350℃，气化产生的粗煤气在洗涤时依据水中含尘量、温度以及压力分为高温煤气水和低温煤气水，高温煤气水依据含尘量、温度以及压力分为变换高温冷凝液和气化含尘气化水，低温煤气水依据含尘量、温度以及压力分为变换低温冷凝液、低压气化煤气水和低压开车煤气水。不同分类的煤气水分别分离回用，整个煤气水的分离回用过程保持大于0.2kPa的微正压操作并采用惰性气体保护，保证系统中VOCs和臭气能够集中处理。
上述煤样经过气化单元、洗涤单元和变换单元处理得到的变换高温冷凝液的含尘量为1785mg/L、温度为170℃、压力为7MPa，气化含尘气化水的含尘量为1650mg/L、温度为197℃、压力为7.0MPa。变换低温冷凝液的含尘量为35mg/L、温度为67.5℃、压力为3.75MP，低压气化煤气水的含尘量为65mg/L、温度为70℃、压力为0.5MPa，低压开车煤气水的含尘量150mg/L、温度为60℃、压力为0.5MPa。
其中，变换高温冷凝液和气化含尘气化水先经中压闪蒸器1脱气后和气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2深度脱出溶解气，所述中压闪蒸器1的闪蒸温度为144℃，压力为0.4MPa，所述第一真空闪蒸器2的闪蒸温度为84.8℃，真空度为50kPa；脱溶解气后的煤气水按照1吨煤气水添加4.8g絮凝剂的比例加入絮凝剂混合后送入沉降槽3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成含水量为28％的泥饼，滤液进入滤液罐13中再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4作为气化低压煤气水的洗涤水为煤锁气洗涤设备和开车煤气洗涤设备回用，剩余的去煤气水生化处理设备。中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入作为脱酸塔5热源，同时脱出闪蒸气中的酸性气。变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气；第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸；脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
整个煤气水分离回用过程的操作压力大于0.2kPa的微正压操作，沉降槽3和煤气水罐4顶部持续通入设置惰性气体作为保护气，保证系统压力大于0.2kPa微正压操作，系统中VOCs和臭气等能够集中收集焚烧或RTO副产蒸汽。沉降槽3和煤气水罐4持续通入惰性气体对它们顶部进行密封的作用是为了防止沉降槽3和煤气水罐4出现负压而从它们的呼吸阀吸入空气，以保持罐内微正压，密封阀正常压力设定值宜为0.2kPa，并应避免与呼吸阀和单呼阀或控制阀等设定压力交集，产生不必要的惰性气循环和运行费用高。
实施例4。
本实施例中的碎煤为含水8％的半焦，煤样经过破碎、筛分后获得粒径为5-50mm煤样，装入碎煤加压气化炉中进行碎煤加压气化，气化压力为3MPa，气化温度为1250℃，气化产生的粗煤气在洗涤时依据水中含尘量、温度以及压力分为高温煤气水和低温煤气水，高温煤气水依据含尘量、温度以及压力分为变换高温冷凝液和气化含尘气化水，低温煤气水依据含尘量、温度以及压力分为变换低温冷凝液、低压气化煤气水和低压开车煤气水。不同分类的煤气水分别分离回用，整个煤气水的分离回用过程保持大于0.2kPa的微正压操作并采用惰性气体保护，保证系统中VOCs和臭气能够集中处理。
上述煤样经过气化单元、洗涤单元和变换单元处理得到的变换高温冷凝液的含尘量为980mg/L、温度为155℃、压力为3MPa，气化含尘气化水的含尘量为1250mg/L、温度为185℃、压力为3.0MPa。变换低温冷凝液的含尘量为30mg/L、温度为66℃、压力为3MPa，低压气化煤气水的含尘量为65mg/L、温度为75℃、压力为0.5MPa，低压开车煤气水的含尘量120mg/L、温度为60℃、压力为0.5MPa。
其中，变换高温冷凝液和气化含尘气化水先经中压闪蒸器1脱气后和气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2深度脱出溶解气，所述中压闪蒸器1的闪蒸温度为142℃，压力为0.4MPa，所述第一真空闪蒸器2的闪蒸温度为82℃，真空度为50kPa；脱溶解气后的煤气水按照1吨煤气水添加3g絮凝剂的比例加入絮凝剂混合后送入沉降槽3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成含水量为23％的泥饼，滤液进入滤液罐13中再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4作为气化低压煤气水的洗涤水为煤锁气洗涤设备和开车煤气洗涤设备回用，剩余的去煤气水生化处理设备。中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入作为脱酸塔5热源，同时脱出闪蒸气中的酸性气。变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气；第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸；脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
整个煤气水分离回用过程的操作压力大于0.2kPa的微正压操作，沉降槽3和煤气水罐4顶部持续通入设置惰性气体作为保护气，保证系统压力大于0.2kPa微正压操作，系统中VOCs和臭气等能够集中收集焚烧或RTO副产蒸汽。沉降槽3和煤气水罐4持续通入惰性气体对它们顶部进行密封的作用是为了防止沉降槽3和煤气水罐4出现负压而从它们的呼吸阀吸入空气，以保持罐内微正压，密封阀正常压力设定为0.4kPa，并应避免与呼吸阀和单呼阀或控制阀等设定压力交集，产生不必要的惰性气循环和运行费用高。
实施例5。
本实施例中的碎煤为含水5％的焦炭，煤样经过破碎、筛分后获得粒径为5-50mm煤样，装入碎煤加压气化炉中进行碎煤加压气化，气化压力为3MPa，气化温度为1250℃，气化产生的粗煤气在洗涤时依据水中含尘量、温度以及压力分为高温煤气水和低温煤气水，高温煤气水依据含尘量、温度以及压力分为变换高温冷凝液和气化含尘气化水，低温煤气水依据含尘量、温度以及压力分为变换低温冷凝液、低压气化煤气水和低压开车煤气水。不同分类的煤气水分别分离回用，整个煤气水的分离回用过程保持大于0.2kPa的微正压操作并采用惰性气体保护，保证系统中VOCs和臭气能够集中处理。
上述煤样经过气化单元、洗涤单元和变换单元处理得到的变换高温冷凝液的含尘量为1200mg/L、温度为165℃、压力为3MPa，气化含尘气化水的含尘量为1800mg/L、温度为185℃、压力为3.0MPa。变换低温冷凝液的含尘量为46mg/L、温度为66℃、压力为3.0MPa，低压气化煤气水的含尘量为84mg/L、温度为75℃、压力为0.5MPa，低压开车煤气水的含尘量150mg/L、温度为78℃、压力为0.7MPa。
其中，变换高温冷凝液和气化含尘气化水先经中压闪蒸器1脱气后和气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器2深度脱出溶解气，所述中压闪蒸器1的闪蒸温度为142℃，压力为0.4MPa，所述第一真空闪蒸器2的闪蒸温度为82℃，真空度为50kPa；脱溶解气后的煤气水按照1吨煤气水添加3g絮凝剂的比例加入絮凝剂混合后送入沉降槽3，沉降在沉降槽3底部的固体物料经压滤机12压滤脱水制成含水量为22％的泥饼，滤液进入滤液罐13中再返回沉降槽3，沉降槽3上部的煤气水送入煤气水罐4作为气化低压煤气水的洗涤水为煤锁气洗涤设备和开车煤气洗涤设备回用，剩余的去煤气水生化处理设备。中压闪蒸器1闪蒸出的闪蒸气从脱酸塔5底部喷入作为脱酸塔5热源，同时脱出闪蒸气中的酸性气。变换低温冷凝液进入并在第二真空闪蒸器8中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔5中脱酸性气；第一真空闪蒸器2和第二真空闪蒸器8闪蒸形成的冷凝液分别进入第一真空闪蒸分离器6和第二真空闪蒸分离器9进行真空闪蒸分离后，继续进入第三真空闪蒸分离器10进行真空闪蒸分离，经过第一真空闪蒸分离器6、第二真空闪蒸分离器9和第三真空闪蒸分离器10冷凝的冷凝液从脱酸塔5塔顶送入脱酸塔5中脱酸；脱酸塔5脱酸得到的脱酸气去硫回收设备，脱酸塔5脱酸后的煤气水进入蒸氨塔7，在蒸氨塔7中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔7中产生的氨水/液氨回收再利用。
整个煤气水分离回用过程的操作压力大于0.2kPa的微正压操作，沉降槽3和煤气水罐4顶部持续通入设置惰性气体作为保护气，保证系统压力大于0.2kPa微正压操作，系统中VOCs和臭气等能够集中收集焚烧或RTO副产蒸汽。沉降槽3和煤气水罐4持续通入惰性气体对它们顶部进行密封的作用是为了防止沉降槽3和煤气水罐4出现负压而从它们的呼吸阀吸入空气，以保持罐内微正压，密封阀正常压力设定为0.5kPa，并应避免与呼吸阀和单呼阀或控制阀等设定压力交集，产生不必要的惰性气循环和运行费用高。
可以理解的是，以上实施方式仅仅是为了说明本发明的原理而采用的示例性实施方式，然而本发明并不局限于此。对于本领域内的普通技术人员而言，在不脱离本发明的精神和实质的情况下，可以做出各种变型和改进，这些变型和改进也视为本发明的保护范围。

Claims (9)

  1. 一种碎煤加压气化煤气水分离及回用系统，其特征在于，包括中压闪蒸器(1)、第一真空闪蒸器(2)、沉降槽(3)、煤气水罐(4)、脱酸塔(5)、第一真空闪蒸分离器(6)、蒸氨塔(7)、第二真空闪蒸器(8)、第二真空闪蒸分离器(9)、第三真空闪蒸分离器(10)、絮凝剂罐(11)、压滤机(12)、滤液罐(13)、若干水泵和管路，其中：
    所述中压闪蒸器(1)的第一进水口与变换高温冷凝液管路连接，中压闪蒸器(1)的第二进水口与气化含尘气化水管路连接，中压闪蒸器(1)的出水口通过管路与第一真空闪蒸器(2)的第一进水口连接，第一真空闪蒸器(2)的第二进水口与低压气化煤气水管路连接，第一真空闪蒸器(2)的第三进水口与低压开车煤气水管路连接，第一真空闪蒸器(2)的出水口通过管路和水泵与沉降槽(3)的进水口连接，沉降槽(3)的出水口通过管路和水泵与压滤机(12)的进水口连接，压滤机(12)的出水口通过管路与滤液罐(13)的进水口连接，滤液罐(13)的出水口通过管路和水泵与沉降槽(3)的进水口连接，沉降槽(3)的进水口还通过管路与絮凝剂罐(11)的出料口连接，沉降槽(3)的煤气水出口通过管路与煤气水罐(4)的煤气水进口连接，煤气水罐(4)的煤气水出口通过管路和水泵与煤气水生化处理设备和煤气水回用设备连接，所述沉降槽(3)和煤气水罐(4)顶部与惰性气体管路密封连接；中压闪蒸器(1)的出气口通过管路与脱酸塔(5)的进气口连接，第二真空闪蒸器(8)的进水口与变换低温冷凝液管路连接，第二真空闪蒸器(8)的出水口通过管路和水泵与脱酸塔(5)的第一进水口连接，脱酸塔(5)的出水口通过管路和水泵与蒸氨塔(7)的进水口连接，蒸氨塔(7)的出水口与粗煤气洗涤设备连接；第一真空闪蒸器(2)的出气口通过管路与第一真空闪蒸分离器(6)的进气口连接，第一真空闪蒸分离器(6)的出气口通过管路与第三真空闪蒸分离器(10)的进气口连接，第一真空闪蒸分离器(6)的出水口通过管路和水泵与脱酸塔(5)的第二进水口连接；第二真空闪蒸器(8)的出气口通过管路与第二真空闪蒸分离器(9)的进气口连接，第二真空闪蒸分离器(9)的出气口通过管路与第三真空闪蒸分离器(10)的进气口连接，第二真空闪蒸分离器(9)的出水口通过管路与脱酸塔(5)的第二进水口连接，第三真空闪蒸分离器(10)的出水口通过管路与脱酸塔(5)的第二进水口连接。
  2. 根据权利要求1所述的碎煤加压气化煤气水分离及回用系统，其特征在于，还包括集油浮子(14)和油罐(15)，所述集油浮子(14)设于煤气水罐(4)内部，集油浮子(14)底部通过软管与油罐(15)连接。
  3. 根据权利要求1或2所述的碎煤加压气化煤气水分离及回用系统，其特征在于，所述煤气水罐(4)和沉降槽(3)顶部的呼吸气排出管道外设有冷却水套管(16)。
  4. 一种碎煤加压气化煤气水分离及回用方法，其特征在于，包括如下步骤：
    S1，变换高温冷凝液和气化含尘气化水经中压闪蒸器(1)脱气后，与气化低压煤气水和气化开车煤气水一起进入第一真空闪蒸器(2)并在第一真空闪蒸器(2)中深度脱出溶解气；
    S2，脱溶解气后的煤气水与来自于絮凝剂罐(11)的絮凝剂混合后送入沉降槽(3)；
    S3，沉降在沉降槽(3)底部的固体物料经压滤机(12)压滤脱水制成泥饼，压滤脱水生成的滤液进入滤液罐(13)中并再返回沉降槽(3)，沉降槽(3)上部的煤气水送入煤气水罐(4)，煤气水罐(4)中的一部分煤气水作为气化低压煤气水的洗涤水为煤气水回用设备回用，剩余的煤气水去煤气水生化处理设备；
    S4，中压闪蒸器(1)闪蒸出的闪蒸气从脱酸塔(5)底部喷入脱酸塔(5)作为脱酸塔(5)的热源，同时脱酸塔(5)脱出闪蒸气中的酸性气；
    S5，变换低温冷凝液进入并在第二真空闪蒸器(8)中脱溶解气，脱除溶解气后的煤气水再送入脱酸塔(5)中脱酸性气；
    S6，第一真空闪蒸器(2)和第二真空闪蒸器(8)闪蒸形成的冷凝液分别进入第一真空闪蒸分离器(6)和第二真空闪蒸分离器(9)进行真空闪蒸分离后，继续进入第三真空闪蒸分离器(10)进行真空闪蒸分离，经过第一真空闪蒸分离器(6)、第二真空闪蒸分离器(9)和第三真空闪蒸分离器(10)冷凝的冷凝液从脱酸塔(5)塔顶送入脱酸塔(5)中脱酸；
    S7，脱酸塔(5)脱酸得到的脱酸气去硫回收设备，脱酸塔(5)脱酸后的煤气水进入蒸氨塔(7)，在蒸氨塔(7)中蒸氨后的煤气水作为洗涤水为粗煤气洗涤设备回用，蒸氨塔(7)中产生的氨水/液氨回收再利用。
  5. 根据权利要求4所述的碎煤加压气化煤气水分离及回用方法，其特征在于，所述变换高温冷凝液为含尘量不大于2000mg/L、温度为150-190℃、压力为3.0-7.0MPa的煤气水；所述气化含尘气化水为含尘量不大于3000mg/L、温度为180-200℃、压力为3.0-7.0MPa的煤气水；所述变换低温冷凝液为含尘量小于50mg/L、温度为40-80℃、压力为3.0-5.0MPa的煤气水；所述低压气化煤气水为含尘量小于100mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水；所述低压开车煤气水为含尘量小于200mg/L、温度为60-80℃、压力为0.5-0.7MPa的煤气水。
  6. 根据权利要求4所述的碎煤加压气化煤气水分离及回用方法，其特征在于，所述中压闪蒸器(1)的闪蒸温度为140-160℃、压力为0.4-0.5MPa。
  7. 根据权利要求4所述的碎煤加压气化煤气水分离及回用方法，其特征在于，所述第一真空闪蒸器(2)的闪蒸温度为80-86℃、真空度为50-60kPa。
  8. 根据权利要求4所述的碎煤加压气化煤气水分离及回用方法，其特征在于，所述絮凝剂的加入量为1吨煤气水加入3-5g絮凝剂。
  9. 根据权利要求4所述的碎煤加压气化煤气水分离及回用方法，其特征在于，所述沉降槽(3)和煤气水罐(4)顶部持续通入惰性气体。
PCT/CN2021/113367 2020-11-19 2021-08-18 碎煤加压气化煤气水分离及回用系统及方法 WO2022105328A1 (zh)

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