CN112299664B - System and method for separating and recycling crushed coal pressurized gasification gas water - Google Patents
System and method for separating and recycling crushed coal pressurized gasification gas water Download PDFInfo
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- CN112299664B CN112299664B CN202011302289.4A CN202011302289A CN112299664B CN 112299664 B CN112299664 B CN 112299664B CN 202011302289 A CN202011302289 A CN 202011302289A CN 112299664 B CN112299664 B CN 112299664B
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 519
- 238000002309 gasification Methods 0.000 title claims abstract description 72
- 239000003245 coal Substances 0.000 title claims abstract description 64
- 238000004064 recycling Methods 0.000 title claims abstract description 59
- 238000000034 method Methods 0.000 title claims abstract description 35
- 239000007789 gas Substances 0.000 claims abstract description 384
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 claims abstract description 128
- 239000003034 coal gas Substances 0.000 claims abstract description 93
- 229910021529 ammonia Inorganic materials 0.000 claims abstract description 60
- 238000000926 separation method Methods 0.000 claims abstract description 52
- 238000004821 distillation Methods 0.000 claims abstract description 47
- 239000011261 inert gas Substances 0.000 claims abstract description 27
- 239000000428 dust Substances 0.000 claims description 89
- 238000001704 evaporation Methods 0.000 claims description 57
- 230000008020 evaporation Effects 0.000 claims description 57
- 238000005406 washing Methods 0.000 claims description 32
- 239000000706 filtrate Substances 0.000 claims description 19
- 230000029058 respiratory gaseous exchange Effects 0.000 claims description 15
- 238000003825 pressing Methods 0.000 claims description 11
- VHUUQVKOLVNVRT-UHFFFAOYSA-N Ammonium hydroxide Chemical compound [NH4+].[OH-] VHUUQVKOLVNVRT-UHFFFAOYSA-N 0.000 claims description 8
- 235000011114 ammonium hydroxide Nutrition 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 239000011343 solid material Substances 0.000 claims description 8
- 238000004062 sedimentation Methods 0.000 claims description 7
- 239000000498 cooling water Substances 0.000 claims description 4
- 239000000203 mixture Substances 0.000 claims description 3
- 239000002912 waste gas Substances 0.000 claims description 3
- 239000008394 flocculating agent Substances 0.000 claims 2
- 230000008569 process Effects 0.000 abstract description 15
- 239000012855 volatile organic compound Substances 0.000 abstract description 15
- 230000008901 benefit Effects 0.000 abstract description 4
- 239000003344 environmental pollutant Substances 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 3
- 231100000719 pollutant Toxicity 0.000 abstract description 3
- 239000002994 raw material Substances 0.000 abstract description 3
- 230000008859 change Effects 0.000 abstract description 2
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 10
- 239000003830 anthracite Substances 0.000 description 10
- 230000018044 dehydration Effects 0.000 description 9
- 238000006297 dehydration reaction Methods 0.000 description 9
- 238000011084 recovery Methods 0.000 description 8
- 238000007789 sealing Methods 0.000 description 7
- 239000006227 byproduct Substances 0.000 description 6
- 239000002245 particle Substances 0.000 description 6
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 5
- 238000007872 degassing Methods 0.000 description 5
- 230000001681 protective effect Effects 0.000 description 5
- 229910052717 sulfur Inorganic materials 0.000 description 5
- 239000011593 sulfur Substances 0.000 description 5
- 230000009466 transformation Effects 0.000 description 5
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 4
- 239000000872 buffer Substances 0.000 description 4
- 238000001816 cooling Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- 239000002817 coal dust Substances 0.000 description 3
- 239000000571 coke Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 150000003839 salts Chemical class 0.000 description 3
- UFWIBTONFRDIAS-UHFFFAOYSA-N Naphthalene Chemical compound C1=CC=CC2=CC=CC=C21 UFWIBTONFRDIAS-UHFFFAOYSA-N 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000005201 scrubbing Methods 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000000112 cooling gas Substances 0.000 description 1
- 235000014113 dietary fatty acids Nutrition 0.000 description 1
- 229930195729 fatty acid Natural products 0.000 description 1
- 239000000194 fatty acid Substances 0.000 description 1
- 150000004665 fatty acids Chemical class 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000001223 reverse osmosis Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
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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
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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
- 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
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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
- 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
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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
- C02F3/00—Biological treatment of water, waste water, or sewage
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- Engineering & Computer Science (AREA)
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Industrial Gases (AREA)
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Abstract
The invention provides a system and a method for separating and recycling crushed coal pressurized gasification coal gas water, belonging to the field of coal gas separation and recycling. According to the invention, different kinds of coal gas and water are separated and recycled respectively, so that the whole system has the advantages of small occupied area, low investment, low running cost, short treatment flow, few equipment, few pollutant discharge points and difficulty in causing environmental pollution. Through setting up equipment such as middling pressure flash vessel, vacuum flash vessel separator and ammonia still to setting up subsider and gas water pitcher top and being connected with inert gas pipeline, make entire system and separation recycling process keep the pressure-fired operation more than 0.2kPa, thereby can guarantee that exhaust VOCs and foul smell can centralized processing in the system. The gas water treated by the deacidification tower is sent to the ammonia distillation tower, so that the gas water going to the biochemical treatment equipment can be subjected to ammonia distillation, the ammonia content in the gas water going to the biochemical treatment equipment can be reduced, and the problem that a biochemical system is difficult to stably operate due to the change of different raw material coals is solved.
Description
Technical Field
The invention relates to the technical field of gas separation and recycling, in particular to a crushed coal pressurized gasification gas water separation and recycling system and method.
Background
Raw gas produced by pressurized gasification of crushed coal contains a large amount of water vapor, dust, and carbonized byproducts such as tar, light oil, naphthalene, phenol, fatty acid, dissolved gas, inorganic salts, and the like, and the temperature is also high. Therefore, it is necessary to cool and wash it to reduce the temperature and remove harmful substances in the raw gas. In the washing and cooling process of the raw gas, the impurity components enter water to form gas water with various components in gas, liquid and solid states, the gas water components are complex, and the content of the various components is different according to different coal types. The coal gas water cannot be directly treated by conventional biochemical, filtering, reverse osmosis and other methods, and the oil, dust, phenol, ammonia and the like in the coal gas water are separated and recovered, so that valuable substances in the wastewater are recovered on the one hand, and certain economic benefit can be generated; on the other hand, the wastewater can meet the water inlet requirement of the common wastewater treatment method, and is discharged after biochemical treatment reaches the national discharge standard.
The technological manual of modern coal chemical industry describes the most classical gas-water separation and recovery process, which is also commonly used in the current crushed coal pressurized gasification technology, specifically, the gasified gas water with the pressure of 3.0-6.0MPa and the transformed cooling gas water are respectively sent into a gas-water separation system, and then are firstly cooled to 90 ℃, then enter a gas-water expander for flash expansion to normal pressure, and the dissolved CO in the gas water is obtained 2 、NH 3 And (3) flash evaporation and separation of partial water vapor and other gases. The flash evaporated coal gas water enters a tar separator at the lower part to separate coal gas water from tar by utilizing density difference, and the dust-containing tar with density larger than that of water is discharged from the bottom and can be used as a product or returned to a gasification furnace for gasification again; the light oil and the gas water with the density less than that of water overflow from the upper part of the tar separator to enter the gas water buffer tank, and part of the gas water is pumped back to gasification for recycling through a high-pressure pump, and the redundant gas water enters the light oil separator. The light oil separator is provided with a coke and TPI plate assembly, on one hand, impurities are filtered, oil drops are condensed and then float on the water surface to form an oil layer, light oil is led out through an overflow weir at the upper part and is sent into an oil storage tank, water at the lower part enters a water chamber after passing through the TPI plate and is led out through the overflow weir, and is sent into a double-medium filter by a pump after passing through a buffer tank to be further dedusted and then sent to a phenol and ammonia recovery device.
However, with the development of the gas technology, the technology gradually develops towards the directions of large-scale, energy conservation, environmental protection, high efficiency and stability, and the current conventional crushed coal pressurized gasification technology gas-water separation and recovery flow cannot meet the modern requirements, and is mainly characterized in that:
1. the existing gas water treatment system gathers different types of gas water from different equipment together to carry out gas water separation and recovery, and a plurality of separators and buffers are arranged in the device flow, so that the whole gas water separation and recovery system has large occupied area, high investment, high operation cost, long flow and multiple equipment, and the pollution discharge points are more, and serious environmental pollution is easy to cause.
2. A plurality of buffers, separators and the like are used in the existing gas-water separation and recovery system, and the equipment is operated at normal pressure, so that the discharged VOCs (Volatile Organic Compounds ), odor and the like can not be collected and then are subjected to centralized treatment, and the field environment is severe.
Disclosure of Invention
In order to solve the technical problems, the invention provides a crushed coal pressurized gasification gas water separation and recycling system and method.
In order to solve the technical problems, the invention adopts the following technical scheme:
The utility model provides a broken coal pressurization gasification gas water separation and recycling system, its includes middling pressure flash vessel, first vacuum flash vessel, settling cask, gas water pitcher, deacidification tower, first vacuum flash separator, ammonia still, second vacuum flash vessel, second vacuum flash separator, third vacuum flash separator, flocculant jar, pressure filter, filter fluid reservoir, a plurality of water pumps and pipeline, wherein: the first water inlet of the medium pressure flash evaporator is connected with a high-temperature condensate pipeline, the second water inlet of the medium pressure flash evaporator is connected with a gasified dust-containing gasified water pipeline, the water outlet of the medium pressure flash evaporator is connected with the first water inlet of the first vacuum flash evaporator through a pipeline, the second water inlet of the first vacuum flash evaporator is connected with a low-pressure gasified gas water pipeline, the third water inlet of the first vacuum flash evaporator is connected with a low-pressure starting gas water pipeline, the water outlet of the first vacuum flash evaporator is connected with the water inlet of a settling tank through a pipeline and a water pump, the water outlet of the settling tank is connected with the water inlet of a filter press through a pipeline and the water pump, the water outlet of the filter press is connected with the first water inlet of the gas tank through a pipeline and the water pump, the water inlet of the settling tank is connected with the gas water inlet of the gas water tank through a pipeline, the first gas water outlet of the gas water tank is connected with a gas water recycling device through a pipeline and the water pump, and the top of the settling tank and the gas water tank is connected with an inert gas pipeline in a sealing manner; the gas outlet of the medium-pressure flash evaporator is connected with the gas inlet of the third vacuum flash separator through a pipeline, the gas outlet of the first vacuum flash evaporator is connected with the gas inlet of the first vacuum flash separator, the water inlet of the second vacuum flash evaporator is connected with the transformed low-temperature condensate pipeline, the water outlet of the second vacuum flash evaporator is connected with the second water inlet of the gas tank through a pipeline and a water pump, the gas outlet of the second vacuum flash evaporator is connected with the gas inlet of the second vacuum flash separator through a pipeline, the water outlet of the second vacuum flash separator is connected with the second water inlet of the gas tank through a pipeline, and the gas outlet of the first vacuum flash separator, the gas outlet of the second vacuum flash separator and the gas outlet of the third vacuum flash separator are all connected with a waste gas pipeline; the second gas water outlet of the gas water tank is connected with the water inlet of the deacidification tower through a pipeline and a water pump, the water outlet of the deacidification tower is connected with the water inlet of the ammonia distillation tower through a pipeline and a water pump, and the water outlet of the ammonia distillation tower is connected with the gas water gasification treatment equipment.
Optionally, the crushed coal pressurized gasification gas water separation and recycling system further comprises an oil collecting float and an oil tank, wherein the oil collecting float is arranged in the gas water tank, and the bottom of the oil collecting float is connected with the oil tank through a hose.
Optionally, cooling water sleeves are arranged outside the breathing gas discharge pipelines at the tops of the gas water tank and the settling tank.
A method for separating and recycling crushed coal pressurized gasification coal gas water comprises the following steps:
s1, after high-temperature condensate is transformed and gasified dust-containing gasified water is degassed by a medium-pressure flash evaporator, the gasified low-pressure gas water and low-pressure starting gas water enter a first vacuum flash evaporator together, and dissolved gas is deeply removed in the first vacuum flash evaporator;
s2, mixing the gas water after the solution gas removal with a flocculant from a flocculant tank, and then feeding the mixture into a settling tank;
s3, carrying out filter pressing dehydration on the solid materials settled at the bottom of the settling tank through a filter press to prepare mud cakes, enabling filtrate generated by filter pressing dehydration to enter a filtrate tank and be sent to a gas water tank, and sending gas water at the upper part of the settling tank to the gas water tank;
s4, removing dissolved gas from the transformed low-temperature condensate in a second vacuum flash evaporator, and delivering the gas water after removing the dissolved gas into a gas water tank;
s5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator and the second vacuum flash evaporator to enter the first vacuum flash evaporator and the second vacuum flash evaporator respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator to enter the third vacuum flash evaporator for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator, the second vacuum flash evaporator and the third vacuum flash evaporator to be also fed into the gas water tank;
S6, taking a part of the gas water in the gas water tank as washing water of gasified low-pressure gas water to be recycled by gas water recycling equipment, enabling the rest of the gas water to enter deacidification tower for deacidification, and enabling the deacidified gas water obtained by deacidification in the deacidification tower to enter ammonia distillation tower for ammonia distillation, enabling the gas water obtained by the deacidification in the ammonia distillation tower to go to gas water biochemical treatment equipment, and recycling ammonia water/liquid ammonia generated in the ammonia distillation tower.
Optionally, the high-temperature condensate is converted into gas water with dust content not more than 2000mg/L, temperature of 150-190 ℃ and pressure of 3.0-7.0 MPa; the gasified dust-containing gasified water is coal gas water with dust content not more than 3000mg/L, temperature of 180-200 ℃ and pressure of 3.0-7.0 MPa; the transformed low-temperature condensate is coal gas water with dust content less than 50mg/L, temperature of 40-80 ℃ and pressure of 3.0-5.0 MPa; the low-pressure gasified gas water is gas water with dust content less than 100mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa; the low-pressure starting gas water is gas water with dust content less than 200mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa.
Optionally, the flash evaporation temperature of the medium pressure flash evaporator is 140-160 ℃ and the pressure is 0.4-0.5MPa.
Optionally, the flash evaporation temperature of the first vacuum flash evaporator is 80-86 ℃ and the vacuum degree is 50-60kPa.
Optionally, the flocculant is added in an amount of 3-5g of flocculant to 1 ton of gas water.
Optionally, inert gas is continuously introduced into the tops of the settling tank and the gas water tank.
The beneficial effects of the invention are as follows:
1. the separation and recycling of the gas water are realized by respectively treating the gas water with different classifications of high-temperature condensate, gasified dust-containing gasified water, low-temperature condensate, gasified low-pressure gas water and low-pressure starting gas water, so that the whole process has less equipment, the occupied area of the whole system is small, the investment is low, the running cost is low, the treatment process is short, the equipment is less, the pollutant discharge points are less, the environmental pollution is not easily caused, and the method has the advantages of energy conservation, environmental protection, high efficiency and stability.
2. By arranging equipment such as a medium-pressure flash evaporator, a vacuum flash separator, an ammonia distillation tower and the like and arranging the tops of a settling tank and a gas water tank to be connected with an inert gas pipeline in a sealing way, the whole system and the separation and reuse process can be operated under micro-positive pressure of more than 0.2kPa, so that the exhaust VOCs and odor in the system can be ensured to be intensively treated, and the site environment is friendly.
3. The whole system has simple equipment and safe and stable operation, and can effectively reduce the cost of gas water treatment.
4. Because the ammonia content directly affects the operation stability of the biochemical system, the invention can reduce the ammonia content in the gas water which goes to the biochemical treatment equipment by sending the gas water which is treated by the deacidification tower into the ammonia distillation tower so as to ensure that the gas water which goes to the biochemical treatment equipment can be distilled through the ammonia distillation tower, thereby solving the problem that the biochemical system is difficult to stably operate due to the change of different raw material coals.
Compared with the existing gas-water separation and recycling system, the system and the method have the advantages that the investment is reduced by 50%, and the running cost is saved by 50%.
Drawings
FIG. 1 is a schematic diagram of the system components of the present invention.
FIG. 2 is a schematic diagram of the connection of the present invention to a gasification unit, a scrubbing unit and a conversion unit.
Detailed Description
The invention will be described in further detail below with reference to the drawings and examples.
As shown in fig. 1, the crushed coal pressurized gasification gas-water separation and recycling system in this embodiment includes a medium pressure flash evaporator 1, a first vacuum flash evaporator 2, a settling tank 3, a gas water tank 4, a deacidification tower 5, a first vacuum flash separator 6, an ammonia distillation tower 7, a second vacuum flash evaporator 8, a second vacuum flash separator 9, a third vacuum flash separator 10, a flocculant tank 11, a filter press 12, a filtrate tank 13, a plurality of water pumps and pipelines, wherein: the first water inlet of the medium-pressure flash evaporator 1 is connected with a high-temperature condensate pipeline, the second water inlet of the medium-pressure flash evaporator 1 is connected with a gasified dust-containing gasified water pipeline, the water outlet of the medium-pressure flash evaporator 1 is connected with the first water inlet of the first vacuum flash evaporator 2 through a pipeline, the second water inlet of the first vacuum flash evaporator 2 is connected with a low-pressure gasification gas water pipeline, the third water inlet of the first vacuum flash evaporator 2 is connected with a low-pressure starting gas water pipeline, the water outlet of the first vacuum flash evaporator 2 is connected with the water inlet of the settling tank 3 through a pipeline and a water pump, the water outlet of the settling tank 3 is connected with the water inlet of the filter press 12 through a pipeline and a water pump, the water outlet of the filter press 12 is connected with the water inlet of the filtrate tank 13 through a pipeline and a water pump, the water inlet of the settling tank 3 is also connected with the discharge port of the flocculant tank 11 through a pipeline, the gas water outlet of the settling tank 3 is connected with the gas water inlet of the water tank 4 through a pipeline, the first gas water outlet of the gas tank 4 is connected with gas water recovery equipment (gas locking washing equipment and starting washing equipment) through a pipeline and a water pump, and the gas top of the settling tank 4 is connected with the inert gas top of the gas tank 4 in a sealed manner; the gas outlet of the medium-pressure flash evaporator 1 is connected with the gas inlet of a third vacuum flash separator 10 through a pipeline, the gas outlet of the first vacuum flash evaporator 2 is connected with the gas inlet of a first vacuum flash separator 6, the water inlet of a second vacuum flash evaporator 8 is connected with a transformed low-temperature condensate pipeline, the water outlet of the second vacuum flash evaporator 8 is connected with the second water inlet of a gas water tank 4 through a pipeline and a water pump, the gas outlet of the second vacuum flash evaporator 8 is connected with the gas inlet of a second vacuum flash separator 9 through a pipeline, the water outlet of the second vacuum flash separator 9 is connected with the second water inlet of the gas water tank 4 through a pipeline, and the gas outlet of the first vacuum flash separator 6, the gas outlet of the second vacuum flash separator 9 and the gas outlet of the third vacuum flash separator 10 are all connected with a waste gas pipeline; the second gas water outlet of the gas water tank 4 is connected with the water inlet of the deacidification tower 5 through a pipeline and a water pump, the water outlet of the deacidification tower 5 is connected with the water inlet of the ammonia still 7 through a pipeline and a water pump, and the water outlet of the ammonia still 7 is connected with the gas water gasification treatment equipment.
As shown in fig. 2, the gasification unit, the washing unit and the conversion unit are connected before the crushed coal pressurized gasification gas water separation and recycling system in the embodiment of the invention. Specifically, crushed coal raw materials are added into a crushed coal pressurized gasification furnace through a coal adding lock hopper to be pressurized and gasified to generate gasified raw coal gas, the gasified raw coal gas reaches a waste heat boiler after being dedusted through a cyclone separator, and after the heat in the coal gas is recovered by the waste heat boiler, the coal gas is continuously subjected to three-stage dedusting through a Venturi washing device and a raw coal gas washing device and then is sent to a conversion device, a precooler, a middle cooling device, a final cooling device and an ammonia washing tower in a conversion unit. Part of the coal gas in the crushed coal pressurized gasification furnace enters the coal gas locking washing equipment, and the other part also enters the starting coal gas washing equipment. The crushed coal is any one of anthracite, coke or semicoke. Wherein, the precooler generates a transformed high-temperature condensate. Intermediate, final cooling equipment and ammonia wash towers produce shifted low temperature condensate. The venturi scrubbing apparatus produces gasified dust-laden gasification water. The coal gas locking washing device generates low-pressure gasified coal gas water. The starting gas washing equipment generates low-pressure starting gas water.
Optionally, the crushed coal pressurized gasification gas-water separation and recycling system further comprises an oil collecting float 14 and an oil tank 15, wherein the oil collecting float 14 is arranged inside the gas water tank 4, the bottom of the oil collecting float 14 is connected with the oil tank 15 through a hose, the height of the oil collecting float 14 can be changed along with the liquid level in the gas water tank 4, and 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 the hose, so that the collection of the light oil is realized.
Optionally, a cooling water sleeve 16 is arranged outside the breathing gas discharge pipelines at the tops of the gas water tank 4 and the sedimentation tank 3. The cooling water sleeve 16 can cool the breathing gas discharged from the breathing gas discharge pipelines at the tops of the gas water tank 4 and the settling tank 3, so that the odor which is easy to condense is condensed and then flows back to the equipment, thereby avoiding the discharge of VOCs, odor and the like from the gas water tank 4 and the settling tank 3.
The embodiment of the invention also provides a method for separating and recycling the crushed coal pressurized gasification gas, which can be realized by adopting the crushed coal pressurized gasification gas separation and recycling system shown in fig. 1, and specifically comprises the following steps:
s1, after the high-temperature condensate and gasified dust-containing gasified water are degassed by the medium-pressure flash evaporator 1, the high-temperature condensate and gasified low-pressure gas water and low-pressure driving gas water enter the first vacuum flash evaporator 2 together, and solution gas is deeply removed from the first vacuum flash evaporator 2.
Optionally, the flash evaporation temperature of the medium pressure flash evaporator 1 is 140-160 ℃ and the pressure is 0.4-0.5MPa. The flash evaporation temperature of the first vacuum flash evaporator 2 is 80-86 ℃ and the vacuum degree is 50-60kPa.
S2, mixing the gas water after the solution gas removal with the flocculant from the flocculant tank 11, and then delivering the mixture into the settling tank 3.
S3, the solid materials settled at the bottom of the settling tank 3 are subjected to filter pressing and dehydration through a filter press 12 to prepare mud cakes, filtrate generated by the filter pressing and dehydration enters a filtrate tank 13 and is sent to a gas water tank 4, and gas water at the upper part of the settling tank 3 is sent to the gas water tank 4.
Optionally, the flocculant is added in an amount of 3-5g of flocculant to 1 ton of gas water.
S4, removing dissolved gas from the transformed low-temperature condensate in a second vacuum flash evaporator 8, and delivering the gas water after removing the dissolved gas into a gas water tank 4.
S5, condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 respectively enter the first vacuum flash evaporator 6 and the second vacuum flash evaporator 9 for vacuum flash evaporation separation, flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 enters the third vacuum flash evaporator 10 for vacuum flash evaporation separation, and condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 is also sent into the gas water tank 4.
S6, taking a part of coal gas water in the coal gas water tank 4 as washing water for gasifying low-pressure coal gas water, recycling the washing water for coal gas water recycling equipment (coal gas locking washing equipment and starting coal gas washing equipment), enabling the rest coal gas water to enter a deacidification tower 5 for deacidification, enabling the deacidified gas water obtained by deacidification of the deacidification tower 5 to enter an ammonia distillation tower 7 for ammonia distillation, enabling the coal gas water obtained by the deacidification of the deacidification tower 5 to go to coal gas water biochemical treatment equipment, and recycling ammonia water/liquid ammonia generated in the ammonia distillation tower 7.
Wherein the high-temperature condensate is gas water with dust content not more than 2000mg/L, temperature of 150-190 ℃ and pressure of 3.0-7.0 MPa; the gasified dust-containing gasified water is coal gas water with dust content not more than 3000mg/L, temperature of 180-200 ℃ and pressure of 3.0-7.0 MPa; the transformed low-temperature condensate is coal gas water with dust content less than 50mg/L, temperature of 40-80 ℃ and pressure of 3.0-5.0 MPa; the low-pressure gasified gas water is gas water with dust content less than 100mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa; the low-pressure starting gas water is gas water with dust content less than 200mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa.
Optionally, inert gas is continuously introduced into the tops of the settling tank 3 and the gas water tank 4, so that micro positive pressure (0.2-0.5 kPa) of more than 0.2kPa is always maintained in the settling tank 3 and the gas water tank 4.
The method provided by the embodiments of the present invention is illustrated by the following examples.
Example 1
The crushed coal in the embodiment is Jincheng anthracite with water content of 5%, the coal sample is crushed and screened to obtain the coal sample with the particle size of 5-50mm, the coal sample is put into a crushed coal pressurized gasification furnace for pressurized gasification, the gasification pressure is 4.0MPa, the gasification temperature is 1250 ℃, the raw coal gas generated by gasification is divided into high-temperature coal gas water and low-temperature coal gas water according to the dust content, the temperature and the pressure in water during washing, the high-temperature coal gas water is divided into transformed high-temperature condensate and gasified dust-containing gasification water according to the dust content, the temperature and the pressure, and the low-temperature coal gas water is divided into transformed low-temperature condensate, low-pressure gasified coal gas water and low-pressure starting coal gas water according to the dust content, the temperature and the pressure. The gas water with different classifications is separated and recycled respectively, and the whole separation and recycling process of the gas water keeps micro-positive pressure operation larger than 0.2kPa and adopts inert gas protection so as to ensure that VOCs and odor in the system can be treated intensively.
The dust content of the transformed high-temperature condensate obtained by the treatment of the coal sample through the gasification unit, the washing unit and the transformation unit is 1900mg/L, the temperature is 150 ℃, the pressure is 4MPa, the dust content of gasified dust-containing gasified water is 2800mg/L, the temperature is 189 ℃, and the pressure is 4.0MPa. The dust content of the transformed low-temperature condensate is 45mg/L, the temperature is 67.5 ℃, the pressure is 3.75MPa, the dust content of the low-pressure gasified gas water is 90mg/L, the temperature is 70 ℃, the pressure is 0.5MPa, the dust content of the low-pressure drive gas water is 180mg/L, the temperature is 65 ℃, and the pressure is 0.65MPa.
Wherein, the main pollutant characteristic data of the high temperature gas water and the low temperature gas water are respectively shown in table 1 and table 2.
TABLE 1
| Project | Unit (B) | Gasifying dust-containing gasified water | High temperature condensate |
| Dust content | mg/L | ＜3000 | ＜2000 |
| Oil content | mg/L | ＜5 | ＜0.06 |
| COD | mg/L | ＜800 | ＜2500 |
| Total salt | mg/L | ＜2000 | ＜300 |
TABLE 2
| Project | Unit (B) | Conversion of low temperature condensate | Low pressure gasified gas water | Low pressure gas water for starting car |
| Dust content | mg/L | ＜50 | ＜50 | ＜200 |
| Oil content | mg/L | ＜65 | ＜80 | ＜100 |
| COD | mg/L | ＜800 | ＜600 | ＜2500 |
| Total salt | mg/L | ＜10 | ＜500 | ＜700 |
The high-temperature condensate and gasified dust-containing gasified water are subjected to degassing by a medium-pressure flash evaporator 1, and then enter a first vacuum flash evaporator 2 together with gasified low-pressure coal gas water and low-pressure starting coal gas water to deeply remove dissolved gas, wherein the flash evaporation temperature of the medium-pressure flash evaporator 1 is 144 ℃, the pressure is 0.4MPa, the flash evaporation temperature of the first vacuum flash evaporator 2 is 84.8 ℃, and the vacuum degree is 50kPa; adding flocculant into the gas water after the solution gas removal according to the proportion of adding 3g flocculant into 1 ton of gas water, mixing, then sending into a settling tank 3, carrying out filter pressing dehydration on solid materials settled at the bottom of the settling tank 3 through a filter press 12 to prepare mud cakes with the water content of 22%, sending filtrate into a filtrate tank 13, then sending into a gas water tank 4, and sending the gas water at the upper part of the settling tank 3 into the gas water tank 4. The low-temperature condensate is transformed to remove dissolved gas in a second vacuum flash evaporator 8, and the gas water after the dissolved gas removal is sent into a gas water tank 4. S5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 to enter a first vacuum flash evaporator 6 and a second vacuum flash evaporator 9 respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 to enter a third vacuum flash evaporator 10 for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 to be also fed into the gas water tank 4; part of the gas water in the gas water tank 4 is used as washing water of gasified low-pressure gas water to be recycled as gas water recycling equipment, the rest of the gas water enters deacidification tower 5 for deacidification, deacidification gas obtained by deacidification in the deacidification tower 5 is subjected to sulfur removal and recycling equipment, the gas water obtained by deacidification in the deacidification tower 5 enters ammonia distillation tower 7 for ammonia distillation, the gas water obtained by ammonia distillation in the ammonia distillation tower 7 is sent to gas water biochemical treatment equipment, and ammonia water/liquid ammonia generated in the ammonia distillation tower 7 is recycled.
The operation pressure of the whole gas water separation and recycling process is micro-positive pressure operation which is more than 0.2kPa, inert gas is continuously introduced into the tops of the sedimentation tank 3 and the gas water tank 4 to serve as protective gas, the micro-positive pressure of the system pressure is ensured to be more than 0.2kPa, and VOCs, odor and the like in the system can be collected intensively to burn or RTO byproduct steam. The effect of continuously introducing inert gas into the settling tank 3 and the gas water tank 4 to seal the tops of the settling tank 3 and the gas water tank 4 is mainly to prevent negative pressure from occurring in the settling tank 3 and the gas water tank 4 and suck air from the breathing valve of the settling tank and the gas water tank to keep micro-positive pressure in the tank, the normal pressure set value of the sealing valve is preferably 0.2kPa, and the intersection with the set pressure of the breathing valve, the single-calling valve or the control valve and the like is avoided, so that unnecessary inert gas circulation and high running cost are generated.
The embodiment of the invention adopts the anthracite crushed coal pressurized gasification and utilizes the characteristics of low oil content, low COD content and low dust content in coal gas water. In this embodiment, anthracite is used for pressurized gasification, and the anthracite has low water content, generally has a total water content of less than 10%, volatile components of less than 10%, high carbon content, high melting point of coal ash, and high ash content. The true density is generally 1.4-1.8g/cm 3 The anthracite has high mineral content and high true density of 1.8-1.9g/cm 3 In addition, the anthracite has high thermal stability, the anthracite is not easy to pulverize when entering the gasification furnace, the amount of coal dust brought out of the gasification furnace is small, and the density difference between coal dust particles and coal gas water is about large, so that the coal dust is easier to separate, and the residence time of the dust-containing coal gas water separator can be shortened.
At present, the water quality requirement of biochemical treatment equipment is that COD is less than or equal to 3500mg/L, pH is between 8.0 and 9.0, oil content is less than or equal to 50mg/L, and BOD is not more than 1100mg/L. The indexes of the current gas water effluent and recycling are shown in table 3, the oil content in the gas water of the biochemical treatment removing equipment is high, and oxidation treatment is needed before biochemical treatment is carried out, so that the COD content is reduced.
TABLE 3 Table 3
After being treated by the method provided by the embodiment of the invention, the ammonia content, COD content and the like in the gas water which is sent to the biochemical treatment equipment and the gas water for gas water recycling are far smaller than those of the gas water obtained by the current gas water separation and recovery system and method.
Example 2
The crushed coal in the embodiment is Jincheng anthracite with water content of 6%, the coal sample is crushed and screened to obtain a coal sample with the particle size of 5-50mm, the coal sample is put into a crushed coal pressurized gasifier for pressurized gasification, the gasification pressure is 5.0MPa, the gasification temperature is 1250 ℃, the raw coal gas generated by gasification is divided into high-temperature coal gas water and low-temperature coal gas water according to the dust content, the temperature and the pressure in water during washing, the high-temperature coal gas water is divided into transformed high-temperature condensate and gasified dust-containing gasified water according to the dust content, the temperature and the pressure, and the low-temperature coal gas water is divided into transformed low-temperature condensate, low-pressure gasified coal gas water and low-pressure driving coal gas water according to the dust content, the temperature and the pressure. The gas water with different classifications is separated and recycled respectively, the micro-positive pressure operation of more than 0.2kPa is kept in the whole gas water separation and recycling process, and inert gas is adopted for protection, so that VOCs and odor in the system can be treated in a centralized way.
The dust content of the transformed high-temperature condensate obtained by the treatment of the coal sample through the gasification unit, the washing unit and the transformation unit is 1800mg/L, the temperature is 158 ℃, the pressure is 5MPa, the dust content of gasified dust-containing gasified water is 1985mg/L, the temperature is 196 ℃, and the pressure is 5.0MPa. The dust content of the transformed low-temperature condensate is 48mg/L, the temperature is 70.5 ℃, the pressure is 4.75MPa, the dust content of the low-pressure gasified gas water is 98mg/L, the temperature is 72 ℃, the pressure is 0.6MPa, the dust content of the low-pressure drive gas water is 180mg/L, the temperature is 75 ℃ and the pressure is 0.55MPa.
The high-temperature condensate and gasified dust-containing gasified water are subjected to degassing by a medium-pressure flash evaporator 1, and gasified low-pressure coal gas water and low-pressure starting coal gas water enter a first vacuum flash evaporator 2 together to deeply separate dissolved gas, wherein the flash evaporation temperature of the medium-pressure flash evaporator 1 is 148 ℃, the pressure is 0.5MPa, the flash evaporation temperature of the first vacuum flash evaporator 2 is 86 ℃, and the vacuum degree is 60kPa; adding flocculant into the gas water after the solution gas removal according to the proportion of adding 4.5g flocculant into 1 ton of gas water, mixing, then sending into a settling tank 3, carrying out filter pressing dehydration on solid materials settled at the bottom of the settling tank 3 through a filter press 12 to prepare mud cakes with the water content of 28%, sending filtrate into a filtrate tank 13, then sending into a gas water tank 4, and sending the gas water at the upper part of the settling tank 3 into the gas water tank 4. The low-temperature condensate is transformed to remove dissolved gas in a second vacuum flash evaporator 8, and the gas water after the dissolved gas removal is sent into a gas water tank 4. S5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 to enter a first vacuum flash evaporator 6 and a second vacuum flash evaporator 9 respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 to enter a third vacuum flash evaporator 10 for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 to be also fed into the gas water tank 4; part of the gas water in the gas water tank 4 is used as washing water of gasified low-pressure gas water to be recycled as gas water recycling equipment, the rest of the gas water enters deacidification tower 5 for deacidification, deacidification gas obtained by deacidification in the deacidification tower 5 is subjected to sulfur removal and recycling equipment, the gas water obtained by deacidification in the deacidification tower 5 enters ammonia distillation tower 7 for ammonia distillation, the gas water obtained by ammonia distillation in the ammonia distillation tower 7 is sent to gas water biochemical treatment equipment, and ammonia water/liquid ammonia generated in the ammonia distillation tower 7 is recycled.
The micro-positive pressure operation with the operation pressure of the whole gas-water separation and recycling process being more than 0.2kPa is performed, inert gas is continuously introduced into the tops of the sedimentation tank 3 and the gas water tank 4 to serve as protective gas, the micro-positive pressure operation with the system pressure being more than 0.2kPa is ensured, and VOCs, odor and the like in the system can be collected intensively to incinerate or RTO byproduct steam. The effect of continuously introducing inert gas into the top of the settling tank 3 and the gas water tank 4 to seal the top of the settling tank 3 and the gas water tank 4 is mainly to prevent negative pressure from occurring on the settling tank 3 and the gas water tank 4 and suck air from the breathing valve of the settling tank and the gas water tank to keep micro-positive pressure in the tank, the normal pressure set value of the sealing valve is preferably 0.2kPa, and the intersection with the set pressure of the breathing valve, the single-calling valve or the control valve and the like is avoided, so that unnecessary inert gas circulation and high operation cost are generated.
Example 3
The crushed coal in the embodiment is the yangquan anthracite with 8% of water, the coal sample is crushed and screened to obtain the coal sample with the particle size of 5-50mm, the coal sample is put into a crushed coal pressurized gasifier for pressurized gasification, the gasification pressure is 7.0MPa, the gasification temperature is 1350 ℃, the raw coal gas generated by gasification is divided into high-temperature coal gas water and low-temperature coal gas water according to the dust content, the temperature and the pressure in water during washing, the high-temperature coal gas water is divided into transformed high-temperature condensate and gasified dust-containing gasification water according to the dust content, the temperature and the pressure, and the low-temperature coal gas water is divided into transformed low-temperature condensate, low-pressure gasified coal gas water and low-pressure starting coal gas water according to the dust content, the temperature and the pressure. The gas water with different classifications is separated and recycled respectively, the micro-positive pressure operation of more than 0.2kPa is kept in the whole gas water separation and recycling process, and inert gas is adopted for protection, so that VOCs and odor in the system can be treated in a centralized way.
The dust content of the transformed high-temperature condensate obtained by the treatment of the coal sample through the gasification unit, the washing unit and the transformation unit is 1785mg/L, the temperature is 170 ℃, the pressure is 7MPa, the dust content of gasified dust-containing gasified water is 1650mg/L, the temperature is 197 ℃ and the pressure is 7.0MPa. The dust content of the transformed low-temperature condensate is 35mg/L, the temperature is 67.5 ℃, the pressure is 3.75MP, the dust content of the low-pressure gasified gas water is 65mg/L, the temperature is 70 ℃, the pressure is 0.5MPa, the dust content of the low-pressure drive gas water is 150mg/L, the temperature is 60 ℃, and the pressure is 0.5MPa.
The high-temperature condensate and gasified dust-containing gasified water are subjected to degassing by a medium-pressure flash evaporator 1, and gasified low-pressure coal gas water and low-pressure starting coal gas water enter a first vacuum flash evaporator 2 together to deeply separate dissolved gas, wherein the flash evaporation temperature of the medium-pressure flash evaporator 1 is 144 ℃, the pressure is 0.4MPa, the flash evaporation temperature of the first vacuum flash evaporator 2 is 84.8 ℃, and the vacuum degree is 50kPa; adding flocculant into the gas water after the solution gas removal according to the proportion of adding 4.8g flocculant into 1 ton of gas water, mixing, then sending into a settling tank 3, carrying out filter pressing dehydration on solid materials settled at the bottom of the settling tank 3 through a filter press 12 to prepare mud cakes with the water content of 28%, sending filtrate into a filtrate tank 13, then sending into a gas water tank 4, and sending the gas water at the upper part of the settling tank 3 into the gas water tank 4. The low-temperature condensate is transformed to remove dissolved gas in a second vacuum flash evaporator 8, and the gas water after the dissolved gas removal is sent into a gas water tank 4. S5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 to enter a first vacuum flash evaporator 6 and a second vacuum flash evaporator 9 respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 to enter a third vacuum flash evaporator 10 for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 to be also fed into the gas water tank 4; part of the gas water in the gas water tank 4 is used as washing water of gasified low-pressure gas water to be recycled as gas water recycling equipment, the rest of the gas water enters deacidification tower 5 for deacidification, deacidification gas obtained by deacidification in the deacidification tower 5 is subjected to sulfur removal and recycling equipment, the gas water obtained by deacidification in the deacidification tower 5 enters ammonia distillation tower 7 for ammonia distillation, the gas water obtained by ammonia distillation in the ammonia distillation tower 7 is sent to gas water biochemical treatment equipment, and ammonia water/liquid ammonia generated in the ammonia distillation tower 7 is recycled.
The micro-positive pressure operation with the operation pressure of the whole gas-water separation and recycling process being more than 0.2kPa is performed, inert gas is continuously introduced into the tops of the sedimentation tank 3 and the gas water tank 4 to serve as protective gas, the micro-positive pressure operation with the system pressure being more than 0.2kPa is ensured, and VOCs, odor and the like in the system can be collected intensively to incinerate or RTO byproduct steam. The purpose of continuously introducing inert gas into the top of the settling tank 3 and the gas water tank 4 to seal the top of the settling tank 3 and the gas water tank 4 is to prevent negative pressure from occurring in the settling tank 3 and the gas water tank 4 and suck air from the breathing valve of the settling tank and the gas water tank to keep micro-positive pressure in the tank, the normal pressure set value of the sealing valve is preferably 0.2kPa, and the intersection with the set pressure of the breathing valve, the single-calling valve or the control valve and the like is avoided, so that unnecessary inert gas circulation and high operation cost are generated.
Example 4
The crushed coal in the embodiment is semicoke with 8% of water, the coal sample is crushed and screened to obtain the coal sample with the particle size of 5-50mm, the coal sample is put into a crushed coal pressurized gasifier for pressurized gasification, the gasification pressure is 3MPa, the gasification temperature is 1250 ℃, the raw coal gas generated by gasification is divided into high-temperature coal gas water and low-temperature coal gas water according to the dust content, temperature and pressure in water during washing, the high-temperature coal gas water is divided into transformed high-temperature condensate and gasified dust-containing gasified water according to the dust content, temperature and pressure, and the low-temperature coal gas water is divided into transformed low-temperature condensate, low-pressure gasified coal gas water and low-pressure driving coal gas water according to the dust content, temperature and pressure. The gas water with different classifications is separated and recycled respectively, the micro-positive pressure operation of more than 0.2kPa is kept in the whole gas water separation and recycling process, and inert gas is adopted for protection, so that VOCs and odor in the system can be treated in a centralized way.
The dust content of the transformed high-temperature condensate obtained by the treatment of the coal sample through the gasification unit, the washing unit and the transformation unit is 980mg/L, the temperature is 155 ℃ and the pressure is 3MPa, and the dust content of gasified dust-containing gasified water is 1250mg/L, the temperature is 185 ℃ and the pressure is 3.0MPa. The dust content of the transformed low-temperature condensate is 30mg/L, the temperature is 66 ℃, the pressure is 3MPa, the dust content of the low-pressure gasified gas water is 65mg/L, the temperature is 75 ℃, the pressure is 0.5MPa, the dust content of the low-pressure start-up gas water is 120mg/L, the temperature is 60 ℃, and the pressure is 0.5MPa.
The high-temperature condensate and gasified dust-containing gasified water are subjected to degassing by a medium-pressure flash evaporator 1, and gasified low-pressure coal gas water and low-pressure starting coal gas water enter a first vacuum flash evaporator 2 together to deeply separate dissolved gas, wherein the flash evaporation temperature of the medium-pressure flash evaporator 1 is 142 ℃, the pressure is 0.4MPa, the flash evaporation temperature of the first vacuum flash evaporator 2 is 82 ℃, and the vacuum degree is 50kPa; adding flocculant into the gas water after the solution gas removal according to the proportion of adding 3g flocculant into 1 ton of gas water, mixing, then sending into a settling tank 3, carrying out filter pressing dehydration on solid materials settled at the bottom of the settling tank 3 through a filter press 12 to prepare mud cakes with the water content of 23%, sending filtrate into a filtrate tank 13, then sending into a gas water tank 4, and sending the gas water at the upper part of the settling tank 3 into the gas water tank 4. The low-temperature condensate is transformed to remove dissolved gas in a second vacuum flash evaporator 8, and the gas water after the dissolved gas removal is sent into a gas water tank 4. S5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 to enter a first vacuum flash evaporator 6 and a second vacuum flash evaporator 9 respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 to enter a third vacuum flash evaporator 10 for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 to be also fed into the gas water tank 4; part of the gas water in the gas water tank 4 is used as washing water of gasified low-pressure gas water to be recycled as gas water recycling equipment, the rest of the gas water enters deacidification tower 5 for deacidification, deacidification gas obtained by deacidification in the deacidification tower 5 is subjected to sulfur removal and recycling equipment, the gas water obtained by deacidification in the deacidification tower 5 enters ammonia distillation tower 7 for ammonia distillation, the gas water obtained by ammonia distillation in the ammonia distillation tower 7 is sent to gas water biochemical treatment equipment, and ammonia water/liquid ammonia generated in the ammonia distillation tower 7 is recycled.
The micro-positive pressure operation with the operation pressure of the whole gas-water separation and recycling process being more than 0.2kPa is performed, inert gas is continuously introduced into the tops of the sedimentation tank 3 and the gas water tank 4 to serve as protective gas, the micro-positive pressure operation with the system pressure being more than 0.2kPa is ensured, and VOCs, odor and the like in the system can be collected intensively to incinerate or RTO byproduct steam. The purpose of continuously introducing inert gas into the tops of the settling tank 3 and the gas water tank 4 to seal the tops of the settling tank 3 and the gas water tank 4 is to prevent negative pressure from occurring in the settling tank 3 and the gas water tank 4 and suck air from the breathing valve of the settling tank 3 and the gas water tank 4 so as to keep micro positive pressure in the tank, the normal pressure of the sealing valve is set to be 0.4kPa, and the intersection with the set pressure of the breathing valve, the single-calling valve or the control valve and the like should be avoided, so that unnecessary inert gas circulation and high operation cost are generated.
Example 5
The crushed coal in the embodiment is coke with water content of 5%, the coal sample is crushed and screened to obtain the coal sample with particle size of 5-50mm, the coal sample is put into a crushed coal pressurized gasifier for pressurized gasification, the gasification pressure is 3MPa, the gasification temperature is 1250 ℃, the raw coal gas generated by gasification is divided into high-temperature coal gas water and low-temperature coal gas water according to the dust content, temperature and pressure in water during washing, the high-temperature coal gas water is divided into transformed high-temperature condensate and gasified dust-containing gasified water according to the dust content, temperature and pressure, and the low-temperature coal gas water is divided into transformed low-temperature condensate, low-pressure gasified coal gas water and low-pressure driving coal gas water according to the dust content, temperature and pressure. The gas water with different classifications is separated and recycled respectively, the micro-positive pressure operation of more than 0.2kPa is kept in the whole gas water separation and recycling process, and inert gas is adopted for protection, so that VOCs and odor in the system can be treated in a centralized way.
The dust content of the transformed high-temperature condensate obtained by the treatment of the coal sample through the gasification unit, the washing unit and the transformation unit is 1200mg/L, the temperature is 165 ℃, the pressure is 3MPa, the dust content of gasified dust-containing gasified water is 1800mg/L, the temperature is 185 ℃, and the pressure is 3.0MPa. The dust content of the transformed low-temperature condensate is 46mg/L, the temperature is 66 ℃, the pressure is 3.0MPa, the dust content of the low-pressure gasified gas water is 84mg/L, the temperature is 75 ℃, the pressure is 0.5MPa, the dust content of the low-pressure start-up gas water is 150mg/L, the temperature is 78 ℃ and the pressure is 0.7MPa.
The high-temperature condensate and gasified dust-containing gasified water are subjected to degassing by a medium-pressure flash evaporator 1, and gasified low-pressure coal gas water and low-pressure starting coal gas water enter a first vacuum flash evaporator 2 together to deeply separate dissolved gas, wherein the flash evaporation temperature of the medium-pressure flash evaporator 1 is 142 ℃, the pressure is 0.4MPa, the flash evaporation temperature of the first vacuum flash evaporator 2 is 82 ℃, and the vacuum degree is 50kPa; adding flocculant into the gas water after the solution gas removal according to the proportion of adding 3g flocculant into 1 ton of gas water, mixing, then sending into a settling tank 3, carrying out filter pressing dehydration on solid materials settled at the bottom of the settling tank 3 through a filter press 12 to prepare mud cakes with the water content of 22%, sending filtrate into a filtrate tank 13, then sending into a gas water tank 4, and sending the gas water at the upper part of the settling tank 3 into the gas water tank 4. The low-temperature condensate is transformed to remove dissolved gas in a second vacuum flash evaporator 8, and the gas water after the dissolved gas removal is sent into a gas water tank 4. S5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator 2 and the second vacuum flash evaporator 8 to enter a first vacuum flash evaporator 6 and a second vacuum flash evaporator 9 respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator 1 to enter a third vacuum flash evaporator 10 for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator 6, the second vacuum flash evaporator 9 and the third vacuum flash evaporator 10 to be also fed into the gas water tank 4; part of the gas water in the gas water tank 4 is used as washing water of gasified low-pressure gas water to be recycled as gas water recycling equipment, the rest of the gas water enters deacidification tower 5 for deacidification, deacidification gas obtained by deacidification in the deacidification tower 5 is subjected to sulfur removal and recycling equipment, the gas water obtained by deacidification in the deacidification tower 5 enters ammonia distillation tower 7 for ammonia distillation, the gas water obtained by ammonia distillation in the ammonia distillation tower 7 is sent to gas water biochemical treatment equipment, and ammonia water/liquid ammonia generated in the ammonia distillation tower 7 is recycled.
The micro-positive pressure operation with the operation pressure of the whole gas-water separation and recycling process being more than 0.2kPa is performed, inert gas is continuously introduced into the tops of the sedimentation tank 3 and the gas water tank 4 to serve as protective gas, the micro-positive pressure operation with the system pressure being more than 0.2kPa is ensured, and VOCs, odor and the like in the system can be collected intensively to incinerate or RTO byproduct steam. The effect of continuously introducing inert gas into the top of the settling tank 3 and the gas water tank 4 to seal the tops of the settling tank 3 and the gas water tank 4 is to prevent the settling tank 3 and the gas water tank 4 from generating negative pressure and suck air from the breathing valve of the settling tank 3 and the gas water tank 4 so as to keep micro-positive pressure in the tank, the normal pressure of the sealing valve is set to be 0.5kPa, and the intersection with the set pressure of the breathing valve, the single-breathing valve or the control valve and the like should be avoided, so that unnecessary inert gas circulation and high operation cost are generated
It is to be understood that the above embodiments are merely illustrative of the application of the principles of the present invention, but not in limitation thereof. Various modifications and improvements may be made by those skilled in the art without departing from the spirit and substance of the invention, and are also considered to be within the scope of the invention.
Claims (6)
1. The crushed coal pressurized gasification gas water separation and recycling method is characterized by being applied to a crushed coal pressurized gasification gas water separation and recycling system, and the crushed coal pressurized gasification gas water separation and recycling system comprises a medium-pressure flash evaporator (1), a first vacuum flash evaporator (2), a settling tank (3), a gas water tank (4), a deacidification tower (5), a first vacuum flash separator (6), an ammonia still (7), a second vacuum flash evaporator (8), a second vacuum flash separator (9), a third vacuum flash separator (10), a flocculant tank (11), a filter press (12), a filtrate tank (13), a plurality of water pumps and pipelines, wherein:
The water inlet of the medium pressure flash evaporator (1) is connected with a high-temperature condensate pipeline, the second water inlet of the medium pressure flash evaporator (1) is connected with a gasified dust-containing gasified water pipeline, the water outlet of the medium pressure flash evaporator (1) is connected with the first water inlet of the first vacuum flash evaporator (2) through a pipeline, the second water inlet of the first vacuum flash evaporator (2) is connected with a low-pressure gasification gas water pipeline, the third water inlet of the first vacuum flash evaporator (2) is connected with a low-pressure starting gas water pipeline, the water outlet of the first vacuum flash evaporator (2) is connected with the water inlet of the settling tank (3) through a pipeline and a water pump, the water outlet of the settling tank (3) is connected with the water inlet of the filter press (12) through a pipeline and a water pump, the water outlet of the filter press (12) is connected with the first water inlet of the gas tank (4) through a pipeline and a water pump, the water inlet of the settling tank (3) is also connected with the discharge port of the low-pressure gasification gas tank (11) through a pipeline, the water outlet of the settling tank (3) is connected with the gas tank (4) through a water inlet of the gas tank (4) and a gas inlet of the gas tank (4) through a water pump, and the gas inlet of the gas tank is sealed and the gas inlet of the gas tank (4); the gas outlet of the medium-pressure flash evaporator (1) is connected with the gas inlet of the third vacuum flash separator (10) through a pipeline, the gas outlet of the first vacuum flash evaporator (2) is connected with the gas inlet of the first vacuum flash separator (6), the water inlet of the second vacuum flash evaporator (8) is connected with the transformed low-temperature condensate pipeline, the water outlet of the second vacuum flash evaporator (8) is connected with the second water inlet of the gas tank (4) through a pipeline and a water pump, the gas outlet of the second vacuum flash evaporator (8) is connected with the gas inlet of the second vacuum flash separator (9) through a pipeline, the water outlet of the second vacuum flash separator (9) is connected with the second water inlet of the gas tank (4) through a pipeline, and the gas outlet of the first vacuum flash separator (6), the gas outlet of the second vacuum flash separator (9) and the gas outlet of the third vacuum flash separator (10) are all connected with a waste gas pipeline; the second coal gas water outlet of the coal gas water tank (4) is connected with the water inlet of the deacidification tower (5) through a pipeline and a water pump, the water outlet of the deacidification tower (5) is connected with the water inlet of the ammonia distillation tower (7) through a pipeline and a water pump, and the water outlet of the ammonia distillation tower (7) is connected with the coal gas water gasification treatment equipment; the crushed coal pressurized gasification gas-water separation and recycling system further comprises an oil collecting float (14) and an oil tank (15), wherein the oil collecting float (14) is arranged inside the gas water tank (4), and the bottom of the oil collecting float (14) is connected with the oil tank (15) through a hose; a cooling water sleeve (16) is arranged outside the breathing gas discharge pipelines at the tops of the gas water tank (4) and the sedimentation tank (3);
The method for separating and recycling the crushed coal pressurized gasification gas water comprises the following steps:
s1, after the high-temperature condensate and gasified dust-containing gasified water are degassed by a medium-pressure flash evaporator (1), the high-temperature condensate and gasified dust-containing gasified water enter a first vacuum flash evaporator (2) together with gasified low-pressure coal gas water and low-pressure starting coal gas water, and solution gas is deeply removed from the first vacuum flash evaporator (2);
s2, mixing the gas water after the solution gas removal with a flocculating agent from a flocculating agent tank (11) and then feeding the mixture into a settling tank (3);
s3, filter-pressing and dehydrating the solid materials settled at the bottom of the settling tank (3) through a filter press (12) to prepare mud cakes, wherein filtrate generated by filter-pressing and dehydrating enters a filtrate tank (13) and is sent to a gas water tank (4), and gas water at the upper part of the settling tank (3) is sent to the gas water tank (4);
s4, removing dissolved gas from the transformed low-temperature condensate in a second vacuum flash evaporator (8), and delivering the gas water after removing the dissolved gas into a gas water tank (4);
s5, enabling condensate formed by flash evaporation of the first vacuum flash evaporator (2) and the second vacuum flash evaporator (8) to enter the first vacuum flash evaporator (6) and the second vacuum flash evaporator (9) respectively for vacuum flash evaporation separation, enabling flash evaporation gas obtained by flash evaporation of the medium-pressure flash evaporator (1) to enter the third vacuum flash evaporator (10) for vacuum flash evaporation separation, and enabling condensate condensed by the first vacuum flash evaporator (6), the second vacuum flash evaporator (9) and the third vacuum flash evaporator (10) to be also fed into the gas water tank (4);
S6, taking a part of coal gas water in the coal gas water tank (4) as washing water of gasified low-pressure coal gas water to be recycled by coal gas water recycling equipment, enabling the rest coal gas water to enter deacidification tower (5) for deacidification, deacidifying the deacidified gas obtained by deacidification of the deacidification tower (5) to enter ammonia distillation tower (7) for ammonia distillation, enabling the coal gas water after ammonia distillation in the ammonia distillation tower (7) to go to coal gas water biochemical treatment equipment, and recycling ammonia water/liquid ammonia generated in the ammonia distillation tower (7).
2. The method for separating and recycling the crushed coal pressurized gasification gas water according to claim 1, wherein the transformed high-temperature condensate is gas water with dust content not more than 2000mg/L, temperature of 150-190 ℃ and pressure of 3.0-7.0 MPa; the gasified dust-containing gasified water is coal gas water with dust content not more than 3000mg/L, temperature of 180-200 ℃ and pressure of 3.0-7.0 MPa; the transformed low-temperature condensate is coal gas water with dust content less than 50mg/L, temperature of 40-80 ℃ and pressure of 3.0-5.0 MPa; the low-pressure gasified gas water is gas water with dust content less than 100mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa; the low-pressure starting gas water is gas water with dust content less than 200mg/L, temperature of 60-80 ℃ and pressure of 0.5-0.7 MPa.
3. The method for separating and recycling the crushed coal pressurized gasification gas water according to claim 1, wherein the flash evaporation temperature of the medium pressure flash evaporator (1) is 140-160 ℃ and the pressure is 0.4-0.5MPa.
4. The method for separating and recycling crushed coal pressurized gasification gas water according to claim 1, wherein the flash evaporation temperature of the first vacuum flash evaporator (2) is 80-86 ℃ and the vacuum degree is 50-60kPa.
5. The method for separating and recycling crushed coal pressurized gasification gas water according to claim 1, wherein the addition amount of the flocculant is 1 ton of gas water, and 3-5g of flocculant is added.
6. The method for separating and recycling the crushed coal pressurized gasification gas from water according to claim 1, wherein inert gas is continuously introduced into the tops of the settling tank (3) and the gas water tank (4).
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| CN112408709A (en) * | 2020-11-19 | 2021-02-26 | 赛鼎工程有限公司 | Crushed coal pressurized gasification gas water separation and recycling system and method capable of recycling sewage |
| CN112299667A (en) * | 2020-11-19 | 2021-02-02 | 赛鼎工程有限公司 | System and method for separating and recycling crushed coal pressure gasification gas water |
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