CN111349475A - Pyrolysis gas fractional condensation and heat gradient utilization system and method - Google Patents
Pyrolysis gas fractional condensation and heat gradient utilization system and method Download PDFInfo
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- 238000000197 pyrolysis Methods 0.000 title claims abstract description 36
- 238000009833 condensation Methods 0.000 title claims abstract description 30
- 230000005494 condensation Effects 0.000 title claims abstract description 30
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000007789 gas Substances 0.000 claims abstract description 194
- 239000003034 coal gas Substances 0.000 claims abstract description 161
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 46
- 238000011084 recovery Methods 0.000 claims abstract description 44
- 239000002918 waste heat Substances 0.000 claims abstract description 42
- 239000012716 precipitator Substances 0.000 claims abstract description 40
- 239000000295 fuel oil Substances 0.000 claims abstract description 30
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 238000001816 cooling Methods 0.000 claims abstract description 13
- 238000000605 extraction Methods 0.000 claims abstract description 6
- 238000004064 recycling Methods 0.000 claims abstract description 5
- 239000007788 liquid Substances 0.000 claims description 28
- 239000000428 dust Substances 0.000 claims description 25
- 239000003921 oil Substances 0.000 claims description 21
- 238000010791 quenching Methods 0.000 claims description 21
- 230000001105 regulatory effect Effects 0.000 claims description 20
- 238000003756 stirring Methods 0.000 claims description 20
- 230000000171 quenching effect Effects 0.000 claims description 13
- 238000002309 gasification Methods 0.000 claims description 6
- 239000012717 electrostatic precipitator Substances 0.000 claims description 5
- 229910001220 stainless steel Inorganic materials 0.000 claims description 4
- 239000010935 stainless steel Substances 0.000 claims description 4
- 238000005507 spraying Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims 3
- 238000004891 communication Methods 0.000 claims 1
- 230000007613 environmental effect Effects 0.000 abstract description 2
- 239000011269 tar Substances 0.000 description 45
- 239000003245 coal Substances 0.000 description 7
- 239000000126 substance Substances 0.000 description 4
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 239000002351 wastewater Substances 0.000 description 3
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 230000000903 blocking effect Effects 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 208000005156 Dehydration Diseases 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 239000013505 freshwater Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 239000003350 kerosene Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000002407 reforming Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 229930195734 saturated hydrocarbon Natural products 0.000 description 1
- 239000004071 soot Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/02—Dust removal
- C10K1/028—Dust removal by electrostatic precipitation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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Abstract
The invention provides a pyrolysis gas fractional condensation and heat gradient utilization system and a method, belongs to the field of pyrolysis gas treatment, and aims to solve the problems that heat is not effectively recovered and tar is not subjected to quality-based extraction in the conventional high-temperature gas cooling process. The system capable of carrying out fractional condensation and heat gradient recycling on high-temperature coal gas generated in the pyrolysis process is provided by arranging equipment such as a high-temperature superheater, a coal gas high-temperature electric precipitator, a coal gas waste heat recovery device, a coal gas cooler and a coal gas low-temperature cooler. Through setting up equipment such as a plurality of fluid-discharge tubes, oil-water separation pond, tar agitator tank and heavy oil agitator tank for this system can also carry out the branch matter to the tar that heat step recycle process produced and draw. Therefore, the system can obviously improve the heat recovery utilization rate of the high-temperature coal gas, realize the gradient utilization of energy and improve the economical efficiency, environmental protection and safety of the system operation.
Description
Technical Field
The invention relates to the technical field of pyrolysis gas treatment, in particular to a pyrolysis gas fractional condensation and heat gradient utilization system and method.
Background
Coal is a main energy source and an important industrial raw material in China, in recent years, the coal industry has been developed greatly, the coal yield is increased rapidly, the productivity level is improved greatly, and outstanding contributions are made to the healthy development of the economy and the society, but the problems of extensive utilization mode of coal, low energy efficiency, serious pollution and the like are not solved fundamentally. In order to further improve the clean and efficient utilization level of coal and effectively relieve the state of rich coal, poor oil and less gas in China, various groups and scientific research institutes in China take coal as a raw material and prepare chemical products such as oil, gas and the like through processes such as pyrolysis gasification and the like. In the pyrolysis gasification process, the generated high-temperature coal gas is usually washed with water to mix and cool dust-containing tar in the coal gas, and the residual gas is processed and utilized to prepare chemical products. The process cannot utilize most heat contained in the high-temperature coal gas in a gradient manner, the energy loss is large, the lost heat is dissipated into the atmosphere in the form of heat, and the quality is not extracted in advance according to the quality of tar in the cooling process.
Disclosure of Invention
In order to solve the technical problems that heat is not effectively recovered and tar is not subjected to quality-based extraction in the existing high-temperature coal gas cooling process, the invention provides a pyrolysis coal gas fractional condensation and heat gradient utilization system and method.
In order to solve the technical problems, the invention adopts the technical scheme that:
the first aspect provides a pyrolysis coal gas fractional condensation and heat cascade utilization system, it includes high temperature over heater, first stop valve, first governing valve, coal gas high temperature electrostatic precipitator, coal gas waste heat recovery device, the second stop valve, the second fluid-discharge tube, the coal gas cooler, the third stop valve, the third fluid-discharge tube, the coal gas low temperature cooler, the fourth stop valve, the fourth fluid-discharge tube, the third governing valve, the electrical tar precipitator, the vapour heat exchanger, the fifth stop valve, the sixth stop valve, the fourth governing valve, the fifth governing valve, the oil-water separation tank, tar agitator tank and heavy oil agitator tank, wherein:
the gas inlet of the high-temperature superheater is connected with a high-temperature gas conveying pipeline, the gas inlet of the high-temperature superheater is connected with a high-temperature steam conveying pipeline, and the gas outlet of the high-temperature superheater is connected with the gas inlet of the gas high-temperature electric dust remover through a conveying pipeline; a gas outlet of the gas high-temperature electric precipitator is connected with a gas inlet of a gas waste heat recovery device through a conveying pipeline, and a water inlet of the gas waste heat recovery device is connected with a water source; a gas outlet of the gas waste heat recovery device is connected with a gas inlet of a gas cooler through a conveying pipeline, and a water inlet of the gas cooler is connected with a water source; the gas outlet of the gas cooler is connected with the gas inlet of the gas low-temperature cooler through a conveying pipeline, and the water inlet of the gas low-temperature cooler is connected with a water source; the coal gas outlet of the coal gas low-temperature cooler is connected with the coal gas inlet of the electrical tar precipitator through a conveying pipeline; the gas inlet of the steam-steam heat exchanger is connected with a high-temperature steam conveying pipeline, and the gas inlet of the steam-steam heat exchanger is connected with the gas outlet of the high-temperature superheater through the conveying pipeline; the first stop valve is arranged on a conveying pipeline in front of a coal gas inlet of the high-temperature superheater; the first regulating valve is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas high-temperature electric dust remover; the second stop valve is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas waste heat recovery device; the second liquid discharge pipe is connected with a condensate outlet of the coal gas waste heat recovery device; the third stop valve is arranged on a conveying pipeline in front of a gas inlet of the gas cooler; the third liquid discharge pipe is connected with a condensate outlet of the gas cooler; the fourth stop valve is arranged on a conveying pipeline in front of a gas inlet of the gas cryocooler; the fourth liquid discharge pipe is connected with a condensate outlet of the coal gas low-temperature cooler; the third regulating valve is arranged on a conveying pipeline in front of a coal gas inlet of the electric tar precipitator; the fifth stop valve is arranged on a high-temperature steam conveying pipeline in front of a gas inlet of the high-temperature superheater; the sixth stop valve is arranged on a conveying pipeline in front of a gas inlet of the steam-steam heat exchanger; the fourth regulating valve is arranged on the conveying pipeline behind the gas outlet of the high-temperature superheater; the fifth regulating valve is arranged on a conveying pipeline in front of a gas inlet of the steam-steam heat exchanger; the second liquid discharge pipe, the third liquid discharge pipe and the fourth liquid discharge pipe are all connected with a liquid inlet of the oil-water separation pool; the tar outlet of the electrical tar precipitator and the tar outlet of the oil-water separation tank are both connected with the tar inlet of the tar stirring tank; and a heavy oil outlet of the oil-water separation pool is connected with a heavy oil inlet of the heavy oil stirring tank.
Optionally, pyrolysis coal gas fractional condensation and heat cascade utilize system still includes second governing valve, coal gas quench tower and first drain pipe, the coal gas quench tower is installed between coal gas high temperature electrostatic precipitator and coal gas waste heat recovery device, and the second governing valve is installed on the pipeline before the coal gas entry of coal gas quench tower, and first drain pipe is connected with the condensate outlet of coal gas quench tower, and first drain pipe still is connected with the inlet of water oil separating tank.
Optionally, the electrical tar precipitator employs a honeycomb electrical tar precipitator.
Optionally, the delivery conduit is a stainless steel tube.
In a second aspect, a pyrolysis gas fractional condensation and heat gradient utilization method is provided, where the pyrolysis gas fractional condensation and heat gradient utilization method adopts the pyrolysis gas fractional condensation and heat gradient utilization system of the first aspect, and includes the following steps:
s1, performing primary heat exchange between the high-temperature steam and high-temperature coal gas generated by pyrolysis gasification in a high-temperature superheater, and feeding the coal gas subjected to primary heat exchange into a coal gas high-temperature electric precipitator;
s2, the coal gas high-temperature electric precipitator removes dust from the coal gas after the preliminary heat exchange, and the coal gas after dust removal enters a coal gas waste heat recovery device;
s3, the gas waste heat recovery device carries out secondary temperature reduction on the dedusted gas to reduce the temperature of the secondarily cooled gas to 80-90 ℃, and the secondarily cooled gas enters a gas cooler;
s4, the gas cooler carries out tertiary cooling on the gas subjected to the secondary cooling to ensure that the temperature of the gas subjected to the tertiary cooling is reduced to 60-70 ℃, and the gas subjected to the tertiary cooling enters a gas cryocooler;
s5, cooling the gas cooled for the third time by the gas cryocooler for four times to reduce the temperature of the gas cooled for the fourth time to 30-40 ℃, and feeding the gas cooled for the fourth time into the electric tar precipitator;
s6, performing grading recycling on heat collected in the process of cooling the coal gas by the high-temperature superheater, the coal gas waste heat recovery device, the coal gas cooler and the coal gas low-temperature cooler;
s7, removing light oil in the gas after the temperature is reduced for four times by the electric tar precipitator, and collecting the light oil;
s8, feeding condensate collected by the coal gas waste heat recovery device, the coal gas cooler and the coal gas low-temperature cooler into an oil-water separation tank for separation, and sending light oil separated from the upper layer of the oil-water separation tank and light oil collected at the bottom of the electric tar precipitator in batches to a tar stirring tank for tar extraction;
and S9, sending the heavy oil at the bottom of the oil-water separation pool to a heavy oil stirring tank, and extracting the heavy oil by the heavy oil stirring tank.
Optionally, the pyrolysis gas fractional condensation and heat cascade utilization method further comprises:
and S10, when the temperature of the gas subjected to the primary heat exchange is higher than 540 ℃, starting a spray device of the gas quenching tower to cool and remove dust from the gas subjected to the primary heat exchange, and feeding the cooled and removed gas into a gas waste heat recovery device.
The invention has the beneficial effects that:
through setting up equipment such as high temperature over heater, coal gas high temperature electrostatic precipitator, coal gas waste heat recovery device, coal gas cooler and coal gas low temperature cooler for high temperature coal gas loops through high temperature over heater, coal gas waste heat recovery device, coal gas cooler and coal gas low temperature cooler, through the interval heat transfer of different temperatures, reaches the fractional condensation effect, thereby provides one kind and can carry out fractional condensation and heat step recycle's system to the high temperature coal gas that the pyrolysis in-process produced. Through setting up equipment such as a plurality of fluid-discharge tubes, oil-water separation pond, tar agitator tank and heavy oil agitator tank for this system can also carry out the branch matter to the tar that the fractional condensation process produced and draw. Therefore, the system can obviously improve the heat recovery utilization rate of the high-temperature coal gas, realize the gradient utilization of energy and improve the economical efficiency, environmental protection and safety of the system operation.
Drawings
FIG. 1 is a schematic diagram of the system components of the present invention.
Detailed Description
The present invention will be described in further detail with reference to the accompanying drawings and examples.
As shown in fig. 1, an embodiment of the present invention provides a pyrolysis gas staged condensation and heat cascade utilization system, which includes a high temperature superheater 1, a first stop valve 2, a first regulating valve 3, a gas high temperature electric precipitator 4, a gas waste heat recovery device 8, a second stop valve 9, a second liquid discharge pipe 10, a gas cooler 11, a third stop valve 12, a third liquid discharge pipe 13, a gas low temperature cooler 14, a fourth stop valve 15, a fourth liquid discharge pipe 16, a third regulating valve 17, an electric tar precipitator 18, a gas-steam heat exchanger 19, a fifth stop valve 20, a sixth stop valve 21, a fourth regulating valve 22, a fifth regulating valve 23, an oil-water separation tank 24, a tar stirring tank 25, and a heavy oil stirring tank 26, wherein: the coal gas inlet of the high-temperature superheater 1 is used for being connected with a high-temperature coal gas conveying pipeline, the gas inlet C of the high-temperature superheater 1 is used for being connected with a high-temperature steam conveying pipeline, and the coal gas outlet B of the high-temperature superheater 1 is connected with the coal gas inlet of the coal gas high-temperature electric dust collector 4 through a conveying pipeline; a gas outlet of the gas high-temperature electric dust collector 4 is connected with a gas inlet F of the gas waste heat recovery device 8 through a conveying pipeline, and a water inlet H of the gas waste heat recovery device 8 is connected with a water source; a gas outlet G of the gas waste heat recovery device 8 is connected with a gas inlet J of the gas cooler 11 through a conveying pipeline, and a water inlet L of the gas cooler 11 is connected with a water source; a coal gas outlet K of the coal gas cooler 11 is connected with a coal gas inlet N of a coal gas low-temperature cooler 14 through a conveying pipeline, and a water inlet P of the coal gas low-temperature cooler 14 is connected with a water source; a coal gas outlet O of the coal gas low-temperature cooler 14 is connected with a coal gas inlet of the electrical tar precipitator 18 through a conveying pipeline; a gas inlet S of the steam-steam heat exchanger 19 is used for being connected with a high-temperature steam conveying pipeline, and a gas inlet T of the steam-steam heat exchanger 19 is connected with a gas outlet D of the high-temperature superheater 1 through a conveying pipeline; the first stop valve 2 is arranged on a conveying pipeline in front of a coal gas inlet A of the high-temperature superheater 1; the first regulating valve 3 is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas high-temperature electric dust remover 4; the second stop valve 9 is arranged on a conveying pipeline in front of a coal gas inlet F of the coal gas waste heat recovery device 8; the second liquid discharge pipe 10 is connected with a condensate outlet I of the coal gas waste heat recovery device 8; the third stop valve 12 is arranged on a conveying pipeline in front of a gas inlet J of the gas cooler 11; the third liquid discharge pipe 13 is connected with a condensate outlet M of the gas cooler 11; the fourth stop valve 15 is installed on a conveying pipeline in front of a gas inlet N of the gas cryocooler 14; the fourth liquid discharge pipe 16 is connected with a condensate outlet Q of the gas cryocooler 14; the third regulating valve 17 is arranged on a conveying pipeline in front of a coal gas inlet of the electrical tar precipitator 18; the fifth stop valve 20 is installed on the high-temperature steam conveying pipeline in front of the gas inlet C of the high-temperature superheater 1; the sixth stop valve 21 is installed on the delivery pipeline in front of the gas inlet S of the steam-steam heat exchanger 19; the fourth regulating valve 22 is installed on the conveying pipeline behind the gas outlet D of the high-temperature superheater 1; the fifth regulating valve 23 is installed on the conveying pipeline in front of the gas inlet T of the steam-steam heat exchanger 19; the second drain pipe 10, the third drain pipe 13 and the fourth drain pipe 16 are all connected with a liquid inlet of an oil-water separation pool 24; the tar outlet of the electrical tar precipitator 18 and the tar outlet of the oil-water separation tank 24 are both connected with the tar inlet of a tar stirring tank 25; the heavy oil outlet of the oil-water separation pool 24 is connected with the heavy oil inlet of the heavy oil stirring tank 26.
Wherein, whether the fifth stop valve 20 and the sixth stop valve 21 are opened or not is determined according to whether the temperature of the high-temperature steam meets the heat exchange condition temperature of the high-temperature superheater 1 or not. When the temperature of the high-temperature steam is higher than 320 ℃, the heat exchange condition temperature of the high-temperature superheater 1 is met, at the moment, the fifth stop valve 20 is opened, and the sixth stop valve 21 is closed. When the temperature of the high-temperature steam is lower than 320 ℃, when the heat exchange condition temperature of the high-temperature superheater 1 is not satisfied, at the moment, the sixth stop valve 21 is opened, the fifth stop valve 20 is closed, the high-temperature steam is firstly processed by the steam-steam heat exchanger 19, and after the temperature of the high-temperature steam satisfies the heat exchange condition temperature of the high-temperature superheater 1, the high-temperature steam is output to the high-temperature superheater 1 through the gas outlet U of the steam-steam heat exchanger 19. In addition, when the steam-steam heat exchanger 19 is in operation, the opening degrees of the fourth regulating valve 22 and the fifth regulating valve 23 need to be adjusted to perform steam heat exchange.
Optionally, pyrolysis coal gas fractional condensation and heat cascade utilize system still includes second governing valve 5, coal gas quench tower 6 and first drain pipe 7, coal gas quench tower 6 is installed between coal gas high temperature electrostatic precipitator 4 and coal gas waste heat recovery device 8, and second governing valve 5 is installed on the pipeline before the coal gas entry of coal gas quench tower 6, and first drain pipe 7 is connected with coal gas quench tower 6's condensate outlet W, and first drain pipe 7 still is connected with oil water separating tank 24's inlet. Specifically, when the pyrolysis gas is condensed in a grading manner and the heat gradient utilization system further comprises a gas quenching tower 6, a gas outlet of the gas high-temperature electric precipitator 4 is connected with a gas inlet of the gas quenching tower 6 through a conveying pipeline, and a gas outlet E of the gas quenching tower 6 is connected with a gas inlet F of the gas waste heat recovery device 8 through a conveying pipeline.
Alternatively, the electrical tar precipitator 18 is a honeycomb electrical tar precipitator. The electrical tar precipitator 18 is a vertical cylindrical device, the top cover and the bottom of the shell are respectively in an elliptical, spherical or conical structure, the top cover is provided with an insulation box and a feed box, and a heating device is arranged on the top cover; the precipitation pole of the electrical tar precipitator 18 is made of stainless steel plates, is hexagonal honeycomb-shaped, and has the characteristics of large treatment and high tar removal efficiency which can reach 99%.
Optionally, the delivery conduit is a stainless steel tube. The straight pipeline is used for avoiding the tar condensation from blocking the pipeline and reducing the turning of the conveying pipeline as much as possible.
The embodiment of the invention also provides a pyrolysis gas fractional condensation and heat gradient utilization method, which adopts the pyrolysis gas fractional condensation and heat gradient utilization system of the embodiment and comprises the following steps:
s1, performing primary heat exchange between the high-temperature steam and high-temperature coal gas generated by pyrolysis gasification in the high-temperature superheater 1, and feeding the coal gas subjected to primary heat exchange into the coal gas high-temperature electric precipitator 4.
Wherein, the high-temperature steam refers to steam with the temperature of 320 ℃ and 330 ℃. The temperature of the high-temperature coal gas can be reduced to about 540 ℃ through primary heat exchange. In step S1, the high-temperature superheater 1 heats the high-temperature steam into superheated steam, and the heat collected at this stage can be used as seal gas for the equipment process, and can also be used to meet the requirements of the driving steam required by the material returning device in the pyrolysis furnace and the auxiliary facility unit, the heat tracing of the pipeline and the equipment, the steam used for the equipment soot blowing, and the like.
S2, the coal gas high-temperature electric precipitator 4 removes dust of the coal gas after the preliminary heat exchange, and the coal gas after dust removal enters the coal gas waste heat recovery device 8.
The coal gas high-temperature electric dust remover 4 can remove fine ash particles carried in the coal gas after primary heat exchange, thereby reducing the ash content of the coal gas and tar products, the dust removal efficiency of the coal gas high-temperature electric dust remover reaches more than 95 percent, and the coal gas high-temperature electric dust remover can ensure that the coal gas and tar products with high quality can be obtained subsequently after dust removal.
S3, the gas waste heat recovery device 8 carries out secondary temperature reduction on the dedusted gas to reduce the temperature of the gas to 80-90 ℃, and the gas after secondary temperature reduction enters the gas cooler 11.
S4, the gas cooler 11 carries out the third temperature reduction on the gas after the second temperature reduction, so that the temperature of the gas after the third temperature reduction is reduced to 60-70 ℃, and the gas after the third temperature reduction enters the gas low temperature cooler 14.
S5, the gas cryocooler 14 carries out four-time temperature reduction on the gas subjected to the three-time temperature reduction, so that the temperature of the gas subjected to the four-time temperature reduction is reduced to 30-40 ℃, and the gas subjected to the four-time temperature reduction enters the electric tar precipitator 18.
And S6, performing grading recycling on the heat collected in the process of cooling the coal gas by the high-temperature superheater 1, the coal gas waste heat recovery device 8, the coal gas cooler 11 and the coal gas low-temperature cooler 14.
It should be noted that, there is no specific precedence relationship between the step S6 and the steps S1, S3, S4, and S5, and after the steps S1, S3, S4, and S5 cool the gas, the heat collected in the process of cooling the gas by the high-temperature superheater 1, the gas waste heat recovery device 8, the gas cooler 11, and the gas cryocooler 14 can be recovered and utilized at an appropriate time as needed.
The water sources connected to the gas waste heat recovery device 8, the gas cooler 11 and the gas cryocooler 14 during operation may be wastewater sources, that is, these devices may use wastewater to cool the gas, and only use fresh water when the vehicle is started (at the system start-up stage), so as to realize the recycling of wastewater resources, and reduce the production cost, resource consumption and pollution discharge.
Through the steps S1 to S6, the grading condensation effect of the high-temperature coal gas generated in the pyrolysis gasification process is realized, the heat generated in the condensation process can be recycled in a gradient manner, and the energy utilization level of the high-temperature coal gas is improved.
S7, the electric tar precipitator 18 removes light oil in the gas after the temperature reduction for four times and collects the light oil.
S8, the condensate collected by the coal gas waste heat recovery device 8, the coal gas cooler 11 and the coal gas low-temperature cooler 14 enters the oil-water separation tank 24 for separation, and the light oil separated from the upper layer of the oil-water separation tank 24 and the light oil collected at the bottom of the electric tar precipitator 18 are sent to the tar stirring tank 25 in batches for tar extraction.
During the working process of the system, tar condensed in the second liquid discharge pipe 10, the third liquid discharge pipe 13 and the fourth liquid discharge pipe 16 needs to be released at irregular time so as to prevent the tar from blocking the pipeline.
After the mixture is stirred, kept stand and layered by the tar stirring tank 25, the upper light oil phase is subjected to secondary dehydration and pressurization to form light oil products containing light components, saturated hydrocarbons, aromatic hydrocarbons, non-hydrocarbons and the like, and the light oil products can be used for reforming and preparing chemical raw materials, extracting high value-added products or modifying the high value-added products into high-grade synthetic oil.
S9, the heavy oil at the bottom of the oil-water separation pool 24 is sent to the heavy oil stirring tank 26, and the heavy oil stirring tank 26 extracts the heavy oil.
The heavy oil product containing asphaltene, non-hydrocarbon and the like is formed by stirring, standing and dehydrating the heavy oil in a heavy oil stirring tank 26 and can be used as fuel oil and long-chain hydrocarbon for preparing diesel oil or kerosene by cracking.
Through the steps S8 and S9, the embodiment of the invention not only realizes the graded utilization of the heat of the pyrolysis gas, but also realizes the quality-based extraction of tar.
Optionally, the pyrolysis gas fractional condensation and heat cascade utilization method further comprises: and S10, when the temperature of the gas subjected to the primary heat exchange is higher than 540 ℃, starting a spraying device of the gas quenching tower 6 to cool and remove dust from the gas subjected to the primary heat exchange, and feeding the cooled and removed gas into the gas waste heat recovery device 8.
The gas quenching tower 6 is only used as a high-temperature gas channel under the normal condition, namely the normal operation stage of the whole system, and is only used as a cooling device when the temperature of the gas entering the gas quenching tower 6 is too high, for example, the temperature of the gas exceeds 540 ℃, and the gas is cooled and dedusted by the spraying device. Wherein, in the starting stage of the system or when the gas high-temperature electric dust remover 4 in the system is in failure, the temperature of the gas after the primary heat exchange is higher than 540 ℃ possibly, and the gas quenching tower 6 is put into use in the situations.
It will be understood that the above embodiments are merely exemplary embodiments taken to illustrate the principles of the present invention, which is not limited thereto. It will be apparent to those skilled in the art that various modifications and improvements can be made without departing from the spirit and substance of the invention, and these modifications and improvements are also considered to be within the scope of the invention.
Claims (6)
1. The utility model provides a pyrolysis gas is condensation and heat cascade utilization system in grades, a serial communication port, including high temperature over heater (1), first stop valve (2), first governing valve (3), coal gas high temperature electrostatic precipitator (4), coal gas waste heat recovery device (8), second stop valve (9), second fluid-discharge tube (10), gas cooler (11), third stop valve (12), third fluid-discharge tube (13), coal gas low temperature cooler (14), fourth stop valve (15), fourth fluid-discharge tube (16), third governing valve (17), electric tar precipitator (18), steam-steam heat exchanger (19), fifth stop valve (20), sixth stop valve (21), fourth governing valve (22), fifth governing valve (23), water oil separating pond (24), tar agitator tank (25) and heavy oil agitator tank (26), wherein:
the coal gas inlet of the high-temperature superheater (1) is used for being connected with a high-temperature coal gas conveying pipeline, the gas inlet of the high-temperature superheater (1) is used for being connected with a high-temperature steam conveying pipeline, and the coal gas outlet of the high-temperature superheater (1) is connected with the coal gas inlet of the coal gas high-temperature electric dust collector (4) through a conveying pipeline; a coal gas outlet of the coal gas high-temperature electric dust remover (4) is connected with a coal gas inlet of a coal gas waste heat recovery device (8) through a conveying pipeline, and a water inlet of the coal gas waste heat recovery device (8) is connected with a water source; a coal gas outlet of the coal gas waste heat recovery device (8) is connected with a coal gas inlet of a coal gas cooler (11) through a conveying pipeline, and a water inlet of the coal gas cooler (11) is connected with a water source; a coal gas outlet of the coal gas cooler (11) is connected with a coal gas inlet of a coal gas low-temperature cooler (14) through a conveying pipeline, and a water inlet of the coal gas low-temperature cooler (14) is connected with a water source; a coal gas outlet of the coal gas low-temperature cooler (14) is connected with a coal gas inlet of the electric tar precipitator (18) through a conveying pipeline; a gas inlet of the steam-steam heat exchanger (19) is used for being connected with a high-temperature steam conveying pipeline, and a gas inlet of the steam-steam heat exchanger (19) is connected with a gas outlet of the high-temperature superheater (1) through the conveying pipeline; the first stop valve (2) is arranged on a conveying pipeline in front of a coal gas inlet of the high-temperature superheater (1); the first regulating valve (3) is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas high-temperature electric dust remover (4); the second stop valve (9) is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas waste heat recovery device (8); the second liquid discharge pipe (10) is connected with a condensate outlet of the coal gas waste heat recovery device (8); the third stop valve (12) is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas cooler (11); the third liquid discharge pipe (13) is connected with a condensate outlet of the gas cooler (11); the fourth stop valve (15) is arranged on a conveying pipeline in front of a coal gas inlet of the coal gas cryocooler (14); the fourth liquid discharge pipe (16) is connected with a condensate outlet of the gas cryocooler (14); the third regulating valve (17) is arranged on a conveying pipeline in front of a coal gas inlet of the electrical tar precipitator (18); the fifth stop valve (20) is arranged on a high-temperature steam conveying pipeline in front of a gas inlet of the high-temperature superheater (1); the sixth stop valve (21) is arranged on a conveying pipeline in front of a gas inlet of the steam-steam heat exchanger (19); the fourth regulating valve (22) is arranged on a conveying pipeline behind a gas outlet of the high-temperature superheater (1); the fifth regulating valve (23) is arranged on a conveying pipeline in front of a gas inlet of the steam-steam heat exchanger (19); the second liquid discharge pipe (10), the third liquid discharge pipe (13) and the fourth liquid discharge pipe (16) are all connected with a liquid inlet of the oil-water separation pool (24); a tar outlet of the electrical tar precipitator (18) and a tar outlet of the oil-water separation tank (24) are both connected with a tar inlet of a tar stirring tank (25); the heavy oil outlet of the oil-water separation pool (24) is connected with the heavy oil inlet of the heavy oil stirring tank (26).
2. The pyrolysis gas fractional condensation and heat cascade utilization system of claim 1, further comprising a second regulating valve (5), a gas quenching tower (6) and a first liquid discharging pipe (7), wherein the gas quenching tower (6) is installed between the gas high-temperature electric precipitator (4) and the gas waste heat recovery device (8), the second regulating valve (5) is installed on a conveying pipeline in front of a gas inlet of the gas quenching tower (6), the first liquid discharging pipe (7) is connected with a condensate outlet of the gas quenching tower (6), and the first liquid discharging pipe (7) is further connected with a liquid inlet of the oil-water separation tank (24).
3. The pyrolysis gas fractional condensation and heat cascade system of claim 1, wherein the electrical tar precipitator (18) is a honeycomb electrical tar precipitator.
4. The pyrolysis gas fractional condensation and heat step utilization system of claim 1, wherein the transport conduit is a stainless steel tube.
5. A pyrolysis gas fractional condensation and heat cascade utilization method, which adopts the pyrolysis gas fractional condensation and heat cascade utilization system of any one of claims 1 to 4, characterized by comprising the following steps:
s1, performing primary heat exchange between the high-temperature steam and high-temperature coal gas generated by pyrolysis gasification in a high-temperature superheater (1), and feeding the coal gas subjected to primary heat exchange into a coal gas high-temperature electric precipitator (4);
s2, the coal gas high-temperature electric precipitator (4) removes dust of the coal gas after the primary heat exchange, and the coal gas after dust removal enters a coal gas waste heat recovery device (8);
s3, the gas waste heat recovery device (8) carries out secondary temperature reduction on the dedusted gas to reduce the temperature of the gas to 80-90 ℃, and the gas after secondary temperature reduction enters a gas cooler (11);
s4, the gas cooler (11) carries out tertiary temperature reduction on the gas subjected to the secondary temperature reduction to enable the temperature of the gas subjected to the tertiary temperature reduction to be reduced to 60-70 ℃, and the gas subjected to the tertiary temperature reduction enters a gas low-temperature cooler (14);
s5, the gas cryocooler (14) carries out four-time temperature reduction on the gas subjected to the three-time temperature reduction, so that the temperature of the gas subjected to the four-time temperature reduction is reduced to 30-40 ℃, and the gas subjected to the four-time temperature reduction enters the electric tar precipitator (18);
s6, carrying out grading recycling on heat collected in the process of cooling the coal gas by the high-temperature superheater (1), the coal gas waste heat recovery device (8), the coal gas cooler (11) and the coal gas low-temperature cooler (14);
s7, removing light oil in the gas after the temperature is lowered for four times by the electric tar precipitator (18), and collecting the light oil;
s8, feeding condensate collected by the coal gas waste heat recovery device (8), the coal gas cooler (11) and the coal gas low-temperature cooler (14) into an oil-water separation tank (24) for separation, and sending light oil separated from the upper layer of the oil-water separation tank (24) and light oil collected at the bottom of the electric tar precipitator (18) to a tar stirring tank (25) in batches for tar extraction;
and S9, sending the heavy oil at the bottom of the oil-water separation pool (24) to a heavy oil stirring tank (26), and extracting the heavy oil from the heavy oil stirring tank (26).
6. The pyrolysis gas fractional condensation and heat step utilization method of claim 5, further comprising:
s10, when the temperature of the gas after the primary heat exchange is higher than 540 ℃, starting a spraying device of the gas quenching tower (6) to cool and remove dust from the gas after the primary heat exchange, and then feeding the gas after the temperature reduction and dust removal into the gas waste heat recovery device (8).
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| CN103013583A (en) * | 2012-12-05 | 2013-04-03 | 浙江大学 | Process for dust removing, cooling and tar oil recovering of pyrolysis coal gas |
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| CN106978202A (en) * | 2017-04-20 | 2017-07-25 | 神雾科技集团股份有限公司 | Pyrolysis of coal system and method |
| CN209307309U (en) * | 2018-12-18 | 2019-08-27 | 中国平煤神马能源化工集团有限责任公司 | A kind of dust-laden gas processing system containing pitch coal |
| CN212076971U (en) * | 2020-04-15 | 2020-12-04 | 浙江大学 | Pyrolysis gas fractional condensation and heat cascade utilization system |
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2020
- 2020-04-15 CN CN202010295060.6A patent/CN111349475A/en active Pending
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103013583A (en) * | 2012-12-05 | 2013-04-03 | 浙江大学 | Process for dust removing, cooling and tar oil recovering of pyrolysis coal gas |
| CN103848476A (en) * | 2012-12-09 | 2014-06-11 | 湖北文理学院 | Multiphase separation process of tar electrofishing wastewater |
| CN106978202A (en) * | 2017-04-20 | 2017-07-25 | 神雾科技集团股份有限公司 | Pyrolysis of coal system and method |
| CN209307309U (en) * | 2018-12-18 | 2019-08-27 | 中国平煤神马能源化工集团有限责任公司 | A kind of dust-laden gas processing system containing pitch coal |
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