CN113943587A - Tar distillation method and system - Google Patents
Tar distillation method and system Download PDFInfo
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- CN113943587A CN113943587A CN202111452455.3A CN202111452455A CN113943587A CN 113943587 A CN113943587 A CN 113943587A CN 202111452455 A CN202111452455 A CN 202111452455A CN 113943587 A CN113943587 A CN 113943587A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G7/00—Distillation of hydrocarbon oils
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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
Abstract
The invention relates to the technical field of tar distillation, and discloses a tar distillation method, which comprises the following steps: s1, pretreating the raw material tar; s2, inputting the pretreated raw material tar into a distillation main tower, and distilling until light oil fractions are produced; s3, after the light component oil fraction is stable, extracting part of the light component oil fraction from the lateral line; s4, heating the material at the bottom of the main tower to be distilled to a certain temperature to reduce fuel; s5, extracting the material part at the bottom of the distillation main tower, distilling the material of the rest part at the bottom of the distillation main tower, and mixing the material of the rest part at the bottom of the distillation main tower with the raw material tar newly input to the bottom of the distillation main tower; and S6, mixing the material extracted from the bottom of the distillation main tower with the extracted light component oil fraction. The invention can reduce the use of fuel energy and reduce the cost. The invention also provides a system for realizing the method.
Description
Technical Field
The invention relates to the technical field of tar distillation, in particular to a tar distillation method and a tar distillation system.
Background
Coal tar is a black or blackish brown sticky liquid with pungent odor generated during coal dry distillation, and is called tar for short. Coal tar can be divided into low-temperature coal tar, medium-temperature coal tar and high-temperature coal tar according to the dry distillation temperature, and the coal tar obtained in coke production belongs to the high-temperature coal tar. It is one of coke oven gas purification products condensed and separated in the process of cooling crude gas. Coal tar is generally used as a raw material for processing and refining to prepare various chemical products, can also be directly utilized, such as a material ingredient of a binder for industrial briquette, formed coke and coal-based activated carbon, and can also be used as a fuel oil, a blast furnace injection fuel, a wood preservative oil and a raw material for burning carbon black. Currently, coal tar is produced primarily by distillation to produce maltenes.
Coal tar distillation (coaltar distillation) refers to a coal tar processing procedure of primarily dividing each component into several fractions enriched with a certain compound or compounds according to different boiling points of each component in the coal tar; generally divided into six fractions of light oil, phenol oil, tar, wash oil, anthracene oil and asphalt, and comprises the steps of deslagging, quality homogenization, dehydration, desalination, distillation and the like.
Dehydration is required before tar distillation. The dehydrated tar is distilled and separated into fractions such as tar light oil, phenol oil, naphthalene oil, wash oil, anthracene oil and the like and maltha. The main equipment includes dewatering tower, main tower (distillation tower), heating furnace, heat exchanger, etc. and the distillation process is completed in a single tower, and the bottom of the distillation tower is used mainly in producing soft asphalt. The process is introduced into the Bao steel in the early eighties, and the maltha is the raw material for producing needle coke (or asphalt coke) in the subsequent working section, so the maltha is produced in the distillation process of tar. When tar is distilled, a large amount of energy needs to be consumed to provide heat for distillation, the cost is high, and the energy utilization rate is low.
The prior art discloses a method for continuously producing carbon black oil on line, which comprises the following steps: (1) distilling and dehydrating the coal tar through a dehydrating tower to separate the coal tar into anhydrous tar and light oil fractions; (2) heating the anhydrous tar in the step (1) through a convection section of a tubular furnace, then sending the heated anhydrous tar into a fraction tower, and carrying out reduced pressure distillation to obtain three mixed oil fractions of maltha, phenolic oil, naphthalene oil and wash oil; (3) controlling the content of the wash oil fraction in the three mixed oil fractions in the step (2) by controlling the temperature and the circulation quantity of the outlet of the soft asphalt at the radiation section of the tubular furnace, and ensuring that the wash oil can be fully mixed with the soft asphalt at the bottom of the tower to obtain a carbon black oil fraction; wherein the distillation in the step (1) is normal pressure distillation, and the temperature of the anhydrous tar is about 240-260 ℃; the coal tar dehydration in the step (1) comprises two steps, namely primary dehydration and final dehydration, wherein the coal tar is subjected to primary dehydration and stands for more than 36 hours at the temperature of 80 ℃, and the moisture in the tar is primarily dehydrated to be less than 4%; finally, centrifuging by adopting a three-phase super centrifuge to dehydrate the coal tar to below 2%; the temperature of the top of the dehydration tower in the step (1): 98-105 ℃; the step (2) adopts reduced pressure distillation, the pressure is-35 to-45 kp, and the temperature of the anhydrous tar after the convection section of the tube furnace is heated is 275 to 280 ℃; controlling the reflux quantity of the distillation tower in the step (2) to be 3-5 t/h, controlling the gas phase pressure at the top of the distillation tower to be-35 to-40 kP and controlling the temperature to be 210-220 ℃; the gas phase pressure at the bottom of the tower is-30 kPa, and the temperature at the bottom of the fraction tower is 285-290 ℃; in the step (3), the outlet temperature of the radiation section of the tubular furnace is 390 +/-1 ℃, and the circulation volume of the maltene is 180-200 t/h. In addition, this patent also discloses an apparatus for continuously producing carbon black oil on line, the apparatus comprising: the device comprises a heat exchange device, a dehydration tower, a condensing cooler, an oil-water separator, an anhydrous tar/carbon black oil heat exchanger, a tubular furnace, a fractionating tower, two oil-mixed condensers, a three oil-mixed cooler, a scrubber, a non-condensable gas cooler, a carbon black oil/tar oil heat exchanger and a carbon black oil cooler, wherein the devices are connected by a pump; a first automatic regulating valve on the dehydration tower; and a second automatic regulating valve is arranged on the fractionating tower. The patent needs to consume a large amount of energy in distillation, and has high cost.
Disclosure of Invention
The invention aims to provide a tar distillation method and a tar distillation system with reduced cost.
In order to achieve the above object, the present invention provides a tar distillation method, comprising the steps of:
s1, pretreating the raw material tar;
s2, inputting the pretreated raw material tar into a distillation main tower, and distilling until light oil fractions are produced;
s3, after the light component oil fraction is stable, extracting part of the light component oil fraction from the lateral line;
s4, heating the material at the bottom of the main tower to be distilled to a certain temperature to reduce fuel;
s5, extracting the material part at the bottom of the distillation main tower, distilling the material of the rest part at the bottom of the distillation main tower, and mixing the material of the rest part at the bottom of the distillation main tower with the raw material tar newly input to the bottom of the distillation main tower;
and S6, mixing the material extracted from the bottom of the distillation main tower with the extracted light component oil fraction.
Preferably, the pretreatment of the raw tar in step S1 includes dehydration and preheating.
Preferably, the raw material tar is fed into a dehydrating tower for dehydration and preheating, and simultaneously, light oil fractions are extracted from the side line of the dehydrating tower.
Preferably, in step S2, the distillation main column is subjected to distillation under reduced pressure.
Preferably, in step S2, after the pretreated raw material tar enters the distillation main tower, atmospheric distillation is performed, and when the temperature of the material at the bottom of the distillation main tower is raised to a certain temperature, the tower inside the distillation main tower is evacuated to make the tower inside the distillation main tower negative pressure.
Preferably, in step S3, the light oil fraction taken out from the side of the distillation main column is a wash oil.
The invention also provides a tar distillation system which comprises a pretreatment device, a distillation main tower, a light component oil fraction extraction device, a tower bottom material extraction device and a mixing device, wherein the pretreatment device, the light component oil fraction extraction device and the tower bottom material extraction device are respectively communicated with the distillation main tower, and the light component oil fraction extraction device and the tower bottom material extraction device are communicated with the mixing device.
As preferred scheme, still include raw materials tar input pipeline, preprocessing device includes dehydration tower and heat transfer device, the dehydration tower is equipped with raw materials tar entry and dehydration tar export, the distillation main tower is equipped with dehydration tar entry and soft pitch export, heat transfer device has first entry, second entry, first export and second export, raw materials tar input pipeline with heat transfer device's first entry intercommunication, the soft pitch export passes through tower bottom material draw-off device with heat transfer device's second entry intercommunication, heat transfer device's first export with raw materials tar entry intercommunication, heat transfer device's second export with mixing arrangement intercommunication, dehydration tar export with dehydration tar entry intercommunication.
Preferably, the light component oil fraction extraction device comprises a side extraction pipeline, an extraction valve and a plurality of tower trays, the plurality of tower trays are sequentially arranged at intervals from bottom to top along the height direction of the distillation main tower, the distillation main tower is provided with an extraction port communicated with the tower trays, one end of the side extraction pipeline is connected to the extraction port, the other end of the side extraction pipeline is connected with the mixing device, and the extraction valve is arranged at the extraction port.
As a preferred scheme, the mixing device comprises a mixing kettle and a heating device, wherein a stirring device is arranged in the mixing kettle, and the heating device is arranged on the mixing kettle to heat materials in the mixing kettle.
Compared with the prior art, the invention has the beneficial effects that:
in the process of distilling the tar, the invention extracts the light component oil fraction from the side line, so that the softening point of the material left at the bottom of the distillation main tower is reduced, the heat absorption efficiency of the material left at the bottom of the distillation main tower is high, the material with low softening point is heated more quickly under the condition of burning the same amount of energy, and can reach higher temperature, therefore, after part of the light component oil fraction is extracted, the energy used for burning and supplying heat can be reduced, the temperature rise of the material at the bottom of the distillation main tower is not influenced, and when the material at the bottom of the distillation main tower is extracted, part of the material with high temperature is still remained at the bottom of the distillation main tower, and after the material is mixed with the new and old materials, heat transfer is carried out between the new and old materials, the temperature of the new input material can be increased to reach high temperature, and at the moment, the energy for burning is not required to be increased due to the entering of the new material, therefore, the energy use can be reduced, the cost is reduced; in addition, after distillation, the material extracted from the bottom of the distillation main tower is the produced maltha, and after part of the light component oil fraction is extracted, the light components in the produced maltha are reduced, so that the quality of the produced maltha is reduced.
Drawings
FIG. 1 is a flow chart of a tar distillation method according to an embodiment of the present invention.
FIG. 2 is a schematic diagram of the construction of a tar distillation system according to an embodiment of the present invention.
In the figure, 1-distillation main column; 2-a tower bottom material extraction device; 3-a mixing device; 4-raw material tar input pipeline; 5-a dehydration column; 6-heat exchange device; 7-side production lines; 8-a production valve; 9-a tray; 10-a blow-down pipe; 11-fraction storage; 12-control valve.
Detailed Description
The following detailed description of embodiments of the present invention is provided in connection with the accompanying drawings and examples. The following examples are intended to illustrate the invention but are not intended to limit the scope of the invention.
In the description of the present invention, it should be noted that the terms "center", "longitudinal", "lateral", "up", "down", "front", "back", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", etc., indicate orientations or positional relationships based on those shown in the drawings, and are only for convenience of description and simplicity of description, but do not indicate or imply that the referred device or element must have a specific orientation, be constructed and operated in a specific orientation, and thus, should not be construed as limiting the present invention. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and are not to be construed as indicating or implying relative importance.
In the description of the present invention, it should be noted that, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, e.g., as meaning either a fixed connection, a removable connection, or an integral connection; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood in specific cases to those skilled in the art.
In addition, in the description of the present invention, "a plurality" means two or more unless otherwise specified.
Example one
As shown in FIG. 1, a tar distillation method according to a preferred embodiment of the present invention comprises the steps of:
s1, pretreating the raw material tar;
s2, inputting the pretreated raw material tar into a distillation main tower, and distilling until light oil fractions are produced;
s3, after the light component oil fraction is stable, extracting part of the light component oil fraction from the lateral line;
s4, heating the material at the bottom of the main tower to be distilled to a certain temperature to reduce fuel;
s5, extracting the material part at the bottom of the distillation main tower, distilling the material of the rest part at the bottom of the distillation main tower, and mixing the material of the rest part at the bottom of the distillation main tower with the raw material tar newly input to the bottom of the distillation main tower;
and S6, mixing the material extracted from the bottom of the distillation main tower with the extracted light component oil fraction.
In the process of distilling the tar, the light component oil fraction is extracted from the side line, so that the softening point of the material left at the bottom of the distillation main tower is reduced, the heat absorption efficiency of the material left at the bottom of the distillation main tower is high, the material with the low softening point is heated more quickly under the condition of burning the same amount of energy, and can reach higher temperature, therefore, after part of the light component oil fraction is extracted, the energy used for burning and supplying heat can be reduced, the heating of the material at the bottom of the distillation main tower is not influenced, moreover, when the material at the bottom of the distillation main tower is extracted, part of the material with high temperature is still remained at the bottom of the distillation main tower, after the material is mixed with the new and old material, heat transfer is carried out between the new and old material, the temperature of the new and input material can be increased more quickly, and at the time, the energy for burning is not required to be increased due to the entering of the new material, therefore, the use of the energy can be reduced, the cost is reduced; in addition, after distillation, the material extracted from the bottom of the distillation main tower is produced maltha, and after part of the light component oil fraction is extracted, the light components in the produced maltha are reduced, so that the quality of the produced maltha is reduced.
Example two
The difference between the present embodiment and the first embodiment is that, on the basis of the first embodiment, the present embodiment further describes step S1.
In this example, in step S1, the pretreatment of the raw material tar includes dehydration and preheating. If the tar contains more water, the dehydration time is prolonged, the production capacity of equipment is reduced, the heat consumption is increased, more fuel energy is consumed by direct distillation, and the cost is increased. In addition, water can form stable emulsion in tar, when the water is heated, emulsion water drops are formed, the emulsion water drops can not be immediately evaporated and are overheated, and when the temperature continues to rise, the water drops are rapidly evaporated, so that the accident of oil flushing caused by sudden boiling is caused.
In this example, the raw material tar was fed to a dehydration column to be dehydrated and preheated, and at the same time, a light oil fraction was taken out at the side of the dehydration column. In the dehydration tower, the raw material tar is primarily dehydrated through thermal standing, and then is finally dehydrated through heating. In the final dehydration process, the temperature reaches about 130 ℃, light component oil fraction is separated out, and part of the light component oil fraction is extracted, so that the light components of the material can be reduced, the softening point of the material is reduced, the temperature of the material is increased more quickly, the heat absorption efficiency is high, the use of fuel energy can be reduced, and the cost is reduced.
Other steps in this embodiment are the same as those in the first embodiment, and are not described herein again.
EXAMPLE III
The present embodiment is different from the second embodiment in that, on the basis of the second embodiment, the present embodiment further describes step S2.
In this example, in step S2, distillation under reduced pressure was carried out in the distillation main column. The gas consumption of reduced pressure distillation is low, the use of fuel energy can be reduced, and the cost is reduced. In addition, the distillation is performed under negative pressure, so that the distillation temperature is reduced, and the coking of the tube furnace is reduced; and the decompression operation can improve the operation environment and is beneficial to environmental protection.
Specifically, in step S2, after the pretreated raw material tar enters the distillation main tower, atmospheric distillation is performed, and when the temperature of the material at the bottom of the distillation main tower is raised to a certain temperature, the tower inside the distillation main tower is vacuumized to make the tower inside the distillation main tower have a negative pressure.
Other steps in this embodiment are the same as those in the embodiment, and are not described herein.
Example four
The present embodiment is different from the third embodiment in that, on the basis of the third embodiment, the present embodiment further describes step S3.
In this example, in step S3, the light oil fraction taken out from the side of the distillation main column is a wash oil. Firstly, in the process of distilling tar, if light oil fraction is to be extracted, the side line is cut from top to bottom to obtain phenol oil, naphthalene oil, wash oil and anthracene oil, therefore, if the phenol oil fraction is produced, the side draw unit is disposed at a higher position of the distillation main column, which is inconvenient to install and monitor, and if the anthracene oil fraction is produced, the side draw unit is disposed at a lower position of the distillation main column, where the fraction and the material are mixed, the produced fraction is a mixture, the proportion meeting the quality requirement is not easy to be controlled in the step of mixing the final extracted fraction with the extracted tower bottom material, therefore, the embodiment selects to extract the wash oil fraction, so that the side extraction device is arranged in the middle of the distillation main tower, the side extraction device is additionally installed, the monitoring and the maintenance are facilitated, in addition, because the certain distance is arranged between the bottom of the tower and the extracted washing oil fraction, the components of the extracted washing oil fraction are simpler, and the mixing proportion of the extracted fraction and the extracted tower bottom material is easy to control to meet the quality requirement. In addition, the temperature for separating out the wash oil fraction is lower than that for separating out the phenol oil and the naphthalene oil, so that the use of fuel can be reduced. In addition, in the current tar distillation, carbon black oil is mainly produced, the market demand of the carbon black oil is larger, the carbon black oil is formed by mixing maltha at the bottom of the tower and fractions in the tower, wherein the maltha is mainly mixed with the wash oil, therefore, the wash oil extracted by the embodiment is mixed with materials extracted from the bottom of the tower, the mixing proportion can be strictly controlled, and the carbon black oil meeting different demands is obtained.
It should be noted that the light oil fraction taken out from the side of the distillation main column in step S3 may be phenol oil, naphthalene oil or anthracene oil, and the wash oil of this embodiment is a preferred choice.
Other steps of this embodiment are the same as those of the embodiment, and are not described herein again.
EXAMPLE five
As shown in fig. 2, the present embodiment provides a tar distillation system, which includes a pretreatment device, a distillation main column 1, a light oil fraction extraction device, a bottoms extraction device 2, and a mixing device 3, wherein the pretreatment device, the light oil fraction extraction device, and the bottoms extraction device 2 are respectively communicated with the distillation main column 1, and the light oil fraction extraction device and the bottoms extraction device 2 are communicated with the mixing device 3. In the embodiment, the light component oil fraction is extracted from the distillation main tower 1 through the light component oil fraction extraction device, so that the light components of the material are reduced, the softening point of the material is further reduced, the heat absorption efficiency of the material can be improved, the temperature is increased more quickly, and the use of fuel energy can be reduced. And then the light component oil fraction extracted by the light component oil fraction extraction device is mixed with part of the tower bottom materials extracted by the tower bottom material extraction device 2 by the mixing device 3 to obtain the maltha or the carbon black oil meeting the quality requirement. In this embodiment, the distillation main column 1 is provided with a temperature sensor for monitoring the temperature of the bottoms material. In addition, the tar distillation system of the embodiment further comprises a negative pressure device, the negative pressure device is connected with the distillation main tower 1, the negative pressure device is used for vacuumizing the distillation main tower 1 and is used for carrying out reduced pressure distillation, a pressure sensor is arranged in the distillation main tower 1, and the pressure sensor is used for monitoring the pressure in the distillation main tower 1.
Further, the tar distillation system of this embodiment still includes raw materials tar input pipeline 4, preprocessing device includes dehydration tower 5 and heat transfer device 6, dehydration tower 5 is equipped with raw materials tar entry and dehydration tar export, distillation main tower 1 is equipped with dehydration tar entry and soft pitch export, heat transfer device 6 has first entry, the second entry, first export and second export, raw materials tar input pipeline 4 and heat transfer device 6's first entry intercommunication, the soft pitch export is through tower bottom material draw-out device 2 and heat transfer device 6's second entry intercommunication, heat transfer device 6's first export and raw materials tar entry intercommunication, heat transfer device 6's second export and mixing arrangement 3 intercommunication, dehydration tar export and dehydration tar entry intercommunication. The material that the material extraction device 2 of tower bottom was taken out from the tower bottom of distillation main tower 1 has higher temperature, can be used to the preheating of raw materials tar, improves energy utilization and rate, reduces the use of fuel energy, reduce cost.
In addition, the light component oil fraction extraction device comprises a side extraction pipeline 7, an extraction valve 8 and a plurality of tower trays 9, wherein the tower trays 9 are sequentially arranged at intervals from bottom to top along the height direction of the distillation main tower 1, the distillation main tower 1 is provided with an extraction port communicated with the tower trays 9, one end of the side extraction pipeline 7 is connected with the extraction port, the other end of the side extraction pipeline 7 is connected with the mixing device 3, and the extraction valve 8 is arranged at the extraction port. During distillation, the fraction continuously moves towards the top of the tower, a tray 9 is arranged at the temperature stage of fractionation of the light component oil fraction, fixed light component oil fraction can be collected, and through holes are formed in the tray 9, so that the light component oil fraction at the higher temperature stage can pass through the trays. The timing of the withdrawal of the light oil fraction can be controlled by the withdrawal valve 8. The side draw line 7 is connected to a blow down pipe 10 from which the light component oil fraction to be produced can be taken for inspection and the light component oil fraction produced ineligibly can be discharged to avoid entering the mixing device 3. Further, the light component oil fraction extraction apparatus further includes a fraction storage apparatus 11, the side extraction line 7 is connected to the fraction storage apparatus 11, and the fraction storage apparatus 11 is connected to the mixing apparatus 3 through a control valve 12, and the amount of the light component oil fraction flowing into the mixing apparatus 3 can be controlled so as to control the mixing ratio of the light component oil fraction and the withdrawn bottoms.
In addition, mixing arrangement 3 is equipped with agitating unit including mixing kettle and heating device in the mixing kettle, and heating device locates on the mixing kettle in order to heat the material in the mixing kettle, and the light component oil fraction of adopting mixes through the stirring with the tower bottom material of taking out, and if ambient temperature is low excessively, accessible heating device makes the tower bottom material of taking out rise in temperature, makes the light component oil fraction of adopting and the tower bottom material of taking out fuse more fully. In this embodiment, the mixing kettle is provided with a detection hole, and the materials extracted from the mixing kettle through the detection hole can be detected, so as to determine and adjust the proportion of the extracted light component oil fraction to the extracted tower bottom materials.
To sum up, the embodiment of the present invention provides a tar distillation method, in the process of tar distillation, a light component oil fraction is extracted from a side line, so that the softening point of a material left at the bottom of a distillation main tower is reduced, the heat absorption efficiency of the material left at the bottom of the distillation main tower is high, and the material with the low softening point is heated more quickly and can reach a higher temperature under the condition of equal amount of energy for combustion, so that after part of the light component oil fraction is extracted, energy for combustion heat supply can be reduced, and the heating of the material at the bottom of the distillation main tower is not affected, and when the material at the bottom of the distillation main tower is extracted, part of the material with the high temperature is still remained at the bottom of the distillation main tower, and after the material is mixed with new and old materials, heat transfer is performed between the new and old materials, so that the temperature of the new and old materials can be heated more quickly and can reach the high temperature, and at this time, the energy for combustion does not need to be increased due to the entering of the new materials, therefore, the use of energy can be reduced, and the cost is reduced; in addition, after distillation, the material extracted from the bottom of the distillation main tower is produced maltha, and after part of the light component oil fraction is extracted, the light components in the produced maltha are reduced, so that the quality of the produced maltha is reduced. In addition, the embodiment of the invention also provides a tar distillation system for realizing the tar distillation method.
The above description is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, various modifications and substitutions can be made without departing from the technical principle of the present invention, and these modifications and substitutions should also be regarded as the protection scope of the present invention.
Claims (10)
1. The tar distillation method is characterized by comprising the following steps:
s1, pretreating the raw material tar;
s2, inputting the pretreated raw material tar into a distillation main tower, and distilling until light oil fractions are produced;
s3, after the light component oil fraction is stable, extracting part of the light component oil fraction from the lateral line;
s4, heating the material at the bottom of the main tower to be distilled to a certain temperature to reduce fuel;
s5, extracting the material part at the bottom of the distillation main tower, distilling the material of the rest part at the bottom of the distillation main tower, and mixing the material of the rest part at the bottom of the distillation main tower with the raw material tar newly input to the bottom of the distillation main tower;
and S6, mixing the material extracted from the bottom of the distillation main tower with the extracted light component oil fraction.
2. The tar distillation method according to claim 1, wherein the pretreatment of the raw tar in step S1 includes dewatering and preheating.
3. The method of distilling tar according to claim 2, wherein the raw tar is introduced into a dehydrating tower to be dehydrated and preheated, and the light oil fraction is taken out at a side of the dehydrating tower.
4. The method of distilling tar according to claim 1, wherein the distillation main column is subjected to distillation under reduced pressure in step S2.
5. The tar distillation method according to claim 4, wherein in step S2, after the pretreated tar enters the main distillation tower, atmospheric distillation is performed, and when the temperature of the material at the bottom of the main distillation tower is raised to a certain temperature, the tower inside the main distillation tower is evacuated to make the tower inside the main distillation tower negative.
6. The method of distilling tar according to claim 1, wherein the light oil fraction taken from the side of the distillation main column is a wash oil in step S3.
7. A tar distillation system is characterized by comprising a pretreatment device, a distillation main tower 1, a light component oil fraction extraction device, a tower bottom material extraction device 2 and a mixing device 3, wherein the pretreatment device, the light component oil fraction extraction device and the tower bottom material extraction device 2 are respectively communicated with the distillation main tower 1, and the light component oil fraction extraction device and the tower bottom material extraction device 2 are communicated with the mixing device 3.
8. The tar distillation system according to claim 7, further comprising a raw tar input pipeline 4, wherein the pretreatment device comprises a dehydration tower (5) and a heat exchange device (6), the dehydration tower (5) is provided with a raw tar inlet and a dehydrated tar outlet, the distillation main tower 1 is provided with a dehydrated tar inlet and a maltha outlet, the heat exchange device (6) is provided with a first inlet, a second inlet, a first outlet and a second outlet, the raw tar input pipeline 4 is communicated with the first inlet of the heat exchange device (6), the maltha outlet is communicated with the second inlet of the heat exchange device (6) through the tower bottom material extraction device 2, the first outlet of the heat exchange device (6) is communicated with the raw tar inlet, the second outlet of the heat exchange device (6) is communicated with the mixing device 3, the dehydrated tar outlet is communicated with the dehydrated tar inlet.
9. The tar distillation system according to claim 7, wherein the light component oil fraction extraction device comprises a side extraction pipeline (7), an extraction valve (8) and a plurality of trays (9), the trays (9) are sequentially arranged from bottom to top along the height direction of the distillation main tower 1 at intervals, the distillation main tower 1 is provided with an extraction port communicated with the trays (9), one end of the side extraction pipeline (7) is connected to the extraction port, the other end of the side extraction pipeline (7) is connected to the mixing device 3, and the extraction valve (8) is arranged at the extraction port.
10. The tar distillation system as claimed in claim 7, wherein the mixing device 3 comprises a mixing kettle and a heating device, the mixing kettle is provided with a stirring device, and the heating device is provided on the mixing kettle to heat the material in the mixing kettle.
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| CN202111452455.3A CN113943587B (en) | 2021-11-30 | 2021-11-30 | Tar distillation method and system |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102161901A (en) * | 2011-03-19 | 2011-08-24 | 宝钢工程技术集团有限公司 | Coal tar alkali-free normal/reduced-pressure distillation process and device |
| CN102161903A (en) * | 2011-03-22 | 2011-08-24 | 宝钢工程技术集团有限公司 | Coal tar alkali-free short-flow normal/reduced-pressure distillation process and device |
| CN103184061A (en) * | 2011-12-30 | 2013-07-03 | 鞍钢集团工程技术有限公司 | Tar processing technology for producing low-ash pitch and device |
| CN107099318A (en) * | 2017-04-24 | 2017-08-29 | 邯郸鑫宝煤化能源科技开发有限公司 | The method and its device of a kind of on-line continuous production carbon black oil |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102161901A (en) * | 2011-03-19 | 2011-08-24 | 宝钢工程技术集团有限公司 | Coal tar alkali-free normal/reduced-pressure distillation process and device |
| CN102161903A (en) * | 2011-03-22 | 2011-08-24 | 宝钢工程技术集团有限公司 | Coal tar alkali-free short-flow normal/reduced-pressure distillation process and device |
| CN103184061A (en) * | 2011-12-30 | 2013-07-03 | 鞍钢集团工程技术有限公司 | Tar processing technology for producing low-ash pitch and device |
| CN107099318A (en) * | 2017-04-24 | 2017-08-29 | 邯郸鑫宝煤化能源科技开发有限公司 | The method and its device of a kind of on-line continuous production carbon black oil |
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