CN218174881U - Production system for preparing needle coke from medium-low temperature coal tar - Google Patents
Production system for preparing needle coke from medium-low temperature coal tar Download PDFInfo
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- CN218174881U CN218174881U CN202222820990.6U CN202222820990U CN218174881U CN 218174881 U CN218174881 U CN 218174881U CN 202222820990 U CN202222820990 U CN 202222820990U CN 218174881 U CN218174881 U CN 218174881U
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Abstract
The utility model provides a well low temperature coal tar preparation needle coke production system, include: the system comprises a first fractionating tower, a coal tar pitch storage tank, a coal tar pitch heating furnace and a coking tower; the first fractionating tower is communicated with a coal tar pitch storage tank, and the fractionation tail oil flowing out of the first fractionating tower enters the coal tar pitch storage tank; the coal tar pitch storage tank is communicated with a coal tar pitch heating furnace, and the fractionation tail oil in the coal tar pitch storage tank enters the coal tar pitch heating furnace for heating; the coal tar pitch heating furnace is communicated with the coking tower, and the coal tar pitch heated by the coal tar pitch heating furnace enters the coking tower to be processed into needle coke; the bottom of the coking tower is provided with a product outlet, and the needle coke in the coking tower is discharged out of the coking tower from the product outlet. The utility model discloses a coal tar pitch of purification is the raw materials in the production process, compares in the tradition and uses the coal tar to produce needle coke device as the raw materials, saves complicated front end preprocessing device, and the device small investment, production easy and simple to handle has good economic nature.
Description
Technical Field
The utility model relates to a needle coke equipment technical field especially relates to a well low temperature coal tar preparation needle coke production system.
Background
The prior needle coke production process mainly comprises the following steps: the method comprises the steps of taking coal tar as a raw material, obtaining raw material refined pitch for needle coke production through a complex and bulky front end pretreatment device, putting the refined pitch into a heating furnace, introducing water vapor, controlling the weight ratio of the steam injection amount to the feeding amount, heating, controlling the outlet temperature of the heating furnace, transferring the refined pitch into a carbonization tower A and a carbonization tower B, and performing hydraulic decoking and feeding preparation on the carbonization tower B when the carbonization tower A performs carbonization reaction, and vice versa. The needle coke product is obtained at the bottom of the tower and is influenced by the front-end pretreatment process and operation, the traditional process has the defects of low yield, unstable product quality and large fluctuation of key quality indexes such as needle coke volatile components, ash content and the like.
In order to optimize the needle coke production process, improve the coke production efficiency, and reduce key quality indexes such as needle coke volatile components and ash content, the raw materials and the coke production process must be improved and optimized, so as to realize the production of high-quality and low-cost needle coke products.
SUMMERY OF THE UTILITY MODEL
The utility model provides a well low temperature coal tar preparation needle coke production system takes place the pyrolytic reaction with coal tar pitch in the coking tower and generates needle coke, compares the tradition and simplifies needle coke production system, has reduced coal tar pretreatment cost, and the small investment, low in production cost, it is effectual to become burnt, and the product quality is high, has good economic nature.
Realize the utility model discloses the technical scheme of purpose as follows:
a production system for preparing needle coke by using medium and low temperature coal tar comprises: the system comprises a first fractionating tower, a coal tar pitch storage tank, a coal tar pitch heating furnace and a coking tower;
the first fractionating tower is communicated with the coal tar pitch storage tank, and the fractionation tail oil flowing out of the first fractionating tower enters the coal tar pitch storage tank;
the coal tar pitch storage tank is communicated with the coal tar pitch heating furnace, and fractionation tail oil in the coal tar pitch storage tank enters the coal tar pitch heating furnace for heating;
the coal tar pitch heating furnace is communicated with the coking tower, and the coal tar pitch heated by the coal tar pitch heating furnace enters the coking tower to be processed into needle coke;
and a product outlet is formed in the bottom of the coking tower, and needle coke in the coking tower is discharged out of the coking tower from the product outlet.
The utility model discloses a high-quality raw materials refined coal tar pitch of production needle coke is regarded as to the fractionation tail oil that first fractionating tower separates, gets into coal tar pitch storage tank buffer memory. Refined coal tar pitch in a coal tar pitch storage tank is conveyed into a coal tar pitch heating furnace through a pressure pump, water is simultaneously injected into an inlet of the coal tar pitch heating furnace (the water injection proportion is 2% -10%), and the refined coal tar pitch is heated to 420-490 ℃ through the coal tar pitch heating furnace and enters the bottom of a coking tower. The refined coal tar pitch is subjected to various complex pyrolysis reactions in the coking tower to generate needle coke, and the needle coke in the coking tower is removed from a product outlet. The utility model discloses take place pyrolysis reaction with coal tar refined pitch in the coking tower and generate needle coke, compare traditional device, simplify needle coke production system, improved raw coke efficiency and product quality.
In a possible implementation manner, the first fractionating tower is communicated with a coal tar delayed coking device, hot high-temperature oil gas generated by the coal tar delayed coking device enters the first fractionating tower, the first fractionating tower fractionates the hot high-temperature oil gas into fractionation tail oil, and the fractionation tail oil enters the coal tar pitch storage tank.
The utility model discloses lower part in getting into first fractionating tower with the hot high temperature oil gas that coal tar delayed coking device comes, hot high temperature oil gas separates out two way light components at first fractionating tower, and light component is first fractionating tower top of the tower product all the way, and another a set of light component is first fractionating tower siding product, and two way light components form mixed oil after heat, the cooling mixes through the heat transfer, should mix the hydrogenation unit raw materials as low reaches as the oil. And the heavy components in the first fractionating tower flow into a coal tar pitch storage tank from the tower bottom, and the heavy components at the tower bottom are used as raw materials for producing needle coke to refine the coal tar pitch and enter the coal tar pitch storage tank.
In one possible implementation, the first fractionation column is further in communication with a hydrogenation unit;
the top end of the first fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device;
the middle part of the first fractionating tower is communicated with a coking diesel oil delivery tank, and the coking diesel oil delivery tank is communicated with a hydrogenation device.
In a possible implementation mode, the coking tower is also communicated with a second fractionating tower, the top end of the coking tower is communicated with the middle part of the second fractionating tower, and the oil gas in the coking tower enters the second fractionating tower;
the bottom end of the second fractionating tower is also communicated with the coal tar pitch storage tank, and the coal tar pitch generated in the second fractionating tower is discharged from the bottom end and enters the coal tar pitch storage tank.
In a possible implementation manner, the coking towers are multiple, and the coking towers are arranged in parallel;
each coking tower is communicated with the coal tar pitch heating furnace, and each coking tower independently processes the coal tar pitch into needle coke.
In one possible implementation mode, the lateral middle part of the second fractionating tower is communicated with the coking diesel oil delivery tank, and the coking diesel oil delivery tank is communicated with the hydrogenation device;
the top end of the second fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device.
In one possible implementation mode, a heat exchange device is arranged on a communicating pipeline between the second fractionating tower and the coking diesel oil delivery tank;
and a heat exchange device is also arranged on a communicating pipeline of the second fractionating tower and the coking gasoline tank.
In one possible implementation mode, a heat exchange device is arranged on a communicating pipeline between the first fractionating tower and the coking diesel oil delivery tank;
the first fractionating tower and the communicating pipe of the coking gasoline tank are also provided with heat exchange devices.
Compared with the prior art, the beneficial effects of the utility model are that:
the utility model discloses a high-quality raw materials refined coal tar pitch of production needle coke is regarded as to the fractionation tail oil that first fractionating tower separates, gets into coal tar pitch storage tank buffer memory. Refined coal tar pitch in a coal tar pitch storage tank is conveyed into a coal tar pitch heating furnace through a pressure pump, water is simultaneously injected into an inlet of the coal tar pitch heating furnace (the water injection proportion is 2% -10%), and the refined coal tar pitch is heated to 420-490 ℃ through the coal tar pitch heating furnace and enters the bottom of a coking tower. The refined coal tar pitch is subjected to various complex pyrolysis reactions in the coking tower to generate needle coke, and the needle coke in the coking tower is removed from a product outlet. The utility model discloses take place coal tar pitch pyrolytic reaction in the coking tower and generate needle coke, compare the coking tower and simplify needle coke production system, have the convenient advantage of production.
Drawings
FIG. 1 is a schematic diagram of a system for producing needle coke from medium-low temperature coal tar.
Detailed Description
The present invention is described in detail with reference to the embodiments shown in the drawings, but it should be understood that these embodiments are not intended to limit the present invention, and those skilled in the art should understand that the functions, methods, or structural equivalents or substitutions made by these embodiments are within the scope of the present invention.
Referring to fig. 1, an embodiment of the present invention provides a system for producing needle coke from medium-low temperature coal tar, including: the system comprises a first fractionating tower, a coal tar pitch storage tank, a coal tar pitch heating furnace and a coking tower; the first fractionating tower is communicated with a coal tar pitch storage tank, and the fractionation tail oil flowing out of the first fractionating tower enters the coal tar pitch storage tank; the coal tar pitch storage tank is communicated with a coal tar pitch heating furnace, and the fractionation tail oil in the coal tar pitch storage tank enters the coal tar pitch heating furnace for heating; the coal tar pitch heating furnace is communicated with the coking tower, and the coal tar pitch heated by the coal tar pitch heating furnace enters the coking tower to be processed into needle coke; the bottom of the coking tower is provided with a product outlet, and needle coke in the coking tower is discharged out of the coking tower from the product outlet.
The utility model discloses the high-quality raw materials refined coal tar pitch of needle coke is regarded as to the fractionation tail oil that first fractionating tower separates, gets into coal tar pitch storage tank buffer memory. Refined coal tar pitch in a coal tar pitch storage tank is conveyed into a coal tar pitch heating furnace through a pressure pump, water is simultaneously injected into an inlet of the coal tar pitch heating furnace (the water injection proportion is 2% -10%), and the refined coal tar pitch is heated to 420-490 ℃ through the coal tar pitch heating furnace and enters the bottom of a coking tower. The refined coal tar pitch is subjected to various complex pyrolysis reactions in a coking tower to generate needle coke, and the needle coke in the coking tower is extracted from a product outlet.
Based on the scheme, please continue to refer to fig. 1, the first fractionating tower is communicated with the coal tar delayed coking device, hot high-temperature oil gas generated by the coal tar delayed coking device enters the first fractionating tower, the first fractionating tower fractionates the hot high-temperature oil gas into fractionation tail oil, and the fractionation tail oil enters the coal tar pitch storage tank.
The embodiment of the utility model provides a lower part in getting into first fractionating tower with the hot high temperature oil gas that coal tar delayed coking device comes, hot high temperature oil gas separates two way light components at first fractionating tower, and light component is first fractionating tower top of the tower product all the way, and another a set of light component is first fractionating tower side product, and two way light components form mixed oil through heat transfer recovery heat, after the cooling mixes, should mix the oil and regard as the hydrogenation unit raw materials in low reaches. And the heavy components in the first fractionating tower flow into a coal tar pitch storage tank from the tower bottom, and the heavy components at the tower bottom are used as raw materials for producing needle coke to refine the coal tar pitch and enter the coal tar pitch storage tank.
The utility model discloses first fractionating tower of embodiment, its effect is: cutting and separating each fraction of hot oil gas from a coke drum of a coal tar delayed coking device, wherein light-component mixed oil is used as a raw material of a hydrogenation device, and heavy-component refined asphalt is used as a raw material for producing needle coke. The utility model discloses coal tar pitch storage tank, its effect is: fully mixing and caching the refined asphalt from the first fractionating tower and the refined asphalt from the second fractionating tower. The utility model discloses coal tar pitch heating furnace, its effect is: the refined asphalt feedstock is heated to a temperature required for pyrolysis to occur. The utility model discloses coking tower, its effect is: providing a pyrolysis reaction site and flash separation of light component hot oil gas.
Preferably, hot high-temperature oil gas from a coke tower of a coal tar delayed coking device enters the middle lower part of a first fractionating tower, a first fractionating tower top product and a first fractionating tower side product of light component fractions are separated, two paths of light components are subjected to heat exchange to recover heat and are cooled and mixed to form a mixed oil product which is used as a raw material of a downstream hydrogenation device, and heavy components at the bottom of the tower are used as a high-quality raw material for producing needle coke to refine coal tar pitch and enter a refined pitch buffer tank for buffering.
It should be noted that, in the embodiment of the present invention, refined asphalt in the buffer tank is sent into the heating furnace through the pressure pump, and the inlet of the heating furnace is simultaneously provided with a water injection flow (water injection ratio is 2% -10%), and is heated to 420-490 ℃ through the heating furnace, and enters the bottom of the coking tower. The coking tower adopts two intermittent alternate operation to realize continuous production. Various complex pyrolysis reactions occur within the coking drum. The method comprises the following steps of firstly, taking out light fractions such as low-molecular-weight alkane, olefin and the like from the top of a coking tower in a gasification escape manner, taking severe pyrolysis, dehydrogenation and aromatization reactions on part of components, simultaneously generating a small amount of hydrogen and low-molecular-weight aromatic light fractions, taking out the light fractions in an oil-gas manner in an escape manner, taking out the light fractions in an oil-gas manner, taking out the light fractions in a polycondensation reaction process in the third stage, starting to form carbonized solids, simultaneously generating a small amount of hydrogen, low-molecular-weight alkane, olefin and aromatic light fractions in an escape manner, taking out the light fractions in an oil-gas manner in the top of the coking tower, further dehydrogenating and dealkylating the semi-coke solids generated in the fourth stage, and completely coking to generate needle-shaped coke products. And (3) extracting light components from the top of the coking tower, gradually enriching the needle coke products from the bottom of the coking tower to the top of the coking tower, and when the needle coke is accumulated to a certain material level height, reversing the tower to operate and continuously produce, wherein the tower with the full material level is shifted to a coke cooling and removing stage, and the needle coke products are removed from the coking tower and extracted for the next continuous feeding production.
Based on the above scheme, with continuing reference to fig. 1, the first fractionating tower is further communicated with the hydrogenation unit; the top end of the first fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device; the middle part of the first fractionating tower is communicated with a coking diesel oil delivery tank, and the coking diesel oil delivery tank is communicated with a hydrogenation device.
Based on the scheme, please continue to refer to fig. 1, the coking tower is also communicated with a second fractionating tower, the top end of the coking tower is communicated with the middle part of the second fractionating tower, and the oil gas in the coking tower enters the second fractionating tower; the bottom end of the second fractionating tower is also communicated with a coal tar pitch storage tank, and the coal tar pitch generated in the second fractionating tower is discharged from the bottom end and enters the coal tar pitch storage tank.
It should be noted that, the second fractionating tower of the embodiment of the present invention mainly functions as follows: cutting and separating each fraction of hot oil gas from a coking tower, taking light component mixed oil as a raw material of a hydrogenation device, and taking heavy component refined asphalt as a raw material for producing needle coke.
Based on the above scheme, please continue to refer to fig. 1, a plurality of coking drums are arranged in parallel; each coking tower is communicated with a coal tar pitch heating furnace, and each coking tower independently converts the coal tar pitch into needle coke.
The utility model discloses hot oil gas of coking tower top extraction gets into lower part in the second fractionating tower, isolate light component fraction second fractionating tower top of the tower product, second fractionating tower siding product, two way light components are through heat transfer recovery heat, after the cooling mixing, form mixed oil, the mixed oil of extracting with first fractionating tower is as low reaches hydrogenation unit raw materials together, the high-quality raw materials refined coal tar pitch of needle coke production is regarded as to heavy component at the bottom of the tower, extract refined coal tar pitch at the bottom of the tower with first fractionating tower and get into refined pitch buffer tank buffer memory together, as the heating furnace feeding.
Based on the scheme, please continue to refer to fig. 1, the middle part of the side of the second fractionating tower is communicated with the coker diesel delivery tank, and the coker diesel delivery tank is communicated with the hydrogenation device; the top end of the second fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device.
Based on the scheme, please continue to refer to fig. 1, a heat exchange device is installed on a communicating pipe between the second fractionating tower and the coker diesel delivery tank; a heat exchange device is also arranged on a communicating pipeline between the second fractionating tower and the coking gasoline tank.
Based on the scheme, please continue to refer to fig. 1, a heat exchange device is installed on a communicating pipe between the first fractionating tower and the coker diesel delivery tank; the first fractionating tower and the communicating pipe of the coking gasoline tank are also provided with heat exchange devices.
The utility model discloses a high-quality raw materials refined coal tar pitch as production needle coke of fractionation tail oil that first fractionating tower separates gets into coal tar pitch storage tank buffer memory. Refined coal tar pitch in a coal tar pitch storage tank is conveyed into a coal tar pitch heating furnace through a pressure pump, water is simultaneously injected into an inlet of the coal tar pitch heating furnace (the water injection proportion is 2% -10%), and the refined coal tar pitch is heated to 420-490 ℃ through the coal tar pitch heating furnace and enters the bottom of a coking tower. The refined coal tar pitch is subjected to various complex pyrolysis reactions in a coking tower to generate needle coke, and the needle coke in the coking tower is extracted from a product outlet.
The above list of details is only for the practical implementation of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent implementations or modifications that do not depart from the technical spirit of the present invention should be included in the scope of the present invention.
It is obvious to a person skilled in the art that the invention is not restricted to details of the above-described exemplary embodiments, but that it can be implemented in other specific forms without departing from the spirit or essential characteristics of the invention. The present embodiments are therefore to be considered in all respects as illustrative and not restrictive, the scope of the invention being indicated by the appended claims rather than by the foregoing description, and all changes which come within the meaning and range of equivalency of the claims are therefore intended to be embraced therein. Any reference sign in a claim should not be construed as limiting the claim concerned.
Furthermore, it should be understood that although the present description refers to embodiments, not every embodiment may contain only a single embodiment, and such description is for clarity only, and those skilled in the art should integrate the description, and the embodiments may be combined as appropriate to form other embodiments understood by those skilled in the art.
Claims (8)
1. A production system for preparing needle coke by using medium and low temperature coal tar is characterized by comprising: the system comprises a first fractionating tower, a coal tar pitch storage tank, a coal tar pitch heating furnace and a coking tower;
the first fractionating tower is communicated with the coal tar pitch storage tank, and the fractionation tail oil flowing out of the first fractionating tower enters the coal tar pitch storage tank;
the coal tar pitch storage tank is communicated with the coal tar pitch heating furnace, and fractionation tail oil in the coal tar pitch storage tank enters the coal tar pitch heating furnace for heating;
the coal tar pitch heating furnace is communicated with the coking tower, and the coal tar pitch heated by the coal tar pitch heating furnace enters the coking tower to be processed into needle coke;
and a product outlet is formed in the bottom of the coking tower, and needle coke in the coking tower is discharged out of the coking tower from the product outlet.
2. The system for producing needle coke from medium and low temperature coal tar according to claim 1, wherein the first fractionating tower is communicated with a coal tar delayed coking device, hot high temperature oil gas generated by the coal tar delayed coking device enters the first fractionating tower, the first fractionating tower fractionates the hot high temperature oil gas into fractionation tail oil, and the fractionation tail oil enters the coal tar pitch storage tank.
3. The system for producing needle coke from medium and low temperature coal tar according to claim 2, wherein the first fractionating tower is further communicated with a hydrogenation device;
the top end of the first fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device;
the middle part of the first fractionating tower is communicated with a coking diesel oil delivery tank, and the coking diesel oil delivery tank is communicated with a hydrogenation device.
4. The system for producing needle coke from medium and low temperature coal tar according to claim 1, wherein the coking tower is further communicated with a second fractionating tower, the top end of the coking tower is communicated with the middle part of the second fractionating tower, and the oil gas in the coking tower enters the second fractionating tower;
the bottom end of the second fractionating tower is also communicated with the coal tar pitch storage tank, and the coal tar pitch generated in the second fractionating tower is discharged from the bottom end and enters the coal tar pitch storage tank.
5. The system for producing needle coke from medium and low temperature coal tar according to claim 1, wherein the number of coking towers is plural, and the plurality of coking towers are arranged in parallel;
each coking tower is communicated with the coal tar pitch heating furnace, and each coking tower independently processes the coal tar pitch into needle coke.
6. The system for producing needle coke from medium and low temperature coal tar according to claim 4, wherein the middle side of the second fractionating tower is communicated with the coking diesel oil delivery tank, and the coking diesel oil delivery tank is communicated with the hydrogenation device;
the top end of the second fractionating tower is communicated with a coking gasoline tank, and the coking gasoline tank is communicated with a hydrogenation device.
7. The system for producing needle coke from medium-low temperature coal tar as claimed in claim 6, wherein a heat exchange device is installed on a communicating pipeline between the second fractionator and the coker diesel oil delivery tank;
and a heat exchange device is also arranged on a communicating pipeline of the second fractionating tower and the coking gasoline tank.
8. The system for producing needle coke from medium and low temperature coal tar according to claim 3, wherein a heat exchange device is installed on a communicating pipeline between the first fractionating tower and the coking diesel oil delivery tank;
a heat exchange device is also arranged on a communicating pipeline between the first fractionating tower and the coking gasoline tank.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202222820990.6U CN218174881U (en) | 2022-10-25 | 2022-10-25 | Production system for preparing needle coke from medium-low temperature coal tar |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202222820990.6U CN218174881U (en) | 2022-10-25 | 2022-10-25 | Production system for preparing needle coke from medium-low temperature coal tar |
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| CN218174881U true CN218174881U (en) | 2022-12-30 |
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| CN202222820990.6U Active CN218174881U (en) | 2022-10-25 | 2022-10-25 | Production system for preparing needle coke from medium-low temperature coal tar |
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