CN219429932U - Needle coke raw material production device - Google Patents
Needle coke raw material production device Download PDFInfo
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- CN219429932U CN219429932U CN202320344739.9U CN202320344739U CN219429932U CN 219429932 U CN219429932 U CN 219429932U CN 202320344739 U CN202320344739 U CN 202320344739U CN 219429932 U CN219429932 U CN 219429932U
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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
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Abstract
The utility model belongs to the technical field of chemical equipment, and discloses a needle coke raw material production device, wherein oil is conveyed to a dehydration tower through a pipeline, a pump and four-stage heat exchange equipment; the top of the dehydration tower is provided with an oil gas outlet which is sequentially communicated with a first oil-water separator and a second oil-water separator through a pipeline and a pump, the first oil-water separator is also communicated with a waste water tank, and the second oil-water separator is communicated with the dehydration tower through a return pipe; the bottom of the dehydration tower is provided with a water-free tar outlet, the water-free tar outlet is communicated with the atmospheric tower through a pipeline, a pump and a heating furnace, the top of the atmospheric tower is provided with a light oil outlet, the light oil outlet is sequentially communicated with a first cooler, a third oil-water separator and a fourth oil-water separator through a pipeline and a valve, the third oil-water separator is also communicated with a wastewater tank, and the fourth oil-water separator is communicated with the atmospheric tower through a return pipe. The needle coke raw material produced by the method meets the requirements of production of high-quality needle coke on raw materials, and can meet the market demands.
Description
Technical Field
The utility model belongs to the technical field of chemical equipment, and particularly relates to a needle coke raw material production device.
Background
Needle coke is a high-quality carbon raw material which is greatly developed in the 21 st century. The needle coke is calcined and graphitized to prepare the carbon product. In addition to the steel industry, needle coke has wide application in industry, national defense, medical treatment, aerospace, atomic energy and other fields, and thus, the needle coke is widely paid attention to various countries.
Needle coke can be classified into coal-based needle coke and petroleum-based needle coke according to the source of raw materials, wherein coal-based needle coke is co-carbonized with coal tar, coal tar pitch, liquid products produced by directly hydrocracking coal, and several raw materials. The coal tar pitch contains a certain amount of quinoline insoluble substances, which are amorphous carbon generated by heating and polymerizing polymer resin substances, coal dust, coke powder and the like brought along with coal gas from a carbonization chamber of a coke oven, and belong to impurities in needle coke raw materials.
The production of high-quality needle coke has the requirements of soft asphalt softening point of 30-40 ℃ and QI value of less than or equal to 3%; however, the softening point of soft pitch of the raw materials for producing coal-based needle coke is generally higher than 45 ℃, and QI value is higher than 5.0%, so that it is difficult to produce needle coke products with qualified quality, and therefore, the problems are needed to be solved to meet the requirements of needle coke production.
Disclosure of Invention
The technical problems to be solved by the utility model are as follows: the needle coke raw material production device overcomes the defects of the prior art, and the produced needle coke raw material meets the requirements of production of high-quality needle coke on the used raw material, namely, the soft asphalt softening point is 30-40 ℃, the QI value is less than or equal to 3 percent, and the market demand can be met.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
a needle coke raw material production device comprises a dehydration tower, wherein raw material tar is conveyed to the dehydration tower through a pipeline, a pump and four-stage heat exchange equipment; the top of the dehydration tower is provided with an oil gas outlet which is sequentially communicated with a first oil-water separator and a second oil-water separator through a pipeline and a pump, the first oil-water separator is also communicated with a waste water tank, and the second oil-water separator is communicated with the dehydration tower through a return pipe; the bottom of the dehydration tower is provided with an anhydrous tar outlet which is communicated with the atmospheric tower through a pipeline, a pump and a heating furnace, the top of the atmospheric tower is provided with a light oil outlet, the light oil outlet is sequentially communicated with a first cooler, a third oil-water separator and a fourth oil-water separator through a pipeline and a valve, the third oil-water separator is also communicated with a wastewater tank, and the fourth oil-water separator is communicated with the atmospheric tower through a return pipe; the side part of the atmospheric tower is sequentially provided with a phenol oil outlet, a naphthalene oil outlet and a wash oil outlet from top to bottom, the phenol oil outlet and the naphthalene oil outlet are respectively communicated with a second cooler and a third cooler through pipelines and valves, and the second cooler and the third cooler are respectively communicated with a phenol-naphthalene mixing tank; the wash oil outlet is communicated to the side tower through a pipeline and a valve; the bottom of the atmospheric tower is provided with a soft asphalt outlet, and the soft asphalt outlet and a material outlet at the bottom of the side tower are respectively communicated to a product storage tank through a pipeline, a pump and a valve.
Preferably, the dehydration tower is a dehydration tower model T84001 phi 2200/1200 multiplied by 4000/5900. The manufacturing method is produced by the equipment factory of the golden tower mechanical limited company of the Feicheng.
The crude tar is recovered by spraying coal gas generated in the coking process with circulating ammonia water and condensing and cooling in a primary cooler. It contains a large amount of moisture. At present, crude tar is used for washing naphthalene, and the moisture content of the tar sent to a tar refining system is still about 4 percent, sometimes even 8 to 10 percent although the crude tar is heated, stood and dehydrated in the prior art.
Tar contains much water, which is detrimental to its distillation operation. In a continuous distillation system of a tube furnace, if tar contains much water, the pressure of the system is obviously increased, the resistance is increased, and the operation system is disturbed. At this time, the tar handling amount must be reduced, otherwise the piping equipment is broken due to high pressure, resulting in fire. Thus, tar must be dehydrated to be distilled. Heating the primarily dehydrated tar to 130 ℃ and sending the primarily dehydrated tar into a dehydration tower, continuously heating the tower bottom to 140 ℃ by using a steam indirect heater, and then sending the primarily dehydrated tar into a tube furnace to remove part of light oil and water, so that the tar is dehydrated to below 0.3% -0.5%.
Preferably, the four-stage heat exchange equipment is a tar/light oil heat exchanger, a tar/naphthalene oil heat exchanger, a soft asphalt/tar heat exchanger and a tar preheater in sequence. Wherein the type of the tar/light oil heat exchanger is H84001 phi 900 multiplied by 7621 F=212 square meters, which is produced by Shandong North electromechanical equipment Co., ltd; the type of the tar/naphthalene oil heat exchanger is H84002 phi 700 multiplied by 6382 F=94.4 square meters, which is produced by the company of Feicheng gold tower machinery Co., ltd; the model of the soft asphalt/tar heat exchanger is H84003 phi 900 x 7432 x 2 F=212 x 2 square meters, which is produced by the company of electromechanical equipment Co., ltd; the model of the tar preheater is H84010 phi 650 multiplied 6361 F=72.9 square meters, which is produced by the company of electromechanical equipment Co., ltd.
Preferably, the first oil-water separator is of the type V84001 Φ1600×5800 v=12.8m 3 Manufactured by Shandong North electromechanical equipment stock Co.Ltd; the second oil-water separator is of the type V84002 Φ1600×5800 v=12.8m 3 Manufactured by Shandong North electromechanical equipment stock Co.Ltd; the third oil-water separator is of the type V84003 Φ1600×5800 v=12.8m 3 Manufactured by Shandong North electromechanical equipment stock Co.Ltd; the fourth oil-water separator is of the type V84004 Φ1600×5800 v=12.8m 3 Manufactured by Shandong North electromechanical devices, inc.
Preferably, the second oil-water separator and the fourth oil-water separator are also communicated with the tar light oil storage tank through pipelines and valves respectively. Temporary storage is carried out on tar and light oil after oil-water separation, and other components are returned to the dehydration tower or the normal pressure tower for continuous separation.
Preferably, a heater is further arranged on the tower body of the dehydration tower, and the heater protrudes out of the tower body; the heater is a steam heater. And recycling the waste heat of the steam for distillation of the dehydration tower, wherein the heated heater is used for heating materials in other working procedures.
Preferably, an external condenser is arranged above the top of the dehydration tower, and the model of the condenser is H84005 phi 550 x 7334 F=70 square meters, which is produced by Feichong gold tower mechanical Co.
Preferably, the heating furnace is a gas heating furnace.
Preferably, the phenolic naphthalene mixing tank is communicated with the oil mixing tank through a pipeline, a pump and a valve. And (5) temporarily storing the mixed oil.
Preferably, the side tower is also communicated to the atmospheric tower through a return pipe. And refluxing the washing oil to the normal pressure tower for continuous separation and purification.
Preferably, the first cooler is of the type H84006 Φ1400×8479 f= 562.4 square meter, manufactured by the company of electromechanical devices, inc. On north of shan; the second cooler is of the type H84008 phi 500 x 3048 F=15.3 square meters manufactured by Shandong North electromechanical equipment Co., ltd; the third cooler is of the type H84009 Φ500×7062f=54.2 square meters, manufactured by the company of the mechanical company of the gold tower, fatty city.
Preferably, the material outlet at the bottom of the side tower is also communicated to the wash oil storage tank through a pipeline, a valve and a pump. And (5) storing the excessive washing oil after the needle coke raw materials are mixed and prepared for standby.
Due to the adoption of the technical scheme, the utility model has the beneficial effects that:
the utility model carries out distillation and steam blowing on raw material crude tar through a dehydration tower to obtain anhydrous tar, then separates the anhydrous tar into phenol oil, naphthalene oil, tar, wash oil and soft asphalt at the bottom of a tower through an atmospheric tower, wherein the phenol oil and the naphthalene oil are used for mixed oil production, the wash oil and the soft asphalt are mixed according to a proportion to prepare raw materials which accord with needle coke production, and the redundant wash oil is temporarily stored for standby, so that the softening point of the produced needle coke raw materials is 36 ℃, the QI value is 2.87%, and the production requirements of the needle coke are completely met.
Drawings
FIG. 1 is a schematic diagram of a structural circuit of an embodiment of the present utility model;
wherein, 1, a dehydration tower; 2. tar/light oil heat exchanger; 3. tar/naphthalene heat exchanger; 4. a maltha/tar heat exchanger; 5. a tar preheater; 6. a first oil-water separator; 7. a second oil-water separator; 8. a waste water tank; 9. a heating furnace; 10. an atmospheric tower; 11. a first cooler; 12. a third oil-water separator; 13. a fourth oil-water separator; 14. a second cooler; 15. a third cooler; 16. a phenolic naphthalene mixing tank; 17. a side tower; 18. a product storage tank; 19. a wash oil storage tank; 20. a tar light oil storage tank.
Detailed Description
The utility model is further illustrated in the following, in conjunction with the accompanying drawings and examples.
Example 1
As shown in fig. 1, the utility model is a needle coke raw material production device, which comprises a dehydration tower 1, raw material tar is conveyed to the dehydration tower 1 through a pipeline, a pump (not marked) and four-stage heat exchange equipment (not marked), wherein the four-stage heat exchange equipment comprises a tar/light oil heat exchanger 2, a tar/naphthalene oil heat exchanger 3, a soft asphalt/tar heat exchanger 4 and a tar preheater 5 in sequence; the top of the dehydration tower 1 is provided with an oil-gas outlet (not shown), the oil-gas outlet is sequentially communicated with a first oil-water separator 6 and a second oil-water separator 7 through a pipeline and a pump, the first oil-water separator 6 is also communicated with a waste water tank 8, and the second oil-water separator 7 is communicated with the dehydration tower 1 through a return pipe (not shown); the bottom of the dehydration tower 1 is provided with an anhydrous tar outlet (not shown), the anhydrous tar outlet is communicated with an atmospheric tower 10 through a pipeline, a pump and a heating furnace 9, the top of the atmospheric tower 10 is provided with a light oil outlet (not shown), the light oil outlet is sequentially communicated with a first cooler 11, a third oil-water separator 12 and a fourth oil-water separator 13 through a pipeline and a valve (not shown), the third oil-water separator 12 is also communicated with a wastewater tank 8, and the fourth oil-water separator 13 is communicated with the atmospheric tower 10 through a return pipe; the side part of the atmospheric tower 10 is sequentially provided with a phenol oil outlet (not shown), a naphthalene oil outlet (not shown) and a wash oil outlet (not shown) from top to bottom, wherein the phenol oil outlet and the naphthalene oil outlet are respectively communicated with a second cooler 14 and a third cooler 15 through pipelines and valves, and the second cooler 14 and the third cooler 15 are respectively communicated with a phenol naphthalene mixing tank 16; the wash oil outlet is communicated to the side tower 17 through a pipeline and a valve; the bottom of the atmospheric tower 10 is provided with a soft asphalt outlet (not shown), the soft asphalt outlet and the material outlet at the bottom of the side tower 17 are respectively communicated to a product storage tank 18 through a pipeline, a pump and a valve, and the material outlet at the bottom of the side tower is also communicated to a wash oil storage tank 19.
The second oil-water separator 7 and the fourth oil-water separator 13 are also respectively communicated with a tar light oil storage tank 20 through pipelines and valves.
The method is practically applied: raw crude tar at about 80 ℃ is subjected to four-stage heat exchange to 135 ℃ by a tar pump matched with a tar/light oil heat exchanger 2, a tar/naphthalene oil heat exchanger 3, a soft asphalt/tar heat exchanger 4 and a tar preheater 5, and then enters a dehydration tower 1 for distillation dehydration. Part of the water and tar light oil in the crude tar is discharged as oil gas through the top of the dehydration tower 1, a condenser (not shown) arranged outside the top of the dehydration tower 1 is condensed to 115 ℃ and then is sent to the first oil-water separator 6 for oil-water separation, the separated wastewater is sent to the wastewater tank 8, the condensed tar light oil flows into the second oil-water separator 7, the separated light oil is extracted into a tar light oil storage tank 20, and other components are returned to the dehydration tower 1 as reflux liquid for continuous separation. The temperature of the anhydrous tar discharged from the bottom of the dehydration tower 1 is 145 ℃, and the anhydrous tar is pumped out by a pump and sent to a normal pressure distillation system.
The anhydrous tar is heated to 330 ℃ by a heating furnace 9, and is supplied to an atmospheric tower 10 in a gas-liquid mixed phase state, and the atmospheric tower 10 is supplied with steam from the bottom of the tower, so that the material is directly steamed and blown. The oil vapor escaping from the top of the atmospheric tower 10 is cooled to about 40 ℃ by a first cooler 11, flows into a third oil-water separator 12 and is subjected to oil-water separation; the separated tar and light oil flows into the fourth oil-water separator 13 again, and is refluxed and extracted by the tar and light oil reflux pump, the reflux oil flows back to the top of the atmospheric tower, and the extracted oil is sent to the tar and light oil storage tank 20.
The phenol oil (165 ℃), the naphthalene oil (200 ℃) and the wash oil (260 ℃) are sequentially extracted from the tower side of the atmospheric tower 10 from top to bottom. The phenol oil is cooled to 40 ℃ by cooling water in the second cooler 14 and then sent to the phenol-naphthalene mixing tank 16. The naphthalene oil is cooled to about 90 ℃ in a third cooler 15 and sent to a phenol naphthalene mixing tank 16.
The wash oil extracted from the side of the atmospheric tower 10 is distilled again by steam in the side tower 17, light fraction escapes from the top of the side tower 17 and returns to the atmospheric tower 10, the wash oil flowing out from the bottom of the side tower 17 is pumped out by the side tower 17 pump, part of the wash oil is proportionally conveyed to the product storage tank 18, and the other wash oil is conveyed to the wash oil storage tank 19 for temporary storage.
The soft asphalt obtained by extracting the light components from the superheated steam blown in from the bottom of the atmospheric tower 10 is transported to a product storage tank 18 in proportion and mixed with wash oil (the ratio of the soft asphalt to the wash oil is 9:1) to be used as needle coke raw material.
It is to be understood that these examples are illustrative of the present utility model and are not intended to limit the scope of the present utility model. Further, it is understood that various changes and modifications may be made by those skilled in the art after reading the teachings of the present utility model, and such equivalents are intended to fall within the scope of the claims appended hereto.
Claims (8)
1. The needle coke raw material production device is characterized in that: the device comprises a dehydration tower, wherein the dehydration tower is communicated with a pipeline, and a pump and four-stage heat exchange equipment are arranged on the pipeline; the top of the dehydration tower is provided with an oil-gas outlet, the oil-gas outlet is sequentially communicated with a first oil-water separator and a second oil-water separator through a pipeline and a pump, the first oil-water separator is also communicated with a wastewater tank, and the second oil-water separator is communicated with the dehydration tower through a return pipe; the bottom of the dehydration tower is provided with an anhydrous tar outlet which is communicated with an atmospheric tower through a pipeline, a pump and a heating furnace, the top of the atmospheric tower is provided with a light oil outlet, the light oil outlet is sequentially communicated with a first cooler, a third oil-water separator and a fourth oil-water separator through a pipeline and a valve, the third oil-water separator is also communicated with a wastewater tank, and the fourth oil-water separator is communicated with the atmospheric tower through a return pipe; the side part of the atmospheric tower is sequentially provided with a phenol oil outlet, a naphthalene oil outlet and a wash oil outlet from top to bottom, the phenol oil outlet and the naphthalene oil outlet are respectively communicated with a second cooler and a third cooler through pipelines and valves, and the second cooler and the third cooler are respectively communicated with a phenol-naphthalene mixing tank; the wash oil outlet is communicated to the side tower through a pipeline and a valve; the bottom of the atmospheric tower is provided with a soft asphalt outlet, and the soft asphalt outlet and a material outlet at the bottom of the side tower are respectively communicated to a product storage tank through a pipeline, a pump and a valve.
2. The needle coke raw material production apparatus according to claim 1, wherein: the four-stage heat exchange equipment is sequentially a tar/light oil heat exchanger, a tar/naphthalene oil heat exchanger, a soft asphalt/tar heat exchanger and a tar preheater.
3. The needle coke raw material production apparatus according to claim 1, wherein: the second oil-water separator and the fourth oil-water separator are also communicated with a tar light oil storage tank through pipelines and valves respectively.
4. The needle coke raw material production apparatus according to claim 1, wherein: and a heater is further arranged on the tower body of the dehydration tower, and protrudes out of the tower body.
5. The needle coke raw material production apparatus according to claim 1, wherein: an external condenser is arranged above the top of the dehydration tower.
6. The needle coke raw material production apparatus according to claim 1, wherein: the phenolic naphthalene mixing tank is communicated to the oil mixing tank through a pipeline, a pump and a valve.
7. The needle coke raw material production apparatus according to claim 1, wherein: the side tower is also communicated to the atmospheric tower through a return pipe.
8. The needle coke raw material production apparatus according to claim 1, wherein: the material outlet at the bottom of the side tower is also communicated to the wash oil storage tank through a pipeline, a valve and a pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320344739.9U CN219429932U (en) | 2023-02-23 | 2023-02-23 | Needle coke raw material production device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202320344739.9U CN219429932U (en) | 2023-02-23 | 2023-02-23 | Needle coke raw material production device |
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| CN219429932U true CN219429932U (en) | 2023-07-28 |
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| CN202320344739.9U Active CN219429932U (en) | 2023-02-23 | 2023-02-23 | Needle coke raw material production device |
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- 2023-02-23 CN CN202320344739.9U patent/CN219429932U/en active Active
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