CN108251143B - Method for preparing asphalt coke by adopting tower bottom asphalt - Google Patents
Method for preparing asphalt coke by adopting tower bottom asphalt Download PDFInfo
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- CN108251143B CN108251143B CN201611240111.5A CN201611240111A CN108251143B CN 108251143 B CN108251143 B CN 108251143B CN 201611240111 A CN201611240111 A CN 201611240111A CN 108251143 B CN108251143 B CN 108251143B
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- tower
- asphalt
- coke
- heating furnace
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
- C10B55/00—Coking mineral oils, bitumen, tar, and the like or mixtures thereof with solid carbonaceous material
Abstract
A method for preparing asphalt coke from tower bottom asphalt, comprising the following steps: 1. taking tower bottom asphalt with a softening point of 60-70 ℃ as a raw materialFeeding the materials into a feeding system through a raw material pump according to the conveying temperature of 140-150 ℃, then feeding the materials into a combined tower through a heat exchanger, and feeding the materials into the bottom of the combined tower according to the conveying temperature of 4-6 m3The heavy oil is added according to the addition amount per hour; 2. preparing the raw materials in the tower into carbonized circulating oil according to the following conditions: the initial boiling point is 280-300 ℃; 14-17% of carbon residue by mass percent; the density at 100 ℃ is 1.168-1.170 g/cm3(ii) a The outflow at 360 ℃ is less than or equal to 10 percent; the circulation ratio is 1.0-1.5; 3. the prepared circulating oil is pumped into a pump through a heating furnace to be pressurized, and is sent into the heating furnace under the control of a flow meter, and the circulating oil enters a coking tower to be subjected to carbonization cracking and condensation reaction after flowing from a convection section to a radiation section of the heating furnace; 4. and the coking tower is subjected to steam blowing, water cooling and coke removal to obtain the pitch coke.
Description
Technical Field
The invention relates to a production and manufacturing technology in the field of coal chemical industry, in particular to a method for preparing asphalt coke by adopting tower bottom asphalt.
Background
The coal chemical industry mainly produces clean energy and products capable of replacing petrochemical industry, such as diesel oil, gasoline, aviation kerosene, liquefied petroleum gas, ethylene raw materials, polypropylene raw materials, alternative fuels (methanol and dimethyl ether) and the like, and the coal chemical industry can form a new coal-energy chemical industry integrated industry by combining with energy and chemical industry technologies. The products processed from coal tar are widely used for preparing plastics, dyes, spices, pesticides, medicines, solvents, preservatives, adhesives, rubbers, carbon products and the like, and comprise a coal tar distillation device, an asphalt coke device, a phenol refining device and the like, wherein the asphalt coke device is a product obtained by further deep processing of asphalt (also called soft asphalt) at the bottom of a coal tar distillation tower after coal tar distillation in coal chemical industry production, and the products comprise heavy oil, light oil, asphalt coke and crude gas.
In the prior art, an asphalt coke device utilizes tar distillation tower bottom asphalt (softening point is 60-70 ℃), heavy medium oil or phenanthrene residual oil or anthracene oil is used for preparing prepared maltha (softening point is 35-40 ℃), the conveying temperature of the prepared maltha is 130 ℃, a certain amount of heavy oil is added for mixing after the maltha is preheated in a combined tower to obtain carbonized circulating oil, the circulating oil is heated to 500 ℃, the carbonized circulating oil enters a coking tower for carbonization cracking and condensation reaction, the coking tower obtains asphalt coke (green coke) through steam blowing, water cooling and decoking, and oil gas is fractionated in the combined tower to obtain heavy oil, light oil and crude gas.
The unit energy consumption corresponding to the method is 190-205 yuan/ton (total energy consumption/asphalt input after preparation).
Disclosure of Invention
The invention aims to solve the technical problem of providing a preparation method of asphalt coke with lower energy consumption.
The technical problem to be solved can be implemented by the following technical scheme.
A method for preparing asphalt coke by adopting tower bottom asphalt comprises the following steps and process requirements:
(1) taking tower bottom asphalt with a softening point of 60-70 ℃ as a raw material, conveying the raw material into a feeding system through a raw material pump at a conveying temperature of 140-150 ℃, conveying the raw material into a combined tower through a heat exchanger, and conveying the combined tower to the bottom of the combined tower according to a thickness of 4-6 m3The heavy oil is added according to the addition amount per hour;
(2) and preparing the raw materials in the combined tower into carbonized circulating oil according to the following conditions:
initial boiling point: 280-300 ℃;
carbon residue according to mass percent: 14-17%;
density at 100 ℃: 1.168-1.170 g/cm3；
Outflow at 360 ℃: less than or equal to 10 percent;
the circulation ratio: 1.0 to 1.5;
(3) the prepared carbonized circulating oil is put into a pump through a heating furnace to be boosted, and is sent into the heating furnace under the control of a flow meter, and the carbonized circulating oil enters a coking tower to carry out carbonization cracking and condensation reaction after flowing from a convection section to a radiation section of the heating furnace;
(4) and the coking tower is subjected to steam blowing, water cooling and coke removal to obtain the pitch coke.
As a further improvement of the technical scheme, the outflow amount of the carbonized circulating oil at 400 ℃ in the step (2): less than or equal to 34.0 percent.
As a further improvement of the technical scheme, the conveying temperature of the raw materials in the step (1) before passing through the heat exchanger is 140-150 ℃.
As one of the preferred embodiments of the present invention, the transport temperature in step (1) is 150 ℃.
Also as one of the preferred embodiments of the present invention, the coke drum is one furnace two drums or two furnaces four drums; the coking towers are alternately used.
As a further improvement of the technical scheme, the temperature of the mixed oil discharged from the heating furnace by the carbonized circulating oil in the step (3) reaches 497-500 ℃.
Further, the circulation ratio in the step (2) adopts the following calculation formula:
charging amount (mass) of heating furnace/asphalt (mass) at bottom of tower-1
(heating furnace volume flow rate × density) ÷ (bottom pitch volume flow rate × density) -1.
By adopting the method for preparing the asphalt coke from the tower bottom asphalt in the technical scheme, the energy is saved, the consumption is reduced by about 10-20%, the development trend of low-carbon clean production is met, and the environmental pollution is reduced. The unit energy consumption of the pitch coke device in the preparation method is reduced to 178-190 yuan/ton (total energy consumption/pitch input at the bottom of the tower).
Drawings
FIG. 1 is a schematic diagram of a process for producing pitch coke according to the present invention;
Detailed Description
The following further describes embodiments of the present invention with reference to the drawings.
The invention aims to provide a novel raw material for producing asphalt coke by an asphalt coke feeding device to obtain heavy oil, light oil, crude gas and asphalt coke (raw coke), the method utilizes the existing asphalt coke device to be suitable for mixing with different tar distillation tower bottom asphalt (different softening points), the mixture is modulated in an asphalt coke device combined tower to obtain circulating oil which accords with carbonization, the circulating oil is heated to 497-500 ℃, the circulating oil enters a coking tower to carry out carbonization cracking and condensation reaction, the coking tower obtains the asphalt coke (raw coke) by steam blowing, water cooling and decoking, and the oil gas is fractionated in the combined tower to obtain the heavy oil, the light oil and the crude gas.
Referring to fig. 1, the conveying temperature of the bottom asphalt is controlled at 140-150 ℃ (preferably 150 ℃), the conveying temperature is high, the conveying of the bottom asphalt is facilitated to increase the fluidity, the bottom asphalt enters the bottom of the combined tower after passing through a heat exchanger, a certain amount of heavy oil is added to the bottom, the adding amount of the heavy oil is increased more than that of the original prepared asphalt, and the adding amount is 4-6 m3The/h heavy oil is prepared into carbonized circulating oil (with the initial boiling point of 280-300 ℃ C., and the initial boiling point of,14-17% of carbon residue (mass percent), 1.168-1.170 g/cm3 in density at 100 ℃, less than or equal to 10% in outflow at 360 ℃ and less than or equal to 34.0% in outflow at 400 ℃, the circulation ratio is controlled to be 1.0-1.5, the carbon residue is loaded into a pump through a heating furnace to be boosted, the pressure is sent into the heating furnace under the control of a flowmeter, the circulating oil flows through a convection section of the heating furnace to a radiation section to be discharged, and the circulating oil enters a coking tower through a four-way valve (a coking tower A and a coking tower B in the figure are two coking towers which can be used alternately; the installation principle of the coking tower of the production device is one furnace with two towers or two furnaces with four towers), the temperature of the mixed oil from the heating furnace reaches 497-500 ℃, the circulating oil enters the coking tower in two states before and after a critical area, most of liquid remains in the coking tower, and the other part of gas overflows from a top volatilization line and enters a combined tower to be fractionated to obtain heavy oil, light oil and crude gas.
The method that the asphalt at the tower bottom enters the bottom of the asphalt coke device is adopted, more heavy oil is used for blending than the method that the blended asphalt (namely the blended soft asphalt mentioned in the prior art) enters the bottom of the asphalt coke device, the device circulation ratio is improved to 1.0-1.5 from 0.8-1.0, the device circulation ratio is blended into the carbonized circulating oil which is in accordance with the production of the asphalt coke by using the low-temperature asphalt, and the carbonized circulating oil is used for carrying out carbonization reaction.
The tower bottom pitch circulation ratio calculation method comprises the following steps:
feeding amount (mass) of heating furnace/asphalt (mass) at bottom of tower-1
(heating furnace volume flow rate x density) ÷ (bottom pitch volume flow rate x density) -1
＝1.0～1.5
Table 1 below compares the data for a batch of bottoms bitumen produced asphalt coke using the process of the present invention to the prior art process.
Table 1:
Claims (5)
1. a method for preparing asphalt coke by adopting tower bottom asphalt is characterized by comprising the following steps and process requirements:
(1) taking tower bottom asphalt with a softening point of 60-70 ℃ as a raw material, conveying the raw material into a feeding system through a raw material pump at a conveying temperature of 140-150 ℃, conveying the raw material into a combined tower through a heat exchanger, and conveying the combined tower to the bottom of the combined tower according to a thickness of 4-6 m3The heavy oil is added according to the addition amount per hour;
(2) and preparing the raw materials in the combined tower into carbonized circulating oil according to the following conditions:
initial boiling point: 280-300 ℃;
carbon residue according to mass percent: 14-17%;
density at 100 ℃: 1.168-1.170 g/cm3；
Outflow at 360 ℃: less than or equal to 10 percent;
the circulation ratio: 1.0 to 1.5;
(3) the prepared carbonized circulating oil is put into a pump through a heating furnace to be boosted, and is sent into the heating furnace under the control of a flow meter, and the carbonized circulating oil enters a coking tower to carry out carbonization cracking and condensation reaction after flowing from a convection section to a radiation section of the heating furnace;
(4) the coking tower is subjected to steam blowing, water cooling and decoking to obtain pitch coke;
wherein, the circulation ratio in the step (2) adopts the following calculation formula:
heating furnace feed rate (mass) ÷ bottom pitch (mass) -1 = (heating furnace volume flow × density) ÷ (bottom pitch volume flow × density) -1.
2. The method for preparing asphalt coke from tower bottom asphalt according to claim 1, wherein the outflow rate of the carbonized cycle oil in step (2) at 400 ℃ is as follows: less than or equal to 34.0 percent.
3. The process for producing bituminous coke using bottom asphalt according to claim 1 or 2, characterized in that the conveying temperature in step (1) is 150 ℃.
4. The method for preparing asphalt coke from asphalt at the bottom of the tower according to claim 1, wherein the coking tower is one furnace two towers or two furnaces four towers.
5. The method for preparing the asphalt coke by adopting the tower bottom asphalt as claimed in claim 1, wherein the temperature of the mixed oil of the carbonized circulating oil from the heating furnace in the step (3) is 497-500 ℃.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201611240111.5A CN108251143B (en) | 2016-12-28 | 2016-12-28 | Method for preparing asphalt coke by adopting tower bottom asphalt |
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| CN201611240111.5A CN108251143B (en) | 2016-12-28 | 2016-12-28 | Method for preparing asphalt coke by adopting tower bottom asphalt |
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| CN108251143A CN108251143A (en) | 2018-07-06 |
| CN108251143B true CN108251143B (en) | 2021-03-05 |
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| CN109319758B (en) * | 2018-10-10 | 2020-09-22 | 中钢集团鞍山热能研究院有限公司 | Co-production process method of mesocarbon microbeads and negative electrode material coke |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3563884A (en) * | 1968-07-15 | 1971-02-16 | Lummus Co | Delayed coking of coal tar pitches |
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Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3563884A (en) * | 1968-07-15 | 1971-02-16 | Lummus Co | Delayed coking of coal tar pitches |
Non-Patent Citations (1)
| Title |
|---|
| 煤焦油软沥青为原料用延迟焦化法生产沥青焦;谢炳华;《宝钢技术》;宝钢技术;19861231;第15-18页 * |
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Address after: 2004-2002 Weisan Road Chemical Office Building, Baoshan District, Shanghai Applicant after: Baowu Carbon Material Technology Co., Ltd. Address before: 2004-2002 Weisan Road Chemical Office Building, Baoshan District, Shanghai Applicant before: Chemical Co., Ltd. of Baoshan Iron and Steel Group, Shanghai |
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Address after: 200942 three chemical engineering office building, Baoshan Iron and steel factory, Shanghai, Baoshan District Patentee after: Baowu Carbon Technology Co.,Ltd. Address before: 200942 three chemical engineering office building, Baoshan Iron and steel factory, Shanghai, Baoshan District Patentee before: BAOWU CARBON MATERIAL TECHNOLOGY Co.,Ltd. |