A processing method for inferior heavy oil and/or inferior residual oil

A low-quality heavy oil and processing method technology, applied in the petroleum industry, hydrotreating process, hydrocarbon oil treatment, etc., can solve the problems of short operation period, more dry gas, more coking, etc., and achieve high light oil yield, The effect of extending the operating cycle and wide application range

Active Publication Date: 2018-11-02
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, there are two deficiencies in the fixed bed process: one is poor adaptability to raw materials, when the Ni+V content of the raw materials is greater than or equal to 200 μg / g, trace carbon residue is greater than or equal to 15% by weight, or the content of asphaltene is greater than or equal to 7 It is more difficult to process at weight %; the second is that the operation cycle is short, and the catalyst is deactivated faster due to carbon deposition and metal deposition
This method pursues a higher conversion rate in the slurry bed reactor, so the yield of the light oil product obtained is relatively high, but it also produces a lot of coking and more dry gas at the same time, and the light oil product obtained requires Secondary treatment such as hydrofinishing, resulting in low conversion of residual oil and / or heavy oil in the overall process

Method used

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  • A processing method for inferior heavy oil and/or inferior residual oil
  • A processing method for inferior heavy oil and/or inferior residual oil
  • A processing method for inferior heavy oil and/or inferior residual oil

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0071] With A as raw material (properties see Table 1), in the slurry bed reactor with C as catalyst (properties see Table 2), material flow chart as figure 1 shown.

[0072] Grind the catalyst and control the particle size to 100-150 mesh by sieving method, and feed it into the slurry bed reactor 1 from bottom to top along with the raw material and hydrogen at 3.0% by weight of the weight of the fresh raw material oil. The operating conditions for controlling the slurry bed reactor 1 are: temperature 420°C, pressure 10MPa, hydrogen-oil volume ratio 1000, space velocity 0.2h -1 . The conversion depth of the material at the outlet of slurry bed reactor 1 is shown in Table 3. The material enters the high-pressure separator 2 from the slurry-bed reactor 1, and the operating conditions of the high-pressure separator 2 include a temperature of 380° C. and a pressure of 10 MPa.

[0073] The liquid component obtained by the material passing through the high-pressure separator 2 an...

Embodiment 2

[0077] Taking B as raw material (see Table 1 for properties), and taking D as catalyst (see Table 2 for properties) in the slurry bed reactor, the material flow chart is as follows figure 1 shown.

[0078] Grind the catalyst and control the particle size to 120-180 mesh by sieving method, and feed it into the slurry bed reactor 1 from bottom to top along with the raw material and hydrogen at 5.0% by weight of the weight of the fresh raw material oil. The operating conditions for controlling the slurry bed reactor 1 are: temperature 380°C, pressure 12MPa, hydrogen-oil volume ratio 1500, space velocity 0.1h -1 . The conversion depth of the material at the outlet of slurry bed reactor 1 is shown in Table 3. The material enters the high-pressure separator 2 from the slurry-bed reactor 1, and the operating conditions of the high-pressure separator 2 include a temperature of 390° C. and a pressure of 9 MPa.

[0079] The liquid component obtained by the material through the high-p...

Embodiment 3

[0086] With A as raw material (properties see Table 1), in the slurry bed reactor with C as catalyst (properties see Table 2), material flow chart as figure 2 shown.

[0087] Grind the catalyst and control the particle size to 200-240 mesh by sieving method, and feed it into the slurry bed reactor 1 from bottom to top along with the raw material and hydrogen at 6.0% by weight of the weight of the fresh raw material oil. Control the operating conditions of slurry bed reactor 1 as follows: temperature 400°C, pressure 10MPa, hydrogen-oil volume ratio 1000, space velocity 0.2h -1 . The conversion depth of the material at the outlet of slurry bed reactor 1 is shown in Table 3. The material enters the high-pressure separator 2 from the slurry-bed reactor 1, and the operating conditions of the high-pressure separator 2 include a temperature of 380° C. and a pressure of 10 MPa.

[0088] The liquid component obtained by the material through the high-pressure separator 2 and the gua...

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Abstract

The invention relates to a processing method of inferior heavy oil and / or inferior residual oil. The method comprises steps as follows: inferior heavy oil and / or inferior residual oil are / is send into a slurry bed reactor and is contacted with a hydrogenation catalyst for a first hydrogenation reaction, then, an obtained product is sent into a high-pressure separator to be separated, hydrogen-containing gas is obtained from the top of the high-pressure separator, a liquid component is obtained from the middle, a heavy material containing a hydrogenation catalyst is obtained from the bottom, the liquid component is sent into a fixed bed reactor for a second hydrogenation reaction, and the conversion level of the inferior heavy oil and / or the inferior residual oil doesn't exceed 50% under the first hydrogenation reaction conditions. By means of the processing method, the inferior heavy oil and / or the inferior residual oil with poorer properties can be treated, basically no coking occurs in the slurry bed reactor and pipelines or the coking amount is smaller, accordingly, the higher light oil yield can be obtained, and the operation cycle of the fixed bed reactor is further prolonged.

Description

technical field [0001] The invention relates to a method for processing inferior heavy oil and / or inferior residual oil. Background technique [0002] Crude oil has become heavy and inferior worldwide, and the proportion of residual oil obtained after primary processing of crude oil has increased sharply. In addition, the processing volume of crude oil has increased year by year, and the output of residual oil has risen sharply. At the same time, crude oil reserves are gradually declining, the market demand for light oil products is increasing year by year, and the price difference between light crude oil and heavy crude oil is also increasing. These factors urgently require the development of residual oil / heavy oil light and efficient use of new technologies. [0003] At present, the technologies for lightening residual oil / heavy oil mainly include two processes: decarburization and hydrogenation. In the decarbonization process, the yield of light oil is low and the produc...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G67/02
Inventor 童凤丫戴立顺李大东杨清河刘佳
Owner CHINA PETROLEUM & CHEM CORP
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