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Combined technology for heavy oil processing

A combined process and heavy oil technology, which is applied in the fields of hydrotreating process, petroleum industry, and hydrocarbon oil treatment, can solve the problem of separation of high softening point asphalt from solvent, high softening point asphalt transportation, difficulty in reducing coke and gas production Rate, affecting the stability of modified products and other issues, to achieve the effect of reducing C7 asphaltene and metal content, increasing API degree, and ensuring stability

Active Publication Date: 2012-12-05
CHINA UNIV OF PETROLEUM (BEIJING)
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  • Summary
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  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

However, in the heavy oil lightening processing technology that has been used or disclosed at present, no matter what kind of combination process is used, it is necessary for the solvent separation in the deoiled asphalt, that is, the deoiled asphalt must be separated from the solvent and then combined with the deoiled asphalt. Into the follow-up combination process, so the two problems of separation of high softening point asphalt from solvent and transportation of high softening point asphalt in the process of solvent deasphalting have not been solved; on the other hand, the current heavy oil processing technology, in order to reduce Difficulty, to a certain extent, can only be at the cost of sacrificing the yield of deasphalted oil, so the amount of deoiled asphalt must be increased, and the oil content in asphalt is higher, which actually increases the amount of coke after thermal reaction of asphalt, that is , it is difficult to reduce the yield of coke and gas; on the other hand, in order to reduce the difficulty of separation of high softening point asphalt and solvent and the difficulty of transportation of high softening point asphalt, the oil in deoiled asphalt is relatively large. During thermal cracking treatment, The condensation reaction of some oil molecules will inevitably lead to an increase in the amount of coke in the thermal reaction, which will affect the liquid yield and the stability of the modified product

Method used

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  • Combined technology for heavy oil processing
  • Combined technology for heavy oil processing
  • Combined technology for heavy oil processing

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0046] Canadian Cold Lake Bitumen (Cold Lake Bitumen), API is 10.2, sulfur content is 4.4wt%, Kang's carbon residue is 13.2wt%, C7 asphaltene is 10.0wt%, Ni and V content are 69μg / g and 182μg / g.

[0047] The oil sand pitch is firstly subjected to atmospheric distillation, and fractionated to obtain a 200-350°C diesel fraction (15.0wt%) and an atmospheric column bottom (residual oil) with a boiling point higher than 350°C.

[0048] The bottom of the atmospheric column uses isobutane (iC4) as the extraction solvent for solvent deasphalting. First, the bottom of the feed is mixed with the main solvent and sent to the extraction tower 4 from the middle or upper part, and the auxiliary solvent is from the lower part of the extraction tower. Enter into countercurrent contact with deoiled asphalt, and again perform enhanced extraction on the asphalt phase extracted by the main solvent. The temperature at the bottom of the extraction tower is 120°C, the temperature at the top of the tower...

Embodiment 2

[0056] Canadian Athabasca oil sand asphalt has an API of 8.9, a sulfur content of 4.60% by weight, a Concord carbon residue CCR of 13.0%, a C7 asphaltene content of 11.03% by weight, and Ni and V contents of 69μg / g and 190μg / g, respectively.

[0057] By adopting atmospheric distillation, a 200-350°C diesel fraction of 12.04% by weight is obtained, and the yield of atmospheric column bottoms (residual oil) is 87.96% by weight.

[0058] The bottom product of the atmospheric column is solvent deasphalted with a mixed solvent of nC4-nC5, and the composition of the extraction solvent is nC4:nC5=50:50 (wt / wt). The specific operation of the solvent deasphalting process is the same as in Example 1, but the total solvent mass ratio is 3.95:1, the main solvent: secondary solvent: dispersing solvent = 0.759: 0.203: 0.038, the extraction tower bottom temperature is 140°C, and the tower top temperature is 160°C. The extraction pressure is 5.0MPa.

[0059] The deasphalted oil discharged from the ...

Embodiment 3

[0065] Canadian Athabasca oil sand asphalt has an API of 8.9, a sulfur content of 4.6wt%, a Concord carbon residue CCR of 13.0%, a C7 asphaltene content of 11.4wt%, and Ni and V contents of 65.4μg / g and 192.6μg / g, respectively.

[0066] Using atmospheric and vacuum distillation, the 200-350℃ diesel fraction was 12.04wt% and the 350-500℃ straight-run wax oil yield was 32.75wt%, and the vacuum column bottoms (boiling point higher than 500℃ residue) yield was 55.21 wt%.

[0067] The residual oil at the bottom of the vacuum column was deasphalted by using n-pentane (nC5) as the extraction solvent, and the specific operation was the same as in Example 1. The total solvent mass ratio is 3.7:1, of which the main solvent: auxiliary solvent: dispersing solvent=0.811:0.135:0.054, the extraction tower bottom temperature is 160°C, the tower top temperature is 170°C, and the extraction pressure is 5.5MPa.

[0068] The deasphalted oil discharged from extraction tower 4 is under supercritical cond...

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Abstract

The invention provides a combined technology for heavy oil processing. The combined technology at least comprises the steps of performing solvent de-asphalting process on a heavy oil raw material and performing thermal cracking process on a de-oiling asphalt phase and a dispersing agent in a thermal cracking reactor after the de-oiling asphalt phase and the dispersing agent are mixed, wherein the de-asphalted oil and thermal cracked oil separated from a thermal cracking reaction product are mixed to obtain a modified oil; and a solvent separated from the thermal cracking reaction product and heavy wax oil are respectively returned to the solvent de-asphalting process to be used circularly and serve as a mixed feeding material to remove the asphaltene. For the implementation of the invention, the combined technology for the heavy oil processing, disclosed by the invention, has the advantages of solving the problem that the asphalt with a high softening point is difficult to separate from the solvent in the transportation and solvent de-asphalting process of the heavy oil, enabling extractable oil component in the heavy oil to avoid a heat treatment, being good for guaranteeing stability of products and improving yield of the modified oil, greatly improving API (American Petroleum Institute) degree, obviously reducing residual carbon value, C7 asphaltene and metal contents, achieving an asphaltene removal rate of higher than 96% and the metal nickel as well as vanadium removal rate of 80%-90%, and being good for producing hydrogenised modified oil with obviously improved quality.

Description

Technical field [0001] The invention relates to a combined process for deep processing of heavy oil, in particular to the process of pre-fractionation, heavy fraction deasphalting and thermal cracking of heavy crude oil, extra-heavy crude oil and oil sand pitch, as well as fixed-bed hydrotreating to produce high The combined process of quality modified oil belongs to the field of heavy oil processing. Background technique [0002] Heavy oil means that the API degree is lower than 20 (the density is higher than 0.932g / cm at 20℃) 3 ) Generally includes heavy crude oil, oil sands bitumen and residual oil. Because of the high density, high viscosity, and high freezing point of heavy crude oil and oil sands, they lose their fluidity at ambient temperature or higher and cannot be transported and processed like conventional crude oil, especially those with an API degree lower than 10 Heavy oil and oil sand bitumen need to be lightened into synthetic oil before being transported to refi...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G55/00C10G69/00
CPCC10G55/04C10G2300/4081C10G2300/4018C10G2300/44C10G2300/206C10G55/00C10G2300/1033C10G69/00C10G21/003C10G21/14C10G69/06
Inventor 赵锁奇孙学文许志明徐春明庄庆发
Owner CHINA UNIV OF PETROLEUM (BEIJING)
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