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Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil

A technology for coal tar and naphtha, which is applied in the field of converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil, can solve the problems of high operating pressure, low yield of light oil and high investment in the hydrocracking section , to achieve the effect of low operating cost, low operating cost and low investment

Active Publication Date: 2020-01-03
SYNFUELS CHINA TECH CO LTD +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

This process does not reprocess the vacuum distillate oil, the yield of light oil is low, and the operating pressure of the suspension bed hydrocracking part is high, the investment is high, and the consumption is large

Method used

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  • Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil
  • Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil
  • Method for converting coal tar/heavy oil into liquefied gas, naphtha and diesel oil

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0107] according to figure 1Shown flow process, coal tar 101 (35250kg / h), the tar slurry 102 (3000kg / h) that contains 25wt% hydrocracking catalyst, the bottom tail oil (7245kg / h) of refining fractionation tower 19 and hydrogen (10200kg / h) mixed, enter the suspension bed reactor 1 for hydrocracking reaction; react under hydrogen, suspension bed hydrocracking catalyst and 425 ° C, 6.5MPaG, the average residence time of the liquid phase in the suspension bed reactor 1 is 60min , the total hydrogen-to-oil ratio at the inlet of the suspended bed reactor 1 is 1500, the feed amount of the hydrocracking catalyst is 2wt% of the raw oil, and the catalyst is Fe-based waste catalyst of the Fischer-Tropsch synthesis process.

[0108] The liquid phase product in the suspended bed reactor 1 is decompressed and enters the suspended bed thermal low pressure separator 2 for separation at 425°C and 2.4 MPaG; the liquid phase separated by the suspended bed thermal low pressure separator 2 enters...

Embodiment 2

[0123] according to figure 2 Shown flow process, coal tar 101 (35250kg / h), the tar slurry 102 (3000kg / h) that contains 25wt% hydrocracking catalyst, the bottom tail oil (7245kg / h) of refining fractionation tower 19 and hydrogen (10200kg / h) mixing, enter the suspension bed reactor 1 for hydrocracking reaction; react under hydrogen, suspension bed hydrocracking catalyst and temperature 425 ° C, pressure 6.5MPaG, the average residence time of the liquid phase in the suspension bed reactor 1 The total hydrogen-to-oil ratio at the inlet of the suspension bed reactor 1 is 1500, the feed amount of the hydrocracking catalyst is 2wt% of the raw oil, and the catalyst is Fe-based spent catalyst of the Fischer-Tropsch synthesis process.

[0124] The liquid phase product in the suspended bed reactor 1 is decompressed and enters the suspended bed thermal low pressure separator 2, and is separated at 425°C and a pressure of 2.4MPaG; the liquid phase separated by the suspended bed thermal l...

Embodiment 3

[0139] The main properties of the heavy oil used in Example 3 are shown in Table 4.

[0140] Table 4 Main properties of heavy oil

[0141] project unit Density(20℃) g / cm 3

0.964 Viscosity.(100℃) mm 2 / S

108.7 Solidifying point ℃ 8.0 colloid m％ 27.67 C7-Asphaltenes m％ 0.25 carbon residue m％ 6.6 Ash m％ 0.089 H / C atomic ratio 1.69 S m％ 0.13 N m％ 0.45 Distillation range ℃ IBP 275 10％ 358 30％ 433 50％ 492 63％ 538 75％ 733 Metal content, μg / g Ni μg / g 11.8 V μg / g 0.35 Ca μg / g 346 Fe μg / g 10.2 acid value / mgKOH.g -1

6.35

[0142] according to image 3 Shown flow process, heavy oil 101 (1840kg / h), the heavy oil slurry 102 (160kg / h) that contains 25wt% hydrocracking reactor, the bottom tail oil (378kg / h) of refining fractionation tower 19 and hydrogen (510kg / h) mixed, enter the suspension b...

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Abstract

The invention relates to a processing method for coal tar / heavy oil, in particular to a method for converting the coal tar / heavy oil into liquefied gas, naphtha and diesel oil. The method comprises the following steps: the coal tar / heavy oil (and / or bottom tail oil of a refining fractionation tower), a hydrocracking catalyst and hydrogen gas are mixed, the mixture enters a suspension bed reactionsection for a hydrocracking reaction, separation is performed, and fractional distillation is performed to obtain unrefined naphtha, unrefined diesel oil, wax oil, and a small amount of gas-phase products; and hydrorefining is performed on the obtained unrefined naphtha, unrefined diesel oil and wax oil, an optional secondary cracking reaction is performed, separation is performed, fractional distillation is performed, and absorption and stabilization are performed to obtain the liquefied gas, naphtha and diesel products through fraction cutting. The method provided by the invention improves the yield of light oil products, prolongs the operation time of equipment sustainable production, reduces the frequency of equipment shutdown check, and provides a processing method for improving economy of the lower-value-added tar / heavy oil.

Description

technical field [0001] The invention relates to a method for converting coal tar / heavy oil into liquefied gas, naphtha and diesel oil. Background technique [0002] In recent years, due to air pollution and smog all over the country, the country has more urgent requirements for clean energy. At the same time, with the rising demand for petroleum products, the amount of oil resources that can be collected is gradually decreasing, and crude oil is gradually showing inferior and heavy quality development. The processing and clean utilization of heavy oil also bring more challenges to the refining industry. China is a country with a lot of coal and a shortage of oil. If coal can be converted into liquid fuels on a large scale with efficient and clean processes, it will effectively alleviate the tightness of oil supply and promote sustainable and stable economic development. With the rapid growth of the international and domestic iron and steel industry, the coking industry is s...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G67/02
CPCC10G67/02C10G2400/00C10G2400/04C10G2400/26
Inventor 郭强田磊杨勇李永旺万会军杨强魏迎春白亮余晓忠
Owner SYNFUELS CHINA TECH CO LTD