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Heavy paraffin oil solvent deasphalting process for reducing recycle ratio of coking unit

A technology of coking equipment and heavy wax oil, which is applied in the petroleum industry and processing hydrocarbon oil, etc. It can solve the problems of high fuel consumption of heating furnace, low load utilization rate, and reduced processing volume, so as to reduce floor space and equipment investment , the effect of reducing the area

Inactive Publication Date: 2010-04-07
雷泽永
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Compared with the low circulation ratio process, the main problems of the conventional circulation ratio process are: the coke formation rate is higher, generally 3-4% higher, resulting in a low total liquid yield of the unit; Repeated circulation between the main equipment heating furnace, coke tower and fractionation tower leads to low utilization rate of the effective load of the device and reduced processing volume; high energy consumption, and the fuel consumption of the heating furnace is about 20% higher
As a result, coking units at home and abroad have encountered the same thorny problem: the quality of heavy wax oil is poor, and it is difficult for downstream units to process
[0010] 3. If you want to use solvent refining or extraction methods, you must solve the problem of large investment costs
Due to the large investment, so far, the coking units of domestic refineries still adopt the conventional cycle ratio process operation

Method used

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  • Heavy paraffin oil solvent deasphalting process for reducing recycle ratio of coking unit
  • Heavy paraffin oil solvent deasphalting process for reducing recycle ratio of coking unit
  • Heavy paraffin oil solvent deasphalting process for reducing recycle ratio of coking unit

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Experimental program
Comparison scheme
Effect test

Embodiment 1

[0072] This embodiment is the two-stage extraction process of thermal combination method, such as figure 1 shown.

[0073] (1) After the heavy wax oil of the first, second and third sets of coking units in the refinery merges, it enters the raw material buffer tank 5 of the solvent deasphalting unit parasitic in the coking unit through the pipeline 4, and then flows through the pipeline 6 into the raw material pump 7. Mix with solvent after pressurization, the temperature is about 152°C, enter the extractor 10 through the pipeline 8, and after solvent extraction, the heavy wax oil is divided into two phases: the discharge from the top pipeline 9 of the extractor 10 contains desorbed A stage of extracting liquid of asphalt oil, colloid and most of the solvents; what is discharged from the lower pipeline 11 of the extractor is deoiled asphalt and a raffinate containing a small amount of solvents.

[0074] (2), one section of extract enters colloid settler 12 after heat exchanger ...

Embodiment 2

[0083] This embodiment is a two-stage extraction process of sharing the heating furnace of the coking unit.

[0084] (1) After the heavy wax oil of the first, second and third sets of coking units in the refinery merges, it enters the raw material buffer tank 5 of the solvent deasphalting unit parasitic in the coking unit through the pipeline 4, and then flows through the pipeline 6 into the raw material pump 7. Mix with solvent after pressurization. At this time, the temperature is about 152°C. After entering the extractor 10 through the pipeline 8 and being extracted by solvent, the heavy wax oil is divided into two phases: what is discharged from the pipeline 9 at the top of the extractor 10 is A section of extract containing deasphalted oil, colloid and most of the solvent; the discharge from the lower pipeline 11 of the extractor is deoiled asphalt and a raffinate containing a small amount of solvent.

[0085] (2), one section of extract enters colloid settler 12 after he...

Embodiment 3

[0095] This embodiment is a one-stage extraction process of thermal combination method, such as image 3 shown.

[0096] (1) After the heavy wax oil of the first, second and third sets of coking units in the refinery merges, it enters the raw material buffer tank 5 of the solvent deasphalting unit parasitic in the coking unit through the pipeline 4, and then flows through the pipeline 6 into the raw material pump 7. Mix with solvent after pressurization. At this time, the temperature is about 152°C. After entering the extractor 10 through the pipeline 8 and being extracted by solvent, the heavy wax oil is divided into two phases: what is discharged from the pipeline 9 at the top of the extractor 10 is A section of extract containing deasphalted oil and most of the solvent; the discharge from the lower line 11 of the extractor is deoiled asphalt and a raffinate containing a small amount of solvent.

[0097] (2), one section of extract enters the booster pump 14 after exchangin...

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Abstract

The invention relates to a heavy paraffin oil solvent deasphalting process for reducing a recycle ratio of a coking unit. For one-stage extract, solvent-containing deoiled asphalt and / or two-stage extract required to be heated in the solvent deasphalting process, a heat exchange method for hot paraffin oil of the coking unit in a heat exchanger or a mode that materials return to the coking unit for heating is adopted to replace a heating furnace in the prior solvent deasphalting device, so that the heating furnace in the solvent deasphalting device is eliminated, investment is saved and the recycle ratio of the coking unit is reduced.

Description

technical field [0001] The invention relates to a heavy wax oil solvent deasphalting process for reducing the circulation ratio of a coking unit. Background technique [0002] The coking unit is one of the important secondary processing units in the refinery, which plays an important role in the economic benefit of the refinery. The coking process uses the heaviest and worst residual oil in the refinery as raw material to produce rich steam, gasoline, diesel oil, wax oil and heavy wax oil through thermal cracking. After exchanging heat with the product, the residual oil raw material enters the lower part of the vaporization section of the main fractionation tower to contact and exchange heat with the high-temperature oil and gas at about 450°C from the outlet of the coke tower. The heavy wax oil in the oil gas is liquefied and enters the bottom of the tower together with the residual oil raw material. Then it is drawn out from the bottom outlet of the fractionating tower, e...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C10G53/00
Inventor 雷泽永
Owner 雷泽永
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