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A light hydrocarbon recovery method and device

A light hydrocarbon recovery and absorbent technology, which is applied in the recovery of liquid hydrocarbon mixtures, chemical instruments and methods, hydrocarbon distillation, etc., can solve the problems of long process, complex operation, high investment and energy consumption, and achieve simple process and efficient separation and recovery , The effect of reducing investment and energy consumption

Active Publication Date: 2022-02-22
SINOPEC ENG +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0005] For the existing light hydrocarbon recovery process technology, the C3 / C4 component is usually recovered first, and then the C2 component is recovered. The process is long, and there is a secondary separation between the components, and the investment and energy consumption are high. , the operation is more complicated

Method used

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  • A light hydrocarbon recovery method and device
  • A light hydrocarbon recovery method and device
  • A light hydrocarbon recovery method and device

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0103] Light hydrocarbon recovery unit, including: hot / cold low fraction oil feed pipeline, debutanizer 1, fractionation tower 2, rich gas desulfurization tower 3, liquid hydrocarbon desulfurization tower 4, compressor 5, cooler 6, aftercooler 7. Gas-liquid separation tank 8, absorption tower 9 and separation unit;

[0104] Wherein, the hot / cold low fraction oil feed line is connected with debutanizer 1;

[0105] The debutanizer is equipped with a condenser and a reflux tank, the bottom of the tower is connected to the fractionation tower 2, the top of the tower is connected to the condenser and the reflux tank in turn, the top of the reflux tank is connected to the rich gas desulfurization tower 3, and the bottom of the tank is connected to the liquid hydrocarbon desulfurization tower 4 connections;

[0106] The top of the rich gas desulfurization tower 3 is connected with the compressor 5, the cooler 6, the aftercooler 7, and the gas-liquid separation tank 8 in sequence;

...

Embodiment 2

[0135] use as figure 2 The process flow chart shown is for oil and gas desulfurization and light hydrocarbon recovery.

[0136] Among them, the difference between this embodiment and embodiment 1 is:

[0137] (6) Separation:

[0138] Demethanization: The liquid phase from the bottom of the gas-liquid separation tank 8 removes methane in the demethanizer 10, and at the same time removes a small part of C2 and components above C2, and the gas phase at the top of the demethanizer 10 returns after cooling The gas-liquid separation tank 8, the liquid phase at the bottom of the tower is sent to the deisobutanizer 14; the operating temperature at the top of the demethanizer 10 is 15-40°C, and the operating pressure is 2.25-2.85MPaG;

[0139] Deisobutanization: The liquid phase from the bottom of the demethanizer 10 is separated in the deisobutanizer 14 for components below C3 and C3, and the separated overhead gas phase is sent to the deethanizer 11, and the liquid phase at the bo...

Embodiment 3

[0151] use as image 3 The process flow chart shown is for oil and gas desulfurization and light hydrocarbon recovery.

[0152] Among them, the difference between this embodiment and embodiment 1 is:

[0153] (6) Separation:

[0154] Demethanization: The liquid phase from the bottom of the gas-liquid separation tank 8 removes methane in the demethanizer 10, and at the same time removes a small part of C2 and components above C2, and the gas phase at the top of the demethanizer 10 returns after cooling The gas-liquid separation tank 8, the liquid phase at the bottom of the tower is sent to the depropanizer I12; the operating temperature at the top of the demethanizer 10 is 15-40°C, and the operating pressure is 2.25-2.85MPaG;

[0155] Depropanization: The liquid phase components from the bottom of the demethanizer 10 are separated in the depropanizer I12, and the separated components of C3 and below C3 are extracted from the top of the depropanizer I12 and then sent to the de...

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Abstract

The invention belongs to the fields of oil refining and chemical industry, and specifically discloses a light hydrocarbon recovery method and device. The method has simple process, moderate operating conditions, low consumption of cooling energy, and can realize the recovery of light hydrocarbons in the hydrocracking process with less equipment. The separation and recovery of ethane, propane and carbon four components can be realized in particular, wherein the recovery rate of ethane is over 97wt%, the recovery rate of propane is over 98wt%, and the methane content in the recovered ethane is Not more than 1 vol%, and the ethane content in the recovered propane is not more than 300ppmv.

Description

technical field [0001] The invention belongs to the field of oil refining and chemical industry, and more specifically relates to a method and a device for recovering light hydrocarbons, and more specifically relates to a device and a method for recovering light hydrocarbons in a hydrocracking process. Background technique [0002] Hydrocracking is one of the main processing technologies in refineries. It mainly uses heavy distillates such as wax oil under high pressure, hydrogenation and catalysts to undergo a series of reactions such as hydrotreating and hydrocracking to achieve heavy oil and light oil. purpose. Hydrocracking will produce a certain amount of C1-C4 light hydrocarbons, with a yield of about 3-8wt%. The recovery of light hydrocarbons in conventional hydrocracking units is mainly for the recovery of liquefied gas (C3 / C4) components, and the process settings are relatively perfect. It is mainly equipped with debutanizer, absorption and desorption tower, stabil...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10G53/00C10G7/00C10G7/12C10G5/04C10G5/06C10G5/00C07C7/00C07C7/04C07C7/11C07C9/06C07C9/08C07C9/10C07C9/12
CPCC10G53/00C10G7/00C10G7/12C10G5/06C10G5/04C10G5/00C07C7/005C07C7/04C07C7/11C10G2300/202C10G2300/207C10G2400/04C10G2400/02
Inventor 黄孟旗吴迪郝少博姚爱智刘凯祥
Owner SINOPEC ENG
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