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Method for processing light hydrocarbons oxidation sweetening tail gas

A technology for oxidatively removing mercaptans and tail gas, applied in chemical instruments and methods, separation methods, and refining hydrocarbon oil, etc., can solve the problems of economic decline, economic impact, increase in operating costs, etc., to improve absorption rate and operation flexibility, The effect of improving the gas-liquid contact effect and reducing the scale of the equipment

Active Publication Date: 2010-02-03
CHINA PETROLEUM & CHEM CORP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The combination of condensation and catalytic oxygen can recover most of the volatile hydrocarbons, and can also achieve up-to-standard discharge of tail gas, but its disadvantages are that the process is long, the operation cost is high, and the economy is affected
Maximizing the recovery of hydrocarbons in the tail gas can increase the income, but generally speaking, when the recovery rate of hydrocarbons reaches a certain limit, the operating costs required to further increase the recovery rate will increase greatly, so the overall economy will decline; Comprehensive emission requirements, how to determine the oxidative sweetening tail gas treatment method and control conditions, to ensure the maximum economy under the premise of meeting the emission standards, is the key research of the oxidative sweetening tail gas treatment method

Method used

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  • Method for processing light hydrocarbons oxidation sweetening tail gas
  • Method for processing light hydrocarbons oxidation sweetening tail gas
  • Method for processing light hydrocarbons oxidation sweetening tail gas

Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0028] Small lab experiments.

[0029] A first-stage pulse bubbling absorption tower is adopted, including a bubbling absorption zone, and the internal components of the absorption tower are determined according to the preferred data in the specific embodiment. The thickness of the liquid phase layer in the bubbling absorption zone is 400mm, and the height of the spray section is 300mm. The absorbents were three different diesel fractions. After absorption, the tail gas is diluted with air and then discharged.

[0030] Gasoline fraction (distillation range 70-170°C) and petroleum ether (distillation range 30-60°C) are simulated by bubbling air through oxidative sweetening tail gas to conduct absorption and recovery tests. The inlet pressure of the gas phase is 0.1MPa (gauge pressure). The outlet is normal pressure, and the results are listed in Table 1, Table 2, and Table 3. (Nm 3 Indicates the standard state cubic meter)

[0031] Table 1 The absorption effect of differen...

Embodiment 2

[0038] An enterprise gasoline oxidative sweetening tail gas contains 32v% hydrocarbons (volume fraction, the same below), the tail gas temperature is 53°C, the oxygen content is 17v%, the pressure is 0.2MPa (gauge pressure), and the flow rate is 70Nm 3 / h or so. A three-stage pulse bubbling absorption tower is adopted, including three bubbling absorption zones and three spraying absorption zones, and the internal components of the absorption tower are determined according to the preferred data in the specific embodiment. The thickness of the liquid layer in the bubbling absorption zone is 350mm, and the height of the spray section is 250mm. The absorbent is catalytic diesel oil, and the liquid-gas ratio is 100L / m 3 , The operating temperature is 25-40°C. The absorbed catalytic diesel oil enters the hydrogenation unit together with other catalytic diesel oils, and the absorbed tail gas is led to the air cooler inlet of the catalytic cracking unit.

[0039] After absorption t...

Embodiment 3

[0041] Same as Example 2, the exhaust gas after absorption treatment, the amount is about 50Nm 3 / h, the concentration of organic matter is about 20g / Nm 3 , the hydrocarbon emission rate was about 1 kg / h. Dilute with air to a total hydrocarbon concentration of 50093000mg / Nm 3 , using a conventional heat storage combustion device for treatment, and the purified gas meets the current national emission standards.

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Abstract

The invention discloses a method for processing light hydrocarbons oxidation sweetening tail gas. The method takes diesel distillate as an absorbent and adopts a countercurrent pulsed bubbling absorption tower; a gas phase is dispersed by a nozzle of the absorption tower, and is contacted with the absorbent in a bubbling absorption area to absorb volatile hydrocarbons in the gas phase; the nozzleof the absorption tower has a bubbling pulse valve structure; and the absorbent flows downwards through a downflow spout arranged on a tower plate of the bubbling absorption area. The method has the advantages of simple process, economy and reasonability, and accordance with environmental protection standards, and can be used for processing various light hydrocarbons oxidation sweetening tail gases.

Description

technical field [0001] The invention relates to a treatment method for hydrocarbon-containing waste gas, in particular to a treatment method for oxidative sweetening tail gas of light hydrocarbons. Background technique [0002] The mercaptan content of light hydrocarbons is one of the important quality indicators, such as liquid hydrocarbons, gasoline, kerosene, etc. The light hydrocarbons produced by many processes contain a certain amount of mercaptans, so appropriate methods are required to remove them. The hydrogenation process can be used for sweetening light hydrocarbons, but the hydrogenation method device is complicated, the investment is large, the operating cost is high, and some indicators of light hydrocarbons (such as the octane number of gasoline) are affected, such as the gasoline disclosed in CN1478866A Desulfurization methods, etc. Oxidative desulfurization is an important method for desulfurization of light hydrocarbons, that is, under certain conditions,...

Claims

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Application Information

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IPC IPC(8): B01D53/14B01D53/18C10G27/00
Inventor 刘忠生王海波方向晨彭德强郭兵兵王有华
Owner CHINA PETROLEUM & CHEM CORP
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