C<2->/C<3+> light dydrocarbon separation method integrating absorption method with fractionation method and C<2->/C<3+> light dydrocarbon separation system

A technology of fractionation and absorption, which is applied in the separation of C2/C3 light hydrocarbons, can solve the problems of lower relative volatility and consume more energy, and achieve the effect of reducing energy consumption of separation and increasing relative volatility

Inactive Publication Date: 2012-08-22
CHINA HUANQIU CONTRACTING & ENG CO LTD
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The relative volatility reduction caused by high pressure makes the fractionation column with the same number of theoretical plates need to consume more energy to meet the expected separation requirements

Method used

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  • C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation method integrating absorption method with fractionation method and C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation system
  • C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation method integrating absorption method with fractionation method and C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation system
  • C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation method integrating absorption method with fractionation method and C&lt;2-&gt;/C&lt;3+&gt; light dydrocarbon separation system

Examples

Experimental program
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Effect test

Embodiment 1

[0037] Embodiment 1 Absorption tower integrated with high-pressure deethanizer tower

[0038] The feed gas and two streams of feed liquid formed after multi-stage pressurization, cooling and condensation, gas-liquid separation, deacidification, and dehydration in the upstream enter the C3 absorption tower 01 and the deethanizer 02 respectively (the three feeds The material is obtained from the upstream system, figure 1 The formation process of the three feeds is not shown, and the use of multiple feeds is one of the common practices in the existing fractionation process)

[0039] like figure 1 As shown, the feed gas first enters the C3 absorption tower 01. The C3 absorption tower 01 is a tower with a simple structure, which is equipped with trays or packing equivalent to about 10 theoretical plates. In the C3 absorber 01, the feed gas is counter-contacted with the absorbent from the deethanizer reflux pump 06 (ie "lean liquor"). The easily soluble component in the feed, i.e...

Embodiment 2

[0046] Embodiment 2 Absorption tower integrated with low-pressure deethanizer

[0047] The feed gas and two streams of feed liquid formed after multi-stage pressurization, cooling and condensation, gas-liquid separation, deacidification, and dehydration in the upstream enter the C3 absorption tower 01 and the deethanizer 02 respectively (the three feeds The material is obtained from the upstream system, figure 2 The formation process of the three feeds is not shown, and the use of multiple feeds is one of the common practices in the existing fractionation process).

[0048] like figure 2 As shown, the feed gas first enters the C3 absorption tower 01. C3 absorption tower 01 is a tower with a simple structure, which is equipped with trays or packing equivalent to about 10 theoretical plates. In the C3 absorber 01, the feed gas is counter-contacted with the absorbent from the deethanizer reflux pump 06 (ie "lean liquor"). The easily soluble component in the feed, i.e. almos...

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Abstract

The invention relates to a C<2-> / C<3+> light dydrocarbon separation method integrating an absorption method with a fractionation method and a C<2-> / C<3+> light dydrocarbon separation system, which are used for separating C<2-> from C<3+> in the process of front-end deethanization. The method comprises the following steps of: separating most C<2-> including light components such as hydrogen and methane in charging material by an absorption tower, and fractionating the residual C<2-> and all C<3+> by a fractionating tower. Absorbent of the absorption tower is 'barren liquor' from the inner part of a system, i.e. some part of liquid phase in a reflow tank of the fractionating tower. Compared with the single fractionation method, the method integrating the absorption method with the fractionation method can save more energy, and can enhance the relative volatility bwtween the light key component and the heavy key component since a deethanization tower adopts lower tower pressure, so that the aim of reducing separation energy consumption can be achieved. When the fractionating tower adopts lower tower pressure from 22-26 Bar (a), the separation energy consumption of the whole system can be obviously lower than that of the prior art only by one more heat exchanger using refrigerant from -47 DEG C to -52 DEG C.

Description

technical field [0001] The present invention relates to a separation method and system of C2 / C3 light hydrocarbons, in particular to a separation method and system of C2 / C3 light hydrocarbons integrated with absorption method and fractionation method, which is used in the pre-deethanization separation process C2 - / C3 + separate. Background technique [0002] Separation of light hydrocarbons refers to hydrogen and C1 to C5 hydrocarbon mixtures (abbreviation: H 2 -C1-C5) for separation. [0003] The carbon two fraction is abbreviated as C2, and the carbon two and lighter fraction is abbreviated as C2 - , the carbon three fraction is abbreviated as C3, and the carbon three and heavier fraction is abbreviated as C3 + . [0004] Most of the existing light hydrocarbon separation technologies use a single fractionation method. Fractional distillation is the only choice in many links of light hydrocarbon separation, but it has the disadvantage of high energy consumption in s...

Claims

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Application Information

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IPC IPC(8): C07C7/11C07C7/04C07C11/04C07C11/06C07C9/04
Inventor 罗自坚徐文浩
Owner CHINA HUANQIU CONTRACTING & ENG CO LTD
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