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Method for recovering high yield and high purity hydrogen and ethylene from refinery dry gas

A refinery dry gas, high-yield technology, applied in chemical instruments and methods, hydrogen separation, hydrocarbons, etc., can solve the problems of high energy consumption, absorbent and equipment investment, and inability to recover hydrogen at the same time, to achieve cold oil The effect of increasing the dew point at the top of the absorption tower, reducing operating costs, and reducing the amount of treatment

Active Publication Date: 2014-09-17
SICHUAN TECHAIRS
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

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Problems solved by technology

The disadvantage of cold oil absorption and separation is that hydrogen cannot be recovered at the same time, and because the raw gas contains most of the components that are not easy to condense, it requires high energy consumption, absorbent and equipment investment, and it is not suitable for the second group of carbon in the dry gas of the refinery. Most of the working conditions where the content is less than 10% (volume ratio)

Method used

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  • Method for recovering high yield and high purity hydrogen and ethylene from refinery dry gas
  • Method for recovering high yield and high purity hydrogen and ethylene from refinery dry gas

Examples

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Comparison scheme
Effect test

Embodiment 1

[0038] Such as figure 1 As shown, the method for recovering hydrogen and ethylene with high yield and high purity from refinery dry gas is characterized in that it comprises the following steps:

[0039] One-stage compression step: dry the refinery with a hydrogen content of 56.2%, an ethane content of 7.2%, an ethylene content of 6.2%, a methane content of 22.2%, a nitrogen content of 5.5%, a carbon dioxide content of 0.9%, and an acid gas content of 1.8%. The pressure of gas (volume ratio) is raised to 0.7Mpa.

[0040] Purification step: use the existing low-temperature methanol washing process to remove carbon dioxide, sulfur dioxide, hydrogen sulfide and other acid gases in the refinery dry gas with a pressure of 0.7 MPa obtained in the first-stage compression step.

[0041] The first-stage PSA regeneration step: send the dry gas from the refinery to the first-stage PSA regeneration tower for pressure swing adsorption at 30°C. It is clear to those skilled in the art that...

Embodiment 2

[0053] Such as figure 1 As shown, the method for recovering hydrogen and ethylene with high yield and high purity from refinery dry gas is characterized in that it comprises the following steps:

[0054] One-stage compression step: dry the refinery with 46.5% hydrogen content, 12.4% ethane content, 6.0% ethylene content, 20% methane content, 9.5% nitrogen content, 2.2% carbon dioxide and above components, and 3.2% acid gas content. The pressure of gas (volume ratio) is raised to 1.0Mpa.

[0055] Purification step: use the existing low-temperature methanol washing process to remove carbon dioxide, sulfur dioxide, hydrogen sulfide and other acid gases in the refinery dry gas with a pressure of 1.0 MPa obtained in the first-stage compression step.

[0056] The first-stage PSA regeneration step: send the dry gas from the refinery to the first-stage PSA regeneration tower for pressure swing adsorption at 30°C. It is clear to those skilled in the art that pressure swing adsorption...

Embodiment 3

[0068] Such as figure 1 As shown, the method for recovering hydrogen and ethylene with high yield and high purity from refinery dry gas is characterized in that it comprises the following steps:

[0069] One-stage compression step: dry the refinery with 18.5% hydrogen content, 14.5% ethane content, 16% ethylene content, 30% methane content, 14.5% nitrogen content, 3.5% carbon 2 or higher component content, and 3% acid gas content. The pressure of gas (volume ratio) is raised to 0.7Mpa.

[0070] Purification step: use the existing low-temperature methanol washing process to remove carbon dioxide, sulfur dioxide, hydrogen sulfide and other acid gases in the refinery dry gas with a pressure of 1.2 MPa obtained in the first-stage compression step.

[0071] The first-stage PSA regeneration step: send the dry gas from the refinery to the first-stage PSA regeneration tower for pressure swing adsorption at 30°C. It is clear to those skilled in the art that pressure swing adsorption ...

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Abstract

The invention discloses a method for recovering high yield and high purity hydrogen and ethylene from refinery dry gas. The method comprises the following steps: a first stage pressure swing adsorption, a second stage pressure swing adsorption, membrane separation, cold oil absorption and coarse distillation. The invention has the advantages that the method combines adsorption separation method, membrane separation method and cold oil absorption method to process refinery dry gas, so as to obtain high purity hydrogen, ethylene and C2 and above gas rich in ethane, ensure high yield, and achieve clear separation of hydrogen, ethylene and gas rich in ethane.

Description

technical field [0001] The invention relates to a waste gas treatment method, in particular to a method for recovering hydrogen and ethylene with high yield and high purity from refinery dry gas. Background technique [0002] The useful components in refinery dry gas are mainly hydrogen, light olefins and light alkanes. These components are very valuable in refinery dry gas, but at present, a large amount of them have not yet been optimally utilized, but are directly used as fuel, and some are even directly ignited to vent. Refinery dry gas contains not only hydrogen, but also a large amount of light olefins and light alkanes. These components can be separated and used separately, which is more beneficial than using them directly as fuel or raw materials for reforming hydrogen production and synthesizing methanol. [0003] The technologies for recovering hydrogen, light olefins and light alkanes from refinery dry gas mainly include cold oil absorption separation method, me...

Claims

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Application Information

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IPC IPC(8): C07C11/04C07C7/00C07C7/04C07C7/12C01B3/50
Inventor 蔡跃明钟雨明张学文陈运钟娅玲
Owner SICHUAN TECHAIRS
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