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Method for separating reaction products produced during preparation of propylene by dehydrogenating propane

A technology for propane dehydrogenation and reaction products, which is applied in distillation purification/separation, diaphragm purification/separation, sustainable manufacturing/processing, etc. Suitability and other issues to achieve the effect of saving equipment costs, high recovery rate and high recovery rate

Active Publication Date: 2012-11-28
WISON ENG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0010] (2) Since the energy of the high-grade refrigerant with a very low temperature comes from the refrigeration compressor, the refrigeration compressor consumes a lot of energy
[0011] (3) The higher the hydrogen content, the lower the temperature at which the reaction product condenses to achieve the same liquefaction rate, and the lower the required refrigerant temperature. shift problem
However, the hydrogen content in the propane dehydrogenation product is high, and the required absorbent circulation is very large, so the oil absorption method is not suitable

Method used

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  • Method for separating reaction products produced during preparation of propylene by dehydrogenating propane
  • Method for separating reaction products produced during preparation of propylene by dehydrogenating propane
  • Method for separating reaction products produced during preparation of propylene by dehydrogenating propane

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Embodiment 1

[0046] The process is attached figure 2 Shown, the material balance table of embodiment 1 is as shown in table 1.

[0047] A certain propane dehydrogenation to propylene reaction product is compressed to 1.8 MPa, and after water cooling, removal of acidic substances and drying, it enters the separation process and is used as the feed of the separation system. The composition is shown in Table 1, stream 101. The stream 101 is cooled and condensed through the process stream and propylene refrigerant in the first cold box L101 and the first heat exchanger E101 in turn, the temperature is lowered to -20°C, and it enters the first-stage flash tank V101. The gas phase 102 at the top of the first-stage flash tank V101 is sent to the membrane separation unit; the liquid phase at the bottom of the tank is sent to the deethanizer T101.

[0048] The feed composition of the membrane separation unit is shown in the stream 102 in Table 1, and the membrane separation unit is separated into...

Embodiment 2

[0066] The process is attached Figure 4 Shown, the material balance table of embodiment 2 is as shown in table 4.

[0067] A certain propane dehydrogenation to propylene reaction product is compressed to 1.0 MPa, and after water cooling, removal of acidic substances and drying, it enters the separation process and is used as the feed of the separation system. The composition is shown in Table 4, stream 301. The stream 301 enters the membrane separation unit and is separated into a hydrogen-rich permeate gas 304 and a hydrocarbon-rich non-permeate stream 303 through the membrane separation unit. The hydrogen purity of membrane-separated permeate gas 304 is higher than 96 mol%, and the hydrogen recovery rate is 35%. Membrane separation unit includes membrane separation feed demister, heating and membrane separator. The temperature of the membrane separator was 50°C. The inlet gas pressure of the membrane separation unit is 0.9 MPa, the pressure of membrane separation permeat...

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Abstract

The invention relates to a method for separating reaction products produced during preparation of propylene by dehydrogenating propane. In the method, reaction products produced during preparation of propylene by dehydrogenating propane are separated in a way of combining membrane separation with cryogenic separation. The method comprises the following steps of: (1) cooling pretreated reaction products produced during preparation of propylene by dehydrogenating propane, condensing, feeding into a first-stage flash tank, conveying a gas phase serving as a hydrogen-rich product on the top of the first-stage flash tank outwards, or further cooling, condensing and feeding into a next-stage flash tank, gradually cooling and condensing and performing flash evaporation in sequence, conveying a gas phase serving as a hydrogen-rich product on the top of a last-stage flash tank outwards, conveying a liquid phase at the bottom of each stage of flash tank to an ethane removing tower, and discharging C3 out of a tower kettle of the ethane removing tower; and (2) separating into high-purity hydrogen permeable gas and hydrocarbon-rich impermeable material flow through membrane separation by using a membrane separation unit arranged in the step (1), conveying hydrogen permeable gas outwards, cooling and condensing hydrocarbon-rich impermeable material flow, and conveying to a next-stage flash tank. Compared with the prior art, the method has the advantages of high propylene recovery rate, low energy consumption and simple flow.

Description

technical field [0001] The invention belongs to the technical field of light hydrocarbon separation, and in particular relates to a method for separating reaction products from propane dehydrogenation to propylene by combining membrane separation and cryogenic separation. Background technique [0002] Propylene is an important petrochemical basic raw material second only to ethylene. It is mainly used in the production of dozens of petrochemical products and raw materials such as polypropylene, propylene oxide, acrylic acid, acrylonitrile, alkylated oil, and high-octane gasoline blending materials. Due to the rapid development of propylene downstream products, the rapid growth of my country's propylene demand has been greatly promoted. Since 2000, the growth rate of propylene demand has exceeded that of ethylene. The existing traditional naphtha steam cracking and catalytic cracking propylene production units can no longer meet the market demand, and other sources of propy...

Claims

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Application Information

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IPC IPC(8): C07C11/06C07C7/04C07C7/144
CPCY02P20/50
Inventor 丁干红李围潮
Owner WISON ENG
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