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Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption

A solvent absorption and separation method technology, applied in the field of oxide conversion to produce olefins and hydrocarbon cracking to produce olefins, can solve problems such as low investment and energy consumption

Active Publication Date: 2009-06-03
WISON ENG
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

The process requires less investment and lower energy consumption, but still requires a propylene refrigeration compressor and a single-stage ethylene refrigeration compressor, and still has a two refrigeration compressor system

Method used

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  • Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption
  • Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption
  • Method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption

Examples

Experimental program
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Effect test

Embodiment 1

[0045] see process image 3 , the outlet gas of a reactor enters the separation process after compression, water washing, alkali washing, removal of methanol and drying and dehydration. The gas S100 is cooled to about 10°C by the feed cooler E101 and enters the flash tank V101 for gas-liquid phase separation. The gas and liquid phases pass through the feed coolers E102 and E103 of the pre-cutting tower respectively and are further cooled, and then enter the pre-cutting tower T101. The top product S308 of the pre-cut tower T101 directly enters an absorption tower T102 with an overhead condenser using propylene refrigerant without further cooling. Absorption tower T102 uses absorbent S327 with carbon five as the main component to absorb carbon two in the feed, and S327 is cooled to -37°C with propylene refrigerant. The discharge S311 of the pre-cutting tower T101 tower kettle is C2, C3 and heavier products, which are directly sent to the deethanizer T201 for the separation of ...

Embodiment 2

[0050] see process figure 2 , the outlet gas of a reactor enters the separation process after compression, water washing, alkali washing, removal of methanol and drying and dehydration. The gas S100 is cooled to about 10°C by the feed cooler E101 and enters the flash tank V101 for gas-liquid phase separation. The gas-liquid phase enters the pre-cut tower T101 after passing through the feed coolers E102 and E103 of the pre-cut tower respectively. The top product S308 of the pre-cutting tower T101 contains all light gases and ethylene accounting for about 11% of the feed, and enters the absorption tower T102. The absorption tower T102 adopts the absorbent S327 with carbon four as the main component to absorb carbon two in the feed. The discharge S311 of the pre-cutting tower T101 tower kettle is C2, C3 and heavier products, which are directly sent to the deethanizer T201 for the separation of C2 and C3. The top product of the deethanizer T201 is C2 fraction, which is separat...

Embodiment 3

[0055] see process Figure 4 , the outlet gas S100 of a certain reactor enters the high-pressure depropanizer T202A after being compressed, washed with water, washed with alkali, dried and dehydrated. The top gas of the high depropanizer T202A tower is further pressurized to 3.6Mpa, and the material is cooled to 2°C to obtain a gas-liquid two-phase, and the gas-liquid phase is further cooled separately. The gas phase enters the pre-cutting tower T101, and the liquid phase is divided into two parts, one part is used as the reflux of the high-pressure depropanizer T202A, and the other part is fed into the pre-cutting tower T101. The tower overhead product S308 of the pre-cutting tower T101 is sent to the absorption tower T102 after being cooled, and this tower adopts the absorbent with propane as the main component to absorb the carbon and dihydrocarbons in the tower overhead product of the pre-cutting tower, and the methane hydrogen S313 is obtained from The tower item is disc...

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Abstract

The invention relates to a method for separating lower hydrocarbon containing light gas by combining distillation and solvent absorption, comprising the steps as follows: (1) pre-disposed gas at the outlet of a reactor is cooled to the temperature ranging from 10 DEG C to -37 DEG C and sent to a pre-cutting tower; (2) the gas at the outlet of the pre-cutting tower is sent to an absorption tower and C1 and C2 in the gas are separated by taking C3 or C4 or C5 or C6 or hydrocarbon mixtures as absorbent; (3) outcomes generated at the bottom of the absorption tower are sent to the pre-cutting tower; with C2 distillate further absorbed and methane and lighter components removed in the pre-cutting tower, the outcome is sent to a deethanizer so that the C2 and C3 are clearly cut. Compared with the prior art, the method has the advantages of little investment, low energy dissipation, high material recovery rate, simple operation, small maintenance quantity, reliable running, requiring no ethane refrigerant compressor, and the like.

Description

technical field [0001] The invention belongs to the technical field of light hydrocarbon separation, and in particular relates to a separation method in the process of producing olefins by conversion of oxides and cracking of hydrocarbons to produce olefins. Background technique [0002] Ethylene and propylene are basic raw materials for the petrochemical industry and have historically been obtained by steam cracking or catalytic cracking of hydrocarbons. In the case of increasingly tight oil supply, people have developed the process of producing low-carbon olefins with oxides, especially methanol and ethanol as raw materials. Alcohols can be produced from natural gas or coal synthesis gas, thus avoiding the use of petroleum resources. [0003] The product composition of the oxide conversion process is similar to that of the cracking furnace outlet product composition of hydrocarbon cracking to ethylene, which are light gases such as hydrogen, nitrogen and light hydrocarbon...

Claims

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Application Information

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Patent Type & Authority Applications(China)
IPC IPC(8): C07C7/04C07C7/11C07C11/02
Inventor 倪进方李立新
Owner WISON ENG
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