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Process for synthesizing methane through synthesis gas

A technology for synthesizing methane and synthesis gas, which can be used in the production of hydrocarbons from oxygen-containing organic compounds, biological raw materials, and ethylene production. Effects of reduced gas cooling process, reduced operating costs and risks, high reaction efficiency

Active Publication Date: 2012-09-26
SHANXI INST OF COAL CHEM CHINESE ACAD OF SCI
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

Due to the use of lower space velocity (2000-14000L / h / Kg), higher reaction temperature (350-500°C) and pressure (2-4.5Mpa), the amount of raw material pretreatment is low, the solvent is easy to volatilize, and the Disadvantages such as high equipment requirements
At the same time, there is only a slurry bed reactor in the process, which is limited by the mass transfer between the gas-liquid-solid three-phase, which affects the conversion and synthesis efficiency of CO.

Method used

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Examples

Experimental program
Comparison scheme
Effect test

Embodiment 1

[0032] Embodiment 1: take by weighing 194.6g of Ni (NO 3 ) 2 ·6H 2 O is prepared as an impregnation solution, impregnated with equal volume and pre-crushed to 20-40 mesh γ-Al 2 o 3 283.3 g of the carrier was left standing for 5 h, dried in an oven at 150 °C for 20 h, and calcined in a muffle furnace at 400 °C for 6 h. That is, the content of α-NiO is 15% (wt), γ-Al 2 o 3 Slurry bed catalyst with a content of 85% (wt), crushed to below 200 mesh for later use.

[0033] Weigh 166.5g of Ni(CH 3 COO) 2 4H 2 O was dissolved in ethylene glycol and prepared as a 1M solution in an oil bath. The preprecipitated 1M anhydrous sodium carbonate solution was used as a precipitating agent, and the catalyst was prepared by coprecipitation at a temperature of 110° C., and the precipitation time was 3 hours. After the precipitation is completed, continue to age at the precipitation temperature for 1 hour, filter with suction, and wash until neutral. The filter cake was dried in an ove...

Embodiment 2

[0037] Embodiment 2: take by weighing 194.6g of Ni (NO 3 ) 2 ·6H 2 O is prepared as an impregnation solution, impregnated with equal volume and pre-crushed to 20-40 mesh γ-Al 2 o 3 450.0 g of the carrier was left standing for 8 h, dried in an oven at 130 °C for 18 h, and calcined in a muffle furnace at 430 °C for 4 h. That is, the content of α-NiO is 10% (wt), γ-Al 2 o 3 Slurry bed catalyst with a content of 90% (wt), crushed to below 200 mesh for use.

[0038] Weigh 166.5g of Ni(CH 3 COO) 2 4H 2 O was dissolved in ethylene glycol and prepared as a 1M solution in an oil bath. The preprecipitated 1M anhydrous sodium carbonate solution was used as a precipitating agent, and the catalyst was prepared by coprecipitation at a temperature of 130° C., and the precipitation time was 2.6 hours. After the precipitation is completed, continue to age at the precipitation temperature for 1 hour, filter with suction, and wash until neutral. The filter cake was dried in an oven at...

Embodiment 3

[0043] Embodiment 3: take by weighing 194.6g of Ni (NO 3 ) 2 ·6H 2 O is prepared as an impregnation solution, impregnated with equal volume and pre-crushed to 20-40 mesh γ-Al 2 o 3 150.0 g of the carrier was left standing for 10 h, dried in an oven at 100 °C for 10 h, and calcined in a muffle furnace at 450 °C for 2 h. That is, the content of α-NiO is 25% (wt), γ-Al 2 o 3 Slurry bed catalyst with a content of 75% (wt), crushed to below 200 mesh for use.

[0044] Weigh 166.5g of Ni(CH 3 COO) 2 4H 2O was dissolved in ethylene glycol and prepared as a 1M solution in an oil bath. The preprecipitated 1M anhydrous sodium carbonate solution was used as a precipitating agent, and the catalyst was prepared by coprecipitation at a temperature of 140° C., and the precipitation time was 1 h. After the precipitation is completed, continue aging at the precipitation temperature for 1.5h, filter with suction, and wash until neutral. The filter cake was dried in an oven at 100 °C f...

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Abstract

The invention relates to a process for synthesizing methane through synthesis gas. The process comprises the following steps of: according to the weight ratio of slurry bubble column methanation catalyst to solvent being 10-30:100, feeding the slurry bubble column methanation catalyst into a slurry bubble column reactor, taking the synthesis gas as a raw material, carrying out methanation reaction, and forming slurry bubble column outlet gas through methane produced through reaction, unconverted CO, H2, a little dimethyl ether produced through reaction, CO2 produced through water gas shift reaction, and the like; and isobarically and isothermally feeding the slurry bubble column outlet gas into a fixed bed reactor filled with fixed bed methanation catalyst, carrying out methanation reaction again on unconverted H2, CO, the CO2 produced through water gas shift reaction, and the like, splitting the little dimethyl ether to generate methane, and separating fixed bed outlet gas to obtain the product gas in a condensation way. The process has the advantages of high CO conversion rate, and high methane selectivity.

Description

technical field [0001] The invention belongs to a process for synthesizing methane, in particular to a process for synthesizing high-purity methane from synthesis gas through a slurry bed reactor connected in series with a fixed bed reactor. Background technique [0002] Methane, commonly known as natural gas, is a high-quality, clean energy. In 2000, my country's natural gas output was 27.73 billion cubic meters, and in 2007 it reached 69.3 billion cubic meters, with an average annual growth rate of 14.0%. It is estimated that China's natural gas demand in 2020 will be 200 billion cubic meters, while the natural gas production in the same period can only reach 140 billion to 160 billion cubic meters [Liu Zhiguang, Gong Huajun, Yu Liming, Discussion on the development of coal-based natural gas in my country, Coal Chemical Industry, 37 (1 ): 1-8, 2009]. The shortage of natural gas resources in my country makes the contradiction between supply and demand increasingly prominen...

Claims

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Application Information

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IPC IPC(8): C07C9/04C07C1/04C07C1/12C07C1/20
CPCY02P30/20Y02P30/40
Inventor 韩怡卓谭猗生解红娟马胜利潘俊轩
Owner SHANXI INST OF COAL CHEM CHINESE ACAD OF SCI
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