A method for producing methane cogeneration liquid fuel from carbonaceous materials

Abstract

A method for producing methane cogeneration liquid fuel from carbonaceous materials, the method comprising: purifying the crude synthesis gas obtained after gasifying the carbonaceous materials to remove impurities in the crude synthesis gas to obtain net synthesis gas; contacting at least part of the net synthesis gas and water with a mixed catalyst, and performing gas-liquid separation on the product obtained after the contact to obtain a gas product and a liquid product, and the mixed catalyst contains a water-gas shift catalyst and a Fischer-Tropsch synthesis catalyst; A methanation gas feedstock is contacted with a methanation catalyst, the methanation gas feedstock contains the gas product, the H in the methanation gas feedstock 2 The molar ratio of / CO is 2.8-3.5. According to the method of the present invention, methane can be produced and co-produced liquid fuel, and the load of water-gas shift in the process can be effectively reduced, energy consumption can be saved, and the utilization efficiency of carbon can be improved, and it can be directly used in the methane production device of the prior art It can be carried out without adding equipment.

Description

technical field

[0001] The invention relates to a method for indirect conversion of carbonaceous materials, more specifically, relates to a method for gasifying carbonaceous materials into synthesis gas, converting synthesis gas into methane gas and co-producing liquid fuel. Background technique

[0002] Based on energy endowment and national energy security considerations, China is actively promoting the strategy of "replacing oil with coal" to convert coal into civil gas, transportation fuel, and basic chemical raw materials. Among them, the coal-to-natural gas technology is the process of using low-rank lignite to produce synthetic gas through gasification, and then converting it into methane, which is used as a gas fuel to replace traditional natural gas.

[0003] The coal-to-natural gas process has high energy efficiency, low water consumption, and relatively mature technology, which is of great significance for developing coal in remote areas of western China, improvin...

Examples

Embodiment 1

[0048] This example is used to illustrate the method for producing methane cogeneration liquid fuel oil from carbonaceous materials provided by the present invention.

[0049] Lignite fragments with a particle size of 5-50 mm (see Table 1 for chemical composition) are gasified into crude synthesis gas with oxygen / water vapor as a gasification agent, and the obtained crude synthesis gas is sequentially cooled, detarred, crude desulfurized, After the fine desulfurization process, the net syngas (see Table 2 for the composition) is obtained, in which (CO+H 2 ) content is 63% by volume, H 2 / CO molar ratio is 1.59;

[0050]The net synthesis gas is divided into two streams, G1 and G2, wherein G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with a fixed bed of a mixed catalyst. The catalyst bed is composed of a water-gas shift catalyst and a Fischer-Tropsch synthesis catalyst. Mixed, the mass ratio of the two is 1:1, where...

Embodiment 2

[0053] The preparation and composition of the net synthesis gas was the same as in Example 1. The entirety of this net synthesis gas is divided into two streams G1 and G2. Among them, G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with the fixed bed of the mixed catalyst. The catalyst bed is formed by mixing the water-gas shift catalyst and the Fischer-Tropsch synthesis catalyst, and the mass ratio of the two is 0.6:1. Among them, the water gas shift catalyst is a Co-Mo catalyst (manufactured by Qingdao Lianxin Company, brand name QDB-03), and the Fischer-Tropsch synthesis catalyst is a molten iron catalyst (Fe 2 o 3 The content is 99.4% by weight, the particle size is 5-20 mesh); the composite reactor inlet temperature is 278°C, the outlet temperature is 332°C, the pressure is 3.33MPa, and the gas space velocity is 2000h -1 , the reacted product is cooled to 40°C by indirect heat exchange, and divided into gas stre...

Embodiment 3

[0056] The preparation and composition of the net synthesis gas was the same as in Example 1. The entirety of this net synthesis gas is divided into two streams G1 and G2. Among them, G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with the fixed bed of the mixed catalyst. The catalyst bed is formed by mixing the water gas shift catalyst and the Fischer-Tropsch synthesis catalyst, and the mass ratio of the two is 3:1, wherein , the water gas shift catalyst is a Co-Mo catalyst (manufacturer is Qingdao Lianxin Company, brand name QDB-03), and the Fischer-Tropsch synthesis catalyst is a supported iron catalyst (32% by weight Fe 2 o 3 -1.5 wt%CuO-0.4 wt%K 2 O-66.1 wt SiO 2 ); the inlet temperature of the synthesis reactor is 221°C, the outlet temperature is 252°C, the pressure is 2.78MPa, and the gas space velocity is 1100h -1 , the reacted product is cooled to 40°C by indirect heat exchange, and divided into gas strea...

technical field

[0001] The invention relates to a method for indirect conversion of carbonaceous materials, more specifically, relates to a method for gasifying carbonaceous materials into synthesis gas, converting synthesis gas into methane gas and co-producing liquid fuel. Background technique

[0002] Based on energy endowment and national energy security considerations, China is actively promoting the strategy of "replacing oil with coal" to convert coal into civil gas, transportation fuel, and basic chemical raw materials. Among them, the coal-to-natural gas technology is the process of using low-rank lignite to produce synthetic gas through gasification, and then converting it into methane, which is used as a gas fuel to replace traditional natural gas.

[0003] The coal-to-natural gas process has high energy efficiency, low water consumption, and relatively mature technology, which is of great significance for developing coal in remote areas of western China, improvin...

Examples

Embodiment 1

[0048] This example is used to illustrate the method for producing methane cogeneration liquid fuel oil from carbonaceous materials provided by the present invention.

[0049] Lignite fragments with a particle size of 5-50 mm (see Table 1 for chemical composition) are gasified into crude synthesis gas with oxygen / water vapor as a gasification agent, and the obtained crude synthesis gas is sequentially cooled, detarred, crude desulfurized, After the fine desulfurization process, the net syngas (see Table 2 for the composition) is obtained, in which (CO+H 2 ) content is 63% by volume, H 2 / CO molar ratio is 1.59;

[0050]The net synthesis gas is divided into two streams, G1 and G2, wherein G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with a fixed bed of a mixed catalyst. The catalyst bed is composed of a water-gas shift catalyst and a Fischer-Tropsch synthesis catalyst. Mixed, the mass ratio of the two is 1:1, where...

Embodiment 2

[0053] The preparation and composition of the net synthesis gas was the same as in Example 1. The entirety of this net synthesis gas is divided into two streams G1 and G2. Among them, G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with the fixed bed of the mixed catalyst. The catalyst bed is formed by mixing the water-gas shift catalyst and the Fischer-Tropsch synthesis catalyst, and the mass ratio of the two is 0.6:1. Among them, the water gas shift catalyst is a Co-Mo catalyst (manufactured by Qingdao Lianxin Company, brand name QDB-03), and the Fischer-Tropsch synthesis catalyst is a molten iron catalyst (Fe 2 o 3 The content is 99.4% by weight, the particle size is 5-20 mesh); the composite reactor inlet temperature is 278°C, the outlet temperature is 332°C, the pressure is 3.33MPa, and the gas space velocity is 2000h -1 , the reacted product is cooled to 40°C by indirect heat exchange, and divided into gas stre...

Embodiment 3

[0056] The preparation and composition of the net synthesis gas was the same as in Example 1. The entirety of this net synthesis gas is divided into two streams G1 and G2. Among them, G1 is sent to the synthesis reactor after heat exchange and temperature rise, and is contacted and reacted with the fixed bed of the mixed catalyst. The catalyst bed is formed by mixing the water gas shift catalyst and the Fischer-Tropsch synthesis catalyst, and the mass ratio of the two is 3:1, wherein , the water gas shift catalyst is a Co-Mo catalyst (manufacturer is Qingdao Lianxin Company, brand name QDB-03), and the Fischer-Tropsch synthesis catalyst is a supported iron catalyst (32% by weight Fe 2 o 3 -1.5 wt%CuO-0.4 wt%K 2 O-66.1 wt SiO 2 ); the inlet temperature of the synthesis reactor is 221°C, the outlet temperature is 252°C, the pressure is 2.78MPa, and the gas space velocity is 1100h -1 , the reacted product is cooled to 40°C by indirect heat exchange, and divided into gas strea...

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