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A coal-to-synthesis gas methanation process without recycle gas

A coal-to-synthesis gas and methanation technology, applied in the chemical industry, can solve the problems of increasing the power consumption of circulating gas and increasing equipment investment, and achieve the effects of improving energy utilization, reducing steam consumption, and reducing power consumption

Active Publication Date: 2017-02-15
CNOOC GAS & POWER GRP +1
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  • Summary
  • Abstract
  • Description
  • Claims
  • Application Information

AI Technical Summary

Problems solved by technology

[0003] The existing coal-to-SNG or LNG methanation technology usually uses complex devices of multiple gas cyclers and heat exchangers to control the temperature, and the cycle gas used is as high as five times, which not only increases equipment investment but also greatly increases Cycle gas power consumption

Method used

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  • A coal-to-synthesis gas methanation process without recycle gas
  • A coal-to-synthesis gas methanation process without recycle gas
  • A coal-to-synthesis gas methanation process without recycle gas

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Experimental program
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Effect test

Embodiment 1

[0021] The schematic diagram of this process is shown in figure 1 ,Such as figure 1 Shown, pressure 3.5MPa, 100000Nm 3 / h of synthesis gas and the total sulfur in the synthesis gas is less than 0.1ppm, f=(n H2 -n CO2 ) / (n CO +n CO2 )=3.005, the specific composition of syngas (volume percent, wet basis) is: H 2 : 64.00, CH 4 : 14.30, CO: 20.10, CO 2 : 0.90, N 2 : 0.50, H 2 O: 0.30. The raw material gas is divided into four streams according to 0.22, 0.15, 0.25, and 0.38 and enters the first, second, third, and fourth methanation reactors respectively. The first stream is heated and mixed with superheated steam at a temperature of 300°C, and then enters the second stream. In a methanation reactor, a methanation reaction is carried out. The gas after the reaction of the first methanation reactor has a temperature of 630°C, and then enters the waste pot for cooling, and by-product steam, and then the outlet gas of the first methanation reactor is divided into two groups...

Embodiment 2

[0023] This embodiment is based on figure 2 The process flow shown is carried out, the pressure is 3.5MPa, 100000Nm 3 / h of synthesis gas and the total sulfur in the synthesis gas is less than 0.1ppm, f=(n H2 -n CO2 ) / (n CO +nCO2 )=3.005, the specific composition of syngas (volume fraction, wet basis) is: H 2 : 64.00, CH 4 : 14.30, CO: 20.10, CO 2 : 0.90, N 2 : 0.50, H 2 O: 0.30. The raw material gas is divided into three streams according to 0.32, 0.21, and 0.47 and enters the first, second, and third methanation reactors respectively. The first stream is heated and mixed with superheated steam (temperature 260°C), and then enters the first methanation reaction In the container, the methanation reaction is carried out. The gas (temperature 650°C) reacted in the first methanation reactor enters the waste pot for cooling and by-product steam, and then the outlet gas of the first methanation reactor is divided into two streams according to the ratio of 0.6 and 0.4 and ...

Embodiment 3

[0025] According to this embodiment image 3 Process flow shown, pressure 3.5MPa, 100000Nm 3 / h of synthesis gas and the total sulfur in the synthesis gas is less than 0.1ppm, f=(n H2 -n CO2 ) / (n CO +n CO2 )=3.005, the specific composition of syngas (volume fraction, wet basis) is: H 2 : 64.00, CH 4 : 14.30, CO: 20.10, CO 2 : 0.90,N 2 : 0.50, H 2 O: 0.30. The raw material gas is divided into three streams according to 0.32, 0.21, and 0.47 and enters the first, second, and third methanation reactors respectively. The first stream is heated and mixed with superheated steam (temperature 260°C), and then enters the first methanation reaction In the container, the methanation reaction is carried out. The gas (temperature 650°C) reacted in the first methanation reactor enters the waste pot for cooling and by-product steam, and then the outlet gas of the first methanation reactor is divided into two streams according to the ratio of 0.6 and 0.4 and enters the second , The ...

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Abstract

The invention belongs to the chemical engineering field, and specifically relates to a coal syngas circulation gas free methanation technology. The technology firstly divides a methanation reactor into two parts, the purified raw material gas is divided into a plurality of gas flows, then the gas flows is introduced into the front methanation reactor, wherein parts of the front methanation reactor are connected through a combination mode of serial connection and parallel connection; the gas in the each level of methanation reactors in the front part goes out from the outlet of the first reactor and the outlet is serially connected to other level methanation reactors, or the gas is divided into a plurality of gas flows and enters other level reactors which are connected through a combination mode of serial connection and parallel connection. The technology adopts water steam as the diluting gas for diluting the raw material gas in a methanation reactor, the water steam is mainly applied to the high temperature methanation reaction technology, the pressure of the by-product namely steam is larger than the methanation reaction pressure, and thus the steam can be directly added into the raw material gas in a methanation reactor. The technology does not need a circulation gas compressor, so the production cost is reduced. Because the methanation reaction is a strong heat dissipation reaction, the added water stream is reduced so as to improve the energy utilization rate.

Description

technical field [0001] The invention belongs to the field of chemical industry, and relates to a method for a methanation process of a gas rich in H2, CO and CO2, in particular to a methanation process of coal-based synthesis gas without circulating gas. Background technique [0002] Coal is the main source of fossil energy in my country, and the reserves of coal are extremely rich. The proven reserves are as high as 1.28 trillion tons. Oil and natural gas resources are relatively scarce, and the domestic oil and gas production is far from meeting the needs of the rapid development of the national economy. We must rely on a large amount of imports to support the development of our country's economy. my country's import of crude oil has increased from 70 million tons in 2000 to 250 million tons in 2011, and its dependence on foreign oil imports reached 55.2% in 2012. In 2009, my country's natural gas production was 830×10 8 N m 3 , an increase of 7.7% compared with 2008. ...

Claims

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Application Information

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Patent Type & Authority Patents(China)
IPC IPC(8): C10L3/08
Inventor 宋鹏飞杨宽辉姚辉超刘玉成侯建国何洋王秀林冯雅晨高振李敬穆祥宇郑珩张瑜张新波
Owner CNOOC GAS & POWER GRP