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Synthesis gas production method to replace natural gas
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A technology to replace natural gas and synthesis gas, applied in gas fuel, petroleum industry, fuel and other directions, can solve the problems of high energy consumption of compressor, short catalyst life, large amount of circulating gas, etc.
Active Publication Date: 2016-08-17
CHINA PETROLEUM & CHEM CORP +1
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Problems solved by technology
[0012] The technical problem to be solved by the present invention is that the prior art has the problems of large amount of high-temperature methanation reaction cycle gas, high compressor energy consumption and short catalyst life, and provides a new method for producing synthetic gas instead of natural gas
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Embodiment 1
[0029] 1 billion Nm 3 / year synthetic gas to replace natural gas plant (8000 operating hours per year), using figure 1 The high-temperature methanation is divided into two stages, and each stage of reactor is divided into two stages of catalyst beds, and the methanation reactor is filled with Ni-based catalysts (including Al 2 o 3 Carrier 60%, nickel 35%), the composition of raw syngas 1 is: (H 2 -3CO) / CO 2 =4, pressure 3.5MPa, feed volume 500,000 Nm 3 / h, divided into two parts, the ratio of primary syngas 2 and secondary syngas 3 is 1:1.5, primary syngas 2 is divided into two streams, and the volume ratio of stream 4 and stream 5 is X 1 : X 2 = 1:1, stream 6 mixed with stream 4 and recycle gas 12 enters the first stage of the first-stage high-temperature methanation reactor 101 at a temperature of 300°C to undergo methanation reaction, the volume ratio of recycle gas 12 and first-stage synthesis gas 2 Vn':W 1 =2.4:1, the outlet gas temperature of the first stage of re...
Embodiment 2
[0032] Same as [Example 1], except that the inlet temperature of the first-stage high-temperature methanation reactor is 320°C, the pressure is 4.5MPa, the reaction outlet temperature is 680°C, the inlet temperature of the second-stage high-temperature methanation reactor is 340°C, the outlet temperature is 700°C, and the pressure is 4.2 MPa , the volume ratio of material 12 to material 11 is 1.5, and the volume ratio Vn':W of cycle gas 12 and a section of synthesis gas 2 1 =2:1, the volume ratio of material 12 to material 11 is 1.4.
[0033] The volume content of each component of natural gas produced by the device is: CH 4 95%, H 2 0.8%, CO 2 2.5%, N 2 1.7%, high-temperature methanation reaction CO conversion rate is 74%, compressor energy consumption is 1700KW, catalyst life is 3.5 years.
Embodiment 3
[0035] With [embodiment 1], only raw material synthesis gas 1 is formed into: (H 2 -3CO) / CO 2 =3.95, the volume ratio of stream 4 and stream 5 X 1 : X 2 = 1:1.5, volume ratio X of stream 8 and stream 9 1 ’ : X 2 ’ = 1:1.15, the volume ratio of material 12 and material 11 is 1.5.
[0036] The volume content of each component of natural gas produced by the device is: CH 4 95.8%, H 2 0.7%, CO 2 1.8%, N 2 1.7%, the high-temperature methanation reaction CO conversion rate is 75%, the compressor energy consumption is 2000KW, and the catalyst life is 4 years.
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Abstract
The invention relates to a method of producing substitute natural gas from synthesis gas, mainly solving problems, namely large using amount of recycle gas, high energy consumption of compressors and short service lifetime of catalysts, of high-temperature methanation reactions in the prior art. According to the technical scheme adopted by the method, the method comprises: a) a step of providing a high-temperature methanation reaction zone including n-stage series-connected reactors, wherein the n is not less than 2, each reactor is divided into m sections of catalyst layers and the m is not less than 2; b) a step of dividing the synthesis gas raw materials into n sections and respectively feeding the n sections of the synthesis gas raw materials into inlets of the reactors at all stages in the high-temperature methanation reaction zone, wherein each section of the synthesis gas raw materials that enters a reactor is then divided into m streams and the m streams respectively enter the corresponding catalyst layers; c) a step of allowing a stream flowing out of an outlet of each of the reactors except the reactor at the final stage to enter the first section of catalyst layer in the reactor at the next stage; and d) a step of shunting the stream Vn flowing out from the reactor at the final stage to obtain a part Vn', and circulating the stream Vn' after the Vn' is condensed to the inlet of the reactor at the first stage. By the technical scheme, the problems are solved well and the method can be used in industrial production of substitute natural gas from synthesis gas.
Description
technical field [0001] The present invention relates to a method for producing substitute natural gas (SNG) from synthesis gas. Background technique [0002] Natural gas is an efficient and clean energy that can make up for the increasingly scarce oil resources to a certain extent. However, in recent years, my country's natural gas demand has grown rapidly, and my country's natural gas reserves are relatively small. It is predicted that the demand for natural gas in China will reach 170-210 billion Nm in 2015 3 , while the natural gas production in the same period can only reach 140 billion Nm 3 , the gap between supply and demand is about 30 billion to 70 billion Nm 3 . In order to solve the contradiction between the supply and demand of natural gas in my country, other alternative ways must be sought. [0003] my country is rich in coal resources, so the methanation of synthetic gas from coal gasification to substitute natural gas (SNG) can effectively alleviate my co...
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