Non-steady state reactor and method for producing synthesis gas
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A reactor and synthesis gas technology, applied in gaseous fuel, petroleum industry, fuel, etc., can solve problems that affect process thermal efficiency, synthesis gas yield, high temperature hot zone, spontaneous combustion and explosion hazards, etc.
Active Publication Date: 2010-06-16
SYNFUELS CHINA TECH CO LTD
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However, there are insurmountable problems in this reactor: there is a high-temperature hot zone in the catalytic bed of the reactor, there is a risk of spontaneous combustion and explosion when the feed preheating temperature is high, the reactor is easy to extinguish, and the bed temperature is difficult to control, etc., so it is difficult to realize industrialization
Since the catalytic partial oxidation of methane on the nickel-based catalyst is divided into two steps: fast oxidation and slow reforming, it is difficult to avoid high-temperature hot spots in the reactor bed. (Catalytic partial oxidation usually adopts mixed feed of raw material gas and oxidant), and the feed cannot be preheated to a very high temperature in the heat storage section, which not only makes it difficult to control the temperature of the reactor bed, but also affects the thermal efficiency of the process and the synthesis gas recovery. Rate
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Embodiment 1
[0102] The present embodiment 1 and 2 are all in figure 1 In the shown reactor device, coal-based Fischer-Tropsch synthesis tail gas (TG) is used as raw material to produce synthesis gas, and the molar composition of the coal-based Fischer-Tropsch synthesis tail gas raw material is CH 4 25%, CO20%, H 2 30%, CO 2 20%, N 2 5%. The catalyst used in the reforming section of the reactor is a commercial steam reforming nickel catalyst; the heat storage section is filled with porcelain Raschig rings. Described reaction and result are as follows:
[0103] The intake flow rate of the raw material gas is 1000kmol / hr, the pressure is 25bar, and the temperature is 300°C; the optimal bypass feed ratio of the raw material gas is 0.38, that is, 62% of the raw material gas enters the combustion chamber through the burner along L11, and the other 38% of the raw material gas The gas enters the reactor from the bypass line L5 or L6 at the bottom of the reactor after being regulated by the f...
Embodiment 2
[0111] With coke oven gas (COG) as raw material, adopt the method identical with embodiment 1, carry out the synthetic gas experiment of regenerative autothermal reforming, result is as follows:
[0112] The composition of coke oven gas is CH 4 32%, CO 9%, H 2 52%, CO 2 3%, N 2 3.7%, O 2 0.3%, the feed flow rate is 1000kmol / hr, the optimal bypass feed ratio is 0.33; the oxygen feed flow rate is 190kmol / hr, and the feed O 2 / CH 4 is 0.59; bypass steam feed flow 600kmol / hr, H in the feed 2 O / CH 4 The ratio is 1.87.
[0113] The half-cycle time of the forced flow direction change in the reactor was 5 minutes.
[0114] After the reactor was started up, it took about 32 flow direction changes to reach a periodic steady state.
[0115] After the reactor reaches a periodic steady state, the fluctuating range of the outlet temperature of the feed preheating heat storage section is 984°C to 973°C, with an hourly average of 982°C; the fluctuating range of the outlet temperature...
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Abstract
The invention discloses a reactor device and method for producing synthesis gas by using gaseous hydrocarbon as a raw material for carrying out heat accumulating type self-heating conversion. The reactor mainly comprises a combustion chamber, a mixing chamber, two reforming sections and two heat accumulating sections. The feeding raw gas of the reactor is divided into two paths of gas, wherein one path of raw gas and oxygen gas enter the combustion chamber from a middle combustion nozzle to carry out heat generating reaction; and after the other path of raw gas is mixed with water vapor, the mixed gas laterally enters the reactor through a gas inlet at one end, the mixed gas carries out pre-reforming reaction in one reforming section after being preheated in one heat accumulating section,the gas after reaction is mixed with the high-temperature gas at the outlet of the combustion chamber, then the mixed gas enters the other reforming section to carry out reforming reaction, and products are discharged after being cooled by the other heat accumulating section. The reactor of the invention is matched with a flow direction switching valve capable of periodically changing the flow direction of the gas in the reactor, thus the purposes of preheating feed materials, carrying out reaction and cooling products in one reactor can be realized. The reactor of the invention can reduce the oxygen consumption in the process, improve the yield and the quality of the synthesis gas and improve the heat efficiency of the overall process.
Description
technical field [0001] The present invention relates to a device and method for producing synthesis gas; further, the synthesis gas production device includes a non-stationary reactor and supporting facilities; the synthesis gas production method uses gaseous hydrocarbons as raw materials, Production of synthesis gas by regenerative autothermal reforming under non-steady conditions. Background technique [0002] The gaseous hydrocarbon raw material involved in the present invention refers to a gas mixture whose main component is gaseous alkanes or olefins, such as natural gas, coke oven gas, refinery gas, Fischer-Tropsch synthesis tail gas, coal bed methane, etc. Generally, such gaseous hydrocarbon feedstocks can be converted into synthesis gas (a mixture of hydrogen and carbon monoxide) by catalytic steam reforming, non-catalytic partial oxidation, autothermal reforming, etc., and then produce liquid fuels or chemicals, synthetic methanol, synthetic ammonia , Production of...
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