Hydrogen production from coking dry gas

Our factory has no requirements for the ratio of methane and ethane in the dry gas. As for whether the carbon-to-hydrogen ratio you mentioned refers to the hydrogen distribution before entering the hydrogenation reactor, the desulfurization hydrogen distribution changes with the properties of the raw materials. When the total sulfur of the feed gas is less than 200×10-6, a hydrogen distribution of more than 300Nm3 can ensure that the sulfur content after desulfurization is less than 0.5×10-6. However, when the processing capacity is not very large and the load of the reactor and hydrogen compressor allows, appropriately increasing the amount of hydrogen distribution (that is, increasing the hydrogen partial pressure) is beneficial to desulfurization. It can also make up for the heat dissipation loss and gas bias caused by too low linear speed. However, the amount of hydrogen distribution cannot be increased too much, because too much hydrogen distribution will cause the linear velocity in the reactor to be too high, which will reduce the reaction timing, which is detrimental to desulfurization. It will also increase the erosion of multiple catalysts and the energy consumption of hydrogen distribution.

Thank you for your explanation. It seems that I have caught some ideas. It seems that the main thing is to adjust the process parameters and then consider the specific operations.

The gas produced by delayed coking (the yield is about 7% to 9%) contains about 10% hydrogen, about 50% CH4 and more than 20% C2, C3, C4 alkanes and other ideal hydrogen production raw materials. The process practice of using the gas produced by the delayed coking unit to produce hydrogen shows that: ①Compared with using light oil as raw material, using the coked rich gas by-product of the delayed coking unit as raw material can significantly reduce the cost of hydrogen, but impurities such as olefins and organic sulfur in the coked rich gas must be properly treated. ②The coking rich gas pretreatment process of absorbing coked gasoline, coking diesel and then absorbing amine desulfurization-hydrogenation-ZnO desulfurization has been proved to be technically feasible and economically reasonable through industrial operation. ③The hydrogenation catalyst JT-G developed by Northwest Chemical Industry Research Institute has good olefin saturation and organic sulfur hydrogenation conversion capabilities under the conditions of low pressure, low temperature, and low hydrogen-to-oil ratio. Generally, hydrogen distribution is between 5% and 10%. As mentioned on the second floor, hydrogen distribution has many benefits. However, it increases the device load under the same hydrogen production. Secondly, the hydrogen distribution does not participate in the conversion reaction and does not absorb heat, which can easily cause the reformer to overheat.

Thanks for this information:handshake.

Thank you, this information is very helpful to me.