5 replies to this topic

[chemicooool]

Our company has a NG based steam reformer for production of H2 and Co as our final utility products. The reformer is designed based on 98% CH4 in NG with reformer outlet temperature at 886degC. But the NG supplied to our company has 90% CH4 and rest are C2 C3 C4 components. The reformer outlet temperature is around 800. All parameters like pressure, inlet temperature and Steam to Carbon reatio are kept according to the design values. I wanted to know wheatear the outlet temperature should be less than designed value at 90% CH4 or it should be more than designed value.

[Bobby Strain]

Since the outlet is close to equilibrium values I expect that the temperature should remain essentially unchanged. You can monitor methane in the product gas as a guide.

 

Bobby

[P.K.Rao]

Since the feed gas composition is different than the design composition (containing lower methane), an increase in steam/carbon ratio may help. This may reduce coke deposit on catalyst in longer run.

[chemicooool]

@bobby
the methane composition or methane slip ,as it is commonly known as, is within the designed range of 3.5mol% in the reformed gas. Only H2/CO ratio as reduced. But the reformer evaluation carried out by our performance monitoring team, the outlet temp at our existing feeding condition and designed CH4 slip should be near about 880 degC. But the same CH4 slip obtained in our operation is at 800 degC. So I wanted to know if the increase in higher HCs in feed will give us designed methane slip at lower temp than the design outlet temp of 887 degc or not.

[chemicooool]

Thank u P K Rao but I m wondering that the CH4 slip in reformer outlet composition is obtained at much lower temp than designed value of 886 degC. Is the increase in higher HCs reason for this low temp?

[chemicooool]

Thank u P K Rao but I m wondering that the CH4 slip in reformer outlet composition is obtained at much lower temp than designed value of 886 degC. Is the increase in higher HCs reason for this low temp?