Process for producing C2 and C3 hydrocarbons
A hydrocarbon stream and product stream technology, applied in the field of producing C2 and C3 hydrocarbons, can solve the problems of high severity, not controlling the total ratio of C3 and C4, and not describing hydrocracking equivalents, etc.
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[0108] In some particularly preferred embodiments,
[0109] Step b) further involves separating C5 from the first hydrocracked product stream for recycling back to the first hydrocracking of step a);
[0110] Step b) further provides a heavy hydrocarbon stream comprising C6+, and
[0111] Subjecting the heavy hydrocarbon stream resulting from step b) to a second hydrocracking in the presence of a second hydrocracking catalyst to produce a second hydrocracked product stream comprising BTX, wherein the second hydrocracking is more severe than the first hydrocracking Hydrogen cracking is more severe.
[0112] system
[0113] In a further aspect, the invention also relates to a process device suitable for carrying out the method of the invention, figure 1 An example of it is shown in . The present invention thus relates to systems for the production of C2 and C3 hydrocarbons, comprising
[0114] - a first hydrocracking unit (101) arranged for a first hydrocracking of a mixe...
Embodiment 1
[0132] A feed consisting of n-pentane was subjected to hydrocracking to determine the effect of hydrocracking conditions on product composition. The experiments were carried out in a 12 mm reactor with the catalyst bed located in the isothermal zone of the reactor heater. The catalysts used were 2 g of Pt on alumina (0.75 wt% Pt loading) and H-ZSM-5 (SiO 2 / Al 2 o 3 =80) mixture.
[0133] The feed stream is fed into the reactor. The feed stream entered the vaporizer zone prior to the reactor where it was vaporized at 280°C and mixed with hydrogen. The conditions used in these experiments were: WHSV=1 / hr, the pressure was 1379 kPa (200 psig) and the molar ratio H 2 / hydrocarbon is 3. The temperature of the isothermal zone in the reactor was varied between 375 and 450°C. The reactor effluent was sampled in the gas phase to an on-line gas chromatograph. Product analysis was performed hourly.
[0134] Table 1: Composition of Hydrocracking Product Effluent
[0135] ...
Embodiment 2
[0139] A feed consisting of n-paraffins was subjected to hydrocracking to determine the effect of hydrocarbon chain length on the degree of conversion. The experiments were carried out in a 12 mm reactor with the catalyst bed located in the isothermal zone of the reactor heater. The catalysts used were 2 g of Pt on alumina (0.75 wt% Pt loading) and H-ZSM-5 (SiO 2 / Al 2 o 3 =80) mixture.
[0140] The feed stream is fed into the reactor. The feed stream entered the vaporizer zone prior to the reactor where it was vaporized at 280°C and mixed with hydrogen. The conditions used in these experiments were: WHSV=1 / hr, the pressure was 1379 kPa (200 psig) and the molar ratio H 2 / hydrocarbon is 3. The temperature of the isothermal zone in the reactor was varied between 300 and 500°C. The reactor effluent was sampled in the gas phase to an on-line gas chromatograph. Product analysis was performed hourly.
[0141] Table 2: Single conversion of n-paraffins
[0142] Fe...
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