A process for catalytic conversion of low value hydrocarbon streams to light olefins
A technology of light olefins and catalysts, applied in the field of catalytic cracking of hydrocarbon raw materials, can solve problems such as unfavorable production of light olefins
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Embodiment 1
[0087] This example illustrates the concept of thermoneutrality by combining endothermic cracking of light coker naphtha (LCN) with exothermic cracking of methanol by hydrothermally inactivated ZSM-5 additive, utilizing catalyst regeneration. The physicochemical properties of fresh ZSM-5 additives are listed in Table 2.
[0088] Table 2 Physicochemical properties of ZSM-5 zeolite-based catalysts
[0089]
ZSM-5 based catalyst
total surface area, m 2 / g
140
Total zeolite surface area, m 2 / g
110
Chemical analysis, weight %
al 2 o 3
18.70
Na 2 o
0.11
P 2 o 5
11.98
ABD, g / cc
0.75
Abrasion Index (ASTM)
3.12
Particle size distribution, wt%
-40 microns
6
-60
28
-80
53
-100
72
APS
77
[0090] Using 100% steam, the above-mentioned ZSM-5 additive can be hydrothermally deactivated for 20 hours at ...
Embodiment 2
[0098] This example further illustrates the endothermic cracking of LCN with heavy feedstocks such as purified oil slurry (CSO ) combined with cracking to obtain thermoneutrality. CSO is a product from the cracking of vacuum gas oil to FCC units. In this experiment, the ZSM-5 additives mentioned in Table 2 were used. In addition, the physicochemical properties of the FCC catalysts used in this experiment are shown in Table 5.
[0099] Table 5 Physicochemical properties of fresh FCC catalysts
[0100]
FCC catalyst
total surface area, m 2 / g
336
Total zeolite surface area, m 2 / g
226
Pore volume, cc / g
0.35
[0101] ABD, g / cc
0.78
Chemical analysis, weight %
al 2 o 3
29.37
Na 2 o
0.28
Re 2 o 3
0.85
Particle size distribution, wt%
-40 microns
4
-80
67
APS
70
Abrasion Index (ASTM)
2.52
...
Embodiment 3
[0109] This example illustrates the concept of sequential cracking of feedstocks based on their cracking capabilities. LCN and n-hexane feedstocks were cracked separately in a fixed fluidized bed microreactor in the presence of a ZSM-5 zeolite based catalyst as described in Example 1 and at different reactor temperatures. The yield structures are listed in Table 8. As shown in Table 8, when light coker naphtha (LCN) and n-hexane were simultaneously cracked under the same conditions at 620 °C, LCN cracking produced high yields of propylene and ethylene and low yields of coke and dry gas, While under the same conditions, n-hexane cracking produces low yields of propylene and ethylene. For low-cracking n-hexane, increasing the cracking degree (reaction temperature of 675°C) can increase the yield of propylene and ethylene, while for easy-cracking LCN, compared with the increase of light olefin yield, it mainly increases Yields of undesired products such as dry gas and coke. Th...
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