CIESC Journal ›› 2020, Vol. 71 ›› Issue (5): 2182-2189.doi: 10.11949/0438-1157.20191483

• Process system engineering • Previous Articles     Next Articles

Multi-objective optimization of co-processing of bio-oil and vacuum gas oil in FCC

Le WU(),Jing WANG,Yuqi WANG,Lan ZHENG   

  1. School of Chemical Engineering, Northwest University, Xi’an 710069, Shaanxi, China
  • Received:2019-12-06 Revised:2020-02-26 Online:2020-05-05 Published:2020-03-16
  • Contact: Le WU E-mail:lewu@nwu.edu.cn

Abstract:

As a potential energy source that can partially replace fossil fuels, biofuels have the advantages of green, renewable, and sulfur-free, but their production costs are generally higher. The co-processing of bio-oil and vacuum gas oil in a fluid catalytic cracker (FCC) can effectively reduce the investment cost of a bio-refinery and the production cost of bio-fuels by utilizing the existing equipment in a refinery. To obtain the optimal biomass raw material and bio-oil production technology, Eco-indicator 99 was used to quantify the environmental impacts of the co-processing process, and a multi-objective optimization model was proposed to simultaneously reduce the economic costs and the environmental impacts. The results showed that catalytic pyrolysis was superior to fast pyrolysis in both reducing economic costs and environmental impacts; the different optimal biomasses were obtained under different objectives; biomass cost accounted for the largest proportion of costs and environmental impacts. Therefore, when optimizing the co-processing process, the environmental impact of the process should be considered. Reducing the biomass consumption is the most effective way to reduce both the costs and environmental impacts of the co-processing process.

Key words: biomass, pyrolysis, vacuum gas oil, co-process, FCC, multi-objective optimization, optimal design

CLC Number: 

  • TQ 021.8

Fig.1

Superstructure of the co-processing process"

Table 1

Price and damage factor of biomass, utilities and by-product"

生物质价格/USD损害因子/pt
纸浆用木/t99.49183.614
工业剩余木/t103.5197.929
秸秆/t143.3438.56
草/t80.68110.97
电/(kW·h)0.070.06486
水/t0.0650.050054
氢气/t1495246.71
生物气/m30.16920.017429

Table 2

Yields of pyrolysis processes/%"

生物质快速热解催化热解

生物

质油

生物气生物焦

生物

质油

生物气生物焦
纸浆用木52.52621.5335312.5
工业剩余木43.312.72427.35215.3
秸秆5525.516.229.327.524
37252625.320.210.3

Table 3

Yields of FCC and HDT processes/%"

生物质油加氢FCC柴油加氢汽油加氢
脱氧生物质油66
汽油48.17.699.5
柴油2391.2

Fig.2

Feasible solutions for the co-processing process"

Fig.3

Mass balance of the co-processing system with minimum TAC(unit: t·h-1)"

Table 4

Cost and environmental impact composition of the operating scheme with minimum TAC"

项目费用/(MUSD·a-1环境影响/( Mpt·a-1)
合计52.14134.33
生物质72.36133.54
7.5269.68
0.000470.00036
氢气
催化剂9.44
生物气-60-6.18
投资费用99.23

Fig.4

Mass balance of the co-processing system with minimum EI and best compromise(unit: t·h-1)"

Table 5

Cost and environmental impact composition of the operating scheme with minimum TAC"

项目费用/(MUSD·a-1)环境影响/(Mpt·a-1)
合计64.8485.73
生物质90.9986.09
7.5269.68
0.000470.00036
氢气
催化剂11.41
生物气-71.16-7.33
投资费用113.32

Table 6

Effects of weight factor on the optimal biomass feedstock and pyrolysis technology"

权重因子最优生物质原料最优热解技术
0工业剩余木催化热解
0.1工业剩余木催化热解
0.2工业剩余木催化热解
0.3工业剩余木催化热解
0.4工业剩余木催化热解
0.5工业剩余木催化热解
0.6纸浆用木催化热解
0.7纸浆用木催化热解
0.8纸浆用木催化热解
0.9纸浆用木催化热解
1纸浆用木催化热解
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