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Acta Chim. Slov. 2024, 71, 388–397
Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
DOI: 10.17344/acsi.2024.8714
Scientific paper
The Reusage of Different Wastes by Using the Multiple’s 
Effect Technique for Sustainable Gasoline Production
Anita Kovač Kralj
Faculty of Chemistry and Chemical Engineering, University of Maribor, Smetanova 17, Maribor, Slovenia
* Corresponding author: E-mail: anita.kovac@um.si 
+386 02 2294454 Fax: +386 02 2527 774
Received: 02-12-2024
Abstract
The unused garbage which is accumulating the landfills, such as raw materials, could be reused for synthetic gasoline 
production. This study presents the multiple’s effect technique, which is based on the reusage of different non, party 
and sorted municipal solid wastes (MSW), or biogas for syngas, converted into synthetic gasoline. The novelties of this 
technique include a basic multiple’s effect parameter (MU
W
), which present a level of waste sorting, an effect of oxygen 
inhibition into different wastes, a simplified mathematical model and simulation with an Aspen Plus
®
 simulator using the 
retrofitted methanol plan converted into the synthetic gasoline production. This technique includes a circular economy 
by using a circulated purified flue gas as raw material, co-products of hydrogen and water.
This technique was tested on an existing methanol process, replacing natural gas with different alternatives of wastes or 
biogas for the synthetic gasoline production. The best alternative was the sorted MSW , which could generate an addi-
tional profit of 4.8 MEUR/a, including the garbage and CO
2
 emission reductions of 0.106·10
6
 t/a and of 0.084 ·10
6
 t/a.
Keywords: Waste; biogas; gasoline production; multiple’s effect; circular economy
1. Introduction
Non-renewable petroleum resources could be re-
placed with gasification of sustainable resources, such as 
waste, intermediate raw materials, bio-waste, for gasoline 
or other synthetic fuels` production, using different cata-
lytic converters of Fischer-Tropsch (FT) synthesis, fixed-
bed reactors, plasma etc.
The Introduction includes in detail the literatures of 
the research of different synthetic production, such as gas-
oline and fuels, including the gasification technique. Lu et 
al. contributed the new research of the selective conversion 
of CO and H
2
 to gasoline products (iso-paraffin and ole-
fin), including the demonstrated effective H-USY zeolite 
supported nano-cobalt bifunctional catalysts for this cata-
lytic reaction, which are prepared by the novel physical 
sputtering process. Compared with H-Mor, H-Beta and 
other zeolite supported catalysts, the H-USY zeolite sup-
ported cobalt catalyst shows the clearest promotional ef-
fect on the activity of Fischer-Tropsch synthesis.
1
 Javed et 
al. presented new research of the high CO
2
 selectivity of 
Fe-based Fischer-Tropsch microcapsule catalysts for gaso-
line production. The novelties of this research were the in-
cluded Silicalite-1 shell turned the Fe/ZSM-5 core’s surface 
hydrophilicity to hydrophobicity, the hydrophobic nature 
of the silicalite-1 layer`s decreased water-gas shift reac-
tion’s kinetics, including CO
2
 selectivity, was decreased by 
suppressing the water-gas shift reaction activity. All zeolite 
supported Fe-based catalysts showed significantly high 
gasoline range hydrocarbons` selectivity (about 60%).
2
Li et al. presented the novelties of the HZSM-5/
MnAPO-11 composite and the catalytic synthesis of 
high-octane gasoline from syngas in flow-type fixed-bed 
reactors, including the highest gasoline yield. The 
HZSM-5/MnAPO-11 composite was prepared via hydro-
thermal synthesis, and the catalytic synthesis of high-oc-
tane gasoline from syngas was studied in flow-type fixed-
bed reactors. The HZSM-5/MnAPO-11 composite showed 
the highest gasoline yield and iso-paraffin selectivity, due 
to the presence of more mesopores and moderate acid 
sites.
3
 Lu and co-workers stated the study of the produc-
tion of gasoline-range hydrocarbons from nitro-
gen-rich syngas over an Mo/HZSM-5 bi-functional cata-
lyst in a bench-scale continuous stainless steel fixed-bed 
reactor with different reaction conditions. The reaction 
conditions, i.e., temperature, pressure and gas hourly space 
velocity, affected the hydrocarbon selectivity significantly. 

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
The novelties included that the nitrogen-rich syngas can 
be converted into gasoline-range hydrocarbon over Mo/
HZSM-5 in one step, and high nitrogen content in syngas 
was found to affect liquid hydrocarbon distribution.
4
Zhang et al. developed the upgrade of the Ni/ASA 
catalysts with various Ni contents, which were prepared 
successfully through a wet impregnation method for the 
gasoline-range hydrocarbons` production from the oli-
gomerization of olefins-rich bio-syngas. The studies of this 
research, which contained the catalytic performance, may 
be relevant to the balance between acid and nickel ion sites 
and fuels, and the high Ni loading amount of Ni/ASA may 
enhance the hydrogenation reaction of olefins.
5
 Liu and 
co-workers presented the novelties of the catalytic perfor-
mance with cobalt nanoparticles embedded into zeolite 
crystals for the direct synthesis of gasoline from syngas. 
The highlights of the research were series CoZ-xN cata-
lysts with a novel cobalt-embedded zeolite structure, the 
coincidence of the rate of silica dissolving and zeolite 
growth was important, and the formation mechanism was 
proposed of the catalyst.
6
Martin and Cirujano contributed the new research 
of the multifunctional heterogeneous catalysts for the tan-
dem CO
2
 hydrogenation Fischer-Tropsch synthesis of gas-
oline, including several iron-containing multifunctional 
catalysts based on metal oxides, carbon or zeolite materi-
als. The novelties of this research were the included advan-
tages of metal oxides, carbons or zeolites as support of the 
active Fe-catalyst, including Fe-support interactions, and 
the electronic and geometric properties of the active sites.
7 
Li et al. presented the new research of the conversion of 
dimethyl ether to gasoline, using a series of nanocrystal 
H[Fe,Al]ZSM-5 zeolite samples with different SiO
2
/Al
2
O
3
 
ratios with a hydrothermal method. The highlights con-
tained zeolite acidity, which was related with the synergis-
tic effect of Al- and Fe-based acid sites, and a catalyst with 
an SiO
2
/Al
2
O
3
 ratio of 45 exhibited the best catalytic per-
formance for a dimethyl ether to gasoline reaction.
8
 Su et 
al. developed the upgrade of the catalysts for dimethyl 
ether conversion to iso-paraffin-rich gasoline, including 
nanosized ZSM-5 (NZ5) and zinc isomorphously substi-
tuted ZSM-5 ([Zenial]NZ5) zeolites with different Si/Me 
ratios in initial gels (Me = Al or Al and Zn). The novelties 
contained iso-paraffin selectivity in gasoline hydrocar-
bons, which was enhanced by Zn incorporation, and 
ZnOH
+
 species showed the excellent hydrogenation activ-
ity for a dimethyl ether to gasoline reaction.
9
Magomedova et al. proposed the upgrade of the syn-
gas-to-gasoline technology for the synthesis of liquid hy-
drocarbons through oxygenates (methanol and dimethyl 
ether), giving a light synthetic oil with a low concentration 
of aromatic compounds (8–16 wt %). The study contained 
dimensionless criteria for heat and mass transfer, which 
were used for plant scaling, and the operation was carried 
out of a pilot plant for syngas to low-aromatic gasoline via 
DME.
10
 Szczygieł and Kułażyński contributed the research 
of the gasoline production from dimethyl ether and meth-
anol, including thermodynamic limitations of synthetic 
fuel production. Thermodynamic analysis of the classic 
methanol-to-gasoline process that employs CO as a raw 
material allowed a comparison with the modified version 
of the process, assessment of their effectiveness, and de-
ductions concerning the possible benefits and losses re-
sulting from replacing CO with carbon dioxide. The use of 
CO as a raw material was clearly more favourable in terms 
of the tendency towards a spontaneous reaction.
11
Rabah presented the upgrade of syngas production 
from  biomass gasification as a potential energy source 
for power generation and manufacturing synthetic gaso-
line and diesel via Fischer-Tropsch synthesis. The operat-
ing conditions under which the objective function and the 
constraint were satisfied were the steam to biomass ratio, 
equivalent ratio, and gasification temperature.
12
 Shiying et 
al. contributed the upgrade of the dual-stage entrained 
flow gasification and CO
2
 cycling in biomass-to-gasoline/
diesel, including design and techno-economic analysis. 
The dual-stage entrained flow gasification avoided sepa -
rate torrefaction of biomass feedstock and provided higher 
cold gas efficiency, which made the addition of steam as a 
gasification agent feasible. The high efficiency of Fe-based 
slurry-phase Fischer-Tropsch synthesis reactors also en-
hanced the gasoline production.
13
 Borugadda et al. ex-
plored the new research of the techno-economic and 
life-cycle assessment of the integrated Fischer-Tropsch 
process in the ethanol industry for bio-diesel and bio-gas-
oline production, using syngas obtained from the gasifica-
tion of dry distillers’ grain. The lab-scale experiment using 
pelletised promoted iron supported on Carbon Nano 
Tubes (Fe/CNT) was used to simulate a plant for the pro-
duction of 1000 kg of syncrude/h.
14
Mascal and Dutta presented the study of the synthe-
sis of highly-branched alkanes, such as iso-alkanes and 
cycloalkanes, for renewable gasoline production from bio-
oil and raw biomass using chemo-catalytic methods. Gas-
oline can be made from biomass pyrolysis gas via the Fis-
cher-Tropsch or methanol-to-gasoline processes, as well as 
the refining of bio-oil, raw biomass, etc.
15
 Hnich et al. in-
vestigated the study of the life cycle sustainability perfor-
mance of synthetic diesel and gasoline from Tunisian date 
palm waste, and compared it with that of conventional fos-
sil fuels. The potential environmental impacts of the bio-
mass-to-liquid system were concluded to be associated 
mainly with direct emissions and the system's demand for 
electricity and oxygen.
16
 Wang et al. designed the upgrade 
of the pilot plant for biomass converted to liquid fuels, in-
cluding gasification, direct synthesis of dimethyl ether 
(DME) and DME to gasoline. The operating results showed 
that both the pressure and gas hourly space velocity 
(GHSV) not only influenced the CO conversion and the 
DME yield, but also had a significant effect on the manip-
ulation of the reaction heat in the adiabatic reactor. High 
pressure and low GHSV favoured the high CO conversion 

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
and the DME yield.
17 
Navas-Anguita et al. presented the 
study of the simulation and life cycle assessment of a bio-
gas-to-liquid plant for the coproduction of synthetic fuels 
(diesel and gasoline) and electricity. The system comprised 
a biogas dry reforming process to produce syngas, Fis-
cher-Tropsch synthesis, and a combined-cycle process. In 
particular, the life-cycle environmental profile of synthetic 
biodiesel as the main product of the biogas-to-liquid plant 
was calculated, and compared with that of conventional 
diesel.
18
Bahri et al. presented the novelties of the synergistic 
effect of a bifunctional mesoporous ZSM-5 supported Fe-
Co catalyst for selective conversion of syngas with a low 
riblet ratio into synthetic fuel. The Fe-Co bimetallic active 
metals were loaded on mesoHZSM-5 with varying Fe-Co 
ratios, with a constant total metal loading of 30%, using 
the sonication process to increase active metal dispersion. 
The catalytic activity was tested in the laboratory scale 
fixed bed reactor.
19
 Aluha and Abatzoglou contributed the 
study of the synthetic fuels from 3-φ Fischer-Tropsch syn-
thesis using syngas feed and novel nanometric catalysts. 
The research presented the novel carbon-supported Co-Fe 
bimetallic catalysts which were synthesised through plas-
ma. All the catalysts reduced in CO or H
2
 showed equal 
activity of about 40% CO conversion.
20
 Ali et al. defined 
the new research of the direct synthesis of liquid fuels and 
aromatics from syngas using the Fischer-Tropsch synthe-
sis reaction on hybrid catalysts containing a highly ordered 
mesoporous FeZrOx bimetal oxide mixed physically with 
Mo-modified ferrierite (Mo/HFER). The hybride FeZ-
rOx-Mo/HFER catalyst showed synergistic effects with a 
higher CO conversion to liquid fuels and aromatics. Opti-
mal hydrophobicity and acidic sites on the Mo/HFER were 
responsible for the enhanced catalytic stability.
21
Selvatico et al. obtained the upgrade of the kinetic 
model, based on Langmuir–Hinshelwood–Hougen–Wat-
son for the Fischer-Tropsch synthesis of fuel, converting it 
into a well-established industrial process simulator. A low 
temperature Fischer-Tropsch process was modelled for the 
middle distillate production.
22 
Wu et al. reported the nov-
elties of the reformation of n-pentane (C
5
H
12
) using meth-
ane (CH
4
) or carbon dioxide (CO
2
) in a temperature-con-
trolled dielectric barrier discharge reactor to produce 
hydrogen and clean carbon-based fuels, by using low-tem-
perature plasma. A mechanistic study suggested that elec-
tron-induced chemistry dominates C
5
H
12
 and the added 
gas conversion, whereas the thermochemistry controls the 
product distribution.
23 
Liu and Larson described the study 
of two routes to produce liquid hydrocarbon fuels from 
solids via synthesis gas, Fischer-Tropsch (FT) synthesis 
and methanol-to-gasoline (MTG). This study compared 
the performance and cost of the Fischer-Tropsch and 
MTG processes on a self-consistent basis. In particular, FT 
and MTG production from coal and coal/biomass co-
feeds were compared, including detailed mass, energy and 
carbon balances.
24 
Dutta et al. provided the new research 
of an overview of producing fuel precursors from biomass 
components, and their catalytic transformation into avia-
tion-, diesel-, and gasoline-range hydrocarbon fuels 
(HCFs), including strategic applications of various organic 
transformations for the molecular design. Emphasis was 
also given to the process conditions and details of the cat-
alysts employed in these processes. The synthesis of HCFs 
was warranted to ensure the high quality and homogeneity 
of the properties, including minimizing the energy in-
put.
25
Santos and Alencar presented the upgrade of the 
syngas production from biomass gasification and its sub-
sequent conversion into fuels through the Fischer-Tropsch 
synthesis. This study included a debate on the main cata-
lysts, industrial process requirements, and chemical reac-
tion kinetics and mechanisms of Fischer-Tropsch synthe-
sis. Lignocellulosic material of biomass would be 
considered a low-cost feedstock to the liquid biofuel pro-
duction on a large scale.
26
 Campanario and Ortiz contrib-
uted the upgrade of the Fischer-Tropsch biofuels` produc-
tion from syngas obtained by supercritical water reforming 
of the bio-oil aqueous phase, including the produced max-
imum biofuels and electrical power. The highlights of this 
research contained the upgraded production of syngas by 
using water-gas-shift, dry reforming and Fischer-Tropsch 
(FT) reactors, and followed the optimal conditions in the 
FT reactor: 220 °C, 40 bar and H
2
/CO ratio of 1.70.
27
Gharibi et al. contributed the study of the meta-
heuristic particle swarm optimization for enhancing ener-
getic and exergetic performances of hydrogen energy pro-
duction from plastic waste gasification. The novelties 
contained were multi-objective particle swarm optimiza-
tion for plastic gasification, using grey relational analysis, 
and achieving lower heating for the polypropylene gasifi-
cation and higher efficiency of cold gas.
28 
Gharibi et al. 
prepared a few novel studies to predict polyethylene waste 
performance in gasification using multilayer perceptron 
(MLP) machine learning algorithms and interpreting 
them using multi-criteria decision-making methods. The 
main aims of this study were to develop MLP artificial 
neural networks and regression models to predict polyeth-
ylene gasification performance with high accuracy.
29 
Mo-
javer et al. prepared the novel thermodynamic assessment 
of an integrated solid oxide fuel cell with a steam biomass 
gasification and high-temperature sodium heat pipes for 
combined heating and power production. The modelling 
and analysis of the system were performed using mass and 
energy conservation laws and equilibrium constants. The 
results of the extended model were confirmed by the ex-
perimental results.
30 
Mojaver et al. defined the multi-ob-
jective optimization using response surface methodology 
and exergy analysis of a novel integrated biomass gasifica-
tion, solid oxide fuel cell and high-temperature sodium 
heat pipe system. Response surface methodology was uti-
lised to investigate the effect of the decision variables on 
the responses, i.e., the electrical power and the exergy effi-

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ciency.
31 
Hasanzadeh and Azdast defined the novel ma-
chine learning utilisation on air gasification of polyethyl-
ene terephthalate waste. The machine learning algorithms 
had good performance in predicting the performance. The 
models for lower heating values and cold gas efficiency 
showed excellent accuracy.
32 
Doniavi et al. improved the 
efficiency of polyethylene gasification. This research was 
focused on the energy, exergy, and environmental impact 
in relation to the material conditions. These models were 
then optimised using a general algebraic modelling sys-
tem. The results indicated that the ideal conditions consist 
of 84.40 % carbon content, 15 % hydrogen content, and no 
oxygen or nitrogen content.
33
Hasanzadeh and Abdalrahman defined a novel re-
search, in which it was recognised that the processing pa-
rameters have a crucial impact on the assessment of poly-
vinyl chloride waste gasification. The study used data 
collected through a validated thermodynamic model, and 
three different regression models were tested and com-
pared in detail. Cold gas efficiency and normalised carbon 
dioxide emission were predicted using linear, quadratic, 
and quadratic with interaction algorithms.
34
 Khalilarya et 
al. contributed a new research, which combined a heat and 
power system which consisted of a gasifier, a micro gas 
turbine, an organic Rankine cycle, a heat exchanger and 
domestic heat recovery. Air, steam, and oxygen were con-
sidered as different gasification mediums. The Taguchi ap -
proach was employed to optimise the generated power in 
the air, steam and oxygen medium cases.
35
 Mojaver et al. 
researched the novel system of a fluidised bed gasifier with 
steam as the gasifying agent. The synthesis of gas composi-
tion and efficiencies of the system were investigated with 
respect to different biomasses considered as gasification 
fuels. The results indicated that the molar fractions of hy-
drogen and carbon dioxide were increased, and the molar 
fraction of carbon monoxide was reduced with the steam 
to biomass ratio.
36
Hasanzadeh et al. improved the gasification model of 
polyethylene waste, by using the Gibbs free energy mini-
misation and Lagrange method of undetermined multipli-
ers. A central composite design was employed, to assess 
and optimise the polyethylene waste gasification. The find -
ings revealed that hydrogen production was improved sig-
nificantly by 48% by raising the steam to polyethylene 
waste ratio according to the water–gas shift and reforming 
reactions.
37
 Mojaver et al. compared the performances be-
tween biomass and plastic waste gasification. The impor -
tant novelty and contribution of this study was the analyt-
ical hierarchy process/technique for order performance by 
similarity to the ideal solution coupled method that was 
employed in gasification of conventional biomass and 
plastic waste, to prioritise the considered criteria and to 
select the best feedstock for gasification.
38
 Mojaver et al. 
presented a new study, in which the steam gasification was 
modelled of polyethylene, polypropylene, polycarbonate 
and polyethylene terephthalate waste. The effects of key 
features, including the steam to plastic waste ratio, temper-
ature, moisture content and pressure, were assessed on hy-
drogen-rich syngas compositions, and the exergy destruc-
tion rate. The Taguchi approach was utilised to investigate 
and optimise the process. The findings revealed that the 
gasification of polypropylene waste led to the highest hy-
drogen production at all the processing conditions.
39
In this study, the gaps in the literature were covered 
about the usage of the different wastes for syngas, and fur-
ther into sustainable synthetic gasoline productions. The 
novelties of this study present the multiple’s effect tech-
nique, which uses the basic multiple’s effect parameter 
(MU
W
) for the different level of waste sorting, including 
the effect of oxygen inhibition into different wastes. The 
contributions of this research include the circular econo-
my by using a simple mathematical model for different 
municipal solid wastes (MSW) from non-sorted to sorted, 
or biogas. The objectives of this study contain the applied 
composition data of different wastes and the simulation 
model by using the Aspen Plus
® 
simulator.
2. The Multiple’s Effect Technique
The nature source, such as petroleum, would be re-
placed by the non-sorted (WNS), partially sorted (WPS), 
or sorted (WS) wastes from landfill or biogas for the sus-
tainable synthetic gasoline production, by using the multi-
ple’s effect technique. This study presents the multiple’s ef-
fect technique, which is based on the reusage of different 
MSW or biogas, supported by a mathematical model and 
the Aspen Plus
®
 simulator for syngas converted into syn-
thetic gasoline. This technique adapts the replacement of 
the existing methanol process to synthetic gasoline pro-
duction, by using the same process units. The simple 
mathematical model uses the basic multiple’ s effect param-
eter (MU
W
), which presents the level of waste sorting 
(MU
W
; MU
WNS
 = 0; MU
WPS
 = 1; MU
WS
 = 2). The sorted 
wastes include the highest value of the multiple’s effect pa-
rameter. The multiple’s effect parameter allows easy calcu-
lation of the product’s production and other important 
amounts from different wastes, including the sustainable 
co-produced raw materials, such as water, hydrogen and 
flue gas.
The synthetic gasoline would be produced from the 
different MSW by using the basic process units (Fig.1), 
which are very similar to methanol production, such as 
gasification of MSW (G-MSW), reforming (Ref), cooling 
(Coo), the first water removing (Rem1-H
2
O), compressing 
(Com), preheating to the reaction’s temperature (PreH-R), 
reacting (R), the first crude product cooling (Coo1-SG), 
the second water removing (Rem2-H
2
O), the second 
crude product cooling (Coo2-SG), the liquid product’s pu-
rification (P-SG), and hydrogen separation from nonreact-
ed gas with a pressure swing adsorption column (PSA-H
2
). 
The adapted process units include the optimal parameters, 

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
effects and characteristics (Fig. 1). MSW should be gassed 
before reforming (G-MSW). The flue gas of gasification, 
such as raw material, would be purified and circulated into 
reforming (Cir-FG).
Different municipal solid wastes (MSW) would be 
converted into syngas by using combustion, gasification 
and reforming. The purified flue gas of combustion (with -
out particles, NO
x
, SO
x
, oxygen and
 
nitrogen), including 
steam and carbon dioxide, is transported circularly into 
the gasification-reforming part, without releasing the out-
let exhaust into the atmosphere. The purified flue gas is 
used as sustainable raw material, which would reduce the 
emissions and amount of clean steam. The different MSW 
are presented with the basic components of C, H
2
, O
2
 and 
N
2
. The non-sorted MSW include lower plastics and 
woods (as components of C and H
2
), because
 
of a higher 
content of rubbers, leathers, textiles, papers, etc (as com-
ponents of O
2
 and N
2
, too). The sorted MSW includes 
more plastics and woods because
 
of the lower content of 
rubbers, leathers, textiles, paper, etc. The carbon and hy-
drogen (F
C,W
, F
H2,W
) are affected mostly by the reactions. 
The amount of oxygen is reducing the production of the 
synthetic gasoline and the neutral nitrogen is filling the 
process flows. The purified and circulated flue gas contains 
the components of CO
2
 and H
2
O, representing a circular 
economy system.
The basic simplified endothermic reaction of Re1 
takes place into the reformer (Ref), which is producing 
syngas with a yield of carbon monoxide (Y
CO,Re1
 = 0.999) 
mostly from the waste's carbon. The circulated carbon di-
oxide from the flue gas (FG) is converted to carbon mon-
oxide with 80% conversion of Re2 reaction (X
FG,CO,Re2
 = 
0.8), and the remaining 20% (or (1 – X
FG,CO,Re2
)) flows into 
the product’s reactor (R).
C + H
2 
+ H
2
O I CO + H
2
 + H
2
O (Re1)
CO
2 
+ H
2
 I CO + H
2
O (Re2)
The syngas converts to the synthetic gasoline (SG) 
from wastes into the reactor (R) by using two basic exo-
thermic reactions (Re3, Re4) with the conversions of CO 
and CO
2 
(X
CO,Re3
 = 0.996, X
CO2,Re4
 = 0.56).
8 CO + 17 H
2 
 I C
8
H
18 
+ 8 H
2
O (Re3)
8 CO
2 
+ 25 H
2 
 I C
8
H
18 
+ 16 H
2
O (Re4)
The carbon molar flow rates (F
C,W
) of different 
wastes (non-sorted, WNS or partially-sorted, WPS, or 
sorted, WS; W = WNS,WPS,WS) are dependent on the 
lowest inlet (F
C,WNS
 = 600 kmol/h) and the difference in 
carbon amounts (ΔF
C
 = 100 kmol/h), including the multi-
Figure 1: The process flow-diagram of the synthetic gasoline production for the different wastes including the parameters.
Figure 2: Flow-diagram of the graphical presentation the carbon 
molar flow rates (F
C,W
) for different wastes by using the multiple’s 
effect technique.

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
ple’s effect parameter (MU
W
; MU
WNS
 = 0; MU
WPS
 = 1; 
MU
WS
 = 2; Eq. 1).
F
C,W
 = F
C,WNS 
+ ΔF
C 
·
 
MU
W
W = WNS, WPS, WS 
(1)
The carbon molar flow rates (F
C,W
) of different 
wastes can be presented graphically by using the multiple’s 
effect technique (Fig. 2).
The reacted synthesised gasoline molar flow rate 
(
r
F
SG,W
; Eq. 4) into reactor (R) from different wastes is de-
pendent on the reactions (Re1 and Re3) of CO reacting 
(
r
F
SG,Re3,W
;
 
Eq. 2) and the circulated CO
2
 molar flow rate 
from the flue gas (F
FG,CO2
 = 240 kmol/h), which takes 
place at the reactions (Re2 and Re3) of CO and CO
2, 
react-
ing for using the reaction of Re4 (
r
F
SG,FG
; Eq. 3), including 
eight gasoline’s molecules (M = 8).
r
F
SG,Re3,W
 = (F
C,W 
· Y
CO,Re1
 · X
CO,Re3
)
 
/M
W = WNS, WPS, WS 
(2)
r
F
SG,FG
 = [(F
FG,CO2 
· X
FG,CO,Re2
 · X
CO,Re3
) + 
(F
FG,CO2 
· (1 – X
FG,CO,Re2
) · X
CO2,Re4
)]/M (3)
      
r
F
SG,W
 = (
r
F
SG,Re3,W 
+ 
r
F
SG,FG
)
W = WNS, WPS, WS 
(4)
The reacted synthesised gasoline (
r
F
SG,W
) is lost be-
cause of the oxygen in the non-sorted waste and the prod-
uct’s cleaning (P-SG) by 4% (Eq. 5; L
P-SG,W
 = 0.04). The 
oxygen in the non-sorted waste acts as an inhibitor, with 
the different losses dependent on the sorting levels 
(L
O2,WNS
 = 0.1, L
O2,WPS
 = 0.05, L
O2,WS
 = 0.0). The total pro-
duced synthesised gasoline (F
SG,W
) can be calculated by 
using Equation 5.
F
SG,W
 = 
r
F
SG,W
 · (1 – L
P-SG,W
)
 
· (1 – L
O2,W
)
W = WNS, WPS, WS 
(5)
The hydrogen molar flow rate (F
H2,W
; Eq. 6) of dif-
ferent wastes, such as coproduct, separates from nonre-
acted gas using the pressure swing adsorption column 
(PSA-H
2
), which is calculated dependent on the lowest 
inlet (F
H2,WNS
 = 1600 kmol/h), the difference of the inlet 
(ΔF
H2,W
 = 100 kmol/h), the lowest reacted amount (
r
F-
H2,WNS
 = 1334 kmol/h) and the reacted difference of the 
hydrogen amount (Δ
r
F
H2
 = 87 kmol/h), including the 
multiple’s effect parameter (MU
W
; MU
WNS
 = 0; MU
WPS
 = 
1; MU
WS
 = 2).
F
H2,W
 = (F
H2,WNS 
+
 
ΔF
H2 
·
 
MU
W
) – 
(
r
F
H2,WNS
 + Δ
r
F
H2 
·
 
MU
W
)
   
W = WNS, WPS, WS 
(6)
The produced water molar flow rate (F
H2O,W
; Eq. 7) 
through the plant is determined with the lowest produced 
(F
H2O,WNS
 = 815 kmol/h) and difference (ΔF
H2O
 = 97 
kmol/h) amounts, including the multiple’s effect parame-
ter (MU
W
; MU
WNS
 = 0; MU
WPS
 = 1; MU
WS
 = 2).
F
H2O,W
 = F
H2O,WNS 
+ ΔF
H2O 
·
 
MU
W
W = WNS, WPS, WS 
(7)
The Re1 reaction needs the inlet steam molar flow 
rate (F
H2O,Re1,W
; Eq. 8) deriving from the flue gas, which is 
dependent on the lowest (F
H2O,re1,WNS
 = 350 kmol/h) and 
difference (ΔF
H2O,Re1
 = 100 kmol/h) amounts, including 
the multiple’ s effect parameter (MU
W
; MU
WNS
 = 0; MU
WPS
 
= 1; MU
WS
 = 2).
F
H2O,Re1,W
 = F
H2O,Re1,WNS 
+ ΔF
H2O,Re1
 · MU
W
W = WNS, WPS, WS 
(8)
The simplified energy analysis includes the needed 
energy of gasification (ϕ
G
 = 25 MW), which is the same for 
all wastes, and reforming (ϕ
ref,W
; Eq. 9), including the 
available energy of the product’s reactor (ϕ
R,W
; Eq. 10). The 
endothermal heat flow rate of the reformer (ϕ
ref,W
; Eq. 9) 
expresses with the lowest (ϕ
ref,WNS
 = 24 MW) and differ-
ence (Δϕ
ref
 = 3.7 MW) of the heat flow rates, including the 
multiple’s effect parameter (MU
W
; MU
WNS
 = 0; MU
WPS
 = 
1; MU
WS
 = 2).
ϕ
ref,W
 = ϕ
ref,WNS 
+ Δϕ
ref 
·
 
MU
W
W = WNS, WPS, WS 
(9)
The exothermal heat flow rate of the product’s reac-
tor (ϕ
R,W
; Eq. 10) is dependent on the lowest (ϕ
R,WNS
 = 37 
MW) and difference (Δϕ
R
 = 4.3 MW) of the heat flow 
rates, including the multiple’s effect parameter (MU
W
; 
MU
WNS
 = 0; MU
WPS
 = 1; MU
WS
 = 2).
Φ
R,W
 = ϕ
R,WNS 
+ Δϕ
R 
·
 
MU
W
W = WNS, WPS, WS 
(10)
The objective function of the retrofit using different 
MSW (OBF
W
; Eq 11) maximises the additional profit. 
The additional income accounts for the product (InSG; 
with price of Co
SG
 = 10 EUR/kmol) and co-product pur-
chases (InH2; with price of Co
H2
 = 3 EUR/kmol). The 
same applied costs, independent of the wastes, include 
the cost of the retrofit (Cret = 5 MEUR/a, including a 
new catalyst), the cost of gasification (Cgas = 3 MEUR/a), 
and the cost of the circulated flue gas (CFG = 1 MEUR/a). 
The applied costs, dependent on the wastes, contain the 
cost of sorting (Csor,W; Eq. 12) and the cost of energy 
analysis (Cen,W; Eq. 13), using 8,000 operating hours 
(O) per year.
 OB F
W = In
SG + InH2− (Cret + Cgas + CFG) − 
(Csor,W + Cen,W) = F
SG,W
 · Co
SG
 · O + F
H2,W
 · Co
H2
 
· O − (C
ret 
+ C
gas
 + C
FG
) − (C
sor,W
 + C
en,W
)
W = WNS, WPS, WS (11)

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
The cost of sorting includes the constant (C
sor
 = 1 
MEUR/a) and variable parts, which is dependent on the 
difference (ΔC
sor
 = 0.4 MEUR/a) cost, including the multi-
ple’s effect parameter (MU
W
; MU
WNS
 = 0; MU
WPS
 = 1; 
MU
WS
 = 2).
C
sor,W
 = C
sor
 + ΔC
sor
 · MU
W
W = WNS, WPS, WS 
(12)
The cost of energy analysis determines the difference 
between endothermal (ϕ
ref,W
) and exothermal (Φ
R,W
) heat 
flow rates, temperatures into both units (T
ref
 = 800 °C and 
T
R
 = 300 °C) and the energy cost (Co
en
 = 100 EUR/(MW 
 
°C a).
C
en,W
 = ϕ
ref,W
 · T
ref
 · Co
en 
−
 
ϕ
R,W
 · T
R
 · Co
en
W = WNS, WPS, WS 
(13)
2. 1. The Multiple’s Effect Technique of Biogas
The simple mathematical model of biogas (BG) is 
even more simplified because of its not so different com-
position as the MSW, therefore, is not necessary use the 
multiple’s effect parameter. The biogas contents are mostly 
components of methane and carbon dioxide (F
CH4,BG
, 
F
CO2,BG
). The flow-diagram of synthetic gasoline produc-
tion from biogas is very similar to the flow-diagram from 
different wastes, only without the circulated flue gas and 
gasification, which is replaced with preheating biogas 
(preH-BG; Fig. 3). The basic reaction of Re5, producing 
syngas from biogas (as molar flow rates of F
CH4,BG
 and 
F
CO2,BG
) takes place during the reformer (Ref), with yields 
of the carbon monoxide from methane (Y
CO,Re5,BG
 = 0.7).
CH
4
 + H
2
O I CO + 3H
2
 (Re5)
The syngas converts to synthetic gasoline from bio-
gas into the reactor (R) by using two basic exothermic re-
actions (Re3, Re4), with the conversions of CO and CO
2 
(X
CO,Re3,BG
 = 0.996, X
CO2,Re4,BG
 = 0.56) .
The reacted synthesised gasoline molar flow rate 
(
r
F
SG,BG
; Eq. 16) from biogas (F
CH4,BG
 = 650 kmol/h and 
F
CO2,BG
 = 350 kmol/h) takes place during the reactions of 
Re3 (Eq. 14) and Re4 (Eq. 15).
r
F
SG,Re3,BG
 = (F
CH4,BG 
· Y
CO,Re5,BG 
· X
CO,Re3,BG
)/M (14)
r
F
SG,Re4,BG
 = (F
CO2,BG 
· X
CO2,Re4,BG
)/M (15)
r
F
SG,BG
 = 
r
F
SG,Re3,BG 
+
 r
F
SG,Re4,BG 
 (16)
The reacted synthesised gasoline (
r
F
SG,BG
) from bio-
gas is lost into the product’s purification unit (P-SG) by 4% 
(L
P-SG,BG
 = 0.04), therefore, the amount of produced syn-
thesised gasoline (F
SG,BG
) is lower (Eq. 17).
F
SG,BG
 = 
r
F
SG,BG
 · (1 – L
P-SG,BG
)
 
(17)
The other processed and energetic parameters are 
not so variable, mostly because of the constant composi-
tion of the biogas.
3. Case Study of The Multiple’s  
Effect Technique for the  
Different Wastes
The synthetic gasoline production of different mu-
nicipal solid wastes (MSW) has been tested by using the 
multiple’s effect technique, which was adapted from the 
existing methanol process for synthetic gasoline produc-
tion, because of very similar process units. The case study 
Figure 3: The process flow-diagram of the synthetic gasoline production for biogas including the parameters.

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Kovač Kralj:   The Reusage of Different Wastes by Using the Multiple’s   ...
of simulated synthetic gasoline production was undertak-
en using the optimal parameters, effects and characteris-
tics from Figure 1, by using the Aspen Plus
®
 simulation. 
The synthetic gasoline production
3
 from waste was simu-
lated by using the verified real thermodynamic method 
and rector model, such as Grayson and Requil from the 
Aspen Plus
®
 simulator. The economic analyses were in-
cluded the applied purchase and operation costs for the 
retrofit.
The total produced synthesised gasolines from 
non-sorted to sorted wastes were determined as the 
amounts of 87, 104 and 121 kmol/h (F
SG,WNS
, F
SG,WPS
, F
S-
G,WS
; Eqs 1–5). The coproduct of hydrogen molar flow 
rates were estimated as the amounts of 266, 279 and 292 
kmol/h (F
H2,WNS
, F
H2,WPS
, F
H2,WS
; Eq. 6).
The produced water molar flow rates were assessed 
as the amounts of 815, 912 and 1009 kmol/h (F
H2O,WNS
, 
F
H2O,WPS
, F
H2O,WS
; Eq. 7). The inlet steam molar flow rates 
were calculated as the amounts of 350, 450 and 550 kmol/h 
(F
 H2O,Re1,WNS
, F
H2O,Re1,WPS
, F
 H2O,Re1,WS
; Eq. 8).
The reformer endothermal heat flow rates were ex-
pressed as energies of 24, 27.7 and 31.4 MW (ϕ
ref,WNS
, 
ϕ
ref,WPS
, ϕ
ref,WS
; Eq. 9). The reactor exothermal heat flows 
were estimated as energies of 37, 41.3 and 45.6 MW 
(ϕ
R,WNS
, ϕ
R,WPS
, ϕ
R,WS
; Eq. 10).
The objective function of the retrofit generated prof-
its of 2.2, 3.6, and 4.8 MEUR/a using the non, partially and 
sorted MSW for synthesised gasoline productions (Eqs 11-
13). The best alternative was the synthesised gasoline pro-
duction of 0.127·10
6
 t/a from sorted MSW , because of the 
highest profit of 4.8 MEUR/a and the garbage reduction of 
0.106·10
6
 t/a into the landfill, including the flue gas and 
CO
2
 emission reductions of 0.164·10
6
 and 0.084 ·10
6
 t/a. 
The hydrogen and processed water coproducts of 4.6·10
3
 
t/a and 0.145·10
6
 t/a could justify the execution too. This 
alternative could be used to reduce the Russian natural gas 
and petroleum inflows into the industries and transports. 
3. 1.  Case Study of the Multiple’s Effect 
Technique for the Biogas
The simple mathematical model of biogas (BG) was 
simulated by using the parameters from Figure 3, which 
were contained mostly in the methane and carbon dioxide 
(F
CH4,BG
 = 650 kmol/h and F
CO2,BG
 = 350 kmol/h). The 
synthesised gasoline (F
SG,BG
) produced was the amount of 
78 kmol/h (Eqs. 14-17). The coproducts of hydrogen and 
processed water produced amounts of 120 and 780 kmol/h 
(F
H2,BG
, F
H2O,BG
). The Re5 reaction needed the amount of 
950 kmol/h (F
H2O,Re5,BG
). The preheating, endothermal 
and exothermal heat flow rates were the energies of 11, 37 
and 27 MW (ϕ
preH-BG
, ϕ
ref,BG
, ϕ
R,BG
).
The objective function of the retrofit generated a 
profit of 1.0 MEUR/a for synthesised gasoline production 
of 0.08·10
6
 t/a from biogas using Equation 11, without the 
costs of gasification, circulated gas and sorted waste, with 
those replacing with cost of biogas (C
BG
 = 1 MUR/a).
The comparisons between all alternatives of different 
raw materials were collected into Table 1, which included 
the data of the synthetic gasoline production. The distinc-
tions between production and energetic molar and heat 
flow rates were fairly linear, because of using the multiple’s 
effect parameter (MU
W
), which was also the best approxi-
mation of the simulated data.
4. Conclusion
The study of synthetic gasoline production from dif-
ferent wastes, such as non, or partially, or sorted wastes, or 
biogas, would be one of the alternatives of petroleum com-
pensation and reductions of the CO
2
 emission and the 
wastes into landfill, by using the multiple’ s effect technique. 
This technique bases on the multiple’s effect parameter 
(MU
W
), which presents the level of waste sorting (MU
W
; 
MU
WNS
 = 0; MU
WPS
 = 1; MU
WS
 = 2), and the sorted waste 
represents the highest value of the multiple’s effect param-
eter. The multiple’s effect parameter could simplify the 
amount calculations of the product and co-product pro-
ductions, including the energies into process units and the 
effect of oxygen inhibition into different wastes. The sus -
tainable synthetic gasoline production would be worked 
according to the principle of the circular economy, includ-
ing that the purified flue gas of gasification would be circu-
lated back into the process.
The calculations of all the presented alternatives 
were performed by using the presented technique, and 
confirmed that the waste should be separated, because of 
the environmental reasons and more profitable synthetic 
gasoline production. The sustainable synthesised gaso-
line production from sorted waste generated the highest 
additional profit of 4.8 MEUR/a, synthesising the amount 
of 0.127 10
6
 t/a of synthetic gasoline. The garbage from 
landfill was reduced by 0.106 10
6
 t/a by using sustainable 
Table 1: The important results comparisons between all alternatives.
Raw. F
SG
, F
H2
, F
H2O
, ϕ
ref
, ϕ
R
, Incomes, Costs, Profit,
material kmol/h kmol/h kmol/h MW MW MEUR/a MEUR/a MEUR/a
WNS 87 266 815 24.0 37.0 13.3 11.1 2.2
WPS 104 279 912 27.7 41.3 15.0 11.4 3.6
WS 121 292 1009 31.4 45.6 16.7 11.9 4.8
BG 78 120 788 37.0 27.0 9.1 8.1 1.0

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synthetic production. The outlet exhausts of the flue gas 
and CO
2
 emission have been lowered into the atmos-
phere by 0.164 10
6
 and 0.084 10
6
 t/a. The hydrogen and 
processed water coproduced the amounts of 4.6 10
3
 t/a 
and 0.145 10
6
 t/a.
This study could be ensured as environmentally sus-
tainable for the commercial synthetic gasoline production, 
because the raw materials will be coming from the garbage 
as useless MSW and flue gas. The feasibility of this project 
could be made more feasible because of the usage of the 
existing available process units. The existing methanol 
process could be replaced with the synthetic gasoline pro-
duction, because of increasing market demand. In this 
case the synthetic gasoline production would be a poten-
tial challenge for replacing the non-renewable petroleum. 
The long-term realisation view of the synthetic gasoline 
production is justified by using the multiple’s effect tech-
nique because of the environmental and economic aspects. 
The potential operation and environmental uncertainties 
of the synthetic gasoline production were low because of 
the usage real model. The multiple’s effect technique has 
simplified the calculation greatly and defined the optimal 
production of biogas from sorted MSW quickly. New re-
search aims to clean the flue gases after gasification and 
return them to the process by using the pressure swing ad-
sorption (PSA) columns with zeolites.
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Povzetek
Predstavljena je metoda večkratnega učinka, ki temelji na uplinjanju in ponovni uporabi trdnih komunalnih odpadkov 
(TKO) ter vključuje osnovni parameter večkratnega učinka (MU
W
; MU
WNS
 = 0; MU
WPS
 = 1; MU
WS
 = 2), ki predstavlja 
stopnjo sortiranja od ne sortiranih do sortiranih TKO. Zaradi tega parametra in uporabe simulatorja Aspen Plus
® 
se 
matematični model poenostavi za iskanje optimalne trajnostne surovine za proizvodnjo sinteznega plina, ki nadomešča 
netrajnosti zemeljski plin za nadaljnjo proizvodnjo metanola. Metodo smo testirali na obstoječem procesu in najboljša 
alternativa so sortirani TKO, s katerimi tudi proizvedemo največ metanola.