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The problems of the annual formation of industrial waste are common to a wide group of industries, particularly chemical, petrochemical, coal, gas, and wood processing. The most typical wastes of these industries are coal tar, waste oils, oil sludge, filter cakes, coal slime, sawdust, wood shavings, etc. Most of these materials and components pose a significant environmental threat. A successful solution to these problems is possible due to the use of auxiliary fuel; boiler modifications; oxy-fuel combustion; and the preparation of multi-component fuels, including the use of additives.
Component |
Ultimate Analysis (wt%) |
Proximate Analysis (wt%) |
Ref. |
||||||||
---|---|---|---|---|---|---|---|---|---|---|---|
C |
H |
O |
N |
S |
Moisture |
Volatile Matter |
Fixed Carbon |
Ash |
Calorific Value (MJ/kg) |
||
Shenhua coal |
69.55 |
3.74 |
10.14 |
0.83 |
0.25 |
8.28 |
29.55 |
54.96 |
7.21 |
27.07 |
[36] |
Samca coal |
75.9 |
5.3 |
12.27 |
0.7 |
5.8 |
- |
36.9 |
- |
22.8 |
- |
[37] |
Coal gangue |
17.5 |
1.26 |
- |
0.56 |
1.28 |
0.75 |
15.07 |
16.31 |
68.62 |
4.82 |
[38] |
Coal slime |
87.2 |
5.1 |
4.5 |
2.1 |
1.1 |
- |
23.1 |
- |
26.5 |
24.83 |
[39] |
Semicoke powders |
69.12 |
1.35 |
10.33 |
0.89 |
0.71 |
0.7 |
15.74 |
67.36 |
16.9 |
- |
[52] |
Pyrolytic carbon black |
93.5 |
2.84 |
<0.01 |
0.46 |
3.2 |
- |
- |
- |
25 |
26 |
[53] |
Textile dyeing sludge |
15.53 |
3.44 |
16.47 |
2.43 |
1.38 |
1.37 |
36.53 |
1.35 |
60.75 |
5.99 |
[54] |
Waste soot |
74.6 |
1.6 |
- |
0.2 |
1.35 |
68.6 |
- |
- |
- |
28.1 |
[55] |
Sewage sludge |
24.83 |
3.31 |
14.39 |
4.47 |
1.13 |
97.95 |
42.74 |
5.39 |
44.58 |
0.77 |
[56] |
Sewage sludge |
13.22 |
2.91 |
19.7 |
2.12 |
0.57 |
5.29 |
31.31 |
2.06 |
61.34 |
5.215 |
[57] |
Coking sludge |
24.48 |
3.15 |
23.68 |
2.36 |
0.94 |
78.97 |
45.48 |
9.14 |
45.38 |
8.49 |
[58] |
Brewery wastewater sludge |
17.6 |
2.93 |
- |
2.41 |
- |
2.33 |
37.72 |
0.09 |
59.86 |
6.56 |
[59] |
Waste lubricating oil |
83.53 |
13.32 |
2.83 |
0.15 |
0.17 |
- |
- |
- |
- |
- |
[60] |
Mineral waste oil |
83.2 |
13.0 |
1.2 |
- |
1.2 |
- |
- |
- |
- |
[37] |
|
Lubricating Oil Wastes |
83.2 |
13 |
1.2 |
- |
1.2 |
- |
- |
- |
- |
44.33 |
[61] |
Waste lubricating oil |
84.02 |
13.31 |
1.92 |
- |
0.75 |
- |
- |
- |
- |
- |
[44] |
Waste cooking oil |
71.84 |
10.14 |
17.71 |
0.06 |
0.01 |
0.08 |
99.15 |
0.56 |
0.24 |
39.24 |
[62] |
Oily sludge |
63.9 |
7.3 |
25.3 |
1.2 |
2.3 |
33.4 |
69.3 |
- |
21.2 |
23 |
[42] |
Bio-oil (from pyrolysis of pine) |
41.47 |
6.37 |
52.05 |
0.11 |
- |
24.7 |
73.1 |
2.1 |
0.1 |
16.9 |
[63] |
Corn stalk |
32.01 |
3.44 |
24.0 |
1.02 |
0.22 |
6.77 |
52.1 |
8.61 |
32.52 |
11.87 |
[64] |
Coal slime |
53.29 |
3.89 |
9.41 |
0.83 |
0.65 |
0.95 |
27.51 |
36.62 |
34.92 |
22.07 |
[57] |
Bamboo residual |
55.51 |
6.12 |
42.05 |
0.21 |
0.11 |
- |
- |
- |
- |
- |
[44] |
Corn silage |
43.40 |
6.17 |
46.70 |
1.02 |
0.93 |
- |
- |
- |
- |
- |
[65] |
Clover grass |
44.90 |
6.8 |
43.30 |
2.2 |
0.3 |
- |
- |
- |
- |
- |
[65] |
Biochar (from pyrolysis of pine) |
86.83 |
3.34 |
9.7 |
0.13 |
- |
2.4 |
16.4 |
80.6 |
3.0 |
28.3 |
[63] |
Fuel |
Installation |
Temperature Conditions |
Ref. |
---|---|---|---|
Stem wood, bark, forest residue, willow, and reed canary grass and pyrolysis oil and solid residue from them |
Tube furnace blown by gas mixtures (air, N2, O2) |
<1400 °C |
[71] |
Emulsion based on water and heating oil; slurry based on water and pyrolytic soot |
Chamber with industrial burners with a total power of 1.2 MW |
Temperature of flue gases > 1100 °C Maximum operating temperature 1430 °C |
[53] |
Spherical particles of corn stalk and bituminous coal |
Reactor (electrical quartz tube), blown by mixtures of O2/N2 and O2/H2O |
800 °C |
[64] |
Sewage sludge with coal–water slurry (CWS) |
Large scale fluidized bed incinerator |
>1000 °C |
[56] |
Wet sewage sludge with wood chips |
Grate-fired boiler with a vibrating grate |
>1000 °C |
[72] |
Pyrolysis oil from sewage sludge, heavy fuel oil |
Laboratory setup with heat sources in the form of two plates |
Temperature of the plates is 500, 550, 600 °C |
[58] |
Slurry based on coal, water and waste soot |
Rotary kiln |
800 °C |
[55] |
Slurries based on coal and liquid waste from petrochemical industry |
Pilot-scale combustion system |
1100–1300 °C at steady combustion |
[73] |
Fuel |
Process |
Characteristics of the Plant |
Temperature |
Key Result |
Ref. |
---|---|---|---|---|---|
Coal–oil–water slurry (COWS) (coal 45–55 wt%, oil 10–20 wt%; water 35 wt%) |
Pyrolysis |
Laboratory tube furnace. The carrier gas: N2, flow rate 0.8 L/min. Experiment time: 30 min. Particle size: 75–100 μm. |
800, 900 and 1000 °C |
An increase in the temperature and the proportion of water in the fuel contributed to an increase in the gas yield up to 2.8 times, while the char yield decreased to 1.4 times. The addition of waste oil resulted in a decrease in CO and CO2, and an increase in CH4 and H2. Pyrolysis gas composition: H2: 80–270 mL/g; CO: 35–110 mL/g; CO2: 22–120 mL/g; CH4: 60–150 mL/g. |
[60] |
Coal wastewater slurry (CWWS) (coal 57.2–62 wt%, water 42.8–38 wt%). |
Gasification |
Industrial CWS gasifier to produce syngas and synthesize ammonia. Syngas output 515,116.8 m3/day. Particle size: 40 μm. |
1350–1400 °C |
The syngas produced by the CWWS gasification has a higher effective gas component (CO + H2) than the CWS. In addition, the use of a waste-based slurry increased cold gas efficiency by 1.57% and carbon conversion by 0.45% in industrial processes. Syngas composition: H2: 30.5%; CO: 48.1%; CO2: 16.3%; CH4: 0.9%; N2: 4.2%. |
[36] |
Waste oil/coal slurry (coal 50 wt%, mineral waste oil 50 wt%). |
Pyrolysis |
Laboratory fluidized bed reactor. Feeding rate 550 g/h. Fuel mass 3 kg. |
625 °C |
The quality of waste oil/coal slurry pyrolysis products was higher compared to coal pyrolysis products. During the slurry pyrolysis, the gas yield increased from 14.2% to 31.6%, and the liquid yield increased from 17.4 to 29.1% in comparison with coal. At the same time, the concentrations of CH4, H2, C2H4, and C2H6 increased by 3.3, 2.5, 32, and 10 times, respectively. Pyrolysis gas composition: H2: 0.5 wt%; CO: 1.6 wt%; CO2: 3.4 wt%; CH4: 4.9 wt%, C2H4, 6.4 wt%; C2H6 3 wt%. |
[37] |
Lubricating Oil Wastes (LOW) |
Pyrolysis |
Laboratory pyrolysis unit. Reactor is heated by an electrical oven. Feeding rate 0.5 g/min. Experiment time 20 min. |
600–700 °C |
Pyrolysis gas composition: H2: 0.01–0.02 g/kg; CO: 0.03–0.04 g/kg; CO2: 0.04–0.08 g/kg; CH4: 0.35–0.93 g/kg; C2H4: 0.5–1 g/kg; C2H6: 0.25–0.47 g/kg. Product Yield by Pyrolysis: char: 0.45–0.6 g/kg; liquids: 3.57–6.04 g/kg; gases: 3.46–5.97 g/kg; |
[61] |
Bamboo residual (BR) and waste lubricating oil (WLO) |
Pyrolysis |
Pyrolyzer with dual catalytic beds HZSM-5 and MgO. Fast pyrolysis: heating rate 2000 °C/s. Particle size: 0.15 μm. |
500–700 °C |
The temperature of 600 °C was optimal due to the relatively high yields of furans and phenols. |
[44] |
Coal water ethanol slurry (CWES) (coal 57 wt%, water 36 wt%, ethanol 7 wt%). |
Gasification |
Pilot-scale entrained flow gasifier. Feeding rate at 20 bar: 96.15 kg/h. |
1100 °C |
When ethanol was used in the slurry, an increase was recorded in syngas heating value (by 9%), syngas flow rate (by 38%), syngas production per 1 kg of slurry (by 25%), cold gas efficiency (by 39%) and carbon conversion efficiency (by 15%). Syngas composition: H2: 34.50 vol%; CO: 29.69 vol%; CO2: 35.33 vol%; CH4: 0.47 vol%. |
[46] |
Textile dyeing sludge (DS) with 20–30 wt% additives (CaO, Ca-bentonite, Kaolin and Fe) |
Pyrolysis |
Two-mode microwave device with 2.45 GHz frequency and the maximum power of 3 kW. Particle size: <1 mm. |
450–750 °C |
Addition of CaO and Fe increased the char yield (in 1.2 times) and H2 contents (in 2.5 times), and decreased CO2 content in the non-condensable gas. Pyrolysis gas composition: Without additives: H2: 20–33 vol%; CO: 12–15 vol%; CO2: 0–65 vol%; CH4: 0–5 vol%. With additives: H2: 12–62 vol%; CO: 15–20 vol%; CO2: 45–65 vol%; CH4: 4–15 vol%. Product Yield by Pyrolysis: char: 60–80 wt%; liquids: 10–14 wt%; gases: 4–15 wt% |
[54] |
Corn starch, clover grass, and corn silage in supercritical water |
Gasification in supercritical water |
Continuous flow reactor |
500–700 °C |
Gasification of biomass in supercritical water is highly temperature-dependent. Almost complete conversion of the feed can be achieved at 700 °C. As the temperature rises, the H2 yield increases, but the CO concentration decreases. Syngas composition: H2: 29.7–34.4 vol%; CO: 0.62–2.8 vol%; CO2: 39.7–43.9 vol%; CH4: 15–20.5 vol%; C2H2: 2.6–4.8 vol%. |
|
Water–semicoke slurry (semicoke 10–30 wt%). |
Gasification in supercritical water |
Supercritical water fluidized bed reactor system. Pressure 23 MPa. Water flow rate 40 g/min, slurry flow rate 20 g/min/ Particle size: <100 μm |
540–660 °C |
The temperature of 600 °C is the most preferred to provide full gasification of the fixed carbon is realized. The use of K2CO3 as a catalyst made it possible to increase the hydrogen yield by 92%. Syngas composition: H2: 50–55 vol%; CO: 2–3 vol%; CO2: 35–38 vol%; CH4: 10–12 vol%. |
[52] |