Experimental Study on Co-Pyrolysis Characteristics of Household Refuse and Two Industrial Solid Wastes

: The caloriﬁc value of household refuse (HR) is greatly improved after classiﬁcation, which includes the implementation of sufﬁcient pyrolysis conditions. Therefore, a better pyrolysis effect can be achieved by co-pyrolysis with industrial solid waste (ISW) with high caloriﬁc value. In this work, HR and ISW were used as raw materials for co-pyrolysis experiments. The inﬂuence on the distribution of three-phase products after co-pyrolysis, the concentration of heavy metals and dioxins in the ﬂue gas, and the distribution of PCDD/Fs isomers were studied. The results showed that, at a temperature of 600 ◦ C and H/C = 1.3, of the formed material, the quantity of pyrolysis gas was approximately 27 wt.%, and the quantity of pyrolysis oil was approximately 40.75 wt.%, which mainly contained alkanes, oleﬁns, and aromatic hydrocarbons. When S/C = 0.008, pyrolysis gas accounted for 25.95 wt.% of the formed material, and pyrolysis oil for 41.95 wt.% of the formed material. The ignition loss rate of pyrolysis coke was approximately 20%, and the maximal caloriﬁc value was 14,217 KJ/kg. According to the thermogravimetric experiment, the co-pyrolysis of HR and ISW can promote the positive reaction of pyrolysis, and the weight loss reached 62% at 550 ◦ C. The emission of gaseous heavy metals was relatively stable, and the concentration of heavy metals slightly decreased. The main heavy metals in the ash were Cu, Fe, and Zn. The emission of dioxins could be effectively reduced by the pyrolysis of HR with ISW, and the produced dioxins were mainly synthesized from de novo synthesis. After pyrolysis, the toxic equivalent of dioxins in the ﬂue gas was reduced from 0.69 to 0.29 ng I-TEQ/Nm 3 , and the distribution of dioxin isomers in the ﬂue gas had little inﬂuence. The experimental results provide a theoretical basis for the application of co-pyrolysis technology with HR and ISW.


Introduction
With economic development and the improvement of living standards, the production of household refuse (HR) is also increasing. In China, HR can generally be divided into four categories: recyclable refuse, kitchen refuse, hazardous refuse, and other refuse. In 2020, the volume of HR collected reached 242 million tons. In 2019, China's industrial solid waste (ISW), which is produced in industrial production activities, reached 3.53 billion tons, but the disposal amount was 8.78 billion tons, which is a large gap. Waste classification has been carried out in many cities in China. Garbage classification generally refers to a series of activities in which garbage is classified, stored, and transported according to certain regulations or standards, so as to be transformed into public resources. Waste classification can improve the resource value and economic value of waste and make the best use of everything; therefore, the calorific value is higher, and reached approximately A previous investigation found that the ISW of the paper and rubber industries contained high contents of carbon and sulfur, respectively, which can improve the quality of pyrolysis products and reduce the concentration of dioxin. Therefore, HR and ISW were used as raw materials for co-pyrolysis. The raw material was crushed into a powder with an average particle size of 0.30 mm. Analysis was carried out in accordance with the proximate analysis of coal (GB/T212-2008) and the determination of chlorine in coal (GB/ T3558-1996).
The results of the composition of household waste and the ultimate (including water content (M), ash (A), volatile matter (V), and fixed carbon (FC)) and proximate analyses of the raw materials are shown in Tables 1 and 2. After waste classification and waste-site sorting and drying, plastics accounted for 41.7% of the HR components, which accounted for a higher proportion than that before classification. In addition, the content of kitchen waste was lower. Therefore, the calorific value of HR could reach 17.031 MJ/kg. The proportion of chlorine in the HR, ISW1, and ISW2 was 0.89%, 0.04%, and 0.01%, respectively. Organic and inorganic chlorine in HR are the main sources of Cl 2 and HCl in flue gas. In the process of co-pyrolysis, chlorine is easily precipitated. When the temperature reaches 600 • C, the chlorine precipitation rate is generally more than 70-80%, which increases the volatility of metals and is a key element for dioxin formation [15,16]. The proportion of sulfur in the HR, ISW1, and ISW2 was 0.7%, 0.07%, and 2.06%, respectively. In the process of co-pyrolysis, sulfur in HR and ISW mainly exists in the form of organic and inorganic sulfur [17].

Experimental Procedures
The co-pyrolysis furnace used in this experiment is shown in Figure 1. Co-pyrolysis took place in a continuous feed-type pyrolysis furnace, which mainly consisted of a carrier gas supply, a pyrolysis furnace chamber, a heating and temperature control system, and a condensing and collecting device. HR and ISW were pyrolyzed in the pyrolysis chamber, which was heated by electric heating modules and centrally controlled by the control cabinet. In this experiment, in order to ensure a constant pyrolysis atmosphere, after the material entered the feeder, the top diaphragm was closed. The baffle moved at a uniform speed to ensure the continuous falling of materials. In the process of waste falling into the furnace, part of the water was removed when it passed through the heating section of the upper part of the furnace. When it dropped to the bottom, it started to pile up and pyrolyze. The generated pyrolysis gas and oil entered the collection and condensation section through the upper inlet opening. In order to prevent the pyrolysis oil from condensing on the wall, a heating module was installed on the upper part of the furnace body and the flue gas pipeline. The pyrolysis oil was collected by the oil collector after condensation on the pipeline, and the pyrolysis gas was discharged from the tail after condensation. The pyrolysis chamber was equipped with two air intakes that could adjust the ratio of pyrolysis gas to air to meet the experimental requirements of the different pyrolysis and gasification atmospheres. A flue gas sampling tube was set in the cavity that could collect the gas produced in the furnace. Ice water circulated through the interlayer of the condensing tube to cool the flowing pyrolytic gas and to collect the pyrolytic oil condensing from the gas. High-purity nitrogen gas was selected as the carrier gas.

Experiment Steps
HR and ISW were mixed in different proportions, and the mass fractions of HR in the sample were 100, 80, and 70 wt.%. The mass of each sample was approximately 1 kg. First, a 1 kg sample was placed in a feeder and purged with 2 L/min nitrogen for 30 min, while heating it at a rate of 10 • C/min. After heating, the nitrogen flow rate was adjusted to 1 L/min. HR and ISW were pyrolyzed in the pyrolysis furnace body; the temperature was controlled at 500, 600, and 700 • C, and maintained for 60 min. The specific working conditions are shown in Table 3. Groups A, B, E, F, and G were used to study the copyrolytic characteristics under different H/C and S/C ratios. Groups B, C, and D were used to study the effect of different temperature levels on co-pyrolysis.

Experiment Steps
HR and ISW were mixed in different proportions, and the mass fractions of HR in the sample were 100, 80, and 70 wt.%. The mass of each sample was approximately 1 kg. First, a 1 kg sample was placed in a feeder and purged with 2 L/min nitrogen for 30 min, while heating it at a rate of 10 °C/min. After heating, the nitrogen flow rate was adjusted to 1 L/min. HR and ISW were pyrolyzed in the pyrolysis furnace body; the temperature was controlled at 500, 600, and 700 °C , and maintained for 60 min. The specific working conditions are shown in Table 3. Groups A, B, E, F, and G were used to study the copyrolytic characteristics under different H/C and S/C ratios. Groups B, C, and D were used to study the effect of different temperature levels on co-pyrolysis.
The pyrolysis oil was condensed by the pipeline and collected by the oil collector. After condensation, the pyrolysis gas was discharged. The flue gas was sampled for approximately 1 h during each sampling, using the constant-speed sampling principle, and flue gas was produced through the membrane and XAD-2 resin, respectively. The toluene solution was placed in an ice bath. In order to ensure the accuracy and stability of the experimental results, each test was carried out in duplicate. At the end of the experiment, samples containing XAD-2 resin, toluene solution, and reaction residue were collected, and their pipes were also collected after being washed with dichloromethane, acetone, and toluene, respectively. Collected samples were sent to the laboratory for low-temperature storage. The pyrolysis coke and pyrolysis oil were collected and stored for subsequent analysis.
In addition, a thermogravimetric analysis of HR and ISW was carried out by using a thermogravimetric analyzer (TGA); HR, ISW, and their mixtures were used as raw materials. The temperature was increased from 25 to 850 °C at a heating rate of 10 °C /min. Thermal gravity (TG) and derivative thermogravimetry (DTG) curves were obtained by collecting and analyzing the data. Then, 99.9% high-purity nitrogen with a flow rate of 50 mL/min was used as the carrier gas to ensure an inert atmosphere during operation.   The pyrolysis oil was condensed by the pipeline and collected by the oil collector. After condensation, the pyrolysis gas was discharged. The flue gas was sampled for approximately 1 h during each sampling, using the constant-speed sampling principle, and flue gas was produced through the membrane and XAD-2 resin, respectively. The toluene solution was placed in an ice bath. In order to ensure the accuracy and stability of the experimental results, each test was carried out in duplicate. At the end of the experiment, samples containing XAD-2 resin, toluene solution, and reaction residue were collected, and their pipes were also collected after being washed with dichloromethane, acetone, and toluene, respectively. Collected samples were sent to the laboratory for lowtemperature storage. The pyrolysis coke and pyrolysis oil were collected and stored for subsequent analysis.
In addition, a thermogravimetric analysis of HR and ISW was carried out by using a thermogravimetric analyzer (TGA); HR, ISW, and their mixtures were used as raw materials. The temperature was increased from 25 to 850 • C at a heating rate of 10 • C/min. Thermal gravity (TG) and derivative thermogravimetry (DTG) curves were obtained by collecting and analyzing the data. Then, 99.9% high-purity nitrogen with a flow rate of 50 mL/min was used as the carrier gas to ensure an inert atmosphere during operation.

Detection Method
According to the USAEPA1613 method [18], dioxin samples were pretreated and analyzed by high-resolution gas chromatography/high-resolution mass spectrometry (HRGC/HRMS, JMS8000D, JEOL). The toxicity equivalent (TEQ) was calculated using the international NATO/CCMS factor, namely I-TEQ [19]. The average recoveries of PCDD/Fs ranged from 55% to 125%, which were within the quality control range.
The GB 16889-2008 landfill pollution control standard (life) of the HJ/T300-2007 leaching procedure (solid-waste leaching toxicity of the acetate buffer method) was used to test the leaching toxicity. A liquid/solid ratio of 20:1 (mL/g) was added to the leach sample at a pH of 2.64 ± 0.05 and a speed of 30 ± 2 revolutions/min, at room temperature (23 ± 2 • C), rotating (18 ± 2 h). Lastly, the concentration of heavy metals in the filtrate was determined by ICP−AES (ICAP6300). The chlorine content in the samples was determined by high-temperature hydrolysis and ion chromatography (ICS-6000, Thermo, China). Figure 2a shows that the pyrolytic process of HR can be divided into three main stages. In the first stage (100-300 • C), the TG curve presented the first weight loss peak, with a weight loss rate of 8.3%. This part mainly included water drying and the decomposition of less stable polymers [20,21]. In the second stage (300-600 • C), the second weight loss peak appeared on the TG curve, which was the main pyrolytic stage of HR, and the weight loss rate was approximately 30.21%. In the third stage (500-800 • C), the TG curve presented a third weight loss peak with a weight loss rate of 11.3%, which was mainly due to the pyrolysis of heavy components, such as long-chain refractory organic macromolecules. Figure 2b,c show the TG/DTG curves of the thermal decomposition of ISW1 and ISW2, respectively. Figure 2b shows that weight loss began around 300 • C, and a significant weight loss peak appeared around 440 • C, with a weight loss rate of 58.5%, which was mainly due to the decomposition of organic matter in ISW1. The weight loss rate decreased significantly when the temperature rose to approximately 500 • C, the weight loss curve became flat after 550 • C, and pyrolysis ended. Figure 2c shows that the pyrolytic trends of ISW 2 and ISW 1 were roughly the same. Weight loss began at 250 • C and the weight loss rate was approximately 56.8% at 450 • C. Figure 2a-c show that there was a large difference between the pyrolytic characteristics of HR and ISW. ISW was pyrolyzed in a relatively narrow temperature range (300-500 • C), while HR was pyrolyzed in a wider temperature range (200-850 • C), because of its complex components. This was mainly due to the fact that the composition of ISW was relatively simple and there was no long-chain refractory materials that could be rapidly pyrolyzed at a low temperature. Figure 2d,e shows the TG/DTG characteristic pyrolytic curves of HR and ISW1 mixed at a 7:3 ratio. The TG curve after mixed ISW1 pyrolysis had a larger weight loss ratio than that of each component alone, reaching approximately 62% in the main weight loss stage. At 600-800 • C, the total weight loss reached approximately 70%, which indicated that the co-pyrolysis of HR and ISW1 could effectively improve the pyrolytic efficiency. When HR and ISW2 were mixed, the weight loss rate was less than that of HR and ISW1, which reached 55.2% at 800 • C.

Analysis of Co-Pyrolytic Products
The yields of pyrolysis gas, pyrolysis oil, and coke are shown in Figure 3. According to Groups B, C, and D, with an increase in temperature, volatiles in the liquid phase were further pyrolyzed, resulting in more gas than liquid. With the increase in temperature from 500 to 700 • C, the yield of pyrolysis oil first increased from 39.35% (D, 500 • C) to 40.75% (B, 600 • C), and finally decreased to 35.15% (C, 700 • C). This may have been due to incomplete pyrolysis and the low yield of pyrolysis oil at a low temperature (500 • C). As the temperature rose to 600 • C, the pyrolytic efficiency was improved, which was due to the yield of pyrolysis oil increasing. As the temperature continued to rise to 700 • C, part of the pyrolysis oil was converted into gas, and the yield of pyrolysis oil decreased. According to the temperature control group (B, C, and D), the co-pyrolysis of HR and ISW occurred most effectively at 600 • C, so the follow-up experiment was carried out at 600 • C.  The S/C ratio also had a similar effect on the co-pyrolysis of HR and ISW. The copyrolysis of HR and ISW2 had a higher oil production rate than that of HR and ISW1, which may have been because there were more organic compounds in rubber, which are conducive to the formation of pyrolysis oil. In Groups A, F, and G, with the decrease in the S/C ratio, the yield of pyrolysis gas and oil slightly decreased, and the proportion of coke slightly increased, which was similar to the co-pyrolytic trend of HR and ISW1, indicating that the S/C ratio had little effect on the yield of co-pyrolytic products. Alkanes, alkenes, and aromatics were the main components of pyrolysis oil. Different feedstocks and temperatures changed the co-pyrolytic conditions, thus changing the distribution of oil products to varying degrees. As shown in Figure 4, when HR and ISW1 were co-pyrolyzed and the temperature was increased from 500 to 700 °C (Groups D, B, and C), the alkene content increased from 14% to 25.6%, the aromatic content increased from 19.5% to 41.2%, and the alkane content decreased from 66.5% to 55.4%. By increasing Compared with HR pyrolysis (A) alone, HR and ISW1 co-pyrolysis (E) reduced the coke yield from 48.25% to 37.8%. The yield of pyrolysis gas and oil increased by 2.85% and 11.7%, respectively, which showed that the co-pyrolysis of HR and ISW1 was beneficial to the occurrence of a pyrolytic reaction and the formation of light molecules. Compared with Groups A, B, and E, with the decrease in the H/C ratio, the yield of pyrolysis oil increased from 37.8% to 40.75%, and the content of coke slightly decreased. Similar results were obtained for Groups A, F, and G. This may have been due to the decrease in the H/C ratio in the raw materials, which promoted the co-pyrolytic process. It may have also been because some components of HR and ISW2 reacted with one another to promote co-pyrolysis.
The S/C ratio also had a similar effect on the co-pyrolysis of HR and ISW. The copyrolysis of HR and ISW2 had a higher oil production rate than that of HR and ISW1, which may have been because there were more organic compounds in rubber, which are conducive to the formation of pyrolysis oil. In Groups A, F, and G, with the decrease in the S/C ratio, the yield of pyrolysis gas and oil slightly decreased, and the proportion of coke slightly increased, which was similar to the co-pyrolytic trend of HR and ISW1, indicating that the S/C ratio had little effect on the yield of co-pyrolytic products.
Alkanes, alkenes, and aromatics were the main components of pyrolysis oil. Different feedstocks and temperatures changed the co-pyrolytic conditions, thus changing the distribution of oil products to varying degrees. As shown in Figure 4, when HR and ISW1 were co-pyrolyzed and the temperature was increased from 500 to 700 • C (Groups D, B, and C), the alkene content increased from 14% to 25.6%, the aromatic content increased from 19.5% to 41.2%, and the alkane content decreased from 66.5% to 55.4%. By increasing the H/C ratio (Groups A, B, and E) of the pyrolytic feedstock, the yield of olefins also increased to a certain extent, but it was lower than that of HR pyrolysis alone. This may have been due to a mutual reaction between materials caused by co-pyrolysis, which promoted the decomposition of olefins into alkanes. With the increase in the H/C ratio, the production of aromatics decreased from 28% to 22.5%. When HR and ISW2 were co-pyrolyzed, with the increase in the S/C ratio, the alkene content increased from 24.3% to 31.1%, while the amount of alkanes and aromatics decreased. In conclusion, when the temperature was between 600 and 700 • C, more pyrolysis oil could be produced from HR and ISW co-pyrolysis. When the H/C and S/C ratios were 1.3 and 0.007, respectively, more pyrolysis oil containing olefin could be obtained. moted the decomposition of olefins into alkanes. With the increase in the H/C ratio, the production of aromatics decreased from 28% to 22.5%. When HR and ISW2 were co-pyrolyzed, with the increase in the S/C ratio, the alkene content increased from 24.3% to 31.1%, while the amount of alkanes and aromatics decreased. In conclusion, when the temperature was between 600 and 700 °C , more pyrolysis oil could be produced from HR and ISW co-pyrolysis. When the H/C and S/C ratios were 1.3 and 0.007, respectively, more pyrolysis oil containing olefin could be obtained. The ignition loss and calorific value of pyrolytic coke are shown in Table 4. When HR and ISW1 co-pyrolyzed, the lowest coke ignition loss rate was 16.2% (C), which was due to the further pyrolysis of coke at a higher temperature. The highest ignition loss rate was 34.1%, because of the low temperature. At a low temperature, coke was the main pyrolytic product, and carbon was mainly found in solid form. When HR and ISW2 co-pyrolyzed, the ignition loss was 41.9%, which was much higher than that of co-pyrolyzed HR and ISW1. Compared with HR pyrolysis alone, co-pyrolyzed coke had a higher calorific value. Therefore, co-pyrolyzed coke could be recycled, which is conducive to improving energy utilization.  The ignition loss and calorific value of pyrolytic coke are shown in Table 4. When HR and ISW1 co-pyrolyzed, the lowest coke ignition loss rate was 16.2% (C), which was due to the further pyrolysis of coke at a higher temperature. The highest ignition loss rate was 34.1%, because of the low temperature. At a low temperature, coke was the main pyrolytic product, and carbon was mainly found in solid form. When HR and ISW2 co-pyrolyzed, the ignition loss was 41.9%, which was much higher than that of co-pyrolyzed HR and ISW1. Compared with HR pyrolysis alone, co-pyrolyzed coke had a higher calorific value. Therefore, co-pyrolyzed coke could be recycled, which is conducive to improving energy utilization.

Emission Characteristics of Heavy Metals
Heavy metals mainly exist in the form of oxides, mineral salts, sulfides, and hydroxides in HR and ISW. Mineral salts and hydroxides are usually converted into oxides or sulfides with better thermal stability during pyrolysis. During co-pyrolysis, due to the characteristics of heavy metals (such as their boiling point), HR composition (chlorine, sulfur, alkali metal content, etc.), and the operating environment in the furnace (i.e., the temperature, time, atmosphere, and catalyst), heavy metals are found in the form of oxides and mineral salts. After the evaporation and condensation process, mineral salts and hydroxides are usually converted into oxides or sulfides with good thermal stability [22,23]. Heavy metals are also important catalysts for the synthesis of dioxins; however, when the amount of heavy metals used as catalysts meets the requirements of a catalytic reaction, the increase in heavy metals has no effect on the reaction rate, and cannot increase the amount of dioxins and their precursors [24].
The emission characteristics of the heavy metals in flue gas in this experiment, under different working conditions, are shown in Table 5. Comparing various working conditions revealed that the emission of gaseous heavy metals was relatively stable. During co-Energies 2021, 14, 6945 9 of 15 pyrolysis, the concentration of heavy metals decreased slightly, and only Ni emissions increased, but the change range was within one order of magnitude. With the temperature increasing from 500 to 700 • C, the content of Cu in the heavy metals decreased from 0.1122 to 0.0136 mg/L, and the amount of Fe decreased from 0.3572 to 0.2478 mg/L. In general, due to the lack of a catalyst, the content of heavy metals in flue gas was relatively stable [25,26]. The co-pyrolysis of HR and ISW generally had little effect on the emission of heavy metals in the gas, and did not aggravate the emission of heavy metals. Additionally, heavy metals may be more easily absorbed by coke, so the heavy metal content in coke should be closely monitored. The heavy metal contents in the coke are shown in Table 6. Except for Cu, Fe, and Zn, the other heavy metals hardly changed. The content of Cu in coke was 2050.4 mg/kg at 100 wt.% of HR. Then, the content was reduced to 149.7 mg/kg when 30 wt.% ISW1 was added. In Groups B-D, with the increase in temperature, the Cu decreased from 310.6 to 149.72 mg/kg, and then increased to 207.75 mg/kg. Fe showed a similar trend. The increase in temperature may have reduced the formation of heavy metals, but when the temperature was higher, the volatilization of chlorine promoted the formation of heavy metals. When HR and ISW2 were co-pyrolyzed, the concentration of heavy metals was higher than that in HR and ISW1, which showed that, in practical applications, much more attention should be paid to the emission of heavy metals.

PCDD/Fs in Flue Gas
The mass concentration of dioxins in flue gas during the co-pyrolysis of HR and ISW is shown in Figure 5a. When the raw material was 100% HR (Group A), the mass concentration of PCDD/Fs in the flue gas after pyrolysis was 3.89 ng/Nm 3 , and when 30% of ISW1 was added (B), the PCDD/F concentration was reduced to 1.66 ng/Nm 3 . When the co-pyrolysis temperature was increased from 500 to 700 • C (C), the PCDD/F concentration in the flue gas after co-pyrolysis was increased from 42.8 ± 1.26 to 2.34 ng/Nm 3 . When the temperature was 500 • C, the concentration of PCDD/Fs was higher, which may have been due to the relatively high content of heavy metals, which provided a metal catalyst for the formation of dioxin [27]. When HR:ISW2 = 7:3 (S/C = 0.08), the concentration of PCDD/Fs was 12.4 ng/Nm 3 . When the mixing ratio was decreased to 8:2 (S/C = 0.07), the concentration of PCDD/Fs was 21.2 ng/Nm 3 . This indicated that the lower S/C ratio made it easier to generate PCDD/Fs [28]. Similarly to previous studies, the presence of sulfur could inhibit the formation of PCDD/Fs to a certain extent [29,30]. Concentrations were higher than those of HR and ISW1, because there were more carbon elements in ISW2, which provided a carbon source for the formation of dioxins [31]. A schematic diagram of the dioxin formation mechanism during pyrolysis is shown in Figure 6. The role of SO 2 in pyrolysis is shown in Table 7. It can be seen from the figure that SO 2 reacts with Cl 2 to produce SO 3 and HCl. This reduces the Cl 2 involved in the chlorination of aromatic hydrocarbon precursors and reduces the production of dioxins at the source. In addition, SO 2 reacts with Cu and other heavy metals to produce CuSO 4 , which consumes the heavy metals involved in de novo synthesis and reduces the generation of dioxins [16,32].
The toxic equivalent of dioxins in flue gas during the co-pyrolysis of HR and ISW is shown in Figure 5b. The toxic equivalent of dioxin in flue gas A was 0.69 ng I-TEQ/Nm 3 . After the addition of ISW1 (30%), the toxicity equivalent of dioxin in the flue gas decreased to 0.29 ng I-TEQ/Nm 3 . This may have been due to the increase in the ratio of carbon to hydrogen during co-pyrolysis, which promoted the pyrolytic process and discharged more carbon in the form of short-chain hydrocarbons and CO, reducing the carbon sources generated by dioxin [33]. When the temperature increased from 600 to 700 • C, the concentration of dioxin in flue gas increased from 0.29 to 0.54 ng I-TEQ/Nm 3 , possibly because the temperature increased and the co-pyrolysis efficiency improved, which promoted PVC decomposition in the raw material and generated hydrogen chloride gas, which, in turn, promoted pyrolysis [34]. At the same time, chlorinated organic compounds formed by pyrolysis, such as chlorobenzene, participated in the formation of dioxins as precursors [35]. Chlorine in flue gas mainly exists in the form of HCI. Relevant experiments have shown that the chlorine source of PCDD/Fs is Cl 2 , not HCl, but it is easy for HCl to react with heavy metals such as Cu to produce Cl 2 [36], which provides a chlorine source for the synthesis of dioxins [37][38][39].
The isomeric distribution of 17 toxic dioxins in pyrolysis flue gas is shown in Figure 7. PCDD/Fs in the flue gas of Group A were mainly distributed in PCDFs, in which the 2,3,7,8-TCDF content was the highest, accounting for 49.27% and indicating that a de novo synthesis reaction was the main method of generating dioxins [40]. In Group B, PCDFs were still the main dioxins in the flue gas, but their proportion was reduced by 4% compared with Group A, indicating that the contribution of the precursor synthesis reaction to dioxin production was further reduced. After increasing the pyrolytic temperature (C), the dioxins found were mainly PCDFs, indicating that the increase in temperature had little effect on the formation of dioxin isomers and that de novo synthesis was still dominant. In the flue gas of Group A, the PCDDs were mainly 2,3,7,8-TCDD and OCDD, accounting for 72.6% of the total concentration of PCDDs, and the PCDFs were mainly 1,2,34,6,7,8-HPCDF and OCDF, the sum of which reached 86.8%. PCDDs in the flue gas of Groups B and C were still mainly 2,3,7,8-TCDD and OCDD, but their proportion was further increased compared with that of Group A. Therefore, the toxic equivalent was increased and PCDFs were mainly 2,3,7,8-TCDF. Compared with Groups A-C, the proportion of PCDFs in Group D was increased to approximately 88%. When the S/C ratio decreased, the PCDF content increased to 92.95%, indicating that the ratio of de novo synthesis was further increased. All in all, the distribution of dioxin isomers in the flue gas during co-pyrolysis was similar to that in the single-pyrolysis flue gas, indicating that the effect of co-pyrolysis on the distribution of dioxin isomers was minor.      Table 7. Reaction of sulfur with key elements in the synthesis of dioxin.

Reaction Equation 1
Cl2 + SO2 + H2O→2HCl + SO3 2 CuO + SO2 + 1/2O2→CuSO4 3 SO2 + CuCl2 + H2O + 1/2O2→CuSO4 + 2HCl The isomeric distribution of 17 toxic dioxins in pyrolysis flue gas is shown in Figure  7. PCDD/Fs in the flue gas of Group A were mainly distributed in PCDFs, in which the 2,3,7,8-TCDF content was the highest, accounting for 49.27% and indicating that a de novo synthesis reaction was the main method of generating dioxins [40]. In Group B, PCDFs were still the main dioxins in the flue gas, but their proportion was reduced by 4% compared with Group A, indicating that the contribution of the precursor synthesis reaction to dioxin production was further reduced. After increasing the pyrolytic temperature (C), the dioxins found were mainly PCDFs, indicating that the increase in temperature had little effect on the formation of dioxin isomers and that de novo synthesis was still dominant. In the flue gas of Group A, the PCDDs were mainly 2,3,7,8-TCDD and OCDD, accounting for 72.6% of the total concentration of PCDDs, and the PCDFs were mainly 1,2,34,6,7,8-HPCDF and OCDF, the sum of which reached 86.8%. PCDDs in the flue gas of Groups B and C were still mainly 2,3,7,8-TCDD and OCDD, but their proportion was further increased compared with that of Group A. Therefore, the toxic equivalent was increased and PCDFs were mainly 2,3,7,8-TCDF. Compared with Groups A-C, the proportion of PCDFs in Group D was increased to approximately 88%. When the S/C ratio decreased, the PCDF content increased to 92.95%, indicating that the ratio of de novo synthesis was further increased. All in all, the distribution of dioxin isomers in the flue gas during co-pyrolysis was similar to that in the single-pyrolysis flue gas, indicating that the effect of co-pyrolysis on the distribution of dioxin isomers was minor.

Conclusions
From the co-pyrolytic experiment using HR and ISW, the following conclusions were drawn: 1. The HR and ISW co-pyrolytic product distribution was relatively uniform compared with HR pyrolysis alone. After mixing with the ISW, the coke yield decreased by

Conclusions
From the co-pyrolytic experiment using HR and ISW, the following conclusions were drawn: 1.
The HR and ISW co-pyrolytic product distribution was relatively uniform compared with HR pyrolysis alone. After mixing with the ISW, the coke yield decreased by approximately 14.6%, and the pyrolysis gas and oil yields slightly increased. Pyrolysis oil took priority, with alkenes, alkanes, and aromatic hydrocarbons. The ignition loss rate of pyrolysis coke was approximately 20%, and the maximal calorific value was 14,217 KJ/kg.

2.
The thermogravimetric experiment showed that the pyrolytic characteristics of HR and ISW differed greatly: ISW pyrolyzed at 300-500 • C, while HR pyrolysis could be completed at 200-800 • C. The co-pyrolysis of HR and ISW was able to promote the forward pyrolytic reaction, and the weight loss rate reached 62% at 550 • C.

3.
During the co-pyrolysis of HR and ISW, the emission of gaseous heavy metals was relatively stable, and the concentration of heavy metals was slightly reduced. HR and ISW co-pyrolysis could effectively reduce dioxin emissions, and the formation of PCDD/Fs was mainly achieved via de novo synthesis. The toxic equivalent of dioxins in the flue gas after mixed pyrolysis decreased from 0.69 to 0.29 ng I-TEQ/Nm 3 . The higher S/C ratio could inhibit the formation of PCDD/Fs. After co-pyrolysis, the distribution of PCDD/Fs isomers in the flue gas had little effect, and PCDFs were the main isomers.