Removal of per- and polyfluoroalkyl substances and organic fluorine from sewage sludge and sea sand by pyrolysis

Hušek, Matěj; Semerád, Jaroslav; Skoblia, Siarhei; Moško, Jaroslav; Kukla, Jaroslav; Beňo, Zdeněk; Jeremiáš, Michal; Cajthaml, Tomáš; Komárek, Michael; Pohořelý, Michael

doi:10.1007/s42773-024-00322-5

Removal of per- and polyfluoroalkyl substances and organic fluorine from sewage sludge and sea sand by pyrolysis

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Published: 27 March 2024

Volume 6, article number 31, (2024)
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Removal of per- and polyfluoroalkyl substances and organic fluorine from sewage sludge and sea sand by pyrolysis

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Matěj Hušek^1,2,
Jaroslav Semerád³,
Siarhei Skoblia⁴,
Jaroslav Moško^1,2,
Jaroslav Kukla⁵,
Zdeněk Beňo⁴,
Michal Jeremiáš²,
Tomáš Cajthaml^3,5,
Michael Komárek⁶ &
…
Michael Pohořelý ORCID: orcid.org/0000-0001-8803-8131^1,2

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Abstract

Pyrolysis is one method for treating sewage sludge, particularly in remote areas or decentralised systems. The end product of pyrolysis, sludge-char, can serve as a soil improver. However, there is a lack of comprehensive data on the organic pollutants’ behaviour in sludge-char. In our work, we focused on the behaviour of per- and polyfluoroalkyl substances (PFASs). Sludge was pyrolyzed at 200–700 °C to determine the minimum safe temperature for effective PFASs removal. It is important to note that PFASs may not only be mineralized but also cleaved to unanalyzed PFASs and other organofluorinated substances. To address this issue, we incorporated additional measurements of organic fluorine in the experiment using combustion ion chromatography (CIC). Due to the inherent heterogeneity of sludge, containing a variety of pollutants and their precursors, we conducted pyrolysis on artificially contaminated sand. This allowed us to assess and compare the behaviour of PFASs in a homogeneous matrix. Based on our analyses, we determined that a temperature greater than 400 °C is imperative for effective PFASs and organic fluorine removal. The results were verified by analyzing samples from a commercial sludge pyrolysis unit at the Bohuslavice-Trutnov WWTP, which confirmed our measurements. In light of these results, it becomes evident that sludge pyrolysis below 400 °C is unsuitable for PFAS removal from sewage sludge.

Graphical Abstract

Highlights

The minimum temperature for significant PFASs and organic fluorine removal was 400 °C.
PFASs were part of primary pyrolysis gas: purification or combustion is necessary.
Contamination by PFASs and their congeners could be monitored with organic fluorine.

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1 Introduction

Per- and polyfluoroalkyl substances (PFASs) are persistent synthetic chemicals with more than 12,000 different species containing carbon–fluorine bonds (EPA 2021). This bond is one of the strongest in organic chemistry; therefore, PFASs are characterised by high chemical and thermal stability and environmental persistence (O’Hagan 2008; Stahl et al. 2011). Depending on the number of carbons in a molecule, PFASs are categorized into long-, short-, and ultrashort-chain groups (Ateia et al. 2019; Buck et al. 2011). PFASs find application in various industrial sectors, such as electroplating, electronics, plastics, firefighting foam, textile impregnation, semiconductors, sports equipment, and pipes due to their different properties, such as low surface tension, non-flammability, hydrophobicity, oleophobicity, or good thermal conductivity (Glüge et al. 2020). However, they can affect the human body's functioning, leading to cancer, changes in sperm quality, cholesterol production, or endocrine gland disruption (Fenton et al. 2021).

Their extensive use results in their spread through waste streams (mainly contaminated water and sewage sludge) into the environment (Munoz et al. 2022; Tavasoli et al. 2021), which can result in their presence in plants and the food chain (Ghisi et al. 2019; Ruan et al. 2015; Semerád et al. 2022). From the available data, the concentration of PFASs (represented by perfluorooctanesulfonic acid (PFOS) and perfluoro-n-octanoic acid (PFOA)) in sewage sludge varies considerably and has been measured in the range of 0.1–1191 ng g⁻¹ (PFOS) and 0.1–1517 ng g⁻¹ (PFOA), respectively (Hall et al. 2021). Even though some authors have already reported PFASs undergo biodegradation in soil (Horst et al. 2020; Zhang et al. 2022b), given their diverse types and the precautionary principle to protect the soil stock, food chain, and human health, we cannot only rely on the self-cleaning function of soil.

Thus, PFAS-containing sludge should not be used for direct material recovery (agriculture or composting) but treated to remove PFASs and other organic pollutants. From our perspective, thermal treatment methods, such as mono-incineration or pyrolysis, are ways of treating sludge to eliminate present organic pollutants (Hušek et al. 2022). Mono-incineration is a centralized solution for large quantities of sludge, while pyrolysis is more applicable in remote areas with annual sludge production greater than 500 t_DM. The resulting sludge-char (solid pyrolysis product) finds application in land reclamation as a soil improver, increases soil permeability and water retention, and serves as a medium- to long-term source of phosphorus (Hušek et al. 2022). However, the requirement is a low content of heavy metals in sludge, as they tend to concentrate in char (Mancinelli et al. 2016; Zhang et al. 2021). In the case of organic pollutants during pyrolysis, residence time and operating temperature are crucial (Buss 2021). However, there is currently still legislative distrust of pyrolysis persists due to the wide range of organic pollutants in sewage sludge and the lack of data on their removal, including PFAS (Huygens et al. 2019; Regulation (EU) 2019/1009).

Several authors have described PFAS behaviour and requirements for their removal in pyrolysis (oxygen-free atmosphere). According to Wang et al. (2022), PFASs’ thermal decomposition occurs in a gas phase or in/on solids depending on their ability to volatilize. Volatilization is affected by the presence of salts, heterogeneity and consistency of surface/matrix, and pyrolysis temperature. Thermal decomposition is influenced by the functional group and its non-fluorinated part of a chain (if present), the perfluorocarbons’ number, reactor type, and reaction atmosphere physicochemical properties. It is also generally affected by temperature, gas content, residence time, and gaseous and solid phases mixing rate (Wang et al. 2022). Alinezhad et al. (2021) highlighted the importance of hydrodefluorination in removing PFASs, temperature, reactor design, and residence time. During hydrodefluorination, the C–F bond is converted to a C–H bond, for which sufficient hydrogen is required. Simultaneously, hydrogen is one of the fluorine acceptors and acts as a reagent (catalyst) in the reaction (Winchell et al. 2021). Hydrogen enters the reaction from residual moisture and sludge composition (Moško et al. 2022, 2020). Decomposition is initiated by both end-chain and random-chain scission (Alinezhad et al. Full size image

Throughout the experiments, including the time before the reactor was placed into the oven and during the reactor’s cooling after the experiments, the inert carrier gas – helium – was continuously supplied to the bottom of the reactor at a constant flow rate of 150 ml min⁻¹. The off-gas from the reactor (mixture of carrier gas, condensing and non-condensing gases) subsequently passed through three ice-bath cooled im**ers containing acetone to trap the condensing part of the off-gas. The non-condensing part was not captured and analyzed. The experimental methodology was adopted and adjusted from our previous work Moško et al. (2021a). The most significant modification is using a steel reactor instead of a quartz reactor to prevent its destruction due to HF release.

2.4 Analysis of PFASs

Five different samples were analyzed for the presence of 37 different PFASs (Additional file 1: Table S1): sea sand, thermally treated sea sand, sewage sludge, sludge-char, and acetone solutions containing absorbed pyrolysis condensate. The PFASs analyzed represented their entire spectrum with respect to the chain length (long and short) and their substitutes (potassium-9-chlorohexadecafluoro-3-oxanonane-1-sulfonate (9Cl-PF3ONS), potassium-11-chloroeicosafluoro-3-oxaundecane-1-sulfonate (11Cl-PF3OUdS), NaDONA (sodium dodecafluoro-3H-4, 8-dioxanonanoate), and HFPO-DA (GenX)). The methodology for analyzing sea sand, sewage sludge, and sludge-chars is consistent with that used in our previous publication by Semerád et al. (2020).

2.4.1 Sample extraction and purification

The artificially contaminated sea sand, sewage sludge, and sludge-char were extracted using previously validated and published method (Semerád et al. 2020). Briefly, within the protocol, solid samples were freeze-dried, greatly homogenized, and extracted by pressurized liquid extraction (PLE) with three cycles of heated methanol (3–5 g, 150 °C and 1500 psi). Afterwards, the obtained extracts were purified using Supelclean™ ENVI-Carb™ columns according to the same publication. Liquid samples, pyrolysis condensates containing acetone as a solvent, were evaporated under a gentle stream of nitrogen and reconstituted in methanol. As in the case of solid sample extracts, these reconstitute condensates were purified equally using the SPE cleaning step prior to the LC–MS/MS analysis.

2.4.2 LC–MS analysis

The quantification of 37 representatives of PFASs has been achieved using the same method and instrumentation as in a previous publication focused on PFAS screening in various matrices (Semerád et al. 2020). Briefly: the LC–MS/MS system consisted of an LC Shimadzu Nexera X2 and Sciex 4500 mass spectrometer operating in negative mode. Targeted PFASs have been separated on a XSelect CSH C18 column (75 × 2.1 mm, 2.5 μm, Waters, USA) equipped with a pre-column. For each analysis, 5 µl of the sample was injected into a column heated to 40 °C, using a gradient elution with a flow rate of 0.6 ml.min⁻¹ and two solvents A: acetonitrile:formic acid (99.5:0.5) and B: water:acetonitrile:formic acid (79.5:20.0:0.5). The gradient was as follows (min, %A): 0, 80; 0.5, 80; 5, 10; 12, 10; 15, 5; 16, 0; 20, 0; 25, 80; 30, and 80. The detailed settings of the mass spectrometer and limits of detection/quantification are shown in Additional file 1: Tables S4a and S4b. Quality control has been introduced and followed the same structure used in a previous publication (Semerád et al. 2022) to achieve reliable results.

2.5 Fluorine content

Total fluorine (Additional file 1: Chapter S7) and organic fluorine have been determined by combustion ion chromatography (CIC). Total organic fluorine was determined using the direct combustion of solid samples (100 ± 1 mg) weighted into quartz. The organic fluorine was determined in organic extract or acetone condensate as follows. Methanol extract of solid materials obtained by PLE (5–10 g) (sewage sludge, sludge-char, or sand) or acetone condensate were concentrated under a gentle stream of nitrogen, transferred into quartz cups, evaporated to dryness and combusted in a combustion module Xprep C-IC (Trace Elemental Instruments) as solid samples. The gas flow rate was 300 ml.min⁻¹ for oxygen and 100 ml.min⁻¹ for argon. The temperatures of the furnaces were 750 and 1000 °C. As an absorption solution, 5 ml of hydrogen peroxide (100 mg.l⁻¹) in MQ water has been used. After the combustion, the Dionex™ ICS-5000 Ion Chromatography System (Thermo Scientific) with Dionex AG18 (4 × 50 mm) guard column and AS18 (4 × 250 mm) anion exchange column together with suppressed conductivity detection by an ADRS600 dynamically regenerated suppressor were used to determine the concentration of fluorides in absorption solution. The run time of the whole method was 30 min and consisted of elution at a flow rate of 1 ml.min⁻¹ and the following gradient: 0–1 min; 10 mM KOH; 1–4 min; from 10 to 23 mM KOH. The mobile phase was prepared by diluting 0.1 M KOH eluent concentrate for ion chromatography (Sigma-Aldrich). The data processing was performed using Chromeleon 7.3 (Thermo Scientific Inc.).

2.6 Data analysis, presentation, mass balance and energy distribution, gas composition, recovery rate, and removal efficiency

The LC–MS/MS data as well as the construction of the calibration curves used for ME determination, were processed by Analyst 1.6.3 software.

The mass balance and energy distribution of the process at 600 °C and gas composition are given in the Additional file 1: Chapter S5, Tables S5, S6, and S7 and Fig. S3, including comments.

The removal efficiency (RE) of PFASs and organic fluorine by pyrolysis was calculated according to Eq. (1).

$$RE=100*\left(1-\frac{{c}_{pyr}*{m}_{pyr}}{{c}_{sam}*{m}_{sam}}\right)$$

(1)

where RE is the removal efficiency in %; c_pyr is the concentration of the substance of interest (PFASs or organic fluorine) in a pyrolyzed sample in ng.g⁻¹_DM; m_pyr is the mass of the sample after pyrolysis in g; c_sam is the concentration of the substance of interest in a sample before pyrolysis in ng g⁻¹_DM, and m_sam is the mass of the sample before pyrolysis in g_DM.

2.7 Bohuslavice-Trutnov sludge-char properties and pollutants analysis

The ash content (A) and ultimate analysis in Table 6 were performed as with the sludge in Chapter 2.2. The PAHs were determined based on ČSN EN 16181, PCBs on ČSN EN 17322, AOX on ČSN EN 16166, pharmaceuticals and personal care products (PPCP), see Moško et al. (2021a). The methodology for determining the structural properties was adopted from our previous publication by Moško et al. (2021b) using ASAP 2020 and ASAP 2050 automated volumetric gas adsorption instruments (Micromeritics). The phosphorus content was determined according to Unified Work Procedures – SOP 62 A ÚKZÚZ by ICP-OES and converted to P₂O₅. The content of the individual heavy metals in Table 7 was established according to the standards: ČSN EN ISO 5961 – Cd, ČSN ISO 8288 – Pb, ČSN 46 5735 – Hg, ČSN EN ISO 15586 – As, and ČSN EN 1233 – Cr.

3 Results and discussion

The chapter is structured into three parts dealing with artificially contaminated sand, sewage sludge, and the commercial sludge pyrolysis unit of the Bohuslavice-Trutnov WWTP. Changes in the PFAS content are discussed against the measured values of organic fluorine. The third part includes an overview of commercial sludge-char’s physical and chemical properties and the current legislation in the Czech Republic that allows sludge-char use on land. The total input concentration of individual PFAS and their change in quantity contained in the solid residues and acetone trap** with temperature are provided in the Supplementary Information (Additional file 1: Chapter S6 – Tables S8, S9, S10, and S11).

3.1 Artificially contaminated sea sand

Sea sand was artificially contaminated with 24 different PFASs (Additional file 1: Table S1) and pyrolyzed at a temperature ranging from 200 to 700 °C. The pyrolysis products were analyzed for 37 different PFASs (Additional file 1: Table S1), where only those PFASs added to the input were detected.

3.1.1 PFAS

3.1.1.1 Solid sample

The initial PFASs contamination in sand 2,000 ± 99.7 ng g⁻¹_DM gradually decreased to 8.3 ± 1.4 ng g⁻¹_DM at 400 °C (Table 1 and Additional file 1: Table S8), indicating direct proportionality to temperature. The removal efficiency of the PFASs analyzed ranged from 2.2 % (200 °C) to ≥ 99.6 % at 400 °C and higher.

Table 1 PFASs concentration in sand, pyrolyzed sand, acetone, and removal efficiency

Full size table

Of all PFASs, n-methyl-perfluoro-1-butane sulphonamide (MeFBSA) and perfluorooctane sulfonamide (FOSA) were the fastest reduced (Additional file 1: Table S8). HFPO-DA (GenX) minimizes faster than perfluorohexanoic acid (PFHxA) with the same number of perfluorinated carbons, indicating lower chain stability, probably related to the presence of a foreign group (HFPO-DA (GenX) – ether) (Sasi et al. 1: Table S9). McNamara et al. (2022) proposed the PFOS degradation pathway during pyrolysis as PFOS – perfluoro-n-heptanoic acid (PFHpA) – perfluoro-n-hexanoic acid (PFHxA) – perfluoro-n-pentanoic acid (PFPeA) – PFBA. At 400 °C, when PFOS content significantly decreased, the amount of the mentioned PFCAs in acetone increased. Overall, representatives from the FASAs group were detected in the acetone solution with the highest content (Additional file 1: Table S9).

After accounting for changes in the individual PFAS contents of both pyrolysed sand and the acetone solution, along with their standard deviations, an increase in the amount of PFHxA, PFOA, PFNA, EtFOSA, and 7:3 FTA was observed at 200 °C and PFHpS at 200 °C and 300 °C (Additional file 1: Tables S8 and S9). Since the sea sand initially lacked the analysed PFAS and organofluorine before contamination (Tables 1 and 2), any observed increases can be attributed to the formation from the PFASs present. For example, PFCAs’ thermal decomposition leads to forming intermediates and PFCAs with shorter chains (Sasi et al. 1), the organofluorines (breakdown products of the PFASs analyzed) persisted in the acetone solution.

3.2 Sewage sludge

The total concentration of PFASs in the analyzed sludge was 203.9 ± 21.5 ng.g⁻¹_DM, with the highest initial concentration observed for PFOS at 166.7 ± 15.2 ng.g⁻¹_DM (Additional file 1: Table S10). Since the Czech Republic does not have a limit for PFASs in sludge, the sludge can be used on agricultural land if the applicable legislative limits are met (see Hušek et al. (2022)). In contrast, Germany has set a PFAS limit of 100 ng.g⁻¹_DM (the sum of PFOS and PFOA) (Röhler et al. 2021), and based on this criterion, our tested sludge would not meet the standards for use on German agricultural land.

3.2.1 PFAS

3.2.1.1 Solid samples (sludge-char)

Out of 37 analyzed PFASs (Additional file 1: Table S1), 18 were detected in the sludge and pyrolysis products (Additional file 1: Table S10). The initial concentration of PFASs in the sludge was 203.9 ± 21.5 ng.g⁻¹_DM (Table 3), with a significant presence of PFOS (most notable), FOSA, fluorinated telomer acid (5:3) (5:3 FTA), and 8:2 FTS (Additional file 1: Table S10). The PFASs content in the sludge-char varied with increasing temperature and, at 500 °C, fell below the LOQ. A removal efficiency of over 99 % for the studied PFASs was already achieved at 400 °C.

Table 3 Average concentrations of PFASs in sewage sludge, sludge-char, and acetone

Full size table

The most stable PFAS in char was PFOS, along with representatives of the FTSAs group (fluorinated telomer sulfonate (FTS): 6:2, 8:2, and 10:2). PFOS has high thermal stability (**, condensed, and trickled into im**er. PFAS could thus be captured in the condensate, along with which they entered the acetone. Conversely, the pi** remained dry during sand pyrolysis.

PFASs contraction peaked at 300 °C and 400 °C. From 500 °C, there was a substantial decrease in the amount of PFAS in acetone, indicating their cleavage or mineralization. Among all the analyzed PFAS, only three were trapped in the acetone: PFHxA, FOSA, and 5:3 FTA (Additional file 1: Table S11). All three PFASs exceeded their input levels. Except for PFHxA at 200 °C, a similar increase was not observed during sand pyrolysis, indicating the likely formation of these PFASs from their precursors and other unanalyzed PFAS present in the sludge.

The overall increase above the PFASs input value was observed at 300 °C, as indicated in Table 3 under the total residual sum. We attributed this phenomenon to the PFASs formation resulting from the cleavage of PFASs unanalysed and their precursors (Aro et al. 2021; Zhang et al. 2022a, b; Zhang and Liang 2021).

3.2.2 Organic fluorine content of solid samples

The organic fluorine content consistently decreased with increasing temperature, drop** from the original concentration of 62.9 ± 8.8 ng.g⁻¹_DM to below LOQ above 400 °C (Table 4). Consequently, neither analysed PFASs nor organic fluorine were detected in our laboratory's pyrolysed sludge above 400 °C, ideally reaching 500 °C. The total fluorine removal after conversion to the inorganic state is provided in Additional file 1: Table S13.

Table 4 Average concentrations of (organic) fluorine in sewage sludge, sludge-char, and acetone

Full size table

3.2.3 Total fluorine content of condensates in acetone

The fluorine content increased with temperature and reached high levels in the acetone compared to the original organic fluorine value of the sludge (Table 4). In this context, we cannot speak specifically about organic fluorine capture but rather of total fluorine (organic and inorganic) trapped in the acetone. Unlike the sea sand, which did not contain fluorine before PFAS application, the sludge contained both fluorine forms. Organic and inorganic fluorine compounds were absorbed in condensate or/and trapped in the acetone, resulting in an increase above the input value.

3.3 WWTP Bohuslavice-Trutnov sludge-char

The commercial sludge pyrolysis unit (PYREG P500 KSF) at the WWTP Bohuslavice-Trutnov – 52,000 PE (Additional file 1: Fig. S1) was put into trial operation in 2020 and approved on October 22, 2021. Sludge is dried in a low-temperature dryer and pyrolyzed at 600 °C for at least 10 min. After leaving the pyrolyzer, primary pyrolysis gas is incinerated in a combustion chamber at 1000–1100 °C (Fuka et al. 2021). The annual capacity of the dryer-pyrolyzer system in use is 3,000 tonnes of mechanically dewatered sludge.

3.3.1 PFASs and organic fluorine removal

Dry sludge and sludge-char were analyzed using the same methods as the other samples tested. Of the 37 PFASs analyzed, 14 were detected. The PFASs concentration in the dry sewage sludge was 100.6 ± 12.0 ng.g⁻¹ and decreased under LOQ after pyrolysis (Table 5). The results are consistent with laboratory-scale analyses: above 500 °C in char and sand, the analyzed PFASs content was below LOQ.

Table 5 PFASs content in dry sludge and sludge-char from Bohuslavice-Trutnov WWTP (in dry matter)

Full size table

The organic fluorine content of the sludge was as high as PFASs, indicating the presence of other substances, such as PFASs (unanalyzed and precursors), pharmaceuticals, or agrochemicals. After pyrolysis in a commercial unit, the sludge-char contained organic fluorine below the LOQ. The sample analyzed showed a similar behaviour to samples prepared under laboratory conditions.

3.3.2 Bohuslavice–Trutnov sludge-char: properties and legislation

The properties of the Bohuslavice–Trutnov sludge-char are listed in Table 6, and the methodology for their determination is available in Chapter 2.7. Our previous papers described the impact of temperature on sludge-char quality, including porosity and H/C ratio (Moško et al. 2021b), organic pollutants content (Moško et al. 2021a), and primary pyrolysis gas energy yield (Moško et al. 2020). Temperatures above 500 °C (ideally at the rated output above 600 °C) can be considered sufficient to influence all these variables positively.

Table 6 Properties of sludge-char from Bohuslavice-Trutnov WWTP (in dry matter)

Full size table

Regarding European Union legislation, the use of sludge-char as a soil improver is currently not supported due to the lack of information on removing organic pollutants (Huygens et al. 2019; Regulation (EU) 2019/1009). However, this regulation does not impact the internal markets of the Member States (Regulation (EU) 2019/1009). In the Czech Republic, the legislation on fertilizers changed on November 1, 2021, (Regulation No. 474/2000 Coll. 2021), and the use of sludge-char on land becomes possible if the legislative limits are met (Table 7), the char obtains necessary registration, and end-of-waste status.

Table 7 Czech legislative pollutants limits for sludge-char used in agriculture land and their content in sludge-char produced at the Bohuslavice-Trutnov WWTP (in dry matter) (Regulation No. 474/2000 Coll.)

Full size table

Sludge-char from Bohuslavice-Trutnov WWTP was registered as a soil improver by the Central Institute for Supervising and Testing in Agriculture of the Czech Republic on March 7, 2022 (UKZUZ 2022). On July 4, 2022, the regional authority removed Bohuslavice sludge-char from the waste catalogue and transferred it to the end-of-waste status (KUKHK 2022).

4 Conclusion

Pyrolysis at 400 °C and above effectively removes monitored PFASs, a finding validated under both laboratory and operational conditions. Conversely, torrefaction and pyrolysis below 400 °C are unsuitable for PFASs removal. Due to the large number of different PFASs, it is advisable to include the analysis of organic fluorine. Organic fluorine includes all PFASs, regardless of functional group, and other fluorine-containing substances such as agrochemicals and certain pharmaceuticals. In our experiments, the organic fluorine content was significantly removed from solid samples from 400 °C onwards, which is in line with the results for PFASs removal.

The amount of PFASs and organic fluorine also changed with temperature in the primary pyrolysis gas trapped in acetone, indicating the capability to evaporate at the expense of the remaining content in the char and sand. This was combined with the short residence time of the primary pyrolysis gas, which was insufficient to destroy the PFASs inside the reactor. Based on these facts, in commercial sludge pyrolysis units, in addition to sufficient heat and appropriate reactor design (residence time), the produced gas must be cleaned or treated in a combustion chamber where the remaining PFASs, organic fluorine, and other organics are oxidized (decomposed).

Due to the diverse range of contaminants, including PFASs, and the sludge-char quality, the minimum operating temperature of a commercial sludge pyrolysis unit should be above 500 °C at a rated output above 600 °C and the residence time of the sludge/sludge-char in the pyrolyzer should be at least 10 min. The resultant sludge-char can be used as a soil improver but will always contain a certain amount of heavy metals concentrated from the sludge. Therefore, usage should be restricted to areas outside of food production, such as land reclamation, green areas, and parks. Further research directions should lead to verifying our results by measuring organic fluorine in other commercial sludge pyrolysis units operating under the above-mentioned conditions and starting a discussion on setting limits for organic fluorine as a new general limit for waste-based materials.

Data availability

The datasets used or analyzed during the current study are available in Supplementary Information and from the corresponding author on reasonable request.

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Acknowledgements

We would like to thank the supporting institutions. Grants from the Ministry of Agriculture of the Czech Republic (QK21020022); Czech Academy of Sciences (AV 21 – Sustainable energy); Technology Agency of the Czech Republic (project No. SS02030008); and University of Chemistry and Technology, Prague (No. A1_FTOP_2024_001 and A2_FTOP_2023_015). Direct funding from the Faculty of Environmental Technology, University of Chemistry and Technology, Prague; Faculty of Science, Charles University; Institute of Microbiology and Institute of Chemical Process Fundamentals, Czech Academy of Sciences; and Faculty of Environmental Sciences, Czech University of Life Sciences Prague.

Funding

This work was supported by the Ministry of Agriculture of the Czech Republic – project QK21020022, Czech Academy of Sciences AV 21 – Sustainable energy, and Specific university research grant No. A1_FTOP_2024_001 and A2_FTOP_2023_015. The work was also supported by the Technology Agency of the Czech Republic (project No. SS02030008, program: Prostředí pro život).

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Institute of Chemical Process Fundamentals, The Czech Academy of Sciences, Rozvojová 1/135, Suchdol, 165 00, Prague 6, Czech Republic
Matěj Hušek, Jaroslav Moško & Michael Pohořelý
Department of Power Engineering, Faculty of Environmental Technology, University of Chemistry and Technology, Prague, Technická 5, 166 28, Prague 6, Czech Republic
Matěj Hušek, Jaroslav Moško, Michal Jeremiáš & Michael Pohořelý
Institute of Microbiology, The Czech Academy of Sciences, Vídeňská 1083, 142 20, Prague 4, Czech Republic
Jaroslav Semerád & Tomáš Cajthaml
Department of Sustainable Fuels and Green Chemistry, Faculty of Environmental Technology, University of Chemistry and Technology, Prague, Technická 5, 166 28, Prague 6, Czech Republic
Siarhei Skoblia & Zdeněk Beňo
Institute for Environmental Studies, Faculty of Science, Charles University, Benátská 2, 128 01, Prague 2, Czech Republic
Jaroslav Kukla & Tomáš Cajthaml
Department of Environmental Geosciences, Faculty of Environmental Sciences, Czech University of Life Sciences Prague, Kamýcká 129, Suchdol, 165 00, Prague, Czech Republic
Michael Komárek

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Matěj Hušek
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Jaroslav Semerád
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Siarhei Skoblia
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Jaroslav Moško
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Zdeněk Beňo
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Michal Jeremiáš
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Tomáš Cajthaml
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Michael Komárek
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Michael Pohořelý
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Contributions

Matěj Hušek: writing-original draft, investigation, visualization, validation, formal analysis, resources; Jaroslav Semerád: methodology, validation, formal analysis, investigation, resources; Siarhei Skoblia: methodology, validation, formal analysis Jaroslav Moško: validation, visualization, writing-review and editing; Jaroslav Kukla: methodology, validation, formal analysis; Zdeněk Beňo: methodology, validation, formal analysis; Michal Jeremiáš: validation, visualization, writing-review and editing; Tomáš Cajthaml: writing-review and editing, project administration, funding acquisition; Michael Komárek: writing-review and editing, project administration, funding acquisition; Michael Pohořelý: conceptualisation, writing-review and editing, supervision, project administration, funding acquisition, resources.

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Correspondence to Michael Pohořelý.

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Handling editor: Hailong Wang

Supplementary Information

Additional file 1: Figure S1.

Map with the location of WWTP Bohuslavice (map source: Mapy.cz). Figure S2. FTIR analysis of sewage sludge and sludge-char. Figure S3. Main gaseous species in non-condensable pyrolysis gas. Table S1. Summary of analysed PFASs (asterisked artificial contaminants for sea sands). Table S2. Selected physical and chemical properties of sewage sludge (in dry matter). Table S3. Elementary analysis of sewage sludge. Table S4a. Detailed settings of the mass spectrometer and limits of detection/quantification. Table S4b. Detailed settings of the mass spectrometer and limits of detection/quantification. Table S5. Mass balance of the sludge pyrolysis and distribution of energy of the sludge among the products. Table S6. Complex compositions of non-condensable pyrolysis gas. Table S7. Main gaseous sulphur compounds in non-condensable pyrolysis gas; expressed as a gram of S per m⁻³. Table S8. PFASs concentration [ng.g.⁻¹] and amount [ng] in sea sand and pyrolyzed sand (average). Table S9. PFASs amount [ng] in acetone from artificially contaminated sea sand pyrolysis (average). Table S10. PFASs concentration [ng.g.⁻¹] and amount [ng] in sewage sludge and sludge char (average). Table S11. PFASs amount [ng] in acetone from sewage sludge pyrolysis (average). Table S12. Change in total fluorine content of sea sand samples. Table S13. Change in total fluorine content of sewage sludge samples. Table S14. Total fluorine content – pyrolysis unit Bohuslavice Trutnov WWTP.

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Hušek, M., Semerád, J., Skoblia, S. et al. Removal of per- and polyfluoroalkyl substances and organic fluorine from sewage sludge and sea sand by pyrolysis. Biochar 6, 31 (2024). https://doi.org/10.1007/s42773-024-00322-5

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Received: 09 October 2023
Revised: 07 March 2024
Accepted: 10 March 2024
Published: 27 March 2024
DOI: https://doi.org/10.1007/s42773-024-00322-5

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Removal of per- and polyfluoroalkyl substances and organic fluorine from sewage sludge and sea sand by pyrolysis

Abstract

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1 Introduction

2.4 Analysis of PFASs

2.4.1 Sample extraction and purification

2.4.2 LC–MS analysis

2.5 Fluorine content

2.6 Data analysis, presentation, mass balance and energy distribution, gas composition, recovery rate, and removal efficiency

2.7 Bohuslavice-Trutnov sludge-char properties and pollutants analysis

3 Results and discussion

3.1 Artificially contaminated sea sand

3.1.1 PFAS

3.1.1.1 Solid sample

3.2 Sewage sludge

3.2.1 PFAS

3.2.1.1 Solid samples (sludge-char)

3.2.2 Organic fluorine content of solid samples

3.2.3 Total fluorine content of condensates in acetone

3.3 WWTP Bohuslavice-Trutnov sludge-char

3.3.1 PFASs and organic fluorine removal

3.3.2 Bohuslavice–Trutnov sludge-char: properties and legislation

4 Conclusion

Data availability

References

Acknowledgements

Funding

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Supplementary Information

Additional file 1: Figure S1.

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