Scholarly article on topic 'Assessment of Food Processing and Pharmaceutical Industrial Wastes as Potential Biosorbents: A Review'

Assessment of Food Processing and Pharmaceutical Industrial Wastes as Potential Biosorbents: A Review Academic research paper on "Chemical sciences"

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Academic research paper on topic "Assessment of Food Processing and Pharmaceutical Industrial Wastes as Potential Biosorbents: A Review"

Hindawi Publishing Corporation BioMed Research International Volume 2014, Article ID 146769, 24 pages http://dx.doi.org/10.1155/2014/146769

Review Article

Assessment of Food Processing and Pharmaceutical Industrial Wastes as Potential Biosorbents: A Review

Hanan E. M. El-Sayed1,2 and Mayyada M. H. El-Sayed3,4,5

1 Mechanical Engineering Department, National Research Centre, Al Bohooth Station, Dokki, Giza 12622, Egypt

2 Civil and Environmental Engineering Department, University of Windsor, 401 Sunset Avenue, Windsor, ON, Canada N9B3P4

3 Chemical Engineering Department, National Research Centre, Al Bohooth Station, Dokki, Giza 12622, Egypt

4 Chemistry Department, American University in Cairo, AUC Avenue, P.O. Box 74, New Cairo, Cairo, Egypt

5 University of Maryland, Baltimore County (UMBC), 252 TRC Building, 5200 Westland Boulevard, Baltimore, MD 21227, USA

Correspondence should be addressed to Mayyada M. H. El-Sayed; mayyada@aucegypt.edu Received 28 February 2014; Revised 3 June 2014; Accepted 3 June 2014; Published 7 July 2014 Academic Editor: Qaisar Mahmood

Copyright © 2014 H. E. M. El-Sayed and M. M. H. El-Sayed. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

There is a growing need for the use of low-cost and ecofriendly adsorbents in water/wastewater treatment applications. Conventional adsorbents as well as biosorbents from different natural and agricultural sources have been extensively studied and reviewed. However, there is a lack of reviews on biosorption utilizing industrial wastes, particularly those of food processing and pharmaceuticals. The current review evaluates the potential of these wastes as biosorbents for the removal of some hazardous contaminants. Sources and applications of these biosorbents are presented, while factors affecting biosorption are discussed. Equilibrium, kinetics, and mechanisms of biosorption are also reviewed. In spite of the wide spread application of these biosorbents in the treatment of heavy metals and dyes, more research is required on other classes of pollutants. In addition, further work should be dedicated to studying scaling up of the process and its economic feasibility. More attention should also be given to enhancing mechanical strength, stability, life time, and reproducibility of the biosorbent. Environmental concerns regarding disposal of consumed biosorbents should be addressed by offering feasible biosorbent regeneration or pollutant immobilization options.

1. Introduction

Increased industrial activities resulted in major environmental problems; one of the most challenging is water pollution and the subsequent scarcity in fresh and clean water resources available for current and future generations. Industrial wastewater contains various toxic compounds such as organics, heavy metals, and dyes which could have potential detrimental effect on human beings and aquatic lives. World Health Organization (WHO) recommended the maximum acceptable concentrations for these compounds in water streams. Dyes are one of the most polluted groups as their complex aromatic structure makes them difficult to be biologically degradable [1-3]. They are produced from different industries in large amounts such as textile, paper, leather, food, cosmetics, and pharmaceuticals. It has recently

been reported that dye production reached 700,000 tons/year worldwide [4]. Dyes are classified into anionic (direct), cationic (basic), acid and reactive, and nonionic (disperse) dyes [5]. Phenols and phenolic compounds are very toxic and of potential harm to human health. Even at very low concentration (0.005 mg/L), phenols could be of significant odor and taste if present in drinking water [6]. Many industries represent the main sources of phenols such as iron and steel, petroleum, paint, paper and pulp, and pharmaceutics. Nitrophenols and chlorophenols are considered the most hazardous phenolic compounds. Heavy metals are another hazardous group of pollutants. Lead, mercury, cadmium, chromium, copper, and arsenic are examples of the most toxic and carcinogenic elements that can exist in industrial effluents. Metal ions accumulate and their amounts are increased along the food chain due to their nonbiodegradable feature

[7, 8]. The main industrial sources of most of these metals are metal finishing and plating, automotive, semiconductor manufacturing, textile, and steel industry.

Removal of such pollutants from different industrial effluents may be achieved physically, chemically, or biologically. Physical processes include adsorption, chelation ion exchange, membrane filtration, and coagulation. Chemical methods include oxidation or advanced oxidation and electrochemical treatment, whereas biological methods could be aerobic, anaerobic, or enzymatic [8-10]. These processes known as conventional treatment methods have several disadvantages mainly, high energy requirements and capital cost and low efficiency. Conventional treatment methods have been extensively reviewed elsewhere [3, 9, 11-13]. Recently, numerous approaches have been proposed by many researchers for the development of nonconventional and low-cost adsorbents.

Biosorption has become an attractive common technique for many reasons. Being a cost-effective, highly efficient, and easily implemented method made it a successful alternative for the conventional ones [14]. Biosorption as a process may be simply defined as an adsorption on the surface of a compound of a biological origin. Being not limited to only one mechanism and also not restricted to a specific type of pollutant offers a wide variety of applications like pollution control, element recycle, and recovery [10]. A biosorbent may be considered "low-cost" if it satisfied the following conditions: (i) abundance in nature, (ii) requirement for minor or no treatment, and (iii) being a waste material or a by-product from other industries [10]. The challenge here is to choose the appropriate biosorbent that suits the target substance. Selection criteria include, but are not limited to, nature of substance to be adsorbed, mechanism involved in the biosorption process, effectiveness of such biosorbent, cost associated with the whole process, and the possibility of biosorbent regeneration for multiple use cycles. Numerous reviews have been reported on the utilization of agricultural-based, dead or living biomass, and natural adsorbents for the removal of dyes [15-21] and heavy metals [22-28]. Few research studies have focused on the removal of organic pollutants, phenols and phenolic compounds, and pesticides using different biosorbents [29-34].

Disposal of different industrial wastes and by-products is considered a major environmental problem. The cost associated with the waste treatment or disposal, transport, and accumulation may sometimes be the most challenging problem in industry. Such problem increases especially in food industries which produce huge amount of wastes and by-products. Utilizing industrial wastes as low-cost effective biosorbents introduces a bifunctional solution from an environmental point of view. That is to say, treating wastewater effluents with these zero-cost waste materials adds value to these wastes while help solving an important environmental issue.

This paper reviews the state-of-the-art endeavors in utilizing industrial food processing and pharmaceutical wastes as effective low-cost biosorbents for water/wastewater treatment. The aim is to assess the potential of these wastes as biosorbents as well as highlight new options to be further

explored and possibilities for improvement. To the best of the authors' knowledge, research dedicated to these particular types of waste has not been reported elsewhere. A comprehensive critical review is presented on (i) the different biosorption techniques and mechanisms, (ii) controlling factors, (iii) equilibrium and kinetics studies, and (iv) recovery and/or pretreatment options. Moreover, concluding remarks will be given at the end along with some suggestions for future work.

2. Sources and Applications of Biosorbents

Adsorption as a process gained much more attention recently after the use of low-cost adsorbents became so popular especially biosorbents [24, 35]. Sources of different types of conventional and nonconventional adsorbents are illustrated in the flow chart in Figure 1.

Biosorbents are a large subclass of low-cost adsorbents that can be subdivided into [36] biomass (dead or living), agricultural wastes, and industrial solid wastes. Dead biomass has been utilized by many researchers as an effective biosor-bent for the removal of different pollutants [37, 38]. It has been favored due to its viability to be applied in presence of toxic substances or with shortage of nutrients without this causing appreciable impact on its sorption efficiency. In addition, dead biomass is more readily desorbed than its living counterpart. Living biomasses including fungi [39,40], algae [41, 42], and other microbial cultures with different strains [43, 44] were also used as low-cost biosorbents. Agricultural-based biosorbents represent a large category of wastes that attracted the attention of many researchers worldwide Utilization of such wastes depended on their local availability. Researchers utilized rice husk and straws [4548], different nut shells [49-51], fruit and vegetable peels or leaves [52-55], wheat bran [56], chitin and chitosan [57-60], and many other wastes of agricultural origin. Applications of industrial solid wastes in biosorption included the use of sludge whether municipal (sewage) [61] or activated sludge produced from different biological processes [62-66].

Less research has been done on industrial food processing and pharmaceutical wastes despite their huge annual worldwide production. Scarcity of relevant reviews was therefore the main motivation of this current work. Biosorbents from these origins are expected to grow by an annual rate of around 5% in the next few years [67]. For example, food processing waste produced annually in Europe has been reported to be about 2.5 x 108 tons [67]. About 20-60% of the processed fruits and vegetables by volume are generated as waste materials. In the United States, the food manufacturing sector is producing a huge amount of food waste; about 44.3 billion pounds have been reported as per the year 2011 [68].

Utilizing these wastes as biosorbents has been applied in the area of water purification and/or wastewater treatment; previous work in this regard is summarized in Table 1. The table presents type and industrial source of the biosorbent, nature of feed solution, type of targeted sorbate, and operating parameters at which maximum removal was attained. These parameters are pH, temperature, adsorbent dose, and

Adsorbents

Conventional

Activated carbon

Silica gel

Natural materials

Living biomass

Zeolites and

other siliconeous materials

Dead biomass

Other microbial cultures

Agricultural solid waste Industrial solid waste

Fibers

Leaves

Food processing and pharma

Fruit peels

Rice straw

Wheat barn

Sludge

Sewage sludge

Activated sludge

Miscellaneous adsorbents

Starch

Red mud

„Fermentation waste

Fly ash

Figure 1: A schematic flow diagram showing the different types of available adsorbents.

the contact time that was required to reach equilibrium. In addition, mode of operation (batch or column) and its corresponding maximum % removal are included in the table. For column systems, the flow rate (F) is also given. Wastes from beverages, tea or coffee, beer or wine, and brewery grains, were used as biosorbents for the removal of many heavy metals and dyes from aqueous solutions [69-83]. Excellent removal efficiencies of up to 99.83% for Cd and 98% for dye sorption onto yeast beer waste [80] and brewery grain wastes [76] were reported. Using beer brewery diatomite waste was recommended for wastewater treatment applications. This is because it released less COD in the industrial wastewater than did the fresh diatomite [81]. Food processing wastes from canning industries were also utilized for the removal of different dyes and heavy metals [84-89]. One particular study was undertaken on real textile wastewater having COD of 426 mg/L, and 97.68% dye removal was achieved when the wastewater sample was spiked with 1mg/L dye [90]. Studies on the effect of several operating conditions on biosorption performance were also conducted. Results yielded removal efficiencies that reached up to 96.4% for the removal of Cd (II) in case of using okra waste [88] and sugar bagasse waste [89]. Wastes from fruit sources especially orange, mango, and pectin-rich fruits were obtained from juice, jam [91-99], and coconut milk industries [100]. Orange peel [92] and wastes [95] were very effective in removing heavy metals, namely, Pb (II) and Cd (II), with efficiencies of 99.5% and 98%, respectively.

A number of researchers in the Mediterranean countries (Turkey, Spain, Italy, etc.) were interested in olive oil wastes since these countries are among the world's biggest olive producers. All types of wastes from olive oil industry such as pomace, pulp, stones, and milling sludge were used for the sorption of heavy metals and dyes from solutions [101110]. Particular work [101] reported almost 100% removal efficiency for Cr (VI) from aqueous solutions using olive pomace. Only one study was found to deal with phenol removal [110] using olive oil pomace and removal efficiency was above 90% in both batch and column modes. In another study that investigated the potential of olive oil mill residues as biosorbents for Cu (II), COD release was reduced to 600 mg/L when the biosorbent was washed twice while sorption performance was not affected [104]. Other work utilized different oil industrial wastes such as palm oil waste [111] or sunflower oil waste [112] in the removal of dyes and heavy metals from aqueous solutions.

Commercial activated carbon has been a very common method of adsorption for a long time. Research is now shifted toward using activated carbon derived from various agricultural as well as industrial sources. In the current review, only activated carbons manufactured from food processing wastes are reported. The method of deriving activated carbon (AC) from these wastes will be explained later in the pretreatment section. AC derived from different industrial waste sources such as olive waste cake [113], empty fruit bunch from palm oil mill [114], tea industry [115], and sago waste [116] was

Table 1: Summary of the different industrial food processing and pharmaceutical waste biosorbents; their sources, applications, and the relevant biosorption parameters.

Type of hiosorhent Source of biosorbent Feed solution Sorbate PH Contact time, min Temperature, ° C Initial concentration of sorbate, mg/L Mode of operation Maximum %removal Biosorbent dose Reference

Mohan breweries and AG25 acid dye of commercial name Alizarin Cyanin Green G

Spent brewery grains (SBG) distilleries Limited, Chennai, India Synthetic dye solution 3.0 75 30 90 Batch 98 0.2 [70]

Tea industry waste Local tea factory in China Aqueous synthetic solution Cd(II) 7.0 180 25 20 Batch 90 5 [72]

Exhausted coffee waste Soluble coffee manufacturer, Catalonia, Spain Aqueous synthetic solution Cr(VI) Cu(II) Ni(II) 3.0 8640 25 1000 Batch - 6.67 [77]

Sugarcane bagasse waste From local alcohol and sugar Industries, City of Ouro Preto, Minas Gerais, Brazil Aqueous synthetic solution Methylene Blue (MB) Gentian Violet 7.0 600 900 25 200 300 Batch - 0.2 [78]

Wine processing waste sludge (WPWS) Ilan Wine-Processing Company, Ilan, Taiwan Aqueous synthetic solution Crttll, IV) 2.0 240 30 100 Batch 36 10 [73]

Wine processing waste sludge (WPWS) Ilan Wine-Processing Co., Ilan, Taiwan Aqueous synthetic solution Ni(II) 5.5 120 50 30 Batch 75 12 [76]

Grape bagasse waste residue Wine production process, Styria region, Austria Effluent from research laboratory Cd(II) Pb(II) 7.0 3.0 45 25 100 Batch - 0.67 [79]

Waste beer yeast Aoke Beer Company in Zhengzhou, Henan province, China Aqueous synthetic solution Cu(II) Pb(II) 5.0 30 20 9.14 32.23 Batch - - [69]

Waste beer yeast Saccharomyces cerevisiae Beer fermentation industry, brewery located near Chennai, India Electroplating effluents Cr(VI) 5.0 120 - - Batch - 0.02 [74]

Suspended brewery yeast waste biomass (SBW) Brewery waste biomass collected from CIUC brewery, Miercurea-Ciuc, Romania Synthetic aqueous solution Cd(II) 5.5 40 50 6 Batch 99.83 9.78 [80]

Beer brewery diatomite waste (SDE) Shan-Hua factory, Tobacco and Liquor Co., TainanTaiwan Synthetic aqueous solution Industrial wastewater from local factory Methylene Blue (MB) basic dye 7.0 1440 25 2.5 Batch - 0.25 [81]

Spent waste beer yeast Saccharomvces cerevisiae Fermentor at a brewery, Chennai, India Battery manufacturing industrial effluent Pb(II) 5.0 120 30 100 Batch - - [82]

Fresh malted sorghum mash waste local malted sorghum beer (pito) brewer at Navrongo, Ghana Synthetic aqueous solution Methylene Blue (MB) basic dye 7.0 18 33 ± 1 50 Batch >90 4 [83]

Brazilian alcoholic beverage

Waste biomass from sugarcane aguardente production, (Lapinha, Bocaiana, Germana and Stainless steel effluent Cr(VI) Fe(III) 4.0 180 25 50 660 Batch 70 50 1 [75]

Taboroa) State of Minas Gerais, Brazil Ni(II) 20 20

Type of biosorbent Source of hiosorhent Feed solution Sorbate pH Contact time, min Temperature, ° C Initial concentration of sorbate, mg/L Mode of operation Maximum %removal Biosorbent dose Reference

Waste biomass Cacha^a Brazilian alcoholic beverage the stillage generated by a liquor distillery (Germana), Minas Gerais, Brazil Stainless steel industrial effluent from Acesita Co., Brazil Fe(III) Ni(II) Cr(VI) 4.0 180 25 7.8 2.7 600 Batch 94 57 25 2 [71]

Rh izop us o ligosp or us biomass Food processing wastewaters Aqueous synthetic solution Cu(II) 5.0 120 30 100 Batch 70 1 [85]

Waste biomass of Phaseolus vulgaris L. A residual hiomass of a

canned food factory in Bartin, Turkey Aqueous synthetic solution Pb(II) 5.0 20 20 100 Batch 92 4 [84]

Waste biomass of Phaseolus vulgaris L. A residual hiomass of a local canned food plant, Turkey Aqueous synthetic solution Textile Reactive Red dye (RR 198) 2.0 20 20 100-300 Batch 99.3 1.6 [86]

Cupuassu shell, Theobroma grandiflorum, (CS) Food residue from jelly industry Belem-PA, Brazil Aqueous synthetic solution Reactive Red dye (RR 194) Direct Blue 53 2.0 480 1080 25 50 Batch - 2.5 [87]

Okra food industrial waste Food waste from food canning processes Aqueous synthetic solution Cd(II) Fe(II) Zn(II) - 90 - 20 Batch 96.4 93.8 79.8 1 [88]

Sugar industrial waste (bagasse waste) Obtained from food canning processes Aqueous synthetic solution Cd(II) Fe(II) - 90 - 20 Batch 96.4 93.8 1 [89]

Pineapple peel, an agricultural effluent Food can processing industries Aqueous synthetic solution Methylene Blue (MB) cationic dye 6.0 400 30 300 Batch 47 1.5 [91]

Waste baker's yeast biomass Pakmaya Yeast Company Izmir, Turkey Aqueous synthetic solution Cd(II) Pb(II) 6.0 5.0 180 30 25 Batch 60 70 1 [131]

Desiccated coconut waste sorbent (DCWS) By-product of Coconut Milk Processing Aqueous synthetic solution Hg(II) 7.4 2880 400 30 50 100 Batch Column - 1 F = 4 mL/min [100]

Acid Blue 74 500 1000 500 10 F = 3 mL/min

Pecan nut shells (C. illinoinensis) biomass Biomass from food factories, Nuevo Leon, Mexico Aqueous synthetic solution (AB74) Reactive Blue 4 (RB4) Acid Blue 25 (AB25) 6.5 30 100 Batch Column [132]

Orange peel Solid waste from local fruit juice industries, Egypt Aqueous synthetic solution Pb(II) Cu(II) Cd(II) 5.0 30 25 20 Batch 99.5 89.57 81.03 4 [101]

Agrumexport, S.L., an

Orange (Citrus sinensis) waste orange juice manufacturing company located in Murcia, Spain Aqueous synthetic solution Cr(III) 4.0 4.0 4320 1523 25 25 100 20 Batch Column 81 57.5 4 [102]

Residues from fruit juice

Pectin-rich fruit wastes and wine production, from a citrus-juice producer (Sunkist), USA Aqueous synthetic solution Cd(II) 5.0 50 - 60 Batch 46 2 [133]

Orange waste From orange juice industry Spain Aqueous synthetic solution Cd(II) 6.0 60 25 100 Batch 98 4 [94]

Type of hiosorhent Source of hiosorhent Feed solution Sorbate pH Contact time, min Temperature, ° C Initial concentration of sorbate, mg/L Mode of operation Maximum %removal Biosorbent dose Reference

Orange waste From orange juice industry Spain Aqueous synthetic solution Cd(II) Zn(II) Cr(III) 4.0 180 180 4320 20 15 15 15 Batch 86 90 95 4 [95]

Peach and Apricot stones Solid wastes of juice and jam industries, Egypt Aqueous synthetic solution Pb(II) 7.0 180 300 - 54.65 Batch 97.64 95.3 10 [97]

Mangifera indka (mango) seed kernel particles Local juice manufacturing industry Aqueous synthetic solution Methylene Blue (MB) cationic dye 8.0 120 30 100 Batch 96.17 0.67 [98]

Mango seeds (MS) Mangifera indka L. Juice producer, Uba-MG, Brazil Aqueous synthetic solution Victazol Orange 3R dye (VO-3R) 2.0 360 25 40 Batch - 2.5 [99]

Waste cider yeast hiomass Fermentation Lab at the College of Food Science and Engineering of Northwest A & F University (Yangling, China) Apple juice solution Patulin (PAT) 4.5 2160 25 0.1 0.2 Batch Column 58.29 5 F = 2 mL/min [117]

Dairy sludge Dairy plant, France Aqueous synthetic solution Pb(II) Cd(II) 5.0 500 20 200 100 Batch >90 0.5-4.0 [129]

The waste pomace of olive oil factory (WPO OF) Turkish Prina, Aegean region, Manisa, Turkey Aqueous synthetic solution Cr(VI) 2.0 120 60 50 100 Batch Column 100 21.74 5 F = 5 mL/min [101]

Solid waste from olive oil production The OS and OMS wastes were provided by the "Cooperativa Nuestra Se~nora desl Castillo" extraction plant located in Vilches, in the province of Jaen (Spain) Aqueous synthetic solution Pb(II) 5.0 120 25 - Batch - 10 [102]

Olive mill waste (OMW) two-phase decanter Mixture of pulp and olive stones from the crushing of olives to obtain the oil, UK Aqueous synthetic solution Pb(II) Cd(II) Cu(II) Hg(II) Fe(II) 7.0 30 20 10 Batch 80 75 10 [103]

Olive mill residues (OMR) Solid residues of oil production, provided by an olive mill in Abruzzo, Italy. Aqueous synthetic solution Cu(II) 5.5 4-5 150-1440 Room temperature 40 40 Batch Column 60% 10 80 [104]

Palm oil mill effluent (POME) sludge Waste sludge from palm oil mill, Felda Taib Andak, Johor, Malaysia Aqueous synthetic solution Methylene Blue (MB) cationic dye 7.5 4320 27 100 Batch - 2 [111]

Sunflower oil Waste hiomass Biomass obtained from a sunflower oil production Facility, Seville, Spain Aqueous synthetic solution (mixed solution) Pb(II) Ni(II) Zn(II) Cu(II) 4.0 - - 10 Column - F = 2 L/h [112]

Crushed olive stone wastes Supplied by an olive oil Producer, Cordoba, Spain Aqueous synthetic solution Pb(II) Ni(II) Cu(II) Cd(II) 5.5 60 20 18.86 4.20 4.35 4.80 Batch 79 70 81 95 13.3 [105]

Type of hiosorhent Source of hiosorhent Feed solution Sorbate pH Contact time, min Temperature, ° C Initial concentration of sorbate, mg/L Mode of operation Maximum %removal Biosorbent dose Reference

Supplied by "ProBeira" an Aqueous

Waste olive cake (OC) olive oil producer, Envendos Portugal synthetic solution Zn(II) 6.0-7.0 120 25 10 Batch 93 1 [108]

From the orujo oil

Olive stones extraction plant "Orujera Ubetense, Sociedad Cooperativa Andaluza," Jaen, Spain Aqueous synthetic Solution Cd(II) 11 360 40 10 Batch 90 0.01 [106]

Supplied by an Italian olive Aqueous Cu(II)

Olive pomace oil production plant synthetic Solution Cd(II) Pb(II) 5.0 60 — — Batch — 10 [107]

Olive pomace Supplied by one of the olive oil production Plants, Jordan Aqueous synthetic Solution Methylene Blue (MB) dye - 240 25 10 40 Batch Column 80 62.25 2 F = 20 mL/min [109]

Olive pomace OP-1 OP-2 OP-3 Solid by-products of olive oil processing mills, the island of Lesvos, Greece. Oil mill waste water (OMWW) Phenol 10.0 120 20 50 500 Batch Column >90 90 10 F = 1 mL/min [110]

Activated carbon derived Olive waste cake from oil Synthetic aqueous solution

from exhausted olive waste factory "Agrozitex" Sfax, Industrial wastewater from Lanaset Grey G 6.0 3000 25 150 Batch 93 1.67 [113]

cake Tunisia local factory

Activated carbon derived Industrial waste from united Methylene Blue dye (MB)

from empty fruit bunch (EFB) palm oil mill, Nibong, Tebal, Malaysia Synthetic aqueous solution 12 — 30 200 Batch — 1 [114]

Activated carbon from tea industry waste (TIWAC) Tea waste from tea processing plant, Black Sea region, Trabzon, Turkey Real water samples Cr(VI) Cr(III) 6.0 30 - 0.2 Batch 0 95-100 2 [115]

Activated carbon from sago waste Sago waste is collected from sago industry Salem district, Tamilnadu, India Synthetic aqueous solution Industrial wastewater from radiator industry Pb(II) 3.5 ± 0.3 180 27 10 Batch 87.34 2 [116]

Phaseolus vulgaris L. Canned food factory Aqueous synthetic solution Acid Red 57 dye Textile wastewater 2.0 20 20 150 1 (spiked wastewater sample) Batch 97.68 1.6 [91]

Ascolor Biotec (Pardubice, Pb(II) Hg(II) Cd(II) 10 50 50

Industrial fungi Pénicillium oxalicum var. Armeniaca Czech Republic) and Ivax Pharmaceuticals Aqueous synthetic solution 5.0 - 20 Batch Up to 85 for Hg 0.3 [118]

(Opava, Czech Republic)

Fruit waste macro fungi Flammulina velutipes Mushroom processing factory Aqueous synthetic solution Cd(II) Pb(II) 6.0 60 25 10 Batch 75 70 18 [130]

Cd(II)

Tolypocladium sp. Czech Industrial Partners Aqueous synthetic solution Pb(II) Hg(II) 5.0 20 — 50 Batch — 0.3 [118]

Table 1: Continued.

Type of hiosorhent Source of hiosorhent Feed solution Sórbate pH Contact time, min Temperature, ° C Initial concentration of sórbate, mg/L Mode of operation Maximum %removal Biosorbent dose Reference

Antibiotic waste P. mutilus SAIDAL antibiotic production complex at Medea (Algeria) Aqueous synthetic solution Basic Blue 41, cationic dye 8.0-9.0 60 30 50 Batch 75 0.5 [119]

Industrial waste of Clitopilus scyphoides (Pleurotus mutilus) fungal hiomass Antibiotic production plant, SAIDAL antibiotic production complex in Medea (Algeria) Aqueous synthetic solution Cd(II) 5.0 15 20 200 Batch 41 1 [120]

Fungal waste hiomass Pharmaceutical companies, Italy Textile wastewater effluents Dye mixtures 3.0 30 25 60-5000 Batch 90 16.7 [121]

Nonliving hiomass Aspergillus fumigatus Fermentation industry, Artemis Pharmaceuticals Limited, HAD, Jeedimetla, Hyderabad, India Aqueous synthetic solution perse mixture Cu(II) Cd(II) Co(II) Ni(II) 7.0 60 - 4.8 2.9 4.8 2.7 2.8 Batch 70 90 20 8 [122]

Nonliving hiomass Aspergillus awamori Industrial complex enzyme preparation Aqueous synthetic solution Cr(VI) 2.0 40 1152 25 Batch 87 1 [124]

Nonliving hiomass Aspergillus awamori Industrial complex enzyme preparation Aqueous synthetic solution Cu(II) 5.0 20 180 100 Batch - 1 [125]

Corynebacterium glutamicum Fermentation industry (BASF-Korea) Aqueous synthetic solution Reactive Black 5 (RB5) 1.0 35 500 500 Batch - 2.5 [127]

Activated carbon from antibiotic waste Industrial antibiotic production Aqueous synthetic solution Hg(II) 5.5 - 30 40 Batch - 0.2 [126]

Fennel hiomass (Foeniculum vulgare) Medical herb, local Unani medicine manufacturing unit at Aligarh, India Aqueous synthetic solution Cd(II) Mixture Cd(II) Ni(II) Zn(II) Cu(II) 4.3 50 50 each 50 100 Batch Column 92 97 10 F = 1 mL/min [123]

successful in biosorption of heavy metals and dyes. In view of the above, it can be inferred that most of the reported studies dealt with the removal of heavy metals and dyes. Clearly, there is lack of work on the removal of other pollutants. One particular research investigated the use of waste cider yeast in removing low concentrations (0.1-0.2 mg/L) of the toxin patulin from applejuice solutions and about 58% removalwas achieved [117].

As for pharmaceutical wastes, they are either fungal or bacterial biomass that could be dead or living. Examples of fungal biomass are Aspergillus niger, Pleurotus mutilus, Trichoderma reesei, Rhizopus arrhizus, Rhizopus nigricans, and Penicillium chrysogenum. Bacterial biomass could be produced from antibiotic fermentation such as Streptomyces spp. or during production of drugs such as Streptomyces noursei, S. rimosus, and S. clavuligerus or during enzyme manufacture such as the bacillus species of B. licheniformis and S. subtilis. Plenty of work was done on applications of pharmaceutical wastes as effective biosorbents for contaminant removal from wastewater [118-123]. For heavy metal removal, the waste Clitopilus scyphoides (Pleurotus mutilus) produced during antibiotic fermentation process was used to remove Cd (II) [120]. A high biosorption capacity of 111 mg/g was obtained within short uptake duration of about 15 min. No pretreatment for the dead biomass was required and the biosorbent was composed predominantly of Ca, Si, and P elements with a total mineral content of 13.5% (w/w). The fungal dead biomass Aspergillus fumigatus is also a fermen-tive waste of antibiotic industry that was utilized in metal biosorption. The sun-dried biomass was pretreated with 5% boiling KOH for 15 min and then thoroughly washed with distilled water till neutral pH was reached. The biosorbent was efficient in removing Cd, Co, Cu, and Ni with the highest efficiency obtained for Cu (72%). More than 90% of metal ions were removed from low-concentration mixtures (0.1 mM). At high concentration of these mixtures, Cu ion was the most competitive among other ions and 70% of which was removed. The fermentation waste mycelium of the fungal biomass, Aspergillus awamori, was produced industrially from an enzyme preparation process. It was then utilized for Cr (VI) removal and a maximum removal efficiency of 87% was obtained [124]. The same biomass, after being treated with 0.5 M NaOH, removed a maximum of 35.97 mg/g Cu (II) from aqueous solutions [125]. Tolypocladium sp. biomass waste was successful in removing Cd, Pb, and Hg [118]. Three different types of fungal biomass from antibiotic industries named Fennel biomass, Foeniculum vulgare, which is a medicinal herb, removed 92% of Cd ion at pH 4.3. Maximum biosorption capacities obtained in batch systems were 21, 24, and 30 mg/g at 30, 40, and 50°C, respectively. Biosorption was spontaneous and endothermic. In single-component packed-bed studies, breakthrough and exhaustive capacities were 10 and 40 mg/g, respectively, while 2 and 12 mg/g were the corresponding capacities for multicomponent systems. Capacities dropped to 0.8 and 4 mg/g in multicomponent saline systems. An antibiotic waste composed of a mixture of Streptomyces fradiae, Micromonospora pururea, and Nocardia mediterranea was chemically activated with K2CO3 to obtain

activated carbon that was utilized as a biosorbent for Hg (II) [126].

For the removal of dyes, Acremonium strictum, Acremo-nium sp., and Penicillium sp. were examined for their potential to decolorize simulated dye baths. A. strictum was found to be the most efficient biosorbent with percentage removal of up to 90% in both acidic and neutral conditions. These biomasses were less active compared to Cunninghamella elegans which is a biomass known to be an efficient biosorbent that removed 97% of the dye color [121]. Clitopilus scyphoides (Pleurotus mutilus) was also used to remove Basic Blue dye [119] and a biosorption capacity of 200 mg/g was obtained within about 60 min, while Reactive Black 5 (RB5) dye was successfully removed by Corynebacterium glutamicum waste produced from lysine fermentation industry [127].

3. Operating Factors Influencing Biosorption

Holistically, the behavior and performance of biosorption are affected by the physical and chemical characteristics of each of the biosorbent and sorbate; in addition to the process operating conditions. Biosorbent and sorbate characteristics include composition, structure, type of charged and uncharged functional groups, and particle size. It was also reported that in biomass sorbents, the composition of the cell wall influences both sorption uptake capacity and selectivity [88,128].

Operating conditions are instrumental biosorption controlling parameters which include pH, temperature, initial sorbate concentration, biosorbent dose, contact time, agitation speed, sorbent particle size, mode of operation, and competition from coions. These operating parameters will be further discussed in more detail.

3.1. Solution pH and Ionic Strength. The pH of sorbate solution plays a vital role in the biosorption process since it influences the charge on the biosorbent functional groups and the dissociation of these groups on the active sites. It also affects sorbate solubility and its degree of ionization. The effect of pH on both uptake capacity and percentage removal was investigated by numerous workers. For heavy metal sorption, it was found that the increase in pH increases uptake capacity of heavy metals such as Cd, Pb, Ni, Cu, and Zn in both the acidic and the neutral range (pH 2-7). The rate of increase under highly acidic conditions (pH 2-4) was mostly higher than that observed at milder acidic conditions (pH 4-6) [6, 72, 84, 100-102, 104, 108, 125,129, 130]. Under basic conditions (pH > 7), heavy metal uptake decreased with pH [100, 101, 108]. Under severe acidic conditions, the very low reported uptake capacities were attributed to the fact that H+ ions compete with the metal ions on the active sites [72, 101, 126] which indicates that biosorption is governed by electrostatic interactions under these conditions. Increase in pH also increased the percentage of metal removal under acidic and neutral pHs [97, 105, 106, 126] and decreased the removal under basic conditions [97]. However for the pharmaceutical waste mycelium of the Aspergillus awamori, the increase of pH from 2.0 to 4.0 decreased the removal

efficiency of Cr (VI) by about 50% [122]. At basic pHs, biosorption uptake decreases owing to metal precipitation which leads on the contrary to increase in metal removal from solution by a possible combined microprecipitation-biosorption mechanism [105-108]. In case of dyes, the behavior of sorption uptake and percentage removal with pH varies according to the type of charge. For cationic dyes such as Methylene Blue (MB) and Basic Blue 41, both removal and uptake are directly proportional to pH [78, 83,91, 98,119] and vice versa for anionic dyes such as Acid Green (AG), Acid Red 57, Reactive Red (RR 198), and Victazol Orange 3R dyes [70, 86, 91, 99]. At high pH, the uptake and removal of cationic dyes increase due to attractive forces between the positively charged dye and the negatively charged functional groups on the biosorbent. One study on the removal of phenols by olive pomace showed that removal efficiency is enhanced by increasing pH [110].

Very limited studies were conducted on the effect of ionic strength where the presence of NaCl [105, 123] and perchlorate salts [105] significantly reduced biosorption due to competition between the salt ions and the sorbate ions on the active sites.

3.2. Initial Sorbate Concentration. The increase in the initial concentration of the sorbate acts as a driving force to overcome the mass transfer resistance and hence increase the uptake. This behavior was reported for both heavy metals and dyes [83, 98,110,125,126,130]. In one study dealing with Hg sorption onto desiccated coconut waste, the concentration-uptake correlation was linear [100].

The percentage removal, on the other hand, was found to decrease with increasing in concentration for the heavy metals Cd, Zn, and Ni onto tea, olive cake wastes, and wine processing sludge, respectively [72, 76, 119] as well as for Cr (VI) and Basic Blue 41 dye onto mycelium of Aspergillus awamori and antibiotic fungal waste, respectively [108,124]. The same behavior was encountered by Methylene Blue dye onto both fresh malted sorghum mash waste and mango seed kernel powder [83, 98] and by Pb onto both activated carbons from sago waste and peach/apricot stones. With the latter adsorbent, removal was almost constant at very low concentrations of Pb (5-100 ppm) [97,116]. With higher initial concentrations, higher equilibrium concentrations in the solution were obtained possibly due to saturation of active sites and this, in turn, decreased the removal efficiency. In addition, the increase in initial concentration decreased sorption rate since it probably reduced diffusion across the boundary layer. However, a different behavior was observed for Acid Green (AG) dye sorbed onto spent brewery grains where the removal initially increased by virtue of the high concentration gradient driving force and then dropped owing to saturation of the sorption active sites [70]. Furthermore, with investigating the sorption of Cd (II), Pb (II), and Cu (II) onto orange peels the dissociation constant for the biosorption interaction decreased exponentially with increase in concentration [101] indicating stronger binding.

3.3. Biosorbent Dose. Generally as the biosorbent dose increases, the number of available active sites increases and

thus consequently enhances the removal [70, 72, 86, 97, 98, 102,110,115,119,120,124,130]. On the other hand, the uptake capacity decreases probably due to decrease in surface area that might be a result of having some of the sorption sites aggregated and overlapped [100,102,108,129]. In a few cases, the removal reaches a peak value then declines [82, 101, 119] and this could be due to saturation of active sites.

3.4. Temperature. The effect of temperature becomes important when dealing with wastewater effluents that are discharged at high temperatures due to processing. For endothermic reactions, biosorption uptake capacity and removal efficiencyincreased with temperature due to increase in surface activity and hence availability of more active sites [76, 80, 83, 98, 113, 120, 123, 124, 129] and vice versa for exothermic reactions [70, 86, 91, 100]. Sorption rate for endothermic reactions was also enhanced as temperature increased and it followed Arrhenius equation [76,106].

3.5. Particle Size of The Sorbent. In most of the reported studies, the initial rate of sorption was rapid and it decreased gradually till it reached an approximately constant value [70, 101,106]. This shows that binding mostly occurs on the solid surface and that film and pore ion diffusion are not significant or have very fast rates. In cases where this did not hold true, either film (boundary layer) or pore (intraparticle) diffusion or a combination of both was the rate limiting step [91,100, 120, 123] When the governing mechanism was the surface reaction, decrease in particle size was shown to improve the uptake [110,119] due to increase in surface area. In addition, the decrease in particle size enhances diffusion and sorption rates since it reduces intraparticle diffusion [108]. In case of very porous biosorbents like pectin wastes, it was found that particle size had no significant effect on Cr (III) sorption since the external surface area does not contribute much to the total surface area [102].

3.6. Agitation Speed. The speed of agitation was found to enhance removal efficiency by reducing mass transfer resistances but only up to an optimal limit above which efficiency drops probably due to biomass fragmentation [82,103,119].

3.7. Mode of Operation. The operational mode influences uptake and % removal because dynamics of batch systems are different from column dynamics. In most studies, dynamic capacity was lower than its batch counterpart; and the same held true for % removal [100-102,104,131]. Column dynamics vary with column dimensions and flow rate. The increase in column height was found to decrease sorption efficiency and increase breakthrough time [102, 109]. An increase in initial concentration of sorbate enhanced sorption capacity and decreased breakthrough time [100, 109]. Increasing the influent flow rate also decreased the breakthrough time [109]. In a dynamic study on the sorption of phenols onto olive pomace, decreasing flow rate and particle size was found to improve sorption capacity [110].

3.8. Competition From Coions. One additional factor affecting biosorption in multicomponent systems is competition

and interference between ions in the sorbate mixture. As a result, the reported individual batch uptake and breakthrough capacities of ions in single-component systems were lower compared to their counterparts in multicomponent systems [123]. However, high removal efficiency (up to 8090%) was achieved in multicomponent systems of heavy metals [71, 103]. It was also suggested that competition is minimized at low ion concentrations [57, 122]. In general, Pb ions showed more competitiveness than Cd ions onto different adsorbents such as grape bagasse [79], olive mill waste [102], biomass from sunflower oil [112], and fruit waste macrofungi [130].

4. Nature and Mechanism of Biosorption

Food and pharmaceutical wastes contain organic compounds such as proteins, amino acids, polysaccharides, phenolics, andacids. Thesecompounds have functional groups that bind to the sorbate cations. Groups include, but are not limited to, amines, hydroxyls, carbonyls, sulfonyls, thiols, and phosphates. Biosorption mechanisms include physical sorption by virtue of Van der Waals forces or by ion exchange electrostatic interactions, chemical sorption by chelation or complexation, and microprecipitation. Generally, a combination of these mechanisms is involved in biosorption [88,132,133].

There are several factors controlling sorption mechanisms, type of ligands or binding sites available on the sorbent; chemical structure and characteristics of the target ions/molecules, physicochemical conditions such as pH, ionic strength, and temperature. There are some general rules for metal binding particularly via complexation. Hard acids such as K+, Na+, Ca2+, and Mg2+ prefer to bind to oxygen ligands, whereas soft acids such as the precious metal ions of Ag, Au, Hg, and Cd preferentially bind covalently to the cell wall via ligands that contain nitrogen or sulfur [132,134].

Sorption onto biomass can generally occur via one or more of the following mechanisms: rapid surface reaction between the sorbate and the active functional groups existing in the cell wall, intracellular accumulation, or precipitation/extracellular accumulation. Surface reaction could be either physical adsorption or chemisorption and is nonmetabolism dependent. Intracellular accumulation takes place when the sorbate migrates across the cell wall. It is a metabolism-dependent process that is influenced by adverse environmental conditions such as lack of nutrients and toxicity. It is also a function of the regular metabolic activities that change the microenvironment surrounding the cell, such as nutrient uptake, metabolic release, and respiration. In living biomass, biosorption is metabolism-dependent and occurs by sorbent uptake across the cell membrane. Therefore, it has its limitations regarding toxicity and maintaining nutrient levels. Biosorption via dead biomass does not suffer from these limitations and occurs on the cell wall where the polysaccharides and proteins have binding sites. However, lower binding capacities and higher desorption tendencies are often encountered [88,135,136].

To elucidate the underlying biosorption mechanism, the functional groups involved in biosorption were determined

by Fourier transform infrared spectroscopy (FTIR) analysis (Table 2). Generically, sorption onto pectin-rich fruit wastes involved hydroxyl and carboxyl groups [94, 95, 101, 102]; whereas sorption onto olive oil wastes involved carboxylic and phenolic groups [102, 108, 111]. Biomass fungal wastes had additional amine groups as in Aspergillus Fumigatus and Aspergillus awamori. These groups were donated by the chitosan and chitin that are predominantly present in the fungal cell walls [122, 124, 125]. A two-step mechanism was suggested for sorption onto Aspergillus awamori where there is an initial adsorption step followed by a chromium reducing step from Cr (VI) to Cr (III). Heavy metal sorption onto okra food wastes and sugar bagasse wastes took place via a combined ion exchange/complexation mechanism where the positively charged metal interacted with the negatively charged wastes. The negative charge on the wastes was owed to the presence of lone pairs of the nitrogen and oxygen atoms that exist in the functional groups of cellulose, lignin, protein, and sugar [88, 89]. The main functional groups responsible for dye sorption onto pecan nut shells and mango seeds were the sulfonyl groups. Mechanism of sorption onto the former biosorbent depended on the number of sulfonic groups present on the dye; these groups interacted with the Ca compounds belonging to the pecan nut shells [131]. The mechanism of dye sorption onto the latter biosorbent entailed association with water molecules which linked the Victazol Orange 3R sulfonic groups to the syringyl groups of the lignin cellulose present in the mango seeds [99]. A variety of functional groups played important roles in the biosorption of Pb onto waste beer yeast. The extent of contribution of these groups was in the descending order: carboxylic, lipids, amines, and phosphates [82]. For the sorption of anionic dyes onto Cupuassu shells, a 3-step mechanism was proposed. It involved an initial rapid step for protonation of the Cupuassu shells functional groups. This was followed by dissociation of the dye agglomerates and their consequent dehydration, then finally electrostatic binding between the negatively charged dye and the positively charged biosorbent. Activated carbon from the pharmaceutical antibiotic waste contained primarily oxygen-containing functional groups such as hydroxyl and carbonyl groups which formed complexes with the mercury ions [126].

The change in pH during sorption could be indicative of the involved mechanism. For example, the decrease in pH during the sorption of heavy metals onto Tolypocladium sp. is a result of proton release probably due to electrostatic interaction between the positively charged metals and the negatively charged carboxylic groups on the adsorbent [107].

5. Equilibrium and Kinetic Modeling Studies

Biosorption equilibrium is governed by isotherm models that are well-known and established in literature. Table 3 [82, 86, 87, 127, 131, 137] summarizes the different isotherm model equations involved in the present review along with their relevant parameters. For the kinetic modeling, the reported studies herein were found to follow either pseudo-first order or pseudo-second order or Elovich models; equations thereof are presented in Table 4 [94, 98,131,137].

Table 2: Suggested biosorption mechanisms based on interacting functional groups.

Biosorbent Sorbate Functional group Mechanism Reference

Orange peel Pb(II) Cu(II) Cd(II) Carboxylic IEX/H-bonding [101]

Orange waste Cr(III) Carboxyl/hydroxyl Chemisorption [102]

Orange waste Cd(II) Carboxyl/hydroxyl — [94]

Orange waste Cd(II) Zn(II) Cr(III) Mainly carboxyl — [95]

Desiccated coconut Hg(II) Hydroxyl/carboxyl/amine Chelation [100]

Pecan nut shells (C. illinoinensis) biomass Acid Blue Reactive Blue Acid Blue Sulfonyl — [132]

Cupuassu shell, Theobroma grandiflorum, (CS) Reactive red dye Direct blue Hydroxyl/carboxylic IEX [87]

Mango seeds (MS) Mangifera indica L. Victazol orange Sulfonyl — [99]

Okra food industrial waste Cd(II) Fe(II) Zn((II) Hydroxyl/carbonyl/amide IEX/complexation [88]

Sugar industrial waste (bagasse waste) Cd(II) Fe(II) Hydroxyl/carbonyl/amide IEX/complexation [89]

Pineapple peel MB dye Hydroxyl/carboxyl/amine — [91]

Olive pomace Pb(II) Cu(II) Cd(II) Carboxylic/phenolic Surface complexation [108]

Olive mill stone Pb(II) Carboxylic IEX [102]

Palm oil mill effluent (POME) sludge Methylene Blue Carboxylic — [111]

Wine processing sludge Ni(II) Amino/carboxyl Physical adsorption/chemical complexation [76]

Spent waste beer yeast Saccharomyces cerevisiae Pb(II) Amine/carboxylic/ phosphates/ sulfhydryl IEX/complexation [82]

Grape bagasse waste residue Cd(II) Pb(II) Carbonyl/hydroxyl — [79]

Phaseolus vulgaris biomass Pb(II) Amino/hydroxyl — [84]

Activated carbon from antibiotic waste Hg(II) Hydroxyl/carbonyl Complexation [126]

Nonliving biomass Aspergillus awamori Cr(VI) Amine — [124]

Nonliving biomass Aspergillus Fumigatus Cd (II) perse mixture Cu(II) Cd(II) Co(II) Ni(II) Hydroxyl/amine Complexation [122]

Fennel biomass (Foeniculum vulgare) Cd(II) Carboxylic/phenolic IEX* [123]

*IEX: ion exchange adsorption.

Table 5 compiles a summary of the sorption parameters pertaining to the studies utilizing food and pharmaceutical waste biosorbents, as predicted by the different well-established models for sorption equilibrium. The table presents only results that were obtained by the best fitting model relevant to each study. In the majority of equilibrium

studies, heavy metals and dyes were shown to follow Lang-muir isotherm. This indicates single-site monolayer binding where the surface of sorbent is homogenous and all sites are equally favorable or nonfavorable from the energetic point of view. Few heavy metals followed Freundlich isotherm which assumes a heterogeneous biosorbent surface; examples are

Table 3: Main adsorption isotherm models involved in the present study.

Adsorption isotherm model

Model parameters

Freundlich

q = KFC1/n

Linear form

logq = log— + - logC

KF: Freundlich isotherm constant that indicates adsorption capacity (mg/g) (L/mg)"

«: measure of adsorption intensity or surface heterogeneity (dimensionless) <j: amount adsorbed at equilibrium, mg/g C: adsorbate concentration at equilibrium, mg/L

Langmuir = qmKLC

q 1 + KlC

Linear form

- - - J_

q qmKLC qm

qm: maximum binding capacity, mg/g Langmuir binding (adsorption) constant, L/mg

qJKsCr

- + (K.C)1 1 + acC&

Ks: Sips binding (adsorption) constant, (L/mg)" h: dimensionless exponent constant

= Sips sorption exponent as = Sips sorption constant (L/mg)

Dubinin-Astakhov

( RTlnÇC^/C))" q = q™exp I--^-I

£: mean free energy of adsorption, KJ/mol h: Dubinin-Astakhov dimensionless exponent T: temperature, K R: universal gas constant, KJ/mol-K

qmcbetc

q = (C-C) [1 + (Cbet - 1) (C/Cs)j Linear form

- , (Cbet - -) C

q (Cs C) q™cbet qmcbet

Alternative form

q=_q,AC_

CBET: BET isotherm constant which indicates energy of surface interaction, L/mg Cs: saturation concentration of adsorbate, mg/L £>s: isotherm constant for BET adsorption in the first layer, L/mg isotherm constant for BET adsorption in upper layers, mg/L

Table 4: Equations of kinetic models involved in the current study.

Kinetic Model

Model Parameters

Pseudo-first order

f=fci (q-q )

Linear Form

log (q-qt) = logq-

fcj: rate constant of pseudo-first order model, min-1 <j: amount adsorbed at equilibrium, mg/g qt: amount adsorbed at time i, mg/g

Pseudo-second order

7ft =fc2(q-qt)2 Linear Form

— = — + If

qt fc2q2 q

fc2: rate constant of pseudo-second order model, g/mg-min

Elovich

qt = - ln («--) + - lnf

a: initial adsorption rate, mmol/g-min Elovich constant, related to extent of surface coverage and activation energy, g/mmol

Cd (II) [123] and Pb (II) [82, 97, 105]. Cd was also shown to follow BET [120] and Sips [94], while Pb was found to follow Sips [102] and Dubinin Astakhov [103]. Several dyes such as Reactive Red (RR 194), Direct Blue 53, Acid Blue 25, and Reactive Black 5 followed Sips isotherm [87, 127, 131], whereas Reactive Red dye (RR 198) and phenols followed Freundlich isotherm [86,110]. In general, it can be observed from the table that sorption capacities of pharmaceutical and fungal biomass wastes for heavy metals and dyes are higher

than those of pectin-rich fruit wastes or olive oil wastes. Sorption in multicomponent systems was well described by either Langmuir as in case of simulated acid bath for wool (SABW) dye mixture [121] or extended Langmuir as in case of binary mixtures of heavy metals [105].

In most reported studies, the pseudo-second order model was found to be the most appropriate fitting model that describes biosorption of heavy metals and dyes onto food and pharmaceutical wastes (Table 6). This indicates that the

Table 5: Equilibrium parameters as predicted by the well-established sorption models.

Biosorbent Target ion/compound Equilibrium model Maximum sorption capacity (mg/g) Sorption constant* pH/temperature (°C) Reference

Local dairy sludge Pb(II) Cd(II) Langmuir 178.6 69.90 0.03 0.05 5/40 [129]

Baker's yeast biomass Cd(II) Pb(II) Langmuir 31.75 60.24 0.092 0.066 6.0/30 5.0/30 [131]

Cider yeast Patulin Langmuir 0.0082 0.064 4.5/25 [117]

Beer yeast Cu(II) Pb(II) Langmuir 0.66 2.27 0.314 0.259 5.0/20 [69]

Spent waste beer yeast Saccharomyces cerevisiae Pb(II) Freundlich — Kf = 0.515 n = 0.842 5.0/30 [82]

Spent brewery grains (SBG) AG25 dye Langmuir 212.76 0.036 3.0/30 [70]

Wine processing sludge Ni(II) Langmuir 3.91 0.113 5.5/50 [76]

Antibiotic waste P. mutilus Cu(II) Langmuir 106.38 0.007 — [119]

Antibiotic waste P. mutilus Basic Blue 41 Langmuir Freundlich 111.00 0.097 Kf = 24.1 n = 2.89 (8.0-9.0)/30 [119]

Phaseolus vulgaris L. Acid Red 57 dye Langmuir 215.13 — 2.0/20 [91]

Phaseolus vulgaris L. Reactive Red 198 Freundlich Kf = 1.99 n = 10.037 [86]

Fruit waste macrofungi Flammulina velutipes Cd(II) Pb(II) Langmuir 8.43 18.35 — 6.0/25 [130]

Industrial fungi Penicillium oxalicum var. Armeniaca Cd(II) Pb(II) Hg(II) Langmuir 35.90 47.40 269.3 0.05 1.01 0.07 5.0/20 [107]

Industrial fungi Tolypocladium sp. Cd(II) Pb(II) Hg(II) Langmuir 11.90 28.40 161.0 1.03 0.61 0.50 5.0/20 [107]

industrial waste of Clitopilus scyphoides (Pleurotus mutilus) fungal biomass Cd(II) BET 45.3 16 bs = 0.03 bL = 0.00 5.0/20 [120]

Fungal waste biomass Simulated acid bath for wool (SABW) dye Langmuir 289.5 0.0114 3.0/25 [121]

biomass of Phaseolus vulgaris L. Pb(II) Langmuir 19.93 0.498 5.0/50 [84]

Fennel biomass (Foeniculum vulgare) Cd(II) Langmuir Freundlich 26.59 0.080 Kf = 3.16 n = 2.29 4.3/50 [123]

Nonliving biomass Aspergillus awamori Cu(II) Langmuir 35.97 0.136 5.0/20 [125]

Corynebacterium glutamicum Reactive Black 5 RB5 Langmuir Sips 419 0.042 ks = 108 as = 0.171 1.0/35 [127]

Rhizopus oligosporus biomass Cu(II) Langmuir 79.37 0.282 5.0/30 [85]

Pectin-rich fruit wastes (lemon peels) Cd(II) Langmuir 22.32 0.015 5.0/— [133]

Orange waste Cd(II) Sips 20.64 0.038 (n = 1.21) 6.0/25 [94]

Orange waste Cd(II) Zn(II) Cr(III) Langmuir 17.66 14.61 22.50 0.004 0.067 0.372 4.0/20 [95]

Biosorbent Target ion/compound Equilibrium model Maximum sorption capacity (mg/g) Sorption constant* pH/temperature (°C) Reference

Orange (Citrus sinensis) Cr(III) Langmuir 36.48 0.403 5.0/25 [102]

Pineapple peel, an agricultural effluent Methylene Blue (MB) cationic dye Langmuir 97.09 0.074 6.0/30 [91]

Peach stones Apricot stones Pb(II) Freundlich — Kf = 0.64 (n = 3.57) Kf = 0.636 (n = 3.54) 7.0/— [97]

Mangifera indica (mango) seed kernel particles Methylene Blue (MB) cationic dye Langmuir 153.846 0.8227 8.0/50 [98]

Desiccated coconut Hg(II) Langmuir 500.00 — 7.4/30 [100]

Pecan nut shells (C. illinoinensis) biomass Acid Blue 74 (AB74) Reactive Blue 4 (RB4) Langmuir Langmuir 4.851 13.410 0.001 0.001 6.5/30 [132]

Acid Blue 25 (AB25) Sips 7.576 Ks = 0.0014 (n = 0.98)

Crushed olive stone wastes Pb(II) Ni(II) Cu(II) Cd(II) Binary mixtures Freundlich Extended Langmuir — — 5.5/20 [105]

Olive pomace Cu(II) Cd(II) Pb(II) Langmuir 1.94 2.98 6.23 0.138 0.046 1.829 5.0/60 [108]

Olive pomace Phenols Freudlich — Kf = 0.267 n= 1.75 10.0/20 [110]

Pomace from olive oil Cr(IV) Langmuir 18.69 0.055 2.0/60 [101]

olive mill residues (OMR) Cu(II) Langmuir 13.50 0.080 5.0/23 [104]

Solid olive stone Pb(II) Sips 6.57 Ks = 0.057 5.0/25 [102]

Olive oil mill Pb(II) Dubinin-Astakhov 23.69 5.0/25 [103]

Palm oil mill effluent (POME) sludge Methylene Blue (MB) cationic dye Langmuir 23.50 0.208 7.6/27 [111]

Sugarcane bagasse waste Methylene Blue (MB) Gentian Violet (GV) Langmuir 202.43 327.83 0.031 0.047 8.0/25 [78]

Fresh malted sorghum mash waste Methylene Blue (MB) basic dye Langmuir 384.6 0.011 7.0/53 [83]

Cupuassu shell, Theobroma grandiflorum, (CS) Reactive Red dye (RR194) Direct Blue 53 Sips 64.1 37.5 Ks = 0.214 (n = 0.89) Ks = 1.560 (n = 0.55) 2.0/25 [87]

Activated carbon derived from exhausted olive waste cake Lanaset Grey G Langmuir 108.70 0.031 6.0/25 [113]

Activated carbon derived from empty fruit bunch (EFB) Methylene Blue dye (MB) Langmuir 344.83 0.060 —/30 [114]

Activated carbon from sago waste Pb(II) Langmuir 14.35 0.095 3.5/27 [116]

'Units depend on the fitting isotherm model and are indicated in Table 3.

Table 6: Kinetic parameters as predicted by the well-established sorption models.

Biosorbent Target ion/compound Kinetic model q (mg/g) Rate constant* pH/temperature (°C)/time (min) Co (mg/L) Reference

Local dairy sludge Pb(II) Cd(II) Pseudo-second order 117.6 44.4 0.27 4.2 5.0/20° C/500 200 100 [129]

Wine processing sludge Cr(VI) Pseudo-second order 2.42 0.070 4.2/50/240 100 [73]

Wine processing sludge Ni(II) Pseudo-second order 3.11 0.226 5.5/50/120 45 [76]

Desiccated coconut Hg(II) Pseudo-second order 447.03 — 7.4/30/60 50 [100]

Pecan nut shells (C. illinoinensis) biomass Acid Blue 74 (AB74) Reactive Blue 4 (RB4) Pseudo-first Pseudo-second 3.271 10.010 0.02 4.35 * 10-4 6.5/30/500 6.5/30/1000 1000 [132]

Acid Blue 25 (AB25) Pseudo-second-order 4.892 7.15 * 10-3 6.5/30/500

Spent brewery grains AG25 dye Pseudo-second order 74.63 0.038 3.0/30/75 90 [70]

Beer brewery diatomite Methylene Blue basic waste (SDE) dye Pseudo-second order 4.92 1.24 7.0/25/1440 2.5 [81]

Antibiotic waste P. mutilus Basic Blue 41 Pseudo-second order 90.91 0.0042 8.0-9.0/30/60 70 [119]

Macrofungal waste from antibiotics Cd(II) Pseudo-second order 82.8 0.0014 5.0/20/15 200 [120]

Fennel biomass (Foeniculum vulgare) Cd(II) Pseudo-second order 9.30 0.476 5.0/30/50 100 [123]

Phaseolus vulgaris L. Reactive Red 198 Pseudo-second order 81.97 0.036 2.0/20/20 — [86]

Nonliving biomass Aspergillus awamori Cu(II) Pseudo-first order 35.00 0.077 5.0/20/180 25 [125]

Corynebacterium glutamicum Reactive Black 5 RB5 Pseudo-second order 370.00 9.4 * 10-5 1.0/25/500 2000 [127]

Phaseolus vulgaris L. Acid Red 57 dye Pseudo-second order 89.49 0.21 2.0/20/20 150 [91]

Fruit waste macrofungi Flammulina velutipes Cd(II) Pb(II) Pseudo-first Pseudo-second order 13.04 2.17 6.0/25/60 10 [130]

Orange (Citrus sinensis) Cr(III) Pseudo-second order 10.97 0.002 5.0/25/4320 100 [102]

Pectin-rich fruit wastes (lemon peels) Cd(II) Pseudo-second order 13.92 0.021 5.0/—/50 19.2 [133]

Orange waste Cd(II) Elovich 333.33 (1/a) 0.004 (1/ß) 6.0/25/60 100 [94]

Mangifera indica (mango) seed kernel particles Methylene Blue (MB) cationic dye Pseudo-first order 115 0.0461 8.0/30/120 175 [98]

Rhizopus oligosporus biomass Cu(II) Pseudo-second order 69.82 0.002 5.0/30/120 100 [85]

Pb(II) 1.12 0.141 18.86

Crushed olive stone wastes Ni(II) Cu(II) Cd(II) Pseudo-second order 0.25 0.26 0.72 3.000 7.497 0.121 5.5/20/60 4.48 4.35 10.56 [105]

Olive stones Cd(II) Pseudo-second order 0.903 3.196 11.0/80/20 10 [106]

Biosorbent Target ion/compound Kinetic model q (mg/g) Rate constant* pH/temperature (°C)/time (min) Co (mg/L) Reference

Palm oil mill effluent (POME) sludge Methylene Blue (MB) cationic dye Pseudo-second order 5.54 0.0072 7.6/27/4320 10 [111]

Olive pomace Methylene Blue (MB) dye Pseudo-second order — 0.0906 —/25/240 10 [109]

Tea industry waste Cd(II) Pseudo-second order 10.6 0.02 7.0/25/180 100 [72]

Pineapple peel, an agricultural effluent Methylene Blue (MB) cationic dye Pseudo-second order 104.17 0.22 x 10-3 6.0/30/400 300 [91]

Okra food waste Cd(II) Fe(II) Pseudo-second order 17.54 20.42 0.009 0.008 —/20/90 20 [88]

Zn(II) 14.99 0.013

Activated carbon

derived from exhausted Lanaset Grey G Pseudo-first order 106.4 0.0019 6.0/25/3000 150 [113]

olive waste cake

Activated carbon from Pseudo-second order

tea industry waste Cr(III) 0.464 1.52 6.0/—/30 0.01 [115]

(TIWAC)

Sugar industry (waste bagasse) Cd(II) Fe(II) Pseudo-first order — 9.3 * 10-5 7.2 * 10-5 —/20/90 20 [89]

Sugarcane bagasse waste Methylene Blue (MB) Pseudo-second order 192.31 0.0012 8.0/25/600 200 [78]

Gentian Violet 357.14 0.00005 8.0/25/900 300

'Units depend on the fitting kinetic model and are indicated in Table 4.

mechanism is that of chemisorption. The model takes into account the three phases of the sorption process; surface reaction, film or external diffusion, and pore or intraparticle diffusion. Generally, time versus uptake trends revealed fast kinetics where almost 90% or more of the material was sorbed within a time range from few minutes to few hours and equilibrium was almost approached. In one instance when Cr (III) was adsorbed onto orange waste, reaching very close to complete equilibrium required a few days [102]. This could be owed to a diffusion-controlled sorption taking place onto the very porous pectin-rich biosorbent as was alluded to in Section 3.5.

6. Pretreatment and Regeneration/Recovery Options

Wastes from most fruit sources are pectin-rich biosorbents of potentially high metal binding abilities. Many studies that involved the use of such biosorbents have undertaken prior chemical pretreatment known as protonation. This process aims at removing excess cations such as Ca2+, Na+, or K+ from the biosorbent before carrying out biosorption experiments to reduce the competition ofthese elements with targeted heavy metals. Moreover, it leads to the creation of negative active sites on the biosorbent surface (at specific pH values) which leads to higher metal uptake capacity [92]. Some researchers utilized HNO3 with predetermined concentration for this chemical pretreatment step. A comparative study [101] was carried out on the performance of treated

and untreated orange peel waste. Results showed higher Cd (II) uptake of 11.2 mg/g in case of chemically treated orange peel as compared to 6.94 mg/g in case of original peel. Similarly, [138] pectin waste was protonated by HNO3 before carrying out batch biosorption experiments for heavy metal removal. It was also suggested in a different study [99] that the use of HCl was successful in acidifying the mango seeds (AMS) in order to improve its removal efficiency to dyes. A faster adsorption process accompanied by increase in adsorption capacity was encountered in case of AMS relative to the original mango seeds (MS). According to them, the protonation using HCl increased the macropore structure of the original MS allowing higher amounts of dyes to be adsorbed.

H2O2 along with thermal treatment was used to treat wine processing sludge in order to remove organic matter before using the biosorbent for the removal of Cr (VI) [73]. This step led to the reduction of Cr (VI) to Cr (III) which reached a percentage of 2-18 at the end of the biosorption experiment. They considered pretreatment as a key factor for any future research to be performed on Cr removal using the same biosorbent. A comparison between chemically treated and untreated waste olive cake biomass during a study for Zn (II) removal from aqueous solutions was conducted [108]. This showed an increase in the removal efficiency of waste treated by NaOH and a reduction in the removal efficiency in case of H2SO4 treated waste.

A combined chemical and physical treatment was performed for baker's yeast waste used for Cd (II) and Pb

(II) removal [139]. Thermal treatment (121°C), NaOH, and ethanol were applied to separate biomass samples and the resulted treated biomass was employed in batch biosorption experiments. The best metal uptake was reported for ethanol treated biomass whereas caustic and thermal. Caustic soda and ethanol were utilized for pretreating the Penicillium oxalicum var. Armeniaca biomass used for heavy metal removal [107]. The purpose was to remove proteins from the biomass sites via caustic treatment which increased biosorption capacity, whereas the opposite was true in case of acidic pretreatment.

Other different chemical treatments either acidic or caustic were employed by other workers in their biosorption studies. Zinc chloride and potassium hydroxide were employed as chemical activating agents for palm oil sludge in a study on the removal of Methylene Blue dye [111]. Results were comparable to commercial activated carbon but chemically treated sludge was recommended for better solution to sludge disposal problems. Simulation of chemical and physical pretreatment was employed in another study on the removal of phenols from industrial wastewaters using olive pomace solid wastes produced from different stages of olive mills [110]. Dried olive pomace denoted OP-1, solvent extracted using hexane and vapor olive pomace (OP-2), solvent extracted and incompletely combusted in boilers, and olive pomace (OP-3) were utilized. Results recommended the use of OP-3 as an effective biosorbent for phenol removal as the reported removal efficiencies exceeded 90%. The use of sugarcane bagasse modified by EDTA dianhydride for the removal of MB and GV dyes was investigated by other workers [78], and there was no sign of its effectiveness as a biosorbent compared to the untreated bagasse. It has also been reported in another study that the physically and chemically treated waste cider yeast was efficient in removing patulin [84]. Heating and chemical addition of either NaOH or ethanol was done during yeast preparation for batch experiments, while calcium alginate was used to form a gel bead (cell immobilization) with and without NaOH treatment for the column study. For batch results, the highest % removal obtained was 58.29% in case of caustic treatment and 44.41% for thermal or ethanol treatment. Column results showed substantial improvement in patulin removal by caustic treated immobilized yeast matrix (100% removal) as compared to untreated yeast (71.42%). Another cell immobilization was performed during a study conducted on the removal of heavy metals using waste biomass from beverage industry [75]. Comparison between the removal efficiencies of both immobilized (on Dowex resin and Chitin) and free biomasses indicated limited improvement in uptake performance. Another study used polyvinyl alcohol for biomass immobilization [122]. This process helped in improving biomass adsorption capacity and regeneration ability. A different study compared the performance of immobilized and suspended brewery waste yeast biomass versus fresh yeast (from baker's) in the removal of Cd (II) from aqueous solutions [80]. An excellent removal efficiency of 99.83% was reported in case of suspended form of brewery waste (SBW) which confirmed its promising potential as an effective low-cost adsorbent.

To test the effect of different functional groups on the removal of some heavy metals (Cd2+, Zn2+, and Cr3+), orange waste biomass was chemically modified by specific reagents [95]. It was suggested that ester treatment was not recommended as a prior modification because it decreased biosorption capacity. Five different chemical reagents were applied to chemically treat the waste beer yeast used in biosorption of lead from electroplating effluents [82]. Lead removal efficiencies were reduced after using all five pretreat-ment methods with drastic effects shown in case of ethanol and HCl treatment. Similar results were reported by the same workers in their study on Cr removal [74]. Their results showed reduction in removal efficiency using all types of treating agents relative to the original biosorbent and they owed this to the creation of modified functional groups.

Some researchers used chemical and physical methods for the preparation of activated carbons produced from different food processing wastes. Four studies were reported for the removal of dyes or heavy metals using AC prepared from exhausted olive waste cake [113], AC prepared from oil palm empty fruit bunch [114], AC prepared from tea waste [115], and AC prepared from sago waste [116]. Chemical activation was performed using sulfuric or phosphoric acids or potassium hydroxide and this was followed by heating to relatively high temperatures or microwave assistant heating as an essential step in all four studies. Reported results showed an outstanding performance for AC from tea industrial waste in Cr (III) removal with an efficiency that almost reached 100%.

As for pharmaceutical wastes, Tolypocladium sp. was treated with methanol to improve its sorption capacity for Hg (II) [107]. Modification of the amino groups on the waste mycelium of Aspergillus awamori via treatment with formaldehyde, acetic anhydride, or sodium iodoacetate did not improve its removal efficiency for Cr (VI) [124]. The treatment of the same biosorbent with sodium hydroxide and dimethyl sulfoxide increased Cu (II) uptake [125]. Among different pretreatments of Corynebacterium glutamicum with HCl, H2SO4, HNO3, NaOH, Na2CO3, NaCl, and CaCl2, the maximum improvement in biosorption capacity for Reactive Black 5 dye was achieved with 0.1 M HNO3. This was attributed to the enhancement of positively charged cell surfaces that attract the negatively charged dyes [127].

Few researchers were interested in desorption processes for either regeneration of the biosorbent for reuse and/or for recovery of the sorbate material. Desorption can be performed by adding acids, bases, inorganic salts, or solvents [129] for metal recovery. This step usually follows the adsorption step and metal recovery rate or metal uptake is calculated to test the effectiveness of the reagent used in desorption. HCl was the most used eluent for the majority of the reported studies [100,101,103-105, 116, 122,123, 129]. The most promising reported results showed that olive mill waste (OMW) maintained its adsorptive capacity for Cd (II) and Pb (II) after ten adsorption-desorption cycles [103]. HCl elution was followed by neutralization with Na2HCO3 [101]. Other workers revealed that exhausted modified orange peel was able to adsorb Pb (II) up to 91.5% after the 4th

cycle. It was concluded in another study that desiccated coconut waste can be used multiple times for Hg sorption and can be regenerated easily using HCl [100]. It was also found in other batch experiments that 41.7% recovery of Fennel biomass could be attained after the 5th cycle using HCl as an eluent [123]. In addition, the relevant column study was very successful and resulted in 87.8% of Cd (II) being eluted in a single-component system and almost 100% in a multicomponent system. Results of using HCl as an eluting agent showed that after the 4th cycle, 6570% of initial Cd (II) can be retained onto Aspergillus Fumigatus, but the biosorbent deteriorated after the 5th cycle [122].

In comparing HCl with other desorping agents, higher Pb (II) desorption rate using HCl as compared to EDTA was reported [26]. However, EDTA manifested better performance than both HCl and CaCl2 (equal desorption effect) in case of Cu (II) desorption but had the disadvantage of damaging the biosorbent sites [104]. Furthermore, the regenerated waste was able to remove 40% of Cu (II). Different results revealed that Pb (II) was better recovered by HNO3 (desorption rate of 76.6%) while Cd (II) was better recovered by HCl (desorption rate of 62.5%) [129]. The desorping agent, HNO3, was utilized in another study where the results showed that the regenerated biomass was successfully capable of desorping Cd (II) even after 5 consecutive cycles [120]. The comparison between the use of HNO3 and double deionized water (DDW) in desorbing Ni (II) showed that DDW was very poor compared to HNO3 [76]. The same acid was also used along with another two desorbing agents, NaNO3 and Ca(NO3)2, to regenerate peels and it was shown that regenerated peels have the same efficiency as the original peels [140]. About 90-100% of Cd (II) was recovered from the peels in 120 min or less. Additionally, HNO3 gave superior removal efficiency of 90% in only 50 min without damaging the peels.

7. Concluding Remarks

Industrial food processing and pharmaceutical wastes are promising biosorbents for treatment of wastewater effluents. They contain functional groups such as hydroxyl, carboxyl, and amine that allow them to interact with metal ions and dye pollutants via physical and/or chemical sorption. Sorption equilibrium in most of the previous studies was best described by Langmuir isotherm suggesting single-site binding. Sorption kinetics was generally fast and it predominantly followed the pseudo-second order model indicating a chemisorption mechanism. Surface reaction as well as film and pore diffusion processes were considered in the model.

Biosorption is influenced by the physical and chemical properties of the sorbent as well as various operating conditions. Numerous workers studied the effect of these parameters in batch systems. However, very few studies were conducted in continuous column systems. The latter is of paramount importance in scaled-up applications. Furthermore, most workers employed synthetic aqueous solutions

rather that real wastewater effluents where competition and interference between ions in the mixture could significantly affect biosorption performance. One parameter that was overlooked is the physical, mechanical, and chemical stability of the sorbent. Mechanical strength of the biosorbent and its resistance to chemicals and microbial degradation are crucial parameters that ensure reproducibility of biosorbent, particularly in continuous operations where the biosorbent is regenerated and reused many times. Maintaining reproducibility for many subsequent cycles has both environmental and economic merits.

Desorption studies are relatively fewer compared to removal studies. The former is particularly important for both biosorbent regeneration and sorbate recovery if of value. Disposing of, landfilling and incineration could be alternatives to discarding the used biosorbent rather than regenerating it. However issues with cost and leaching of toxic compounds in the soil and ground water make them sometimes unfavorable options. Under very strong binding conditions, where the equilibrium binding constant is high, leaching and metal release are minimized.

Biosorbent performance could be enhanced by chemical, thermal, or chemical/thermal pretreatment and/or immobilization. Pretreatment could be performed to remove unde-sired organic compounds, proteins, or competing ions from the biosorbent and hence improve biosorption capacity and efficiency. In other cases, pretreatment is undertaken to add new functional groups to the biosorbent that can possibly enhance biosorption. However in some cases, pretreatment gave adverse effects. Prior characterization studies on the biosorbent may help in selecting the suitable treatment option.

Biosorption utilizing industrial food processing and pharmaceutical wastes could provide a cost-effective ecofriendly viable means of treating wastewater effluents, while making good use of waste materials. However, more work should focus on scaling up the proposed biosorption processes and studying their technoeconomic feasibility. Research should also be extended to using these biosorbents for treatment of different classes of contaminants such as phenolic compounds and mycotoxins.

Conflict of Interests

The authors declare that there is no conflict of interests regarding the publication of this paper.

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