Purification of human antibodies from transgenic corn using aqueous two‐phase systems

A recombinant human antibody expressed in corn was purified using aqueous two‐phase extraction. The antibody was an immunoglobulin G fully unglycosylated. Using systems of different compositions and/or pHs in each of one or two partitioning stages followed by one more stage in which the antibody was precipitated at the liquid/liquid interface facilitated the removal of different impurities in each stage. The best system yields a product 72% pure (22‐fold purification) with a yield of 49%. The optimum extraction was done in two partitioning stages followed by an interfacial precipitation stage using poly(ethylene)glycol/potassium phosphate systems. NaCl was added to the first stage to eliminate large molecular weight impurities. The pH in the first stage was kept at 6 but a pH of 8 was used in the second stage and in the precipitation stage. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Downstream antibody purification using aqueous two‐phase extraction

The extraction of antibodies using a polyethylene glycol (PEG)‐citrate aqueous two‐phase system (ATPS) was investigated. Studies using purified monoclonal antibody (mAb) identified operating ranges for successful phase formation and factors that significantly affected antibody partitioning. The separation of antibody and host cell protein (HCP) from clarified cell culture media was examined using statistical design of experiments (DOE). The partitioning of antibody was nearly complete over the entire range of the operating space examined. A model of the HCP partitioning was generated in which both NaCl and citrate concentrations were identified as significant factors. To achieve the highest purity, the partitioning of HCP from cell culture fluid into the product containing phase was minimized using a Steepest Descent algorithm. An optimal ATPS consisting of 14.0% (w/w) PEG, 8.4% (w/w) citrate, and 7.2% (w/w) NaCl at pH 7.2 resulted in a product yield of 89%, an approximate 7.6‐fold reduction in HCP levels relative to the clarified cell culture fluid before extraction and an overall purity of 70%. A system consisting of 15% (w/w) PEG, 8% (w/w) citrate, and 15% (w/w) NaCl at pH 5.5 reduced product‐related impurities (aggregates and low molecular product fragments) from ～40% to less than 0.5% while achieving 95% product recovery. At the experimental conditions that were optimized in the batch mode, a scale‐up model for the use of counter‐current extraction technology was developed to identify potential improvements in purity and recovery that could be realized in the continuous operational mode. © 2010 American Institute of Chemical Engineers Biotechnol. Prog., 2010     

Potential Aqueous Two‐Phase Processes for the Primary Recovery of Colored Protein from Microbial Origin

The primary recovery of c‐phycocyanin and b‐phycoerythrin from Spirulina maxima and Porphyridium cruentum, respectively, using an established extraction strategy was selected as a practical model system to study the generic application of polyethylene glycol (PEG)‐phosphate aqueous two‐phase systems (ATPS). The generic practical implementation of ATPS extraction was evaluated for the recovery of colored proteins from microbial origin. A comparison of the influence of system parameters, such as PEG molecular mass, concentration of PEG as well as salt, system pH and volume ratio, on the partition behavior of c‐phycocyanin and b‐phycoerythrin was carried out to determine under which conditions target colored protein and contaminants concentrate to opposite phases. One‐stage processes are proposed for the primary recovery of the colored proteins. PEG1450‐phosphate ATPS extraction (volume ratio (V_R) equal to 0.3, tie‐line length (TLL) of 34 % w/w and system pH 7.0) for the recovery of c‐phycocyanin from Spirulina maxima resulted in a primary recovery process that produced a protein purity of 2.1 ± 0.2 (defined as the relationship of 620 nm to 280 nm absorbance) and a product yield of 98 % [w/w]. PEG1000‐phosphate ATPS extraction (i.e., V_R = 1.0, PEG 1000, TLL 50 % w/w and system pH 7.0) was preferred for the recovery of b‐phycoerythrin from Porphyridium cruentum, which resulted in a protein purity of 2.8 ± 0.2 (defined as the relationship of 545 nm to 280 nm absorbance) and a product yield of 82 % [w/w]. The purity of c‐phycocyanin and b‐phycoerythrin from the crude extract increased 3‐ and 4‐fold, respectively, after ATPS. The results reported herein demonstrated the benefits of the practical generic application of ATPS for the primary recovery of colored proteins from microbial origin as a first step for the development of purification processes.     

Enantioseparation of Racemic Flurbiprofen by Aqueous Two‐Phase Extraction With Binary Chiral Selectors of L‐dioctyl Tartrate and L‐tryptophan

A novel method for chiral separation of flurbiprofen enantiomers was developed using aqueous two‐phase extraction (ATPE) coupled with biphasic recognition chiral extraction (BRCE). An aqueous two‐phase system (ATPS) was used as an extracting solvent which was composed of ethanol (35.0% w/w) and ammonium sulfate (18.0% w/w). The chiral selectors in ATPS for BRCE consideration were L‐dioctyl tartrate and L‐tryptophan, which were screened from amino acids, β‐cyclodextrin derivatives, and L‐tartrate esters. Factors such as the amounts of L‐dioctyl tartrate and L‐tryptophan, pH, flurbiprofen concentration, and the operation temperature were investigated in terms of chiral separation of flurbiprofen enantiomers. The optimum conditions were as follows: L‐dioctyl tartrate, 80 mg; L‐tryptophan, 40 mg; pH, 4.0; flurbiprofen concentration, 0.10 mmol/L; and temperature, 25 °C. The maximum separation factor α for flurbiprofen enantiomers could reach 2.34. The mechanism of chiral separation of flurbiprofen enantiomers is discussed and studied. The results showed that synergistic extraction has been established by L‐dioctyl tartrate and L‐tryptophan, which enantioselectively recognized R‐ and S‐enantiomers in top and bottom phases, respectively. Compared to conventional liquid–liquid extraction, ATPE coupled with BRCE possessed higher separation efficiency and enantioselectivity without the use of any other organic solvents. The proposed method is a potential and powerful alternative to conventional extraction for separation of various enantiomers. Chirality 27:650–657, 2015. © 2015 Wiley Periodicals, Inc.     

Continuous purification of antibodies from cell culture supernatant with aqueous two-phase systems: From concept to process

An aqueous two-phase extraction (ATPE) process based on a PEG/phosphate system was developed for the capture of human immunoglobulin G and successfully applied to a Chinese hamster ovary and a PER.C6® cell supernatant. A continuous ATPE process incorporating three different steps (extraction, back-extraction, and washing) was set up and validated in a pump mixer-settler battery. Most of the higher molecular weight cell supernatant impurities were removed during the extraction step, while most of the lower molecular weight impurities were removed during the subsequent steps. A global recovery yield of 80% and a final protein purity of more than 99% were obtained for the IgG purification from a CHO cell supernatant, representing a 155-fold reduction in the protein/IgG ratio. For the purification of IgG from a PER.C6® cell supernatant, a global recovery yield of 100%, and a host cell protein purity were attained, representing a 22-fold reduction in the host cell protein/IgG ratio. These results, thus, open promising perspectives for the application of the developed ATPE process as a platform for the capture of antibodies. In fact, this new process has shown the ability to successfully recover and purify different antibodies from distinct cell culture supernatants. This technology can also overcome some of the limitations encountered using the typical chromatographic processes, besides inherent advantages of scalability, process integration, capability of continuous operation, and economic feasibility.     

Bioprocess intensification: a potential aqueous two-phase process for the primary recovery of B-phycoerythrin from Porphyridium cruentum

A process for the primary recovery of B-phycoerythrin from Porphyridium cruentum exploiting aqueous two-phase systems (ATPS) was developed in order to reduce the number of unit operations and benefit from an increased yield of the protein product. The evaluation of system parameters such as poly(ethylene glycol) (PEG) molecular mass, concentration of PEG as well as salt, system pH and volume ratio was carried out to determine under which conditions the B-phycoerythrin and contaminants concentrate to opposite phases. PEG 1450-phosphate ATPS proved to be suitable for the recovery of B-phycoerythrin because the target protein concentrated to the top phase whilst the protein contaminants and cell debris concentrated in the bottom phase. An extraction ATPS stage comprising volume ratio (Vr) equal to 1.0, PEG 1450 24.9% (w/w), phosphate 12.6% (w/w) and system pH of 8.0 allowed B-phycoerythrin recovery with a purity of 2.9 (estimated as the relation of the 545-280 nm absorbances). The use of ATPS resulted in a primary recovery process that produced a protein purity of 2.9 +/- 0.2 and an overall product yield of 77.0% (w/w). The results reported demonstrated the practical implementation of ATPS for the design of a primary recovery process as a first step for the commercial purification of B-phycoerythrin produced by P. cruentum.     

High‐throughput process development of purification alternatives for the protein avidin

With an increased number of applications in the field of the avidin‐biotin technology, the resulting demand for highly‐purified protein avidin has drawn our attention to the purification process of avidin that naturally occurs in chicken egg white. The high‐throughput process development (HTPD) methodology was exploited, in order to evaluate purification process alternatives to commonly used ion‐exchange chromatography. In a high‐throughput format, process parameters for aqueous two‐phase extraction, selective precipitation with salts and polyethylene glycol, and hydrophobic interaction and mixed‐mode column chromatography experiments were performed. The HTPD strategy was complemented by a high‐throughput tandem high‐performance liquid chromatography assay for protein quantification. Suitable conditions for the separation of avidin from the major impurities ovalbumin, ovomucoid, ovotransferrin, and lysozyme were identified in the screening experiments. By combination of polyethylene glycol precipitation with subsequent resolubilization and separation in a polyethylene glycol/sulfate/sodium chloride two‐phase system an avidin purity of 77% was obtained with a yield >90% while at the same time achieving a significant reduction of the process volume. The two‐phase extraction and precipitation results were largely confirmed in larger scale with scale‐up factors of 230 and 133, respectively. Seamless processing of the avidin enriched bottom phase was found feasible by using mixed‐mode chromatography. By gradient elution a final avidin purity of at least 97% and yield >90% was obtained in the elution pool. The presented identification of a new and beneficial alternative for the purification of the high value protein thus represents a successful implementation of HTPD for an industrially relevant purification task. © 2015 American Institute of Chemical Engineers Biotechnol. Prog., 31:957–973, 2015     

Experimental and Model Studies on Continuous Separation of 2‐Phenylpropionic Acid Enantiomers by Enantioselective Liquid–Liquid Extraction in Centrifugal Contactor Separators

Multistage enantioselective liquid–liquid extraction (ELLE) of 2‐phenylpropionic acid (2‐PPA) enantiomers using hydroxypropyl‐β‐cyclodextrin (HP‐β‐CD) as extractant was studied experimentally in a counter‐current cascade of centrifugal contactor separators (CCSs). Performance of the process was evaluated by purity (enantiomeric excess, ee) and yield (Y). A multistage equilibrium model was established on the basis of single‐stage model for chiral extraction of 2‐PPA enantiomers and the law of mass conservation. A series of experiments on the extract phase/washing phase ratio (W/O ratio), extractant concentration, the pH value of aqueous phase, and the number of stages was conducted to verify the multistage equilibrium model. It was found that model predictions were in good agreement with the experimental results. The model was applied to predict and optimize the symmetrical separation of 2‐PPA enantiomers. The optimal conditions for symmetric separation involves a W/O ratio of 0.6, pH of 2.5, and HP‐β‐CD concentration of 0.1 mol L^?1 at a temperature of 278 K, where ee_eq (equal enantiomeric excess) can reach up to 37% and Y_eq (equal yield) to 69%. By simulation and optimization, the minimum number of stages was evaluated at 98 and 106 for ee_eq > 95% and ee_eq > 97%. Chirality 28:235–244, 2016. © 2016 Wiley Periodicals, Inc. Research highlights are as follows:

相似文献   

An integrated practical implementation of continuous aqueous two‐phase systems for the recovery of human IgG: From the microdevice to a multistage bench‐scale mixer‐settler device

Aqueous two‐phase systems (ATPS) are a liquid‐liquid extraction technology with clear process benefits; however, its lack of industrial embracement is still a challenge to overcome. Antibodies are a potential product to be recovered by ATPS in a commercial context. The objective of this work is to present a more integral approach of the different isolated strategies that have arisen in order to enable a practical, generic implementation of ATPS, using human immunoglobulin G (IgG) as experimental model. A microfluidic device is used for ATPS parameters preselection for product recovery. ATPS were continuously operated in a mixer‐settler device in one stage, multistage and multistage with recirculation configuration. Single‐stage pure IgG extraction with a polyethylene glycol (PEG) 3350‐phophates ATPS within continuous operation allowed a 65% recovery. Further implementation of a multistage platform promoted a higher particle partitioning reaching a 90% recovery. The processing of IgG from a cell supernatant culture harvest in a multistage system with top phase recirculation resulted in 78% IgG recovery in bottom phase. This work conjugates three not widely spread methodologies for ATPS: microfluidics, continuous and multistage operation.     

Evaluation of different primary recovery methods for E. coli-derived recombinant human growth hormone and compatibility with further down-stream purification

Due to advances in fermentation technology, it is now possible to obtain fermentation broth with over 30% solids. The high solid content makes the clarification step difficult, especially at large scale. The primary protein recovery step is challenging due to the heterogeneous solution of soluble and insoluble material. In this study, we compare different primary recovery routes and the compatibility with the initial capture chromatography step. The primary recovery routes studied are standard clarification by centrifugation and extraction in aqueous two-phase systems. The compatibility of the feed streams from the different primary recovery steps with the first chromatography step is addressed. An anion-exchange column was used as the first capture column in the purification process. The aqueous two-phase system was composed of a random copolymer of ethylene oxide and propylene oxide (EOPO) in combination with a waxy starch. The target protein in this study was human growth hormone (hGH) produced in recombinant Escherichia coli. The purity of hGH in the top phase after aqueous two-phase extraction was found to be significantly higher than in clarified homogenate supernatant and increased as the EOPO polymer concentration in the aqueous two-phase system increased. Stability of the supernatant and EOPO top phases and hGH were determined by turbidity measurements and LC-MS assay. All of the feed-streams from the primary recovery steps were compatible with the anion-exchange chromatography step; however, the capacity of the resin was strongly dependent on the purity of the load. Different process aspects, e.g., resin capacity, viscosity, purification, and yield of hGH and scalability are compared.     

Fractionation and purification of the phycobiliproteins from Spirulina platensis

C-Phycocyanin and allophycocyanin of Spirulina platensis are fractionated and purified using a non-chromatographic method namely, aqueous two phase extraction for the first time. Optimized process parameters of aqueous two phase extraction (PEG 4000/potassium phosphate of tie line length 18.64% with a phase volume ratio 1.45) resulted in pure C-phycocyanin and allophycocyanin with a purity of 3.23 and 0.74, respectively, in a single extraction. Multiple extractions (two) improved the purity of C-phycocyanin from 3.23 to 4.02. Integration of aqueous two phase extraction with membrane process not only facilitated the separation of phase forming components from the products and also increased the purity of allophycocyanin from 0.74 to 1.5.     

Purification of IgG and albumin from human plasma by aqueous two phase system fractionation

The current shortages in human plasma products at global levels justify the development of new, cost effective plasma fractionation methods. We have developed a fractionation process to obtain immunoglobulin G (IgG) and albumin‐enriched fractions based on polymer‐salt aqueous two phase system (ATPS). A small‐scale (0.02 L) ATPS composed of polyethyleneglycol 3350 (PEG), potassium phosphate and sodium chloride, at pH 6.1, was evaluated and subjected to 50‐fold scale‐up (1 L). Further purification of the fractions was performed using caprylic acid precipitation and ion exchange chromatography. Similar yield and purity were obtained at both small and large scales. IgG precipitated in the PEG rich upper phase at 83% recovery and 2.75‐fold purification factor. An 81% pure albumin fraction was obtained in the salt rich bottom phase with a 91% yield. After polishing, IgG was obtained at a recovery of 70% and a purity of 92%. Corresponding values for albumin were 91% and 90%. This IgG and albumin fractionation technology deserves further evaluation as it may represent a potential alternative to conventional plasma fractionation methods. © 2012 American Institute of Chemical Engineers Biotechnol. Prog., 28: 1005–1011, 2012     

Aqueous two-phase assisted by ultrasound for the extraction of anthocyanins from Lycium ruthenicum Murr.

In this study, an efficient ultrasound-assisted aqueous two-phase extraction method was used for the extraction of anthocyanins from Lycium ruthenicum Murr. An ethanol/ammonium sulfate system was chosen for the aqueous two-phase system due to its fine partitioning and recycling behaviors. Single-factor experiments were conducted to determine the optimized composition of the system, and the response surface methodology was used for the further optimization of the ultrasound-assisted aqueous two-phase extraction. The optimal conditions were as follows: a salt concentration of 20%, an ethanol concentration of 25%, an extraction time of 33.7?min, an extraction temperature of 25°C, a liquid/solid ratio of 50:1 w/w, pH value of 3.98, and an ultrasound power of 600?W. Under the above conditions, the yields of anthocyanins reached 4.71?mg/g dry sample. For the further purification, D-101 resin was used, and the purity of anthocyanins reached 25.3%. In conclusion, ultrasound-assisted aqueous two-phase extraction was an efficient, ecofriendly, and economical method, and it may be a promising technique for extracting bioactive components from plants.     

Reverse micellar extraction for downstream processing of lipase: Effect of various parameters on extraction

Reverse micellar extraction of lipase using cationic surfactant cetyltrimethylammonium bromide (CTAB) was investigated. The effect of various process parameters on both forward and backward extraction of lipase from crude extract was studied to optimize its yield and purity. Forward extraction of lipase was found to be maximum using Tris buffer at pH 9.0 containing 0.10 M NaCl in aqueous phase and 0.20 M CTAB in organic phase consisting of isooctane, butanol and hexanol. In case of backward extraction, lipase was extracted from the organic phase to a fresh aqueous phase in 0.05 M potassium phosphate buffer (pH 7.0) containing 1.0 M KCl. The activity recovery, extraction efficiency and purification factor of lipase were found to be 82.72%, 40.27% and 4.09-fold, respectively. The studies also indicated that the organic phase recovered after back extraction could be reused for the extraction of lipase from crude extract.     

Simultaneous extraction and concentration of penicillin G by hollow fiber renewal liquid membrane

In this article, hollow fiber renewal liquid membrane (HFRLM) technique was used for recovery of penicillin G from aqueous solution. The organic solution of 7 vol % di‐n‐octylamine (DOA) + 30 vol % iso‐octanol + kerosene was used as liquid membrane phase, and Na₂CO₃ aqueous solution was used as stripping phase. Experiments were performed as a function of carrier concentration in the organic phase, organic/aqueous volume ratio, pH, and initial penicillin G concentration in the feed phase, pH in the stripping phase, flow rates, etc. The results showed that the HFRLM process was stable and could carry out simultaneous extraction and concentration of penicillin G from aqueous solutions. As a carrier facilitated transport process, the addition of DOA in organic phase could greatly enhance the mass transfer rate; and there was a favorable organic/aqueous volume ratio of 1:20 to 1:30 for this system. The mass transfer flux and overall mass transfer coefficient increased with decreasing pH in the feed phase and increasing pH in the stripping phase, because of variation of the mass transfer driving force caused by pH gradient and distribution equilibrium. The flow rate of the shell side had significant influence on the mass transfer performance, whereas the effect of flow rate of lumen side on the mass transfer performance was slight because of the mass transfer intensification of renewal effect in the lumen side. The results indicated that the HFRLM process was a promising method for the recovery of penicillin G from aqueous solutions. © 2009 American Institute of Chemical Engineers Biotechnol. Prog., 2009     

Protein extraction by Winsor‐III microemulsion systems

Proteins (bovine serum albumin (BSA), α‐chymotrypsin, cytochrome c, and lysozyme) were extracted from 0.5 to 2.0 g L^?1 aqueous solution by adding an equal volume of isooctane solution that contained a surfactant mixture (Aerosol‐OT, or AOT, and a 1,3‐dioxolane (or cyclic ketal) alkyl ethoxylate, CK‐2,13‐E_5.6), producing a three‐phase (Winsor‐III) microemulsion with a middle, bicontinuous microemulsion, phase highly concentrated in protein (5–13 g L^?1) and small in volume (12–20% of entire volume). Greater than 90% forward extraction was achieved within a few minutes. Robust W‐III microemulsion systems were formulated at 40°C, or at 25°C by including a surfactant with shorter ethoxylate length, CK‐2,13‐E₃, or 1.5% NaCl (aq). Successful forward extraction correlated with high partitioning of AOT in the middle phase (>95%). The driving force for forward extraction was mainly electrostatic attractions imposed by the anionic surfactant AOT, with the exception of BSA at high ionic strength, which interacted via hydrophobic interactions. Through use of aqueous stripping solutions of high ionic strength (5.0 wt %) and/or pH 12.0 (to negate the electrostatic attractive driving force), cytochrome c and α‐chymotrypsin were back extracted from the middle phase at >75% by mass, with the specific activity of recovered α‐chymotrypsin being >90% of its original value. © 2011 American Institute of Chemical Engineers Biotechnol. Prog., 2011     

Enantioseparation of N-protected α-amino acid derivatives by liquid-liquid extraction technique employing stereoselective ion-pair formation with a carbamoylated quinine derivative

Two-phase liquid-liquid extraction experiments were undertaken to study the enantioselective transport of the chiral N-protected α-amino acid derivatives from an aqueous buffer solution into an organic phase employing highly lipophilic carbamoylated quinine as chiral selector and phase transfer carrier, respectively. The chiral separation, derived from enantioselective ion-pair formation and differential solubility in the aqueous and organic phases of diastereomeric associates thus formed has been shown to be primarily dependent on the structure of the selectand, the nature of the organic solvent, the molar ratio of a given chiral selector to selectand in the two phases, and the pH of the aqueous phase. Extracted enantiomers were recovered by back-extraction using a relatively polar acidic medium in which the selector is barely insoluble. Thus, the enantiomeric purity of N-(3,5-dinitrobenzoyl)-leucine exceeded 95% enantiomeric excess with 70% overall yield with a single extraction and back-extraction step. Chirality 9:268–273, 1997. © 1997 Wiley-Liss, Inc.     

Water extraction of pyrolysis oil: the first step for the recovery of renewable chemicals

The interest in biomass as a source of renewable energy and chemicals has been increasing in keeping up with the transition to a sustainable bio-based economy. An important initial step of chemicals recovery from biomass-derived pyrolysis oil is water extraction where most of polar compounds are isolated in the aqueous phase. This study was done to investigate the effects of stirring rate and water-to-oil ratio on the extraction capability (distribution coefficient and yield), water content, and atomic composition of both aqueous and organic phases. The results show that the stirring rate above 300 rpm has no influence on the equilibrium. Increasing the water-to-oil ratio dilutes the aqueous phase without changing the atomic distribution. Forest residue-derived pyrolysis oil should be extracted at a water-to-oil ratio of 0.65-0.7, whereas pine-derived pyrolysis oil is preferably extracted at the lowest feasible water-to-oil ratio where complete phase separation occurs, which is 0.5 in this study.     

Preparative Enantioseparation of β‐Substituted‐2‐Phenylpropionic Acids by Countercurrent Chromatography With Substituted β‐Cyclodextrin as Chiral Selectors

Preparative enantioseparation of four β‐substituted‐2‐phenylpropionic acids was performed by countercurrent chromatography with substituted β‐cyclodextrin as chiral selectors. The two‐phase solvent system was composed of n‐hexane‐ethyl acetate‐0.10 mol L‐1 of phosphate buffer solution at pH 2.67 containing 0.10 mol L^‐1 of hydroxypropyl‐β‐cyclodextrin (HP‐β‐CD) or sulfobutylether‐β‐cyclodextrin (SBE‐β‐CD). The influence factors, including the type of substituted β‐cyclodextrin, composition of organic phase, concentration of chiral selector, pH value of the aqueous phase, and equilibrium temperature were optimized by enantioselective liquid–liquid extraction. Under the optimum separation conditions, 100 mg of 2‐phenylbutyric acid, 100 mg of tropic acid, and 50 mg of 2,3‐diphenylpropionic acid were successfully enantioseparated by high‐speed countercurrent chromatography, and the recovery of the (±)‐enantiomers was in the range of 90–91% for (±)‐2‐phenylbutyric acid, 91–92% for (±)‐tropic acid, 85–87% for (±)‐2,3‐diphenylpropionic acid with purity of over 97%, 96%, and 98%, respectively. The formation of 1:1 stoichiometric inclusion complex of β‐substituted‐2‐phenylpropionic acids with HP‐β‐CD was determined by UV spectrophotometry and the inclusion constants were calculated by a modified Benesi‐Hildebrand equation. The results showed that different enantioselectivities among different racemates were mainly caused by different enantiorecognition between each enantiomer and HP‐β‐CD, while it might be partially caused by different inclusion capacity between racemic solutes and HP‐β‐CD. Chirality 27:795–801, 2015. © 2015 Wiley Periodicals, Inc.