Streamlined downstream process for efficient and sustainable (Fab')₂ antivenom preparation

Abstract

Background:

Antivenoms are the only validated treatment against snakebite envenoming. Numerous drawbacks pertaining to their availability, safety and efficacy are becoming increasingly evident due to low sustainability of current productions. Technological innovation of procedures generating therapeutics of higher purity and better physicochemical characteristics at acceptable cost is necessary. The objective was to develop at laboratory scale a compact, feasible and economically viable platform for preparation of equine F(ab')₂ antivenom against Vipera ammodytes ammodytes venom and to support it with efficiency data, to enable estimation of the process cost-effectiveness.

Methods:

The principle of simultaneous caprylic acid precipitation and pepsin digestion has been implemented into plasma downstream processing. Balance between incomplete IgG breakdown, F(ab')₂ over-digestion and loss of the active drug's protective efficacy was achieved by adjusting pepsin to a 1:30 substrate ratio (w/w) and setting pH at 3.2. Precipitation and digestion co-performance required 2 h-long incubation at 21 °C. Final polishing was accomplished by a combination of diafiltration and flow-through chromatography. In vivo neutralization potency of the F(ab')₂ product against the venom's lethal toxicity was determined.

Results:

Only three consecutive steps, performed under finely tuned conditions, were sufficient for preservation of the highest process recovery with the overall yield of 74%, comparing favorably to others. At the same time, regulatory requirements were met. Final product was aggregate- and pepsin-free. Its composition profile was analyzed by mass spectrometry as a quality control check. Impurities, present in minor traces, were identified mostly as IgG/IgM fragments, contributing to active drug. Specific activity of the F(ab')₂ preparation with respect to the plasma was increased 3.9-fold.

Conclusion:

A highly streamlined mode for production of equine F(ab')₂ antivenom was engineered. In addition to preservation of the highest process yield and fulfillment of the regulatory demands, performance simplicity and rapidity in the laboratory setting were demonstrated. Suitability for large-scale manufacturing appears promising.

Keywords:
Antivenom downstream processing; F(ab')₂ immunotherapy; Hyperimmune plasma; Ion-exchange chromatography; Mass spectrometry

Background

Envenoming following snakebite is a very common medical emergency responsible for enormous suffering all over the world. In 2017 the WHO added this public health problem to its list of Category A neglected tropical diseases [1]. In 2019 a comprehensive strategy was developed to reduce the number of snakebite deaths and disability cases by 50% before 2030.

Passive immunotherapy with animal-derived antivenoms, containing either immunoglobulin G (IgG) or its derivative fractionation products, F(ab')₂ or Fab, has been the only validated treatment for snakebite envenoming for decades [2]. Antivenoms were recognized as essential medicines more than a century ago and number of technological platforms for their production are available. Yet, we are currently faced with severe shortages, especially in sub-Saharan Africa and parts of Asia, but even in high-income countries. Two moments are critical. There is a need for implementation of better immunization protocols yielding plasma material of higher potency. Advances in the design of sustainable manufacturing strategies generating available, safe and efficient life-saving medications are another necessity. One of the most widely used approaches for antivenom production as the initial step employs a salting-out procedure [3-7], which is associated with a low-purity profile of the final product or excessive formation of aggregates [8, 9]. Caprylic acid as an alternative precipitating agent [10] has been introduced into the preparation of a whole series of equine or ovine IgG- or F(ab')₂-based antivenoms [11-17]. Purification principles based on caprylic acid have been proven more beneficial than salt-mediated methods due to selective precipitation of non-IgG plasma proteins [18, 19]. Thus, the active drug (IgG) remains in a solubilized state, preserving conformation and/or structural stability.

Some antivenom manufacturers perform enzyme-mediated removal of the Fc portion from IgG molecules that can be accomplished upon their purification [20], on unfractionated plasma [16, 20, 21] or simultaneously with the precipitation of unwanted proteins using caprylic acid, as demonstrated on ovine serum [17]. Aside from the doubtful role of the Fc fraction in adverse reactions [18, 19, 22, 23], its removal reduces the quantity of foreign material in the product intended for use in humans, thus increasing specific activity and at least partially contributing to safety improvement. Although both F(ab')₂ and Fab antivenoms are currently involved in snakebite management [20], fewer laboratories have adopted the production of the latter ones for commercial purposes [24]. Specifically, in vast majority of cases F(ab')₂ antivenoms have been considered more efficacious in a clinical setting owing to their pharmacokinetic properties, which are valid for longer retention in systemic circulation, and possession of two antigen-binding sites, mediating the venom-neutralization activity through formation of large, stable and precipitable complexes [20, 25].

Additional procedures, most notably ion-exchange chromatography, have been introduced to increase the product's purity after an initial processing step, such as salting-out or caprylic acid fractionation of pepsin-digested plasma [16, 24]. The anion-exchange approach is favored for pragmatic reasons, since contaminants bind to the column, whereas IgGs or their fragments, present at much higher concentrations, remain unhindered [24, 26]. Affinity chromatography for the purification of F(ab')₂ fragments has also been suggested [27], although its application for industrial manufacture is largely impractical from the standpoint of cost [24].

Recently, we have proposed a refinement strategy [28] as an attempt to offer a new perspective for overcoming cost-efficiency difficulties associated with antivenom production. It has been demonstrated on equine plasma and consisted of caprylic acid-mediated fractionation, depletion of precipitating agent from the IgG-enriched fraction, pepsin digestion, diafiltration of the F(ab')₂-based preparation and its final refinement by the flow-through chromatography. Although all regulatory requirements concerning yield, purity and aggregate content have been successfully fulfilled, we were challenged to lay the foundations for the development of an even more sustainable approach. The main intention was to achieve it through simplification and reduction of processing steps, performed under cost-reducing and finely tuned conditions. To the best of our knowledge, for the first time, caprylic acid precipitation has been undertaken simultaneously with pepsin digestion and applied to manufacturing of equine antivenom. Following diafiltration and chromatography, F(ab')₂-based final product of high yield and quality was obtained. Furthermore, the recovery of active drug was precisely quantified in each processing step, enabling accurate estimation of the procedure's cost-effectiveness.

Methods

Snake venom, plasma pools, animals and reagents

Vipera ammodytes ammodytes venom samples, two pools of V. ammodytes ammodytes-specific hyperimmune horse plasma (HHP) and NIH Ola/Hsd mice (18-20 g) of both sexes for lethal toxicity neutralization assay were obtained from the Institute of Immunology Inc. (Croatia). Bovine serum albumin (BSA), caprylic acid (≥ 98%), dithiothreitol (DTT), iodoacetamide (IAA), 2-(N-morpholino) ethanesulphonic acid (MES) monohydrate, o-phenylenediamine dihydrochloride (OPD), thimerosal, Tris base and Tween 20 were from Sigma-Aldrich (USA). Pepsin (from porcine gastric mucosa, 0.7 Ph. Eur. U mg^-1) was from Merck (Germany). Goat anti-horse F(ab')₂ IgG conjugated with horseradish peroxidase (HRP) was from antibodies-online (Germany). All other chemicals for buffers and solutions were from Kemika (Croatia), unless otherwise stated.

Optimization of F(ab')₂ preparation by caprylic acid precipitation and pepsin digestion co-performance

As a starting point, incubation duration (from 1 to 6 h or overnight) and temperature (23 or 37 °C) were investigated. HHP was heated at 56 °C for 1 h. After centrifugation at 3,200 × g for 40 min and discarding the pellet, supernatant was acidified to pH 3.2 using 6 M HCl. Subsequently, caprylic acid and pepsin in 0.15 M NaCl were added while vigorously stirring (750 rpm) in a thermomixer (Eppendorf, Germany). In every 2-fold diluted reaction mixture (V = 1 mL), the final concentration of caprylic acid was 2% (V/V) and the pepsin-to-IgG ratio was 1:75 (w/w). At timed intervals, solutions were neutralized by mixing with 1 M Tris base and centrifuged again (2,800 × g, 45 min). Supernatants were collected and filtered through cellulose acetate filters with a pore size of 5 μm (Sartorius, Germany).

Subsequently, the pepsin-to-IgG ratio (X1) and temperature (X2), each at two levels (marked with minus (-) for the lower and plus (+) for the higher level), were further selected to study their impact on the outcome of a simultaneously performed precipitation and digestion. The incubation duration producing the highest yield (i.e. 2 h) was selected according to results from the experiment described above. Investigated factors' values were 1:30 or 1:75 (w/w) for the pepsin-to-IgG ratio and 21 or 25 °C for temperature. A full factorial design was employed [29], resulting in 4 experimental runs. Each was performed in triplicate. The main effect of each factor was calculated according to Eq. (1),

$$E_X=\frac{2*\sum {\overline{Y}}_j^{+}}{n}-\frac{2*\sum {\overline{Y}}_j^{-}}{n}$$ (1)

where index X represents factors 1 or 2, n is the total number of experimental runs (4), while $${\overline{Y}}_j^{-}$$ and $${\overline{Y}}_j^{+}$$ are F(ab')₂ yields (%) obtained at the - and + level of each factor. The significance of the given factors was determined by means of ANOVA using the software Statistica 13.5 (StatSoft, TIBCO Software Inc.).

Protein products of simultaneous precipitation and digestion step were analyzed by SDS-PAGE. Preliminarily, in low-scale experiments, yield and purity were monitored by size-exclusion chromatography (SEC). When optimal conditions were achieved, the procedure was scaled up 20-fold and F(ab')₂ quantity was measured by ELISA (as described in "ELISA assay for F(ab')₂ content determination" section).

Diafiltration and flow-through chromatography for the final polishing

Following simultaneous precipitation and digestion of HHP, the supernatant (crude F(ab')₂) was diafiltrated into 20 mM MES + 0.15 M NaCl, pH 5.0, using a Vivaspin centrifugal concentrator (Sartorius, Germany) with a molecular weight cutoff (MWCO) polyethersulphone membrane of 50 kDa. The resultant preparation was marked as pure F(ab')₂.

Diafiltrated samples of pure F(ab')₂ were loaded (2 mL per run) to pre-equilibrated CIM QA disk (V = 0.34 mL; BIA Separations, Slovenia) with 20 mM MES + 0.15 M NaCl binding buffer, pH 5.0, at a flow rate of 2 mL min^-1 on an ÄKTA chromatography system (GE Healthcare, USA). The absorbance was monitored at 280 nm. After collecting the flow-through fractions (referred to as ultrapure F(ab')₂), the bound components were eluted from the column with binding buffer containing 1 M NaCl.

Electrophoretic and chromatographic profiling

The purity of the F(ab')₂ sample (20 μg) in each processing step was examined by SDS-PAGE analysis according to the manufacturer's protocol using MES-containing running buffer in combination with 4-12% Bis-Tris gel under non-reducing conditions in an Xcell SureLock Mini-Cell (Invitrogen, USA). Staining was carried out with acidic Coomassie Brilliant Blue (CBB) R250 or, alternatively, AgNO₃ for "negative" detection of pepsin remains [30]. As the first dimension of 2D gel electrophoresis, a ZOOM IPGRunner Mini-Cell (Invitrogen, USA) was used in combination with immobilized pH gradient (IPG) strip (7 cm long, linear pH 3-10; Invitrogen, USA) rehydrated with F(ab')₂ sample (350 μg). The following step voltage protocol was applied: 200 V for 20 min, 450 V for 15 min, 750 V for 15 min and 2,000 V for 6 h. For the second dimension, 4-12% Bis-Tris gel was used as described above after reduction (20 mM DTT) and alkylation (125 mM IAA). CBB R250-stained protein spots served as starting material for mass spectrometry (MS) analysis.

SEC analysis, which was employed for monitoring of F(ab')₂ purity in all three purification steps, was performed on TSK-Gel G3000SWXL column (7.8 × 300 mm; Tosoh Bioscience, Japan) with 0.1 M phosphate-sulfate running buffer, pH 6.6, at a flow rate of 0.5 mL min^-1 on a Waters HPLC system (Waters, USA). The sample (2 mg mL^-1) was loaded to column in a volume of 50 μL per run. The effluent was monitored at 280 nm. For determination of F(ab')₂ molecular weight, thyroglobulin (M _r 665,000), γ-globulin (M _r 150,000), ovalbumin (M _r 44,300) and ribonuclease A (M _r 13,700) were used as standards.

MALDI-MS analysis

Excised protein spots obtained by 2D gel electrophoresis of F(ab')₂ sample were prepared and analyzed by MALDI MS/MS on an ultrafleXtreme (Bruker, Germany), as described by Kurtović et al. [28]. Proteins were considered to be confidently identified after submitting peptide sequencing data to Mascot (taxonomy "other mammalians") and receiving statistically significant scores for at least two peptides per protein. If data on only one peptide were available, theoretical molecular masses and pI values of the database entry were compared to experimental 2D gel electrophoresis results and, in the case of agreement, the identification was considered to be correct.

Protein, IgG and F(ab')₂ concentration determination

Throughout the isolation procedure, the total protein concentration was estimated spectrophotometrically by use of the Eq. (2) [31],

$$\gamma \left[mg{mL}^{-1}mL\right]=(A_{228.5nm}–A_{234.5nm})\times f\times dilutionfactor$$ (2)

where Ehresmann's factor "f" for equine IgG of 0.2553 was used [32].

The IgG concentration in each HHP was measured by ELISA, as described previously [28].

F(ab')₂ content in samples from HHP processing was determined by ELISA according to the protocol from Kurtović et al. [28]. European viper venom antiserum (Zagreb antivenom; Institute of Immunology Inc., Croatia) was used as the standard. Considering composition differences in subclass and/or venom-specific antibody distribution between each investigated sample and the standard, a recently developed principle for F(ab')₂ estimation that uses sample-specific correction was applied [32]. Namely, F(ab')₂ preparation of the highest purity (referred to as ultrapure F(ab')₂), which was processed from the respective HHP and precisely quantified, served as the internal reference. Its concentration was calculated as: [SEC-determined purity in percentage / 100%) × γ(protein) ].

Yield was calculated as: [ (γ(F(ab')₂) × dilution factor) / (γ(IgG) in HHP × 0.67) ] × 100%. IgG and F(ab')₂ concentrations were measured by the respective ELISA assays, as described above. Purities of intermediates and the final product were expressed as: [γ(F(ab')₂) / γ(protein) ] × 100%, where total protein concentration was determined spectrophotometrically according to Eq. (2). SEC monitoring for purity profiling was also included.

ED₅₀ test

The potential of HHP and final F(ab')₂ preparation to neutralize the venom's lethal toxicity was determined by the lethal toxicity neutralization assay in mice [33]. The lethal toxicity neutralization potency (R) was expressed as the number of LD₅₀ venom doses that can be neutralized by 1 mL of undiluted sample and calculated by Eq. (3),

$$R=(\mathrm{T}\mathrm{v}-1)\mathrm{}/\mathrm{}{\mathrm{E}\mathrm{D}}_{50}$$ (3)

where Tv represents the number of LD₅₀ venom doses inoculated per mouse [34]. The R-value was used as a measure of the protective efficacy of each sample. Specific activity (LD₅₀ mg^-1) was calculated as a ratio of R-value and either active drug (F(ab')₂) or total protein concentration.

Results

Optimization of F(ab')₂ preparation

Initially, all experimental conditions were adopted from our previously developed downstream processing strategy in which extraction of IgGs and their subsequent enzymatic cleavage were performed as two separate operating units with an interposed diafiltration-mediated removal of precipitating agent [28]. Namely, heat-treated HHP, acidified to pH 3.2, was fractionated and digested at once by simultaneous incubation with 2% caprylic acid (V/V) and pepsin, the latter in a quantity 75-times lower than the measured IgG content (1:75, w/w). Temperature was set to 37 °C. SDS-PAGE analysis of samples from 1.5 and 2 h incubation durations revealed major contaminations of F(ab')₂ products (Fig. 1A, left panel). In addition, following diafiltration on a 50 kDa membrane, total protein concentration in each retentate was decreased by approximately 60%, indicating loss of the target component.

In the neasxt experiment, the impact of temperature reduction on the efficiency of contaminants removal and boosting of F(ab')₂ yield was examined. Incubation was performed at 23 °C from 1 to 6 h or overnight. The other operating parameters remained unchanged. SDS-PAGE analysis revealed that even a short reaction time was sufficient to achieve precipitation of almost all unwanted plasma proteins and complete hydrolysis of IgG material remaining in supernatant (Fig. 1A, right panel). High purity of around 90% was achieved post-diafiltrationally, while yield declined with prolongation of incubation (Fig. 1B). The highest one of around 80% was obtained when digestion was terminated after 2 h.

A previous experiment indicated appropriateness of 2-h long incubation at 23 °C. Finally, the pepsin-to-IgG ratio (1:30 or 1:75, w/w) and temperature (21 or 25 °C) were examined according to the full factorial design. Their impact on F(ab')₂ yield is presented in Figure 1C. The main effect estimates E _X for each factor are indicated in Figure 1D. Statistical analysis showed that only factor X1 (pepsin-to-IgG ratio) had significant influence on response variables (α = 0.01) in the tested range of its values. A higher pepsin concentration improved yield. At the same time, it slightly impaired purity, probably due to the contribution of the enzyme itself. Accordingly, a pepsin-to-IgG ratio of 1:30 (w/w) and temperature of 21 °C, which positively affected yield, although not significantly, were selected as optimal conditions.

Figure 1.
Optimization of F(ab')₂ preparation. (A) SDS-PAGE analysis of samples (20 μg) obtained by simultaneous caprylic acid precipitation and pepsin digestion of HHP at 37 or 23 °C. Lane 1, HHP; Lane 2, sample obtained at 37 °C with 1.5 h-long incubation; Lane 3, molecular weight standards; lanes 4-8, samples obtained at 23 °C with duration of incubation as indicated. Staining was performed with CBB R250. (B) Time-course of SEC-determined yields and purities of F(ab')₂ preparations obtained by precipitation and digestion co-performance at 23 °C following diafiltration on a 50 kDa membrane. Results are given as mean +/- standard error. (C) Optimization of precipitation and digestion co-performance step with respect to the pepsin-to-IgG ratio and temperature studied according to full factorial experimental design. Mean yield (ο) of active drug obtained post-diafiltrationally at higher and lower level of each experimental factor (X1 - pepsin-to-IgG ratio, X2 - temperature) in comparison to mean value (full line) and 95% confidence interval (dashed lines) from the overall set of experiments. (D) Pareto plot of effect estimates. The absolute value of the main effect for each factor (|E _x |) is presented in horizontal columns. The critical effect values for significance level of α = 0.01 is marked by a vertical line.

F(ab')₂ preparation under optimized conditions and final polishing

In the first step, fractionation of HHP (Fig. 2A) with 2% (V/V) caprylic acid and digestion of plasma proteins, utilizing pepsin at a concentration 30-times lower than the measured IgG content (1:30, w/w), were co-performed. The established conditions, pH of 3.2 in the reaction mixture and 21 °C, proved supportive for concerted precipitation and enzymatic cleavage. For a 2 h incubation duration, a significant reduction of contamination in the supernatant occurred, while the whole IgG fraction that remained in solution underwent limited hydrolysis, resulting in F(ab')₂ fragments as the dominant product (crude F(ab')₂) (Figs. 2B and 3A) at the expected molecular weight (91.7 ± 1.7 kDa, n = 12) and with satisfactory recovery (Table 1). Specifically, the average yield of the first step was around 85%.

Enhancement of purity approaching 90% was achieved through diafiltration-mediated removal of small molecular fragments of Fc and digestion by-products of albumin and other plasma proteins (Figs. 2C and 3A, Table 1). Following diafiltration as an intermediate step, pure F(ab')₂ was obtained. SEC revealed absence of aggregates from F(ab')₂-enriched product, either crude (Fig. 2B) or pure (Fig. 2C).

In the third purification step residual by-product contaminants, especially pepsin, were removed from the pure F(ab')₂ by anion-exchange chromatography. Optimal conditions were adopted from our previous research, i.e., exclusive adsorption of the enzyme and other acidic impurities to the column while the target compound passes unhindered [28]. Final polishing produced an active drug (ultrapure F(ab')₂) of approximately 97% purity and without any loss (Fig. 2D, Table 1). The recovery of CIM QA chromatography step was 100.9 ± 4.3% (n = 11). The overall yield was 74% (Table 1). The final product was free from aggregates (Fig. 2D) and depleted from pepsin, as confirmed by SDS-PAGE analysis and absence of ''negative'' band at position corresponding to its molecular weight following silver staining (Fig. 3B).

Figure 2.
The assessment of purification steps by size-exclusion chromatography. The analysis was performed on a TSK-Gel G3000SWXL column (7.8 × 300 mm) with 0.1 M phosphate-sulfate running buffer, pH 6.6, at a flow rate of 0.5 mL min^-1. The sample (2 mg mL^-1) was loaded to the column in a volume of 50 μL per run. (A) Heat-treated plasma. (B) F(ab')₂ fraction obtained by simultaneous 2% caprylic acid (V/V) precipitation and pepsin digestion before (crude IgG) and (C) after diafiltration using a 50 kDa membrane (pure IgG). (D) Ultrapure F(ab')₂ preparation - flow-through fraction from anion-exchange chromatography performed at pH 5.0. Detection: UV at 280 nm.

Figure 3.
Gel electrophoresis of representative samples from purification process on 4-12% gel. (A) SDS-PAGE analysis of HHP (40 μg) and F(ab')₂ fractions (20 μg) under non-reducing conditions with CBB R250 staining. Lane 1, molecular weight standards; Lane 2, HHP; Lane 3, F(ab')₂ fraction obtained by simultaneous 2% caprylic acid (V/V) precipitation and pepsin digestion (crude F(ab')₂); Lane 4, F(ab')₂ fraction after diafiltration (pure F(ab')₂); lanes 5 and 6, F(ab')₂ preparation using CIM QA chromatography (ultrapure F(ab')₂). (B) SDS-PAGE analysis of F(ab')₂ fractions (20 μg) under non-reducing conditions with silver staining. Lanes 1-4 correspond to lanes 3-6 from (A). "Negatively" silver-stained bands corresponding to pepsin are denoted by arrow. (C) 2D gel electrophoresis of the final product. In the first dimension F(ab')₂ (350 μg) was focused using IPG strip under denaturing conditions (linear pH 3-10). Prior second dimension IPG strip was reduced, alkylated and loaded to a 4-12% gel. Proteins were detected with CBB R250 and identified by MS/MS analysis (LC = light chain, HC = heavy chain). Molecular mass markers are on the left side.

Table 1.
Purities and yields of the intermediates and the final product obtained by developed downstream processing protocol. Two different plasma pools (HHP1 and HHP2) were used. IgG purities in HHPs, before and after thermal treatment, are expressed as means from n measurements +/- 95% confidence interval. IgG yields in thermally treated HHPs, as well as F(ab')₂ purities and yields, are given as means from n independent process performances +/- 95% confidence interval.

Processing step	Product	IgG/F(ab')2 purity (%)	IgG/F(ab')2 yield (%)*	Overall IgG/F(ab')2 yield (%)
	HHP1	47.8 ± 2.9 (n = 17)	n.a.	n.a.
	HHP2	41.5 ± 2.8 (n = 15)	n.a.	n.a.
Heat denaturation	Thermally treated HHP1	46.9 ± 4.1 (n = 9)	91.6 ± 2.4 (n = 8)	91.6 ± 2.4 (n = 8)
	Thermally treated HHP2	44.0 ± 3.2 (n = 26)
Precipitation and digestion	Crude F(ab')2	60.4 ± 1.7 (n = 5)	85.2 ± 6.1 (n = 6)	76.8 ± 5.5 (n = 6)
Diafiltration	Pure F(ab')2	86.7 ± 6.4 (n = 6)	95.9 ± 6.1 (n = 6)	73.6 ± 6.1 (n = 6)
Anion-exchange HPLC	Ultrapure F(ab')2	97.3 ± 4.0 (n = 8)	100.9 ± 4.3 (n = 11)	74.3 ± 5.9 (n = 8)

• *Yield in relation to the preceding processing step

MS/MS analysis of the final product

MS/MS analysis of protein spots obtained by 2D gel electrophoresis, intentionally performed by sample overloading for even minor contaminants to appear, confirmed high purity of the final product which predominantly consisted of F(ab')₂ fragments since mostly peptides from the IgG heavy chain (constant region) and the light chain (variable region) were identified. In the most abundant protein spots on 2D gel, unique peptides from the IgM heavy chain were detected. The rest of the discrete protein spots contained only traces of transthyretin and inter-alpha-trypsin inhibitor (Fig. 3C, ^{Additional file 1}).

Protective efficacy of F(ab')₂ preparation

Neutralization potencies of HHP and F(ab')₂-based preparation, together with specific activities of their IgGs or F(ab')₂ fragments, are summarized in Table 2. According to the lethal toxicity neutralization assay in mice, no loss of the specific activity of the active drug in the final product with respect to that in starting material occurred. Purification factor of 3.9-fold, calculated as a ratio of specific activities of F(ab')₂ preparation and HHP, was achieved (Table 2).

Table 2.
In vivo neutralization potencies of HHP and F(ab')₂ with specific activities. Purification factors obtained through manufacturing procedure are indicated. Results are expressed as means from n independently performed experiments +/- standard deviation.

		Plasma	Ultrapure F(ab')2
R a	[LD50 mL-1]	44.0 ± 15.9 (n = 7)	94.1 ± 5.9 (n = 2)
γ(IgG) / (Fab')2b	[mg mL-1]	27.3 ± 2.3 (n = 9)	29.3 ± 0.2 (43.7 ± 0.3)* (n = 3)
Specific activity of active drugc	[LD50 mg-1]	1.6 ± 0.6	2.2 ± 0.1
γ(protein)d	[mg mL-1]	58.2 ± 4.4 (n = 25)	30.1 ± 0.2 (n = 3)
Specific activity of samplee	[LD50 mg-1]	0.8 ± 0.3	3.1 ± 0.2
Purification factorf	[× ]	1.0	3.9

• ^a
  Lethal toxicity neutralization potency. ^bIgG or F(ab')₂ mass concentration. ^cSpecific activity of active drug in the sample calculated as ratio of R to γ(IgG) or γ(F(ab')₂), respectively. ^dTotal protein mass concentration. ^eSpecific activity of the sample calculated as ratio of R to γ(protein). ^fPurification factor calculated as ratio of specific activities of F(ab')₂ product and HHP.
• *Assumption of molecular weight reduction of the active drug due to Fc removal was considered

Discussion

An effective strategy for antivenom preparation from equine plasma raised against V. ammodytes ammodytes venom is described. A highly stratified methodology was employed in which the elimination of the Fc part of IgGs occurred simultaneously with other plasma proteins, followed by further contaminant removal from the target compound, F(ab')₂, by diafiltration and flow-through chromatography. Only three consecutive processing steps are sufficient to accomplish high yield, precisely quantified throughout the manufacturing procedure, and fulfilling the regulatory demands. In each phase the target compound was intentionally kept in solution to reduce the possibility of any conformational and/or structural change. The approach might be of great importance in large-scale manufacturing due to the ease of discarding precipitated unwanted proteins.

Initially, heat-treated plasma was exposed to the concurrent action of caprylic acid (2%, V/V) and pepsin (enzyme:IgG = 1:75, w/w) at pH 3.2 for 1.5 h. According to SDS-PAGE analysis, a temperature, set at 37 °C, proved unsupportive for precipitation of unwanted cleavage products (Fig. 1A). Furthermore, unexpectedly low total protein yield was obtained after diafiltration on a 50 kDa membrane, indicating that IgGs were probably over-digested. The single-reagent format has been conceptualized by Al-Abdulla et al. [17] who employed it for preparation of antivenom from ovine serum. Under conditions similar to ours, with the exception of a slightly higher pH (3.5) and longer incubation (4 h), they succeeded in obtaining F(ab')₂-based product, reporting 94% purity following subsequent downstream processing steps, while a yield of around 58% could be calculated from provided data. Evidently, since two systems with their own specificities, including different immunoglobulin profiles, were involved, process terms established on ovine-originating starting material were not simply transferrable to equine plasma whose manipulation required an individualized approach. Therefore, in our work every step has been optimized de novo until finely tuned conditions for production of equine antivenom were achieved.

Lowering the temperature solved F(ab')₂ contamination and loss issues (Fig. 1B), while use of pepsin at a higher concentration significantly improved yield (Figs. 1C and 1D). Under optimal conditions (temperature of 21 °C, enzyme: IgG = 1:30, w/w) only a 2 h incubation duration was sufficient to obtain crude F(ab')₂ (Figs. 2B and 3A) with yield exceeding 70% (Table 1). It is noteworthy to mention the importance of the caprylic acid-mediated precipitation step in the overall purification process. Its implementation not only contributes to virus safety [20], but also, as we demonstrated, enables effective F(ab')₂ preparation with rational pepsin amount even at a lower temperature, which opens up space for simplification of the production equipment and reduction of cost. For monitoring of the process efficiency and purity profiling, ELISA with sample-specific correction of results [32] for IgG quantification in plasma was preferentially chosen over other quantification methods such as SEC and densitometry, where overlapping of peaks/bands due to poor resolution or influence of protein type on surface area and intensity of developed color, respectively, is highly probable, leading to inaccurate result interpretation [35, 36, 37].

Enhancement of purity approaching 90% was achieved through diafiltration-mediated removal of small molecular fragments of most likely Fc, albumin and other plasma protein digestion by-products (Table 1). Surprisingly, SEC analysis revealed absence of aggregates from F(ab')₂-enriched product, either crude (Fig. 2B) or pure (Fig. 2C). In our "first precipitation then cleavage" concept diafiltration as an intermediate step between caprylic acid fractionation and pepsin digestion was shown to be crucial for obtaining the final product of satisfactory composition [28]. Specifically, only removal of precipitating agent from IgG substrate prior to addition of enzyme ensured obtaining of F(ab')₂ sample almost completely free of aggregates. In the refinement protocol presented herein, IgGs or F(ab')₂ fragments remain protected from unwanted phenomena during their exposure to conditions involving mutual presence of caprylic acid and pepsin. Absence of aggregation might be associated with lower incubation temperature.

Diafiltration was only partially effective for pepsin elimination, as already reported by others [26], and presented in our own research [28]. Therefore, a third purification step was introduced in which the equine plasma-derived F(ab')₂ preparation was additionally polished by anion-exchange chromatography at pH 5.0 in the flow-through mode that enables efficient binding of residual acidic impurities, including the remaining pepsin, and unhindered passing of active drug [28]. The purity of 97% (Table 1) was somewhat poorer in comparison to that achieved by our originally developed downstream processing strategy, but is nevertheless within the range of methods published for some other F(ab')₂ products which were prepared by various methodologies from hyperimmune plasma or serum on both the laboratory and manufacturing scale [16, 17, 27, 36, 38].

In order to get a deeper insight into contaminations of the final preparation, 2D gel electrophoresis and MS/MS analysis were performed (Fig. 3C, ^{Additional file 1}). This approach can also be considered as a further step for quality insurance. The great majority of protein spots have been attributed to IgG fragments. Some low-abundance protein spots, especially those of 15 kDa or less, were not successfully identified, either because of lack of material or insufficiently generated peptides.

An overall yield of around 74% (Table 1) was comparable to the process recovery obtained by our alternative scheme [28]. It appeared also as good as or even better than yields associated with enhanced-pepsin digestion (66-70%) and single-reagent protocols (56-60%) for refinement of ovine serum [17], assuming, as stated, that IgGs at concentrations between 30 and 32 g L^-1 are commonly found in immunized sheep [21]. Although scarce, reports of efficiencies of downstream processing strategies for production of F(ab')₂ antitoxins from pepsin-digested horse plasma are also in the literature, all being lower than the efficiency of the procedure herein described. When as additional steps either caprylic acid fractionation followed by ion-exchange chromatography [16] or combination of ion-exchange and affinity chromatography were employed [38], antibody activity recoveries of 65 and 41% were accomplished, respectively. Morais and Massaldi [39] reported that, under quite similar pH/time conditions, purified IgGs were cleaved to F(ab')₂ fragments with 65% recovery of antigen-binding activity, measured by competitive ELISA stated to be in close correlation with ED₅₀ assay.

Specific activity of F(ab')₂ fragments at first appeared higher in comparison to that of the whole IgG molecules in starting plasma, although the difference is a consequence of protein content reduction in the final product due to Fc part removal. When the decrease in molecular weight of F(ab')₂ fragments in relation to IgGs was considered, active drugs in the final product (F(ab')₂) and in the respective plasma pool (IgG) were of comparable specific activities, proving that the Fc fraction is not relevant for the blocking of venom toxins. This finding supports our previous research [28] and agrees with the in vivo neutralization potency data provided by Segura et al. [36]. The fully preserved protective efficacy of F(ab')₂ fragments, comparable to that of IgGs in plasma, implies that manufacturing process conditions did not affect significantly tertiary structure of the active drug nor provoked either loss of neutralizing IgG subclasses or redistribution of the venom-specific antibody content.

Conclusion

Fractionation of the venom-specific equine plasma employing compressed mode was independently repeated several times on two plasma pools of slightly different protective efficacy and by two analysts. Although appearing slightly inferior in comparison to our standard procedure with respect to purity, it resulted in an aggregate- and pepsin-free active drug with overall yield that was as good as or better than others so far reported. In addition to good physicochemical profile and high recovery of the product, the performance simplicity together with the short production cycle time in the laboratory setting were demonstrated. The suitability for large-scale antivenom manufacturing looks promising, but still needs to be addressed.

Acknowledgments

The authors would like to thank N. Pavlović for help with statistical analysis and M. Tunjić for technical assistance.

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• Availability of data and materials

  All data generated or analyzed during the study are included in this article.

• Funding

  This work has been supported by Croatian Science Foundation (grant IP-2014-09-4915 to BH) and bilateral Croatian-Austrian project (grant HR 13/2016 to MMD).

• Ethics approval

  Animal experimentation was approved by the Croatian Ministry of Agriculture, Veterinary and Food Safety Directorate (UP/I-322-01/17-01/75, permission no. 525-10/0255-17-6). The approval is based on the positive opinion of the National Ethics Committee (EP 110/2017). The protocols for animal care and handling were in accordance with the guideline of the Croatian Law on Animal Welfare (2017), which strictly complies with EC Directive (2010/63/EU).

• Consent for publication

  Not applicable.

Supplementary material

The following online material is available for this article:

Additional file 1. (A) Two-dimensional gel electrophoresis (2DE) of F(ab')₂-based final product (same sample as in Fig. 3C) with annotations of protein spots subjected to MS/MS analysis. (B) List of proteins identified in the final F(ab')₂ sample. Proteins are denoted by the same numbers as in (A). Other protein spots remained unidentified.

Erratum:

• In the article entitled “Streamlined downstream process for efficient and sustainable F(ab')₂ antivenom preparation”, DOI: 10.1590/2358-2936e20200025, published in Journal of Venomous Animals and Toxins including Tropical Diseases, 2020, 26,
  Page 1, in the title, where it was written:
  “Streamlined downstream process for efficient and sustainable (Fab’)₂ antivenom preparation”
  Must be read:
  “Streamlined downstream process for efficient and sustainable F(ab’)₂ antivenom preparation”
  And in page 8, Table 2, first column, where it was written:
  “γ(IgG) / (Fab')₂”
  Must be read:
  “γ(IgG) / F(ab')₂”
  The correction does not affect the discussion or conclusions of the original article.

Publication Dates

• Publication in this collection
  27 July 2020
• Date of issue
  2020

History

• Received
  02 Mar 2020
• Accepted
  06 July 2020