“Inclonals”

Full-length antibodies and antibodies that ferry a cargo to target cells are desired biopharmaceuticals. We describe the production of full-length IgGs and IgG-toxin fusion proteins in E. coli. In the presented examples of anti CD30 and anti EGF-receptor antibodies, the antibody heavy and light chains or toxin fusions thereof were expressed in separate bacterial cultures, where they accumulated as insoluble inclusion bodies. Following refolding and purification, a high yield (up to 50 mg /L of shake flask culture) of highly purified (>90%) full-length antibodies and antibody-toxin fusions were obtained. The bacterially produced antibodies, named "Inclonals," equaled the performance of the same IgGs that were produced using conventional mammalian cell culture in binding properties as well as in cell killing potency. The rapid and cost effective IgG production process and the high quality of the resultant product may make the bacterial production of full-length IgG and IgG-drug fusion proteins an attractive option for antibody production. and a significant contribution to recombinant antibody technology.     

单克隆抗体生产过程中二硫键还原成因及预防方法

单克隆抗体生产过程中二硫键的还原是生物制药领域中的一个常见技术难题,可产生低分子量碎片,影响产品质量,导致蛋白纯度降低、稳定性下降,影响药物的安全性和有效性。抗体二硫键还原实质上是由细胞内的硫氧还蛋白系统和谷胱甘肽系统引起的可逆氧化还原反应,并与具体生产过程参数有关。近年来,随着抗体药物和哺乳动物细胞培养工艺规模的发展,二硫键还原问题频繁发生。为解决此问题,研究人员不断尝试并建立了多种预防方法以保证产品质量。概述了抗体二硫键结构、二硫键还原的主要成因及生产过程中的形成因素,重点阐述了消除或减缓抗体二硫键还原的方法、对策,并列举了几种可行的过程分析技术,以期为单克隆抗体药物生产制造工艺的进一步优化提供参考。     

Red colored IgG4 caused by vitamin B12 from cell culture media combined with disulfide reduction at harvest

While many antibody therapeutics are formulated at low concentration (~10–20 mg/mL) for intravenous administration, high concentration (> 100 mg/mL) formulations may be required for subcutaneous delivery in certain clinical indications. For such high concentration formulations, product color is more apparent due to the higher molecular density across a given path-length. Color is therefore a product quality attribute that must be well-understood and controlled, to demonstrate process consistency and enable clinical trial blinding. Upon concentration of an IgG4 product at the 2000 L manufacturing scale, variability in product color, ranging from yellow to red, was observed. A small-scale experimental model was developed to assess the effect of processing conditions (medium composition and harvest conditions) on final bulk drug substance (BDS) color. The model was used to demonstrate that, for two distinct IgG4 products, red coloration occurred only in the presence of disulfide reduction-mediated antibody dissociation. The red color-causing component was identified as vitamin B₁₂, in the hydroxocobalamin form, and the extent of red color was correlated with the cobalt (vitamin B₁₂) concentration in the final pools. The intensity of redness in the final BDS was modulated by changing the concentration of vitamin B₁₂ in the cell culture media.     

Impact of media and antifoam selection on monoclonal antibody production and quality using a high throughput micro‐bioreactor system

Monoclonal antibody production in commercial scale cell culture bioprocessing requires a thorough understanding of the engineering process and components used throughout manufacturing. It is important to identify high impact components early on during the lifecycle of a biotechnology‐derived product. While cell culture media selection is of obvious importance to the health and productivity of mammalian bioreactor operations, other components such as antifoam selection can also play an important role in bioreactor cell culture. Silicone polymer‐based antifoams were known to have negative impacts on cell health, production, and downstream filtration and purification operations. High throughput screening in micro‐scale bioreactors provides an efficient strategy to identify initial operating parameters. Here, we utilized a micro‐scale parallel bioreactor system to study an IgG1 producing CHO cell line, to screen Dynamis, ProCHO5, PowerCHO2, EX‐Cell Advanced, and OptiCHO media, and 204, C, EX‐Cell, SE‐15, and Y‐30 antifoams and their impacts on IgG1 production, cell growth, aggregation, and process control. This study found ProCHO5, EX‐Cell Advanced, and PowerCHO2 media supported strong cellular growth profiles, with an IVCD of 25‐35 × 10⁶ cells‐d/mL, while maintaining specific antibody production (Q_p > 2 pg/cell‐d) for our model cell line and a monomer percentage above 94%. Antifoams C, EX‐Cell, and SE‐15 were capable of providing adequate control of foaming while antifoam 204 and Y‐30 noticeably stunted cellular growth. This work highlights the utility of high throughput micro bioreactors and the importance of identifying both positive and negative impacts of media and antifoam selection on a model IgG1 producing CHO cell line. © 2017 The Authors Biotechnology Progress published by Wiley Periodicals, Inc. on behalf of American Institute of Chemical Engineers Biotechnol. Prog., 34:262–270, 2018     

“Inclonals”: IgGs and IgG-enzyme fusion proteins produced in an E. coli expression-refolding system

Full-length antibodies and antibodies that ferry a cargo to target cells are desired biopharmaceuticals. We describe the production of full-length IgGs and IgG-toxin fusion proteins in E. coli. In the presented examples of anti CD30 and anti EGF-receptor antibodies, the antibody heavy and light chains or toxin fusions thereof were expressed in separate bacterial cultures, where they accumulated as insoluble inclusion bodies. Following refolding and purification, high yields (up to 50 mg/L of shake flask culture) of highly purified (>90%) full-length antibodies and antibody-toxin fusions were obtained. The bacterially produced antibodies, named “Inclonals,” equaled the performance of the same IgGs that were produced using conventional mammalian cell culture in binding properties as well as in cell killing potency. The rapid and cost effective IgG production process and the high quality of the resultant product may make the bacterial production of full-length IgG and IgG-drug fusion proteins an attractive option for antibody production and a significant contribution to recombinant antibody technology.Key words: IgG, IgG-toxin fusion protein, CD30, EGFR, PE38, inclusion bodies, refolding     

Removal of a C-terminal serine residue proximal to the inter-chain disulfide bond of a human IgG1 lambda light chain mediates enhanced antibody stability and antibody dependent cell-mediated cytotoxicity

Optimization of biophysical properties is a critical success factor for the developability of monoclonal antibodies with potential therapeutic applications. The inter-domain disulfide bond between light chain (Lc) and heavy chain (Hc) in human IgG1 lends structural support for antibody scaffold stability, optimal antigen binding, and normal Fc function. Recently, human IgG1λ has been suggested to exhibit significantly greater susceptibility to reduction of the inter Lc-Hc disulfide bond relative to the same disulfide bond in human IgG1κ. To understand the molecular basis for this observed difference in stability, the sequence and structure of human IgG1λ and human IgG1κ were compared. Based on this Lc comparison, three single mutations were made in the λ Lc proximal to the cysteine residue, which forms a disulfide bond with the Hc. We determined that deletion of S214 (dS) improved resistance of the association between Lc and Hc to thermal stress. In addition, deletion of this terminal serine from the Lc of IgG1λ provided further benefit, including an increase in stability at elevated pH, increased yield from transient transfection, and improved in vitro antibody dependent cell-mediated cytotoxicity (ADCC). These observations support the conclusion that the presence of the terminal serine of the λ Lc creates a weaker inter-chain disulfide bond between the Lc and Hc, leading to slightly reduced stability and a potential compromise in IgG1λ function. Our data from a human IgG1λ provide a basis for further investigation of the effects of deleting terminal serine from λLc on the stability and function of other human IgG1λ antibodies.     

High‐efficiency affinity precipitation of multiple industrial mAbs and Fc‐fusion proteins from cell culture harvests using Z‐ELP‐E2 nanocages

Affinity precipitation using Z‐elastin‐like polypeptide‐functionalized E2 protein nanocages has been shown to be a promising alternative to Protein A chromatography for monoclonal antibody (mAb) purification. We have previously described a high‐yielding, affinity precipitation process capable of rapidly capturing mAbs from cell culture through spontaneous, multivalent crosslinking into large aggregates. To challenge the capabilities of this technology, nanocage affinity precipitation was investigated using four industrial mAbs (mAbs A–D) and one Fc fusion protein (Fc A) with diverse molecular properties. A molar binding ratio of 3:1 Z:mAb was sufficient to precipitate >95% mAb in solution for all molecules evaluated at ambient temperature without added salt. The effect of solution pH on aggregation kinetics was studied using a simplified two‐step model to investigate the protein interactions that occur during mAb–nanocage crosslinking and to determine the optimal solution pH for precipitation. After centrifugation, the pelleted mAb–nanocage complex remained insoluble and was capable of being washed at pH ≥ 5 and eluted with at pH < 4 with >90% mAb recovery for all molecules. The four mAbs and one Fc fusion were purified from cell culture using optimal process conditions, and >94% yield and >97% monomer content were obtained. mAb A–D purification resulted in a 99.9% reduction in host cell protein and >99.99% reduction in DNA from the cell culture fluids. Nanocage affinity precipitation was equivalent to or exceeded expected Protein A chromatography performance. This study highlights the benefits of nanoparticle crosslinking for enhanced affinity capture and presents a robust platform that can be applied to any target mAb or Fc‐containing proteins with minimal optimization of process parameters.     

Effect of process change from perfusion to fed-batch on product comparability for biosimilar monoclonal antibody

A fed-batch process for the production of biosimilar monoclonal antibody was developed. Since the brand product is produced by perfusion process, the impact of process change from perfusion to fed-batch on product quality and cell performance was evaluated. Perfusion culture was performed at 0.47–1.00 (v/v/d) perfusion rate by spin-filter method with 15–17 μm mesh. Culture parameters such as pH (6.8–7.2), dissolved oxygen (40–70% air saturation), temperature (37 °C) and agitation speed (250 rpm) were applied in both culture modes. In terms of cell performance, volumetric productivity increased 3.7 times while process performance increased 7.5 times in fed-batch culture due to 10 times higher scalability. Considering the glycosylation pattern and charge variants, no significant changes in product quality were observed upon process change, although intact IgG level slightly decreased in fed-batch mode. The change of production media showed more effect on glycosylation patterns than the operation in different culture modes. Furthermore, there were no differences in biological activity, including TNFα, FcγRIIIa, and C1q-binding affinity. Through a scale-up study from 3 L to 12,500 L, it was confirmed that cell performance and product quality could be maintained. In conclusion, product quality of the fed-batch process was comparable to that of the reference product.     

Pretreatments for enhancing clarification efficiency of depth filtration during production of monoclonal antibody therapeutics

High cell density, high product titer mammalian cell culture is the new paradigm for production of recombinant proteins. While the typical motivation is to get a high product titer, additional undesirable outcomes often include an increase in percentage solids in the cell culture fluid (cellular debris and sub-micron colloids), thereby offering new challenges to downstream processing. This article focuses on scouting and comparison of different approaches used for clarification of cell culture fluid. The approaches include centrifugation followed by depth filtration, direct depth filtration without centrifugation and feed pretreatment with use of specially designed density gradient filtration to improve efficiency of clarification and removal of process contaminants from feed stream. The work also evaluates impact of three different pretreatment approaches, namely pH adjustment to acidic condition, metal cation (calcium phosphate) flocculation, and polycationic polymer flocculation (using polymer-I and polymer-II). The results obtained indicate that the use of pretreatment significantly improves the clarification efficiency of depth filtration. Pretreatment options like polycationic polymer-I based flocculation resulted in a >5 fold reduction in filter area requirement as well as >6 fold reduction in HCDNA while retaining acceptable recovery of the IgG (>98%). Thus, pretreatment offers a significant reduction in the depth filtration footprint (~5–6 fold decrease in filter area requirement). However, one must take into consideration the process development time required, capital cost, consumable cost, cost of the pretreatment chemical, cost of testing to demonstrate clearance of treatment agent, ease of scale-ability, and process robustness when finalizing the optimal clarification approach.     

Red colored IgG4 caused by vitamin B12 from cell culture media combined with disulfide reduction at harvest

While many antibody therapeutics are formulated at low concentration (~10–20 mg/mL) for intravenous administration, high concentration (> 100 mg/mL) formulations may be required for subcutaneous delivery in certain clinical indications. For such high concentration formulations, product color is more apparent due to the higher molecular density across a given path-length. Color is therefore a product quality attribute that must be well-understood and controlled, to demonstrate process consistency and enable clinical trial blinding. Upon concentration of an IgG4 product at the 2000 L manufacturing scale, variability in product color, ranging from yellow to red, was observed. A small-scale experimental model was developed to assess the effect of processing conditions (medium composition and harvest conditions) on final bulk drug substance (BDS) color. The model was used to demonstrate that, for two distinct IgG4 products, red coloration occurred only in the presence of disulfide reduction-mediated antibody dissociation. The red color-causing component was identified as vitamin B₁₂, in the hydroxocobalamin form, and the extent of red color was correlated with the cobalt (vitamin B₁₂) concentration in the final pools. The intensity of redness in the final BDS was modulated by changing the concentration of vitamin B₁₂ in the cell culture media.     

Impacts on product quality attributes of monoclonal antibodies produced in CHO cell bioreactor cultures during intentional mycoplasma contamination events

A mycoplasma contamination event in a biomanufacturing facility can result in costly cleanups and potential drug shortages. Mycoplasma may survive in mammalian cell cultures with only subtle changes to the culture and penetrate the standard 0.2-µm filters used in the clarification of harvested cell culture fluid. Previously, we reported a study regarding the ability of Mycoplasma arginini to persist in a single-use, perfusion rocking bioreactor system containing a Chinese hamster ovary (CHO) DG44 cell line expressing a model monoclonal immunoglobulin G 1 (IgG1) antibody. Our previous work showed that M. arginini affects CHO cell growth profile, viability, nutrient consumption, oxygen use, and waste production at varying timepoints after M. arginini introduction to the culture. Careful evaluation of certain identified process parameters over time may be used to indicate mycoplasma contamination in CHO cell cultures in a bioreactor before detection from a traditional method. In this report, we studied the changes in the IgG1 product quality produced by CHO cells considered to be induced by the M. arginini contamination events. We observed changes in critical quality attributes correlated with the duration of contamination, including increased acidic charge variants and high mannose species, which were further modeled using principal component analysis to explore the relationships among M. arginini contamination, CHO cell growth and metabolites, and IgG1 product quality attributes. Finally, partial least square models using NIR spectral data were used to establish predictions of high levels (≥10⁴ colony-forming unit [CFU/ml]) of M. arginini contamination, but prediction of levels below 10⁴ CFU/ml were not reliable. Contamination of CHO cells with M. arginini resulted in significant reduction of antibody product quality, highlighting the importance of rapid microbiological testing and mycoplasma testing during particularly long upstream bioprocesses to ensure product safety and quality.     

Development of a generic transient transfection process at 100 L scale

We have developed a generic transient transfection process at 100 L scale, using HEK293-EBNA cells and PEI as the transfection reagent for the production of recombinant IgG. The process, including large-scale plasmid preparation, expression at bioreactor scale, capture, purification and, if necessary, endotoxin removal allows reproducible production of more than 0.5 g IgG for in vitro and in vivo studies. We compared the performance of two HEK cell lines, investigated the effect of conditioned medium, optimized the DNA:PEI ratio and implemented a feed strategy to prolong the culture time to increase product yield. The transient transfection protocol developed enables a closed process from seeding culture to protein capture. The challenge of performing a medium exchange before transfection at large scale is solved by applying a continuous centrifugation step between the seeding bioreactor and the production bioreactor. After 7–8 days the harvest and capture is performed in a one-step operation using a Streamline expanded bed chromatography system. Following a polishing step the purified antibody is transferred to the final formulation buffer. The method has shown to be reproducible at 10, 50, and 100 L scale expressing between 5 and 8 mg L⁻¹ IgG.     

Cationic polymer precipitation for enhanced impurity removal in downstream processing

Precipitation can be used for the removal of impurities early in the downstream purification process of biologics, with the soluble product remaining in the filtrate through microfiltration. The objective of this study was to examine the use of polyallylamine (PAA) precipitation to increase the purity of product via higher host cell protein removal to enhance polysorbate excipient stability to enable a longer shelf life. Experiments were performed using three monoclonal antibodies (mAbs) with different properties of isoelectric point and IgG subclass. High throughput workflows were established to quickly screen precipitation conditions as a function of pH, conductivity and PAA concentrations. Process analytical tools (PATs) were used to evaluate the size distribution of particles and inform the optimal precipitation condition. Minimal pressure increase was observed during depth filtration of the precipitates. The precipitation was scaled up to 20L size and the extensive characterization of precipitated samples after protein A chromatography showed >75% reduction of host cell protein (HCP) concentrations (by ELISA), >90% reduction of number of HCP species (by mass spectrometry), and >99.8% reduction of DNA. The stability of polysorbate containing formulation buffers for all three mAbs in the protein A purified intermediates was improved at least 25% after PAA precipitation. Mass spectrometry was used to obtain additional understanding of the interaction between PAA and HCPs with different properties. Minimal impact on product quality and <5% yield loss after precipitation were observed while the residual PAA was <9 ppm. These results expand the toolbox in downstream purification to solve HCP clearance issues for programs with purification challenges, while also providing important insights into the integration of precipitation–depth filtration and the current platform process for the purification of biologics.     

Multistage continuous countercurrent diafiltration for formulation of monoclonal antibodies

There is growing interest in the development of fully integrated and continuous biomanufacturing processes for the production of monoclonal antibody products. A recent study has demonstrated the feasibility of using a two-stage countercurrent diafiltration (DF) process for continuous product formulation, but this system did not provide sufficient levels of buffer exchange for most applications. The objective of this study was to design and test a three-stage countercurrent DF system that could achieve at least 99.9% buffer exchange over 24 hr of continuous operation. Experimental data were obtained using concentrated solutions of human immunoglobulin G as a model protein, with the extent of vitamin B₁₂ removal used to track the extent of DF. Pall Cadence™ inline concentrators with Delta 30 kD regenerated cellulose membranes were used in the three stages to achieve high conversion in a single pass. The three-stage system showed stable operation with >99.9% vitamin B₁₂ removal and a minimal increase in pressure over the full 24 hr. Modules were effectively cleaned using sodium hydroxide, with nearly complete recovery of water permeability. A simple economic analysis was presented that accounts for the trade-offs between quantity of buffer used and membrane costs for this type of countercurrent staged DF process. The results provide important insights to the design and operation of a continuous process for antibody formulation.     

Generation and evaluation of anti-mouse IgG IgY as secondary antibody

Abstract

In order to evaluate the possibility of using IgY as the secondary antibody in immunoassay, specific IgY (1: 128,000) was generated by immunizing hens with mouse serum IgG purified by protein A column. IgY was extracted from egg yolk by polyethylene glycol 6000 (PEG-6000), and further purified using protein M affinity chromatography column. The purified IgY was conjugated with horseradish peroxidase (HRP) and fluorescein?isothiocyanate (FITC), in that order. The reactivity of conjugated antibodies was evaluated by ELISA, Western blot and Immunofluorescence, demonstrating that the obtained IgY was able to conjugate with enzymes, react with mouse primary IgG antibody, and subsequently amplify the antigen-antibody signals in different immune reaction conditions, in a comparable secondary effect to conventional goat anti-mouse IgG antibody. The obtained conjugated antibodies showed high stability in broad pH ranges (4–10; >70%) and high thermostability at 37?°C for 84?h (>85%). Despite the need to further consider and evaluate the industrial standardization and production process, our data provided the primary evidence that conjugated IgY antibodies can be used as a secondary antibody for broad immunological analysis.     

Molecular and enzymatic characterisation of Schistosoma mansoni thioredoxin

Defense against oxidative damage can be mediated through glutathione and/or thioredoxin utilising systems. Here, we report the identification and characterisation of a thioredoxin from Schistosoma mansoni. The predicted protein has similarity to previously characterised thioredoxins including conservation of the redox active site. Recombinant six-histidine tagged schistosome thioredoxin had insulin reduction activity and supported the enzymatic function of thioredoxin reductase and thioredoxin peroxidase. By Western blotting, all mammalian stages of the schistosome lifecycle expresses thioredoxin. Thioredoxin is present in egg secretory products and antibodies against the recombinant protein produce the circumoval precipitin reaction. This is the first identification of defined antigen producing this reaction. Furthermore, thioredoxin is a novel egg immunogen as it elicits an antibody response in schistosome-infected mice. The most significant IgG production against thioredoxin occurs after parasite oviposition commences. These observations suggest that thioredoxin participates in processes vital to the parasite and may facilitate the passage and survival of eggs across inflamed host tissues.     

Superoxide production by dinitrophenyl-derivatized thioredoxin reductase--a model for the mechanism and correlation to immunostimulation by dinitrohalobenzenes

Mammalian thioredoxin reductase catalyzes NADPH dependent reduction of a wide variety of substrates and plays a central role in redox regulation and antioxidant defence. Recently the enzyme was discovered to be a selenoprotein with a catalytically active penultimate selenocysteine residue. Dinitrohalobenzenes irreversibly inhibit the enzyme with a concomitant induction of an NADPH oxidase activity, producing superoxide. A model explaining the reactivity of dinitrohalobenzenes with thioredoxin reductase is presented, involving dinitrophenyl-derivatization of both the selenocysteine residue and its neighboring cysteine residue, reduction by NADPH of the enzyme-bound flavin in dinitrophenyl-alkylated enzyme (dnp-TrxR), followed by two consecutive one-electron transfers from the flavin to nitro groups of the dnp-moieties in dnp-TrxR, forming nitro anion radicals. The nitro radicals react with oxygen to form superoxide, again generating dnp-TrxR with an oxidized flavin, which may then follow another cycle of NADPH-dependent superoxide production. Dinitrohalobenzene compounds are well known for their immunostimulatory properties. Here it is proposed that the inflammatory components of this immunostimulation can be mediated by interaction with the thioredoxin system, via effects on cell function by superoxide production, oxidative stress and increased extracellular levels of thioredoxin.     

Mechanism of antibody reduction in cell culture production processes

We recently observed a significant disulfide reduction problem during the scale‐up of a manufacturing process for a therapeutic antibody using a CHO expression system. Under certain conditions, extensive reduction of inter‐chain disulfide bonds of an antibody produced by CHO cell culture may occur during the harvest operations and/or the protein A chromatography step, resulting in the observation of antibody fragments (light chain, heavy chain, and various combination of both) in the protein A pools. Although all conditions leading to disulfide reduction have not been completely identified, an excessive amount of mechanical cell lysis generated at the harvest step appears to be an important requirement for antibody reduction (Trexler‐Schmidt et al., 2010 ). We have been able to determine the mechanism by which the antibody is reduced despite the fact that not all requirements for antibody reduction were identified. Here we present data strongly suggesting that the antibody reduction was caused by a thioredoxin system or other reducing enzymes with thioredoxin‐like activity. The intracellular reducing enzymes and their substrates/cofactors apparently were released into the harvest cell culture fluid (HCCF) when cells were exposed to mechanical cell shear during harvest operations. Surprisingly, the reducing activity in the HCCF can last for a long period of time, causing the reduction of inter‐chain disulfide bonds in an antibody. Our findings provide a basis for designing methods to prevent the antibody reduction during the manufacturing process. Biotechnol. Bioeng. 2010;107:622–632. © 2010 Wiley Periodicals, Inc.     

Thioredoxin 1 is responsible for antibody disulfide reduction in CHO cell culture

During large-scale manufacturing of an IgG1 monoclonal antibody in Chinese hamster ovary (CHO) cells, reduction of the antibody's disulfide bonds was observed. We present evidence that mammalian thioredoxin 1 (TXN1) is the terminal enzyme responsible for this reduction event. We demonstrate a marked prevention of IgG1 disulfide bond reduction in a cell-density dependent manner by knocking down expression of TXN1 via lentivirus transduction of short hairpin RNA.     

Efficient production of bispecific IgG of different isotypes and species of origin in single mammalian cells

Bispecific IgG production in single host cells has been a much sought-after goal to support the clinical development of these complex molecules. Current routes to single cell production of bispecific IgG include engineering heavy chains for heterodimerization and redesign of Fab arms for selective pairing of cognate heavy and light chains. Here, we describe novel designs to facilitate selective Fab arm assembly in conjunction with previously described knobs-into-holes mutations for preferential heavy chain heterodimerization. The top Fab designs for selective pairing, namely variants v10 and v11, support near quantitative assembly of bispecific IgG in single cells for multiple different antibody pairs as judged by high-resolution mass spectrometry. Single-cell and in vitro-assembled bispecific IgG have comparable physical, in vitro biological and in vivo pharmacokinetics properties. Efficient single-cell production of bispecific IgG was demonstrated for human IgG₁, IgG₂ and IgG₄ thereby allowing the heavy chain isotype to be tailored for specific therapeutic applications. Additionally, a reverse chimeric bispecific IgG_2a with humanized variable domains and mouse constant domains was generated for preclinical proof-of-concept studies in mice. Efficient production of a bispecific IgG in stably transfected mammalian (CHO) cells was shown. Individual clones with stable titer and bispecific IgG composition for >120 days were readily identified. Such long-term cell line stability is needed for commercial manufacture of bispecific IgG. The single-cell bispecific IgG designs developed here may be broadly applicable to biotechnology research, including screening bispecific IgG panels, and to support clinical development.