Targeting of CCL2-CCR2-Glycosaminoglycan Axis Using a CCL2 Decoy Protein Attenuates Metastasis through Inhibition of Tumor Cell Seeding.

The CCL2-CCR2 chemokine axis has an important role in cancer progression where it contributes to metastatic dissemination of several cancer types (e.g., colon, breast, prostate). Tumor cell-derived CCL2 was shown to promote the recruitment of CCR2(+)/Ly6C(hi) monocytes and to induce vascular permeability of CCR2(+) endothelial cells in the lungs. Here we describe a novel decoy protein consisting of a CCL2 mutant protein fused to human serum albumin (dnCCL2-HSA chimera) with enhanced binding affinity to glycosaminoglycans that was tested in vivo. The monocyte-mediated tumor cell transendothelial migration was strongly reduced upon unfused dnCCL2 mutant treatment in vitro. dnCCL2-HSA chimera had an extended serum half-life and thus a prolonged exposure in vivo compared with the dnCCL2 mutant. dnCCL2-HSA chimera bound to the lung vasculature but caused minimal alterations in the leukocyte recruitment to the lungs. However, dnCCL2-HSA chimera treatment strongly reduced both lung vascular permeability and tumor cell seeding. Metastasis of MC-38GFP, 3LL, and LLC1 cells was significantly attenuated upon dnCCL2-HSA chimera treatment. Tumor cell seeding to the lungs resulted in enhanced expression of a proteoglycan syndecan-4 by endothelial cells that correlated with accumulation of the dnCCL2-HSA chimera in the vicinity of tumor cells. These findings demonstrate that the CCL2-based decoy protein effectively binds to the activated endothelium in lungs and blocks tumor cell extravasation through inhibition of vascular permeability.

Designing a mutant CCL2-HSA chimera with high glycosaminoglycan-binding affinity and selectivity.

Chemokines like CCL2 mediate leukocyte migration to inflammatory sites by binding to G-protein coupled receptors on the target cell as well as to glycosaminoglycans (GAGs) on the endothelium of the inflamed tissue. We have recently shown that the dominant-negative Met-CCL2 mutant Y13A/S21K/Q23R with improved GAG binding affinity is highly bio-active in several animal models of inflammatory diseases. For chronic indications, we have performed here a fusion to human serum albumin (HSA) in order to extend the serum half-life of the chemokine mutant. To compensate a potential drop in GAG-binding affinity due to steric hindrance by HSA, a series of novel CCL2 mutants was generated with additional basic amino acids which were genetically introduced at sites oriented towards the GAG ligand. From this set of mutants, the Met-CCL2 variant Y13A/N17K/S21K/Q23K/S34K exhibited high GAG-binding affinity and a similar selectivity as wild type (wt) CCL2. From a set of different HSA-chemokine chimeric constructs, the linked HSA(C34A)(Gly)4Ser-Met-CCL2(Y13A/N17K/S21K/Q23K/S34K) fusion protein was found to show the best overall GAG-binding characteristics. Molecular modeling demonstrated an energetically beneficial fold of this novel protein chimera. This was experimentally supported by GdmCl-induced unfolding studies, in which the fusion construct exhibited a well-defined secondary structure and a transition point significantly higher than both the wt and the unfused CCL2 mutant protein. Unlike the wt chemokine, the quaternary structure of the HSA-fusion protein is monomeric according to size-exclusion chromatography experiments. In competition experiments, the HSA-fusion construct displaced only two of seven unrelated chemokines from heparan sulfate, whereas the unfused CCL2 mutant protein displaced five other chemokines. The most effective concentration of the HSA-fusion protein in inhibiting CCL2-mediated monocyte attachment to endothelial cells, as detected in the flow chamber, was 8.6 µg/ml. This novel HSA-fusion protein exhibits not only high affinity but also selective displacement of chemokines from GAGs binding. HSA is therefore proposed to be a highly promising scaffold candidate for therapeutic, GAG-targeting chemokine mutants.

Mathematical modelling and process optimization of a continuous 5-stage bioreactor cascade for production of poly[-(R)-3-hydroxybutyrate] by Cupriavidus necator.

A multistage system for poly(hydroxyalkanoate) (PHA) production consisting of five continuous stirred tank reactors in series (5-CSTR) with Cupriavidus necator DSM 545 as production strain was modelled using formal kinetic relations. Partially growth-associated production of PHA under nitrogen limited growth was chosen as modelling strategy, thus the Luedeking-Piret's model of partial growth-associated product synthesis was applied as working hypothesis. Specific growth rate relations adjusted for double substrate (C and N source) limited growth according to Megee et al. and Mankad-Bungay relation were tested. The first stage of the reactor cascade was modelled according to the principle of nutrient balanced continuous biomass production system, the second one as two substrate controlled process, while the three subsequent reactors were adjusted to produce PHB under continuous C source fed and nitrogen deficiency. Simulated results of production obtained by the applied mathematical models and computational optimization indicate that PHB productivity of the whole system could be significantly increased (from experimentally achieved 2.14 g L(-1) h(-1) to simulated 9.95 g L(-1) h(-1)) if certain experimental conditions would have been applied (overall dilution rate, C and N source feed concentration). Additionally, supplemental feeding strategy for switching from batch to continuous mode of cultivation was proposed to avoid substrate inhibition.

Continuous production of poly([R]-3-hydroxybutyrate) by Cupriavidus necator in a multistage bioreactor cascade.

Poly(hydroxyalkanoates) (PHAs) constitute biodegradable polyesters and are considered among the most promising candidates to replace common petrochemical plastics in various applications. To date, all commercial processes for PHA production employ microbial discontinuous fed-batch fermentations. These processes feature drawbacks such as varying product quality and the inevitable periods of downtime for preparation and post-treatment of the bioreactor equipment. An unprecedented approach to PHA production was chosen in the presented work using a multistage system consisting of five continuous stirred tank reactors in series (5-SCR), which can be considered as a process engineering substitute of a continuous tubular plug flow reactor. The first stage of the reactor cascade is the site of balanced bacterial growth; thereafter, the fermentation broth is continuously fed from the first into the subsequent reactors, where PHA accumulation takes place under nitrogen-limiting conditions. Cupriavidus necator was used as production strain. The focus of the experimental work was devoted to the development of a PHA production process characterized by high productivity and high intracellular polymer content. The results of the experimental work with the reactor cascade demonstrated its potential in terms of volumetric and specific productivity (1.85 g L⁻¹ h⁻¹ and 0.100 g g⁻¹ h⁻¹, respectively), polymer content (77%, w/w) and polymer properties (M (w) = 665 kg/mol, PDI = 2.6). Thus, implementing the technology for 5-SCR production of PHB results in an economically viable process. The study compares the outcome of the work with literature data from continuous two-stage PHA production and industrial PHA production in fed-batch mode.

Biosynthesis and characterization of polyhydroxyalkanoates in the polysaccharide-degrading marine bacterium Saccharophagus degradans ATCC 43961.

The marine bacterium Saccharophagus degradans was investigated for the synthesis of polyhydroxyalkanoates (PHAs), using glucose as the sole source of carbon in a two-step batch culture. In the first step the microorganism grew under nutrient balanced conditions; in the second step the cells were cultivated under limitation of nitrogen source. The biopolymer accumulated in S. degradans cells was detected by Nile red staining and FT-IR analysis. From GC-MS analysis, it was found that this strain produced a homopolymer of 3-hydroxybutyric acid. The cellular polymer concentration, its molecular mass, glass transition temperature, melting point and heat of fusion were 17.2+/-2.7% of dry cell weight, 54.2+/-0.6 kDa, 37.4+/-6.0 degrees C, 165.6+/-5.5 degrees C and 59.6+/-2.2 J g(-1), respectively. This work is the first report determining the capacity of S. degradans to synthesize PHAs.

Potential of various archae- and eubacterial strains as industrial polyhydroxyalkanoate producers from whey.

Three different microbial wild-type strains are compared with respect to their potential as industrial scale polyhydroxyalkanoate (PHA) producers from the feed stock whey lactose. The halophilic archaeon Haloferax mediterranei as well as two eubacterial strains (Pseudomonas hydrogenovora and Hydrogenophaga pseudoflava) are investigated. H. mediterranei accumulated 50 wt.-% of poly-3-(hydroxybutyrate-co-8%-hydroxyvalerate) from hydrolyzed whey without addition of 3-hydroxyvalerate (3HV) precursors (specific productivity q(p): 9.1 mg x g(-1) x h(-1)). Using P. hydrogenovora, the final percentage of poly-3-hydroxybutyrate (PHB) amounted to 12 wt.-% (q(p): 2.9 mg x g(-1) x h(-1)). With H. pseudoflava, it was possible to reach 40 wt.-% P-3(HB-co-5%-HV) on non-hydrolyzed whey lactose plus addition of valeric acid as 3HV precursor (q(p): 12.5 mg x g(-1) x h(-1)). A detailed characterization of the isolated biopolyesters and an evaluation with regard to the economic feasibility completes the study.

Assessment of formal and low structured kinetic modeling of polyhydroxyalkanoate synthesis from complex substrates.

A formal kinetic mathematical model for poly-(3-hydroxybutyrate-co-3-hydroxyvalerate-co-4-hydroxybutyrate) [P(3HB-co-3HV-co-4HB)] terpolyester synthesis from glucose and galactose derived from whey permeate supplemented with gamma-butyrolactone by the archaeon Haloferax mediterranei was created. Further, a low structured mathematical model for poly-3-hydroxybutyrate synthesis from whey permeate by Pseudomonas hydrogenovora was developed. In both cases, biosyntheses for obtaining the experimental data used for compiling the models were performed via fed-batch cultivations. The model developed for H. mediterranei consists of 10 differential and 11 algebraic equations, including 27 kinetic constants. The model compiled for P. hydrogenovora encompasses 10 differential and 3 algebraic equations, including 36 kinetic constants. Both models were solved by Runge-Kuta variable step numerical integration with Monte Carlo parameter optimization procedure. Difficulties arising from the modeling of redirection of metabolic fluxes from biomass growth toward polyhydroxyalkanoate synthesis and byproducts are discussed.