Optimization of Direct Lysine Decarboxylase Biotransformation for Cadaverine Production with Whole-Cell Biocatalysts at High Lysine ConcentrationS
Optimization of Direct Lysine Decarboxylase Biotransformation for Cadaverine Production with Whole-Cell Biocatalysts at High Lysine ConcentrationS
Journal of Microbiology and Biotechnology. 2015. Jul, 25(7): 1108-1113
Copyright © 2015, The Korean Society For Microbiology And Biotechnology
  • Received : December 18, 2014
  • Accepted : February 12, 2015
  • Published : July 28, 2015
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About the Authors
Hyun Joong Kim
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Yong Hyun Kim
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Ji-Hyun Shin
Department of Biological and Chemical Engineering, Hongik University, Sejong city, Republic of Korea
Shashi Kant Bhatia
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Ganesan Sathiyanarayanan
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Hyung-Min Seo
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Kwon Young Choi
Department of Environmental Engineering, Ajou University, Suwon 443-749, Republic of Korea
Yung-Hun Yang
Department of Biological Engineering, College of Engineering, Konkuk University, Seoul 143-701, Republic of Korea
Kyungmoon Park
Department of Biological and Chemical Engineering, Hongik University, Sejong city, Republic of Korea

Cadaverine (1,5-diaminopentane) is an important industrial chemical with a wide range of applications. Although there have been many efforts to produce cadaverine through fermentation, there are not many reports of the direct cadaverine production from lysine using biotransformation. Whole-cell reactions were examined using a recombinant Escherichia coli strain overexpressing the E. coli MG1655 cadA gene, and various parameters were investigated for the whole-cell bioconversion of lysine to cadaverine. A high concentration of lysine resulted in the synthesis of pyridoxal-5’-phosphate (PLP) and it was found to be a critical control factor for the biotransformation of lysine to cadaverine. When 0.025 mM PLP and 1.75 M lysine in 500 mM sodium acetate buffer (pH6) were used, consumption of 91% lysine and conversion of about 80% lysine to cadaverine were successfully achieved.
Currently, the worldwide annual consumption of amino acids is estimated to be over 4 million tons, and the annual demand for amino acids, such as monosodium-glutamatebased flavor enhancers or feed additives comprising mainly L -lysine, D , L -methionine, and L -threonine, is estimated to be much higher than 1 million tons of each amino acid for industrial processes [4 , 9] . L -Lysine is an essential amino acid and is commonly used as a food additive for humans and animals [4 , 17] . Lysine can also be used as a precursor for the synthesis of various industrially valuable products, such as caprolactam, cadaverine, glutaric acid, 5- aminovaleric acid, and so on [1 , 11] . Cadaverine is a diamine compound produced by protein hydrolysis during the putrefaction of animal tissue. The biosynthesis of cadaverine is a well-documented process and it is an endproduct of decarboxylation of lysine, with immense applications in the drug industry and other industrial sectors [8 , 20 , 21] . Bioprocessing of cadaverine is an economic process and, specifically, the production of biopolyamides from renewable feedstocks could be an alternative and also replacement for commercial polyamides derived from petrochemicals [5 , 6 , 10 , 25] . In the petroleum industry, 1,5-pentanediamine (cadaverine) can be produced from the starting material of 1,5-dichloropentane (obtainable from tetrahydropyran), glutarodinitrile, or glutaraldehyde [7] . However, it can also be obtained from the natural lysine decarboxylation process, which exists in several microorganisms such as Corynebacterium glutamicum and Escherichia coli [16 , 22] . So far, many efforts have been focused on the production of cadaverine from the fermentation of glucose and other simple sugars by metabolic engineering. There are only a few reports on the lysine conversion into cadaverine and it is complicated to control the processes to avoid several stages of reaction [6 , 15] . However, considering that the conventional production system of lysine is very well established and lysine itself is readily available at a reasonable price, the biotransformation of lysine to cadaverine seems to be quite efficient and economical. In addition, there is also a complication to construct a whole-cell factory that utilizes lysine for the synthesis of cadaverine and to start lysine decarboxylation system optimization for the industrial production of cadaverine. However, recent literature evidenced that the construction of microbial cell factories for lysine decarboxylation could be possible, and they reported that the bioconversion of lysine to cadaverine is merely dependent on the low concentration of lysine as substrate in a metabolically engineered system. [12] . Hence, we hypothesized that the lysine bioconversion could be possible at high-concentration reactions and we have constructed an engineered E. coli system for the direct conversion of lysine to cadaverine and to demonstrate the ability to develop an economic bioprocess that can be performed at high substrate concentrations.
Materials and Methods
- Chemical Reagents
The chemical reagents used in this study, such as cadaverine, pyridoxal-5-phosphate, sodium acetate anhydrate, and L -lysine monohydrochloride, were purchased from Sigma Aldrich Co. (USA). The derivatization reagent, diethyl ethoxymethylenemalonate (DEEMM), was purchased from Fluka Co. (Japan), and sodium borate decahydrate was purchased from Sigma Aldrich Co. (USA). To examine direct application to a lysine-based fermentation system, liquid lysine produced from fermentation was used and kindly donated by Paekwang Industry Co. (Korea).
- Bacterial Strain and Media
For plasmid construction, E. coli strains were grown at 37℃ in Luria–Bertani (LB) medium (10 g/l tryptone, 5 g/l yeast extract, and 5 g/l sodium chloride) supplemented with 50 µg/ml kanamycin (Km) for selection and screening purposes. The genomic DNA of E. coli K12 MG1655 was used for cloning cadA . The coding region of cadA was amplified by PCR using the primers cadAF (5’-CGTCGTGGATCCATGAACGTTATTGC AATATTAATCACA-3’) and cadAR (5’-ATATAAGCTTTCCCGCGATTTTTAGGAC TCG-3’). The PCR product was then digested with restriction enzymes ( Bam HI and Hin dIII), and inserted into the vector pET24ma using the same restriction enzymes. The pET24ma vector (constructed by Dr. David Sourdive, Pasteur Institute, France) contains a p15A replication origin [18] . The constructed plasmid was transformed into E. coli BL21 (DE3) competent cells. After transformation, the cells were cultivated at 30℃ in a shaking incubator (Han-Beak Science Co., Korea) at 200 rpm. The pre-culture was prepared by inoculating a single transformant colony from an agar plate into 5 ml of LB medium in a 14 ml round-bottom tube, prior to incubating for 16 h with shaking. One milliliter of the pre-culture was used as the seed for production in 50 ml of LB medium (15 µg/ml kanamycin and 0.1 mM iso-propyl-β- D -thiogalactopyranoside) in a 250 ml Erlenmeyer flask and it was incubated at 30℃ with shaking. After 16 h, the culture was harvested by centrifugation at 13,000 rpm for 5 min at 4°C, and the cell pellet was washed with 50 mM sodium acetate buffer (pH 6.0) and then suspended in the same buffer. The cell suspension was stored at 4℃ until further use, and referred to as whole cells.
- Whole-Cell Reaction
The activity of lysine decarboxylase was determined using the whole cells as a catalyst. The assay was performed at 37℃ in a total volume of 500 µl, containing 500 mM sodium acetate buffer (pH 6.0), 1 M L -lysine, 0.1 mM pyridoxal-5-phosphate, and 20 µl of the whole-cell suspension, at 37℃ in a water bath. The reaction was stopped by heating the reaction mixture at 100℃ for 5 min. One unit of activity (mmol/cell dry weight (mg)/min) was defined as the amount of enzyme producing 1 mmol of cadaverine per minute at 37℃. The whole cells used in the following experiments had 30.27 units of activity.
- Derivatization and HPLC Analysis
Diamine derivatives were obtained in a mixture of 300 µl of borate buffer (50 mM, pH 9), 100 µl of methanol, 47 µl of distilled water, 50 µl of target sample, and 3 µl of DEEMM without pretreatment [2] . The sample was then heated at 70℃ for 2 h to allow complete degradation of excess DEEMM and reagent by-products. Analysis using a high-performance liquid chromatography (HPLC, YL-9100; Korea) was performed after derivatization of reaction products with DEEMM. The equipment consisted of a binary pump, an in-line degasser, an autosampler, and a column thermostat. Chromatographic separation was done using a reverse-phase C18 column (Agilent ZORBAX SB-C18 column, 4.6 × 250 mm, 5 µm particle size) and the column temperature was maintained at 35°C. The mobile phase was composed of 100% acetonitrile (A) and 25 mM acetate buffer (pH 4.8, B). The flow rate was maintained at 1 ml/min and the composition of the mobile phase was programmed (as shown in Fig. S1).
Results and Discussion
- Effects of Initial pH on Whole-Cell Reaction
Initially, the enzyme reaction was carried out with purified CadA, which had high enzymatic activity. The high concentration of CadA protein was easily precipitated at 4℃ after His-tag purification. Consequently, several steps were performed for the purification to make the whole cell reaction preferable. The optimal pH of lysine decarboxlyase was reported to be around pH 6 [19] . However, the new optimal conditions for the lysine biotransformation system needed to be determined. The whole-cell reactions were conducted with the initial pH range of 5-10 in the reaction buffer, and it was found that pH 6 to 8 showing the highest enzymatic activity, at which most lysine added was used by the whole cells and about 95% of lysine was consumed and converted into cadaverine ( Fig. 1 ). The final pH was around 8.5 after 2 h of reaction, regardless of the initial pH. The conversion of lysine into cadaverine was finished within 15 min when 500 mM of lysine was used. The overall pH increase was not a sudden process because the reaction mixture uses a high-concentration buffer (around 500 mM sodium acetate buffer) and there is a diffusion limitation in the small-scale reaction. The difference between lysine consumption and cadaverine production may be ascribed to leftover lysine and cadaverine in the cells, and to the production of by-products such as N-acetyldiaminopentane. Our current results agree with those of Kind et al. [14] .
PPT Slide
Lager Image
Effects of initial pH on lysine consumption (▐ ) and cadaverine conversion (●) after 2 h reaction of 500 mM lysine at different initial pHs.
- Examination of Substrate Inhibition
The reaction was carried out at 37℃ at pH 6 using 500 mM sodium acetate buffer and 0.1 mM pyridoxal-5-phosphate with different concentrations of substrate. The substrate conversion profiles are shown in Fig. 2 . After 2 h of reaction, lysine was fully converted to cadaverine up to 1 M concentration (data not shown). However, substrate inhibition was observed from 1.25 M, resulting in some residual lysine ( Fig. 2 ). To achieve higher lysine concentration of the reaction, the amount of whole cell was increased by adding 50% and 100% of enzyme to the initial whole-cell concentration (30.27 units). Although, some lysine remained after 2 h of reaction at high concentrations of lysine, it was observed that higher amounts of lysine decarboxylase could increase the conversion ratio of lysine into cadaverine and the overall consumption ratio of lysine was estimated around 80% at 1.25 M substrate concentration. The maximum substrate conversion by whole cells was 95%, 94%, and 92% from 1.25, 1.5, and 1.75 M concentration of substrate lysine, respectively.
PPT Slide
Lager Image
Effects of lysine concentration and biocatalyst concentration on lysine consumption ratio. Concentrations of 30.27 units (black bar), 45.41 units (gray bar), and 60.54 units (white bar) were tested.
- Effects of Adding Exogenous PLP to the Reaction Buffer
The requirement of PLP for the activity of lysine decarbolxyase is well known, especially for enzyme reactions [13 , 23] . However, there are no reports on the direct effect of adding exogenous PL P to a mixture of whole cells expressing lysine decarboxylase. Therefore, the effect of PLP concentration was examined ( Fig. 3 ). When no PLP was added, lysine consumption was only 20% for the 1 M lysine to cadaverine reaction. When more than 0.025 mM of PLP was added, the lysine consumption was recovered, suggesting that the whole-cell reaction also requires a certain amount of PLP as a cofactor to enable the 1 M lysine to cadaverine reaction. PLP is one of the critical control factors for the production of cadaverine at high concentrations of lysine, unlike the growth-based production of cadaverine through fermentation [21 , 22] .
PPT Slide
Lager Image
Effects of PLP concentration on lysine consumption ratio (▐ ) and cadaverine conversion ratio ( ● ).
- Effect of Buffer on pH and Activity
The reaction buffer is normally used to reduce the fluctuations in pH caused by the final product and to improve the enzymatic reaction [3 , 24] . In this study, we examined the effect of the buffer in the whole-cell reactions. To monitor the time-dependent conversion of lysine to cadaverine and to evaluate the effects of the buffer on pH change, the reaction and time-dependent data were compared in 500 µl reaction volumes containing 1 M lysine with and without 500 mM of sodium acetate buffer (pH 6.0). Unlike our initial expectation, the pH was increased by cadaverine production and the experimental results showed similar patterns of cadaverine production with and without buffer ( Figs. 4 A and 4 B). Almost 50% of lysine was consumed within 20 min and monitoring of the reaction revealed a dramatic increase of the pH to over pH 8 without buffer. Although pH differences were shown, the overall conversion ratio was quite similar. This seems to be due to the fast enzymatic reaction in the small-scale reaction, and the robustness of the whole-cell catalysis to resist the pH changes. When pH optimization was performed, the cadaverine conversion rate was negatively affected at above pH 9. However, the results of nonbuffered experiments revealed that there was no significant increase of the pH above 9. As we obtained the results from this study, it is possible to produce cadaverine from the lysine decarboxylation reaction without adding buffer in a small-scale level, although further optimization may be needed to scale up the reaction without buffer.
PPT Slide
Lager Image
Effect of buffer on reaction pH and cadaverine production. Change of pH with (black circle) or without buffer (white circle) (A), and the production of cadaverine (white) and the consumption of lysine (black) from purified lysine at different time points with (circle) or without buffer (Triangle) (B). Production of cadaverine (white) and the consumption of lysine (black) from lysine-containing fermentation liquid with (circle) or without buffer (Triangle) (C).
- Bioconversion of Fermented Lysine Liquid into Cadaverine Using Whole-Cell System
Bioconversion of liquid lysine obtained through fermentation was evaluated using a whole-cell engineered system. The color of the liquid lysine is dark brown and it has pH 10.2 with 4.35 M of lysine content. The fermented liquid also possesses 165 mM of cadaverine produced from an industrial Corynebacterium strain. During the whole-cell reaction, the pH was decreased to 6 by the addition of 1 N HCl and the solution was diluted to 1 M of lysine to avoid possible substrate inhibition and 30.27 units of whole cells was used. The whole-cell reaction demonstrated 80% of lysine consumption after 2 h of reaction ( Fig. 4 C), which was relatively slower than the previous reaction with purified lysine ( Fig. 4 B). This may be due to the presence of inhibitors produced during the lysine fermentation process. However, quite a similar pattern was observed as with the previous data ( Fig. 4 C). Although, the cadaverine productivity was relatively low compared with the case using purified lysine substrate, it demonstrated the possible application of the whole cells to the direct utilization of crude lysine solution for cadaverine production.
In conclusion, we showed here the direct conversion of lysine to cadaverine at high concentrations of substrate, and proved it is a quite feasible and practical approach based on the well-established engineered E. coli system for cadaverine production from lysine. Following optimization of several factors such as initial pH, substrate concentration, and PLP concentration, the exogenous addition of PLP was found to be one of the key factors to promote a high molar cadaverine production from the whole-cell reactions. Considering that the conventional production system of lysine is very well established and lysine itself is readily available at a reasonable price, then the biotransformation of lysine to cadaverine is a completely greener, efficient, and economical bioprocess and also an alternative for chemical synthesis.
This work was partially supported by the R&D Program of MOTIE/KEIT (10047910, Production of bio-based cadaverine and polymerization of bio-polyamide 510), the Basic Science Research Program (NRF-2013R1A1A2A10004690) and grant from the National Research Foundation of Korea (NRF-2011-619-E0002), funded by the Ministry of Education. This study was also supported by the Korea Ministry of Environment through Converging Technology Project (2012-000620001).
Adkins J , Jordan J , Nielsen DR 2013 EngineeringEscherichia colifor renewable production of the 5-carbon polyamide building-blocks 5-aminovalerate and glutarate. Biotechnol. Bioeng. 110 1726 - 1734    DOI : 10.1002/bit.24828
Alaiz M , Navarro JL , Giron J , Vioque E 1992 Amino acid analysis by high-performance liquid chromatography after derivatization with diethyl ethoxymethylenemalonate. J. Chromatogr. 591 181 - 186    DOI : 10.1016/0021-9673(92)80236-N
Alberty RA , Bock RM 1953 Alteration of the kinetic properties of an enzyme by the binding of buffer, inhibitor, or substrate. Proc. Natl. Acad. Sci. USA 39 895 - 900    DOI : 10.1073/pnas.39.9.895
Anastassiadis S. 2007 L-Lysine fermentation. Recent Pat. Biotechnol. 1 11 - 24    DOI : 10.2174/187220807779813947
Buschke N , Becker J , Schafer R , Kiefer P , Biedendieck R , Wittmann C 2013 Systems metabolic engineering of xyloseutilizingCorynebacterium glutamicumfor production of 1,5-diaminopentane. Biotechnol. J. 8 557 - 570    DOI : 10.1002/biot.201200367
Buschke N , Schroder H , Wittmann C 2011 Metabolic engineering ofCorynebacterium glutamicumfor production of 1,5-diaminopentane from hemicellulose. Biotechnol. J. 6 306 - 317    DOI : 10.1002/biot.201000304
Eller K , Henkes E , Rossbacher R , Hoke H 2000 Amines, Aliphatic.Ullmann’s Encyclopedia of Industrial Chemistry.
Gale EF , Epps HM 1944 Studies on bacterial amino-acid decarboxylases: 1. L (+)-lysine decarboxylase. Biochem. J. 38 232 - 242    DOI : 10.1042/bj0380232
Hermann T 2003 Industrial production of amino acids by coryneform bacteria. J. Biotechnol. 104 155 - 172    DOI : 10.1016/S0168-1656(03)00149-4
Ikeda N , Miyamoto M , Adachi N , Nakano M , Tanaka T , Kondo A 2013 Direct cadaverine production from cellobiose using beta-glucosidase displayingEscherichia coli. AMB Express. 3 67 -    DOI : 10.1186/2191-0855-3-67
Jang YS , Kim B , Shin JH , Choi YJ , Choi S , Song CW 2012 Bio-based production of C2-C6 platform chemicals. Biotechnol. Bioeng. 109 2437 - 2459    DOI : 10.1002/bit.24599
Kanjee U , Gutsche I , Alexopoulos E , Zhao B , El Bakkouri M , Thibault G 2011 Linkage between the bacterial acid stress and stringent responses: the structure of the inducible lysine decarboxylase. EMBO J. 30 931 - 944    DOI : 10.1038/emboj.2011.5
Kind S , Jeong WK , Schroder H , Wittmann C 2010 Systemswide metabolic pathway engineering inCorynebacterium glutamicumfor bio-based production of diaminopentane. Metab. Eng. 12 341 - 351    DOI : 10.1016/j.ymben.2010.03.005
Kind S , Jeong WK , Schroder H , Zelder O , Wittmann C 2000 Identification and elimination of the competing Nacetyldiaminopentane pathway for improved production of diaminopentane byCorynebacterium glutamicum. Appl. Environ. Microbiol. 76 5175 - 5180    DOI : 10.1128/AEM.00834-10
Kind S , Neubauer S , Becker J , Yamamoto M , Volkert M , Abendroth GV 2014 From zero to hero - production of bio-based nylon from renewable resources using engineeredCorynebacterium glutamicum. Metab. Eng. 25 113 - 123    DOI : 10.1016/j.ymben.2014.05.007
Kind S , Wittmann C 2011 Bio-based production of the platform chemical 1,5-diaminopentane. Appl. Microbiol. Biotechnol. 91 1287 - 1296    DOI : 10.1007/s00253-011-3457-2
Koffas MA , Jung GY , Stephanopoulos G 2003 Engineering metabolism and product formation inCorynebacterium glutamicumby coordinated gene overexpression. Metab. Eng. 5 32 - 41    DOI : 10.1016/S1096-7176(03)00002-8
Lee SG , Lee JO , Yi JK , Kim BG 2002 Production of cytidine 5’-monophosphateN-acetylneuraminic acid using recombinantEscherichia colias a biocatalyst. Biotechnol. Bioeng. 80 516 - 524    DOI : 10.1002/bit.10398
Lemonnier M , Lane D 1998 Expression of the second lysine decarboxylase gene ofEscherichia coli. Microbiology 144 751 - 760    DOI : 10.1099/00221287-144-3-751
Meng SY , Bennett GN 1992 Nucleotide sequence of theEscherichia coli cadoperon: a system for neutralization of low extracellular pH. J. Bacteriol. 174 2659 - 2669
Mimitsuka T , Sawai H , Hatsu M , Yamada K 2007 Metabolic engineering ofCorynebacterium glutamicumfor cadaverine fermentation. Biosci. Biotechnol. Biochem. 71 2130 - 2135    DOI : 10.1271/bbb.60699
Qian ZG , Xia XX , Lee SY 2011 Metabolic engineering ofEscherichia colifor the production of cadaverine: a five carbon diamine. Biotechnol. Bioeng. 108 93 - 103    DOI : 10.1002/bit.22918
Sabo DL , Fischer EH 1974 Chemical properties ofEscherichia colilysine decarboxylase including a segment of its pyridoxal 5’-phosphate binding site. Biochemistry 13 670 - 676    DOI : 10.1021/bi00701a006
Sarciaux JM , Mansour S , Hageman MJ , Nail SL 1999 Effects of buffer composition and processing conditions on aggregation of bovine IgG during freeze-drying. J. Pharm. Sci. 88 1354 - 1361    DOI : 10.1021/js980383n
Tateno T , Okada Y , Tsuchidate T , Tanaka T , Fukuda H , Kondo A 2009 Direct production of cadaverine from soluble starch usingCorynebacterium glutamicumcoexpressing alphaamylase and lysine decarboxylase. Appl. Microbiol. Biotechnol. 82 115 - 121    DOI : 10.1007/s00253-008-1751-4