U.S. patent application number 13/108294 was filed with the patent office on 2011-11-17 for process for plasmid dna fermentation.
This patent application is currently assigned to Nature Technology Corp.. Invention is credited to Aaron E. CARNES, James A. Williams.
Application Number | 20110281304 13/108294 |
Document ID | / |
Family ID | 35968127 |
Filed Date | 2011-11-17 |
United States Patent
Application |
20110281304 |
Kind Code |
A1 |
CARNES; Aaron E. ; et
al. |
November 17, 2011 |
PROCESS FOR PLASMID DNA FERMENTATION
Abstract
Improvements in plasmid DNA production technology are needed to
insure the economic feasibility of future DNA vaccines and DNA
therapeutics. General methods are described, by means of which it
is possible to dramatically increase plasmid DNA productivity in a
fermentor. These processes feature fed-batch fermentation
strategies, combined with novel growth and induction phase
temperature shifts.
Inventors: |
CARNES; Aaron E.; (Lincoln,
NE) ; Williams; James A.; (Lincoln, NE) |
Assignee: |
Nature Technology Corp.
Lincoln
NE
|
Family ID: |
35968127 |
Appl. No.: |
13/108294 |
Filed: |
May 16, 2011 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
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11573825 |
Feb 16, 2007 |
7943377 |
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PCT/US05/29238 |
Aug 16, 2005 |
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13108294 |
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60603000 |
Aug 19, 2004 |
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Current U.S.
Class: |
435/91.1 |
Current CPC
Class: |
C12N 15/69 20130101;
C12P 19/34 20130101; C12N 15/74 20130101; C12N 15/70 20130101; A61K
48/0091 20130101 |
Class at
Publication: |
435/91.1 |
International
Class: |
C12P 19/34 20060101
C12P019/34 |
Claims
1. A method for fed-batch fermentation production of covalently
closed super-coiled plasmid DNA comprising the steps of: A) growing
bacterial cells containing a plasmid, cosmid, or bacterial
artificial chromosome replicon at a reduced temperature during a
fed-batch phase; and B) restricting growth rate of the bacterial
cells during the fed-batch phase by nutrient limitation; and C)
inducing plasmid production by increasing temperature; and D)
continuing growth at elevated temperature to accumulate plasmid
product.
Description
CROSS-REFERENCE TO RELATED APPLICATIONS
[0001] This application is a continuation of U.S. patent
application Ser. No. 11/573,825, filed on Feb. 16, 2007, in the
United States Patent and Trademark Office, currently pending, which
is a National Phase of International Patent Application No
PCT/US05/29238, filed Aug. 16, 2005, which claims the benefit of
U.S. Provisional Patent Application No. 60/603,000, filed Aug. 19,
2004, the disclosures of which are incorporated herein by
reference.
STATEMENT REGARDING FEDERALLY SPONSORED RESEARCH OR DEVELOPMENT
[0002] Not Applicable
FIELD OF THE INVENTION
[0003] The present invention relates to the production of
covalently closed circular (ccc) recombinant DNA molecules such as
plasmids, cosmids, bacterial artificial chromosomes (BACs),
bacteriophages, viral vectors and hybrids thereof, and more
particularly is a method for production of the said DNA molecules
at high levels in fermentation culture.
BACKGROUND OF THE INVENTION
[0004] The present invention relates to the production of
covalently closed circular (ccc) recombinant DNA molecules. Such
molecules are useful in biotechnology, transgenic organisms, gene
therapy, therapeutic vaccination, agriculture and DNA vaccines.
[0005] With the invention in mind, a search of the prior art was
conducted. E. coli plasmids have long been the single most
important source of recombinant DNA molecules used by researchers
and by industry. Today, plasmid DNA is becoming increasingly
important as the next generation of biotechnology products (gene
medicines and DNA vaccines) make their way into clinical trials,
and eventually into the pharmaceutical marketplace. Plasmid DNA
vaccines may find application as preventive vaccines for viral,
bacterial, or parasitic diseases; immunizing agents for the
preparation of hyper immune globulin products; therapeutic vaccines
for infectious diseases; or as cancer vaccines. Plasmids are also
utilized in gene therapy or gene replacement applications, wherein
the desired gene product is expressed from the plasmid after
administration to the patient.
[0006] Today, the FDA standards are not defined except in
preliminary form (see: FDA Points to Consider on Plasmid DNA
Vaccines for Preventive Infectious Disease Indications, 1996).
However, in the future, international standards for plasmid DNA
purity are likely to be the same or very similar to those that are
used for recombinant protein products similarly produced from E.
coli fermentation, and such standards exceed the current purity
attainable from established methods. Most glaringly, the accepted
standard of <100 pg host genomic DNA per dose (see: FDA Points
to consider in the characterization of cell lines used to produce
biologics, 1993) is far below the levels currently attainable for
purified plasmid preparations (100 pg per 1 mg dose is equivalent
to one part per ten million).
[0007] The basic methods for obtaining plasmids (by bacterial
fermentation), and for their purification (e.g., by the alkaline
lysis method (Birnboim, H C, Doly J. 1979, Nucleic Acids Res. 7:
1513-1523)) are well-known. Initially, the fermented bacterial cell
paste is resuspended and lysed (using a combination of sodium
hydroxide and sodium dodecylsulfate), after which the solution is
neutralized by the addition of acidic salt (e.g., potassium
acetate), which precipitates the bacterial DNA and the majority of
cell debris. The bulk of super-coiled plasmid DNA remains in
solution, along with contaminating bacterial RNA, DNA and proteins,
as well as E. coli endotoxin (lipopolysaccharide, or LPS). The
soluble fraction is then separated by filtration and subjected to a
variety of purification steps, which may include: RNase digestion;
chromatography (ion exchange gel filtration, hydroxyapatite, gel
filtration, hydrophobic interaction, reverse phase, HPLC, etc.);
diafiltration; organic extraction, selective precipitation,
etc.
[0008] Clearly, increasing the purity of the starting material and
achieving better downstream purification are essential goals for
manufacturing clinical grade DNA on an industrial scale.
Fermentation Media Considerations
[0009] Design of a balanced medium is based on the cell's energy
requirements and elemental composition. Typically, the nutritional
requirements are satisfied by either minimal media or semi-defined
media. Semi-defined media contain complex components such as yeast
extract, casamino acids, and peptones. The addition of complex
components supplies growth factors, amino acids, purines and
pyrimidines and often supports higher cell densities.
[0010] Carbon accounts for half of the cellular composition.
Accordingly, carbon is included in the highest amounts. The carbon
source provides energy and biomass, and is usually utilized as the
limiting nutrient. Glucose is the conventional carbon source. It is
metabolized very efficiently and therefore gives a higher cellular
yield. However, high glucose concentrations cause undesirable
acetate production due to metabolic overflow (known as the Crabtree
effect). Glycerol is also used and is often the preferred carbon
source in batch cultures. Although cellular yields from glycerol
are slightly smaller than from glucose, glycerol does not cause as
high of levels of acetate production and can be used at higher
concentrations without being inhibitory. Glycerol also supports
reduced maximum specific growth rates.
[0011] The requirement for nitrogen may be satisfied by inorganic
or organic nitrogen sources. Ammonia and ammonium salts (e.g.
NH.sub.4Cl, (NH.sub.4).sub.2SO.sub.4) are used in minimal media.
Semi-defined media supply nitrogen either partly or entirely from
complex components, including yeast extract, peptones, and casamino
acids.
[0012] Minerals are required for growth, metabolism, and enzymatic
reactions. Magnesium, phosphorus, potassium, and sulfur are
typically added as distinct media components. Di- and monopotassium
phosphates provide potassium and phosphorous and also function as
buffering agents in certain proportions. Magnesium sulfate
heptahydrate is often used as the source of magnesium and sulfur.
Other essential minerals include calcium, copper, cobalt, iron,
manganese, molybdenum and zinc. These are required in smaller
amounts and are often supplied by addition of a trace minerals
solution, though they are usually present as impurities in the
major ingredients. Osmolarity is adjusted with sodium chloride.
[0013] The use of animal-derived products, and in particular bovine
products, in plasmid manufacture is unacceptable due to the risk of
prion or virus contamination. All media components should be
certified animal product free. Vegetable-derived substitutes are
available for many components which have animal origin (e.g.
vegetable glycerol, soy peptone).
Plasmid Fermentation Process Considerations
Growth Rate
[0014] The use of reduced growth rate is the unifying principle in
high quality, high yield plasmid fermentations. High growth rates
have been associated with acetate production, plasmid instability,
and lower percentages of super-coiled plasmid. A reduced growth
rate alleviates growth rate-dependent plasmid instability by
providing time for plasmid replication to synchronize with cell
division.
Growth Conditions
[0015] Fermentation gives us the ability to control and monitor
many of the parameters that affect plasmid quality and yield.
Super-coiling is known to be affected by oxygen and temperature
(Dorman C J et al. 1988 J. Bacteriol. 179: 2816-2826), (Goldstein
E, Drlica K. 1984 Proc Natl Acad Sci USA. 81: 4046-4050). Oxygen
has been shown to play a role in plasmid stability. One study
(Hopkins D J, Betenbaugh M J, Dhurjati P. 1987 Biotechnol Bioeng.
29: 85-91) found that a single drop in dissolved oxygen
concentration to 5% of air saturation led to rapid loss in plasmid
stability. Another study (Namdev P K, Irwin N, Thompson B G, Gray M
R. 1993 Biotechnol Bioeng. 41: 666-670) showed that fluctuations in
oxygen input lead to plasmid instability. Furthermore, the
formation of nicked plasmids and multimers can be affected by many
parameters, including temperature, pH, dissolved oxygen, nutrient
concentration, and growth rate (Durland R H, Eastman E M. 1998 Adv
Drug Deliver Rev. 30: 33-48). The optimal temperature for E. coli
growth is 37.degree. C. However, lower temperatures (30-37.degree.
C.) may be used in batch fermentation to cause a reduced maximum
specific growth rate. Higher temperatures (36-45.degree. C.) can
also be employed to induce selective plasmid amplification with
some replication origins such as pUC, and pMM1 (Wong E M, Muesing M
A, Polisky, B. 1982 Proc Natl Acad Sci USA. 79: 3570-3574),
(Lin-Chao S, Chen W T, Wong T T. 1992 Mol. Microbio. 6: 3385-3393)
and runaway replicon R plasmids. Hamann et. al. 2000 (Hamann C W,
Nielsen J, Ingerslev E. 2000 World Patent Application WO0028048)
report a process for the production of R plasmids wherein plasmid
production is maintained at a low level (by use of low temperature)
to avoid retardation of growth due to plasmid DNA synthesis; once
the host cell population is high, plasmid production is induced by
temperature shifting.
Batch Fermentation
[0016] Batch fermentation has the main advantage of simplicity. All
nutrients that will be utilized for cell growth and plasmid
production throughout the culture period are present at the time of
inoculation. A batch fermentation has a lag phase, exponential
growth phase, and stationary phase. The use of a suitable inoculum
(1-5% of the culture volume) will reduce the length of the lag
phase. During the exponential phase all nutrients are in excess;
thus the specific growth rate will be essentially the maximum
specific growth rate, .mu..sub.max, as predicted by Monod kinetics.
As discussed previously, reduced growth rates are desirable for
plasmid production. In batch fermentation the growth rate can only
be reduced by reducing .mu..sub.max. This has been achieved by
growth at lower temperatures and by growth on glycerol instead of
glucose. Batch fermentation at 30.degree. C. using glycerol will
typically result in .mu..sub.max.ltoreq.0.3 h.sup.-1, which is
sufficient to prevent deleterious acetate accumulation and growth
rate associated plasmid instability (Thatcher D R, Hitchcock A,
Hanak J A J, Varley D L. 2003 U.S. Pat. No. 6,503,738). Glycerol
can also be used at much higher concentrations than glucose without
being inhibitory, leading to higher biomass yields. Generally,
biomass yields of up to 60 g/L DCW can be obtained with batch
fermentation.
Fed-Batch Fermentation
[0017] Fed-batch fermentation is especially useful for plasmid
production. Controlled addition of a limiting nutrient allows for
control of growth rate at rates <.mu..sub.max. Also, fed-batch
fermentation results in higher yields. The key to fed-batch
fermentation is supplying substrate at a rate such that it is
completely consumed. As a result, residual substrate concentration
is approximately zero and maximum conversion of substrate is
obtained. Metabolic overflow from excess substrate is avoided,
reducing the formation of inhibitory acetate.
[0018] Fed-batch fermentation starts with a batch phase. Cells are
inoculated into an initial volume of medium that contains all
non-limiting nutrients and an initial concentration of the limiting
substrate. Controlled feeding of the limiting nutrient begins once
the cells have consumed the initial amount of substrate.
[0019] One of the simplest and most effective feeding strategies is
exponential feeding. This method allows the culture to grow at a
predetermined rate less than .mu..sub.max without the need of
feedback control. The fermentation begins with a batch mode
containing a non-inhibitory concentration of substrate. The cells
grow at .mu..sub.max until the substrate is exhausted, at which
point the nutrient feeding begins.
[0020] The DO-stat and pH-stat methods are fairly easy to implement
since most standard fermentor systems include dissolved oxygen and
pH monitoring. Trends in dissolved oxygen (DO) and pH can indicate
whether substrate is available to the cells. Exhaustion of
substrate causes decreased oxygen uptake and the DO concentration
in the medium rises. The pH also rises due to consumption of
metabolic acids. Feeding is triggered when DO or pH rises above a
set threshold. The growth rate can be adjusted by changing the DO
or pH threshold value.
Exemplary Plasmid Fermentation Processes
[0021] Examination of current yields reveal that typical laboratory
shake flask culture produces from 1-5 mg of plasmid DNA/L of
culture, whereas a computer controlled fermentor can produce,
typically, from 10-250 mg/L.
[0022] Lahijani et al. (Lahijani R, Hulley G, Soriano G, Horn N A,
Marquet M. 1996 Human Gene Therapy 7: 1971-1980) have reported
using a pBR322-derived plasmid with a temperature sensitive single
point mutation (pUC origin) in a fermentation with exponential
feeding and a temperature shift from 37.degree. C. to 42-45.degree.
C. They achieved a plasmid yield of 220 mg/L in a 10 L fermentor.
The same plasmid without the mutation in batch fermentation (pBR322
derived origin) at 30.degree. C. yielded only 3 mg/L plasmid.
Friehs et al. (Friehs K, Flaschel E, Schleef M, Schmidt T. 2003
U.S. Pat. No. 6,664,078) describe a fed-batch process using a
glycerol yeast extract medium with DO-stat feedback controlled
feeding. The fermentation started with an initial batch volume of
7.5 L. Agitation was increased to keep DO above 30%. Feed medium
was pumped in when DO reached a threshold setpoint of 45%. The
culture reached stationary phase after 41 hours, yielding 60 g/L
DCW and 230 mg/L of plasmid. Chen (Chen, W. 1999 U.S. Pat. No.
5,955,323) used a fed-batch process in semi-defined medium with
combination DO-stat and pH-stat feedback control. DO and pH
threshold setpoints were 50% and 7.2, respectively. When DO dropped
below 30% because of high metabolic activity agitation speed was
increased by a percentage of the previous speed. In a 7 L
fermentor, this strategy led to a specific growth rate of 0.13
h.sup.-1 and plasmid yields of 82-98 mg/L. Durland and Eastman,
Supra, 1998 report batch fermentation at 37.degree. C. in a
proprietary medium. Their process typically yields 130 mg/L and has
yielded as high as 250 mg/L.
[0023] Even in view of the prior art, there remains a need for a
cost effective method for high purity plasmid DNA production. The
fermentation media and processes described above incorporate what
is currently known in the art to improve plasmid productivity, such
as reduced growth rate and plasmid copy number induction with high
temperature. These processes plateau at about 200-250 mg plasmid
DNAIL. This low yield imposes a cost and purity burden on
commercialization of plasmid DNA production processes. Although
economies of scale will reduce the cost of DNA significantly in the
future, a far more economical solution to this problem is needed in
order to achieve the desired cost. As well, international standards
for plasmid DNA purity are likely to be the same or very similar to
those that are used for recombinant protein products similarly
produced from E. coli fermentation, and such standards exceed the
current purity attainable from established methods. Increasing the
yield (mg of DNA/gram of cell paste) in fermentation would both
decrease the cost and increase the purity of the DNA (because it
reduces the amount of material being processed).
DISCLOSURE OF THE INVENTION
[0024] The invention is a method for production of DNA replicons,
utilizing improved batch and fed-batch processes for plasmid
production. Specifically, a method of fed-batch fermentation is
disclosed in which plasmid-containing E. coli cells are grown at a
reduced temperature during the fed-batch phase, during which growth
rate is restricted, followed by a temperature up-shift and
continued growth at elevated temperature in order to accumulate
plasmid, whereby the temperature shift an restricted growth rate
improves yield and purity of plasmid. In a preferred embodiment,
the reduced growth rate is determined to maintain the plasmid yield
below approximately 2 mg/L/OD. In another preferred embodiment, the
reduced temperature is around 30.degree. C. In another preferred
embodiment, the temperature up-shift is to approximately
36-45.degree. C. In another preferred embodiment, the plasmid
contains a ColE1-derived replication origin. In yet another
preferred embodiment, the plasmid contains a pMB1 replication
origin containing the pUC G to A mutation. In still another
preferred embodiment, the plasmid is derived from the VR1012
backbone. In one highly preferred embodiment, the fermentation
media is substantially a semi-defined glycerol media. In yet a
final preferred embodiment, a pBR322-derived plasmid is grown in E.
coli in fed-batch fermentation during which growth rate is
restricted during the fed batch phase an growth is continued to
accumulate plasmid product. Summarizing, these processes feature
high cell density cultivation strategies, combined with novel
growth and induction phase temperature shifts. In the production of
pBR322-derived origin containing DNA replicons, fed-batch
fermentation is performed at restricted cell growth rate. In the
production of temperature inducible DNA replicons (e.g. pUC or pMM1
origin containing plasmids) the fed-batch fermentation is performed
at restricted cell growth rate and reduced temperature during the
growth phase; plasmid production is then induced by temperature up
shift. These processes dramatically improve plasmid DNA
fermentation yield, while maintaining or improving plasmid
integrity, relative to the processes described in the art.
BRIEF SUMMARY OF THE INVENTION
[0025] It is a purpose and/or objective of the present invention to
provide fermentation processes for the production of plasmid DNA.
Another objective and/or purpose of the invention is to improve
plasmid DNA production yield in fermentation culture. Yet another
objective and/or purpose of the invention is to improve plasmid DNA
quality in fermentation culture. Yet another objective and/or
purpose of the invention is to reduce impurities in purified
plasmid DNA. Another disclosure is improved fermentation processes
that, compared to processes defined in the art are improved by:
increased yield of plasmid through induction of plasmid levels
after biomass production; improved yield and integrity with toxic
or unstable plasmids through maintenance of low plasmid levels
during biomass production; increased quality of plasmid by reduced
levels of nicked (open circular) or linearized versions of the
plasmid; increased quality of plasmid by increase in the percent
monomer of plasmid; simplified production using robust, automated
control parameters and feeds; simplified scaling due to growth
control and reduced oxygen supplementation required during growth;
reduced levels of impurities after plasmid purification due to
enriched levels of plasmid in the feed stream into downstream
processing; and improved regulatory compliance by elimination of
all animal product derived components.
[0026] Further objects and advantages of the invention will become
apparent from a consideration of the drawings and ensuing
description.
BRIEF DESCRIPTION OF THE DRAWING FIGURES
[0027] FIG. 1 shows a pBR322-derived plasmid fed-batch fermentation
in E. coli with NTC3019 media.
[0028] FIG. 2 shows a pUC plasmid batch fermentation in E. coli
with NTC3018 media.
[0029] FIG. 3 shows a gWiz GFP plasmid fed-batch fermentation in E.
coli with NTC3019 medium.
[0030] FIG. 4 shows a gWiz GFP inducible fed-batch fermentation in
E. coli with NTC3019 medium (37.degree. C. or 42.degree. C.
induction).
[0031] FIG. 5 illustrates an inducible fed-batch fermentation
process.
DETAILED DESCRIPTION OF THE INVENTION
[0032] Turning now to the drawings, FIG. 1. shows a pBR322-derived
plasmid fed-batch fermentation in E. coli with NTC3019 media,
revealing: (a) typical growth and plasmid productivity profile of
pBR322-derived plasmids in E. coli during fed-batch fermentation
with NTC3019 media; and (b) plasmid DNA produced by the NTC3019
media fed-batch fermentation process is highly super-coiled and
free of nicked and open circle isoforms.
[0033] In FIG. 2, the plasmid growth and productivity profile of a
pUC plasmid (pW2.0) batch fermentation in E. coli with NTC3018
media is shown. The pW2.0 plasmid in batch fermentation reached a
cell density of 57 OD600 and yielded 230 mg plasmid/L.
[0034] In FIG. 3, a gWiz GFP plasmid fed-batch fermentation in E.
coli with NTC3019 medium is shown: (a) growth and control parameter
profile (dissolved oxygen, temperature, agitation) of a fed-batch
fermentation profile of gWiz GFP; (b) fluorescence microscopy of
cells stained with SYBR Green I shows filamentation at the plateau
(left), whereas growth resumed and filamentation was reduced after
the temperature was reduced to 33.degree. C. (right).
[0035] In FIG. 4, a gWiz GFP inducible fed-batch fermentation in E.
coli with NTC3019 medium (37.degree. C. or 42.degree. C. induction)
is shown: (a) growth and plasmid productivity profile of a
gWiz-GFP/E. coli DH5.alpha. fermentation with a
30.fwdarw.37.degree. C. temperature shift at 35 hours is revealed,
plasmid yield reached 670 mg/L; and (b) growth and plasmid
productivity profile of a gWiz-GFP/E. coli DH5.alpha. fermentation
with a 30.fwdarw.42.degree. C. temperature shift at 35 hours is
demonstrated. Plasmid yield reached 1100 mg/L.
[0036] In FIG. 5, the inducible fed-batch fermentation process is
illustrated.
Definitions
ccc: Covalently Closed Circular
[0037] ColE1 derived origin: Origin of replicated derived from
ColE1 type plasmid (e.g. pMB1, ColE1) by deletion (e.g. pBR322
derived origin) and/or base change (e.g. pUC from pMB1, pMM1, pMM5
from ColE1 etc) DNA replicon: plasmids, cosmids, bacterial
artificial chromosomes (BACs) bacteriophages, viral vectors and
hybrids thereof. NTC3018 fermentation media: Glycerol semi defined
batch fermentation media NTC3019 fermentation media: Glycerol semi
defined fed-batch fermentation media pDNA: Plasmid DNA
pBR322-derived origin: pMB1 origin from pBR322, in which the rop
(repressor of primer) gene has been deleted plasmid: plasmids,
cosmids, bacterial artificial chromosomes (BACs), bacteriophages,
viral vectors and hybrids thereof pUC origin: pBR322-derived
origin, with G to A transition that increases copy number at
elevated temperature semi-defined glycerol media: fermentation
media that contains complex nitrogen source (e.g. yeast extract,
soy extract) and glycerol carbon source
[0038] The invention relates to methods for production of
covalently closed circular (ccc) recombinant DNA molecules such as
plasmids, cosmids, bacterial artificial chromosomes (BACs),
bacteriophages, viral vectors and hybrids thereof (herein
collectively referred to as plasmids) in a bacterial production
host, using a mechanical fermentation vessel.
[0039] Fermentation processes described in the art are not optimal,
with suboptimal plasmid yield, quality (e.g. nicking or
linearization of plasmid), poor scalability (e.g. due to excessive
oxygen supplementation requirements), and restricted application
(e.g. inability to use with plasmids containing unstable or toxic
sequences). The invention is a method for improving yield and
purity of plasmid DNA during fermentation culture. A cost effective
approach to high yield fermentation has been developed that
utilizes an inducible fed batch fermentation process to improve
plasmid yield and purity.
Plasmid Production Process and Media Preferred Embodiments
[0040] In one preferred embodiment for production of pBR322-derived
plasmids, fed-batch fermentation is performed at a restricted cell
growth rate. This process dramatically improves plasmid DNA
fermentation yield, while maintaining or improving plasmid
integrity, relative to the processes described in the art.
[0041] Using this process with moderate copy plasmids (e.g. pBR322
replication origin, with ROP gene deleted, herein referred to as
pBR322-derived plasmids), plasmid yields of 250-450 mg/L and cell
densities of 120 OD.sub.600 have been achieved with an automated
fed-batch fermentation process at 37.degree. C. with feeding
controlled to maintain a specific growth rate of 0.12 hr.sup.-1.
This is a 100 fold improvement over reported yields (Lahijani et
al., Supra, 1996). The molecular basis for this novel dramatic
improvement is unknown. Regardless of the mechanism, application of
the invention to production of other plasmids will increase
fermentation productivity, without loss of plasmid quality.
[0042] In one preferred embodiment for production of temperature
inducible DNA replicons (e.g. pUC or pMM1 origin containing
plasmids) the fed-batch fermentation is performed at restricted
cell growth rate and reduced temperature during the growth phase;
plasmid production is then induced by temperature up shift. This
process dramatically improves plasmid DNA fermentation yield, while
maintaining or improving plasmid integrity, relative to the
processes described in the art.
[0043] This novel strategy for high yield plasmid production of
high-copy origin containing plasmids (e.g. pUC origin) disclosed
herein results in unexpected high plasmid productivity and plasmid
quality. In addition, growth rate is reduced during the fed-batch
phase. The process is shown in FIG. 5. This novel combination of
elements has not been applied to the production of ColE1 derived
origin plasmids and when tested gave the new and unexpected result
of improved productivity. Thus, we teach a new use (improved
productivity) for the combination of reduced growth rate with 1)
reduced temperature for growth and biomass production, and 2)
increased temperature for induction of plasmid production.
[0044] The discovery that the combination of an initial reduced
temperature growth phase with a later high temperature production
phase results in improved overall growth, biomass, and plasmid
yield is novel and unexpected, and is not taught in the art. Hamann
et al., Supra, 2000 used a temperature inducible fermentation
specifically to reduce metabolic burden associated with R plasmids
during growth. The strategy was utilized for production of R
plasmids, and was not taught for ColE1 origin containing plasmids.
As well, Hamann et al., Supra, 2000 does not contemplate improving
overall productivity with this strategy. Thus, this combination of
elements has not been suggested in the art to improve yield. There
is a synergism between the combination which is greater than the
sum of the parts as revealed by the improved productivity. As well,
the high yield fermentations fill a long felt but unsolved need
since the numerous previous processes described in the art over the
last 10 years have failed to teach high yield fermentation. In
summary, we teach a new combination of elements for ColE1 origin
containing plasmid production, comprising slow growth combined with
temperature induction that demonstrated the unexpected and
surprising new use of improved plasmid productivity.
[0045] Application of the inducible fed-batch fermentation process
for production of high copy plasmids resulted in yields of 1100
mg/L plasmid DNA, and OD.sub.600 of 100. This is a five fold
improvement over yields obtained with fermentation processes
defined in the art. The DNA purified from all these processes is of
a high quality, being essentially 100% super-coiled. We contemplate
use of the batch and fed-batch fermentation processes described
herein to improve plasmid productivity.
[0046] The inducible fed-batch process described herein maintained
low plasmid levels (<2 mg/L/OD.sub.600 for VR1012 derived
vectors) throughout the biomass production phase of the process,
and facilitated unexpected and unprecedented ultra high plasmid
production (>6 mg/L/OD.sub.600 for VR1012 derived vectors) after
biomass production. High specific yields are very desirable since
increased plasmid yield per gram of bacteria leads directly to
higher final product purities. We contemplate utilizing the
temperature shift of the invention to keep plasmid levels low
(<2 mg/L/OD.sub.600 for VR1012 derived vectors) throughout
growth, inducing plasmid production to high levels (>3
mg/L/OD.sub.600 for VR1012 derived vectors) after biomass
production. These levels are a guideline for production of VR1012
derived vectors. Other plasmids may be tolerated at higher or lower
levels than 2 mg/L/OD.sub.600 during the growth phase. The maximal
plasmid level during the growth phase that maintains acceptable
metabolic burden, plasmid stability, and enhanced productivity
after temperature shift can be determined experimentally for each
new plasmid by one of average skill in the art.
Fermentation Media Alternative Embodiments
[0047] Exemplary animal product free fermentation media
formulations, NTC3018 (batch), NTC3019 (fed-batch) may be utilized
in practicing the invention. These media are optimized
semi-synthetic growth media, containing glycerol carbon source,
yeast extract nitrogen source, and trace metals, salts and buffers.
It is anticipated that substitution of this media for those
described in the art will also result in improved plasmid
productivity using the fermentation processes as described
herein.
[0048] Alternative non-animal sourced nitrogen sources for use in
NTC3018 and NTC3019 media are contemplated. As a complex media
component, yeast extract provides nitrogen, amino acids, vitamins,
and carbon. Possible components of complex media (e.g. yeast or soy
extracts) key to cell metabolism during plasmid production include
limiting amino acids, vitamins, trace minerals and alternative
carbon sources. By way of example, we contemplate use of
alternative yeast extract preparations, soy preparation (e.g.
select soytone, or phytone peptone from BD Biosciences) or other
vegetable preparations (e.g. pea flower peptones from Oxoid) in
NTC3018 and NTC3019 media.
[0049] Variations in the defined elements of the media are also
contemplated. For example, increased phosphate or magnesium is
contemplated, either as increases in the batch media component, or
as additions to the feed in fed-batch fermentation. Further
optimization of the media, by systematic component evaluation can
be performed by one skilled in the art of fermentation.
[0050] Additives to the media are contemplated when utilizing
certain auxotrophic cell lines. For example, cell lines such as
Stb12 (InVitrogen Corp.) that contain the proAB deletion may need
amino acid supplementation, or an alternative nitrogen source rich
in proline, to achieve maximal growth. Such modifications can be
determined by one of average skill in the art of fermentation.
[0051] We also contemplate use of the batch and fed-batch
fermentation processes described herein with plasmid fermentation
media described in the art. This includes defined media such as
those disclosed by Soubrier (Soubrier F. 2004 US Patent application
2004/0142452). Preferred media to use with the fed-batch
fermentation processes of the invention are glycerol media
formulations with semi-defined feeds, such as NTC3019 and those
disclosed in Lahijani et al., Supra, 1996, Friehs et al., Supra,
2003, Chen Supra, 1999. and Urthaler et al (Urthaler J, Roman N,
Ascher C, Woehrer H.2005 US Patent Application 2005/0026177).
Fermentation Process Alternative Embodiments
[0052] Improved fed-batch and batch processes for plasmid
production are disclosed herein. These feature exponential feed
strategies, combined with novel growth and induction phase
temperature shifts.
[0053] In practicing the fed-batch processes of the invention, we
contemplate various feeding strategies to reduce growth rate,
including feedback, feed-forward, and predetermined control of
nutrient feeding. For example, nutrient feed may be added according
to a carbon limiting exponential feeding strategy. We anticipate
variation of this feeding strategy to control growth rate within
acceptable ranges. Preferred growth rate ranges are .mu.=0.05 to
0.3 hr.sup.-1. A preferred target growth rate is .mu.=0.12
hr.sup.-1. Acceptable growth rate ranges will be plasmid specific
and can be determined experimentally by those skilled in the
art.
[0054] In practicing the fed-batch processes of the invention, we
contemplate various batching strategies to reduce production time.
The semi-defined nutrient included in the batch phase can be
adjusted, to allow the batch phase to proceed to higher or biomass
concentrations. In the case of higher biomass concentration,
overall fermentation time is reduced since growth is faster in the
batch phase compared to the fed-batch phase. We anticipate
variation of this batching strategy to control the start of the
fed-batch phase of the process. Preferred OD.sub.600 ranges for the
fed-batch phase to start are from 1 to 60. Acceptable fed-batch
starting OD.sub.600 ranges may be plasmid specific and can be
determined experimentally by those skilled in the art.
[0055] In practicing the inducible fed-batch and batch processes of
the invention, we contemplate various temperature shifting
strategies from the growth to the induction phase. The growth phase
can be performed at temperatures from 25-37.degree. C., preferably
at 30-37.degree. C. For high copy plasmids, the growth phase is
most preferably 30-32.degree. C. The induction phase can be
performed at temperatures from 33-45.degree. C., and preferably
37-42.degree. C.
[0056] In practicing the inducible processes with temperature
shifting strategies, we contemplate using nutrient concentration,
biomass concentration; or optical density as an indicator of when
to switch from the growth phase to the induction phase. Regular
sampling of the fermentation culture can provide material to obtain
biomass or optical density measurements and the temperature shift
can be performed at a certain biomass concentration. Online sensors
can also be used to provide continuous monitoring of biomass
concentration and the fermentor can be set to automatically perform
the temperature shift at a specified biomass concentration. In
practicing the inducible fed-batch process with temperature
shifting strategies we also contemplate performing the temperature
shift once a certain amount of feed nutrient has been added.
[0057] In practicing the inducible processes with temperature
shifting strategies, we contemplate using higher temperatures
during the growth phase to minimize production times. The inducible
fed-batch process described herein maintained low (<2
mg/L/OD.sub.600) plasmid levels throughout the growth phase of the
process. The maximal temperature that can be utilized during the
growth phase that maintains acceptable metabolic burden, plasmid
stability, and enhanced productivity after temperature shift will
be plasmid specific and will vary between different plasmid
backbones. For example, some plasmids may be tolerated at much
higher levels than 2 mg/L/OD.sub.600. As well, plasmid productivity
may vary at low temperature, such that some plasmids may not
produce as high levels of plasmid. In these cases, we contemplate
using higher temperatures during the growth phase. Additionally,
increased maximal temperatures may be tolerated during the initial
batch phase due to unrestricted growth and corresponding lower
plasmid copy numbers (FIG. 5). The maximal temperature that can be
utilized during the growth phase (batch and fed-batch components),
that maintains acceptable metabolic burden, plasmid stability, and
enhanced productivity after temperature shift can be determined
experimentally by one of average skill in the art.
Plasmids and Host Strains
[0058] We contemplate use of the invention in the production of
plasmids with a variety of origins of replication, that are either
high copy, low copy and moderate copy, and are either temperature
inducible or not. Some preferred origins of replication, and
plasmids incorporating them, are outlined in Table 1. Modifications
to these origins are known in the art, and are also contemplated
for use.
TABLE-US-00001 TABLE 1 Replication origins Parent Copy Origin
Regulation High copy Derivation Number Therapeutic plasmids pMB1
Antisense RNAI binds pUC origin (Rop deletion and second 50 at
37.degree. C., Multiple (pcDNA3, RNAII. Rop accessory site mutation
that alters RNAI/II 175 at 42.degree. C. pVAX, VR1012, etc) protein
stabilizes interaction at 37 and 42, not 30 C.) (log phase)
interaction pUC origin with second site enhancer Not pDNAVACCultra
increases copy number 14-50% determined Rop deletion 30 at
37.degree. C. pCMVKm2 and 42.degree. C. (log phase) G to T mutation
(extends RNAI, 1000 (phase Not described attenuating represser; not
conditional) not Plasmid is 65% total DNA indicated) ColEI Same as
pMB1 pMM1, pMM7 (Rop deletion and 2000 in pVC0396.dagger. second
site mutation that alters stationary RNAI/RNAII interaction at 37
and 42, phase not 30 C.). pMM7 is >50% total DNA in (pMM7)
stationary phase R6K .pi. rep protein binds Host strain pir-116
mutant (.pi. rep 200 pCpG, pBoost (ori .alpha., iteron, copy number
protein copy-up mutation in 250 pCOR ori .beta. ori dependent
activation oligomerization domain removed from .gamma.) (low) or
repression plasmid and provided in trans from (high) chromosome) R1
RepA initiator protein Temperature inducible copy number 2000 Not
described binds non repeated using dual origin mutant (plasmid is
75% (mutant) target. Antisense CopA total DNA) represser binds RepA
RepA controlled by temperature 1000 pCWH24-6 leader (CopT).
inducible lambda P.sub.R promoter and (P.sub.R Auxiliary CopB
protein temperature sensitive lambda repressor controlled)
represses RepA controlled. (Plasmid is 50% total DNA) expression.
pKL1 Rep A initiator protein Rep A initiator protein overexpression
>2500 Not described represses repA on separate plasmid or on
chromosome transcription as hexamer .dagger.pVC0396 is an optimized
vector backbone, for insertion of eukaryotic expression
cassettes
[0059] Alternative host strains are contemplated. E. coli strain
DH5.alpha. is a widely used host for plasmid production. Its key
qualities include the recA mutation, which minimizes non-specific
recombination of cloned DNA, and the endA1 mutation, eliminating
non-specific digestion of plasmid by Endonuclease I. In addition to
DH5.alpha., a variety of other strains are suited for plasmid
production; a non limiting, list of exemplary E. coli host strains
is shown in Table 2.
TABLE-US-00002 TABLE 2 Host strains Strain Genotype Source DH1
recA1 endA1 hsdR17(rk-, mk+) phoA supE44 .lamda.- thi-1 gyrA96
relA1 DH5.alpha. F.sup.- .PHI.80dlacZ.DELTA.M15 .DELTA.(lacZYA
-argF) U169 recA1 endA1 Invitrogen hsdR17(rk-, mk+) phoA supE44
.lamda.- thi-1 gyrA96 relA1 DH10B F.sup.- mcrA
.DELTA.(mrr-shdRMS-mrcBC), .PHI.80dlacZ.DELTA.M15 .DELTA.lacZ74,
Invitrogen deoR, recA1, endA1, araD139, .DELTA.(ara-leu)7697, galU,
galK, .lamda.-, rpsL, nupG JM109 endA1, recA1 gyrA96, thi,
hsdR17(rk-, mk+) relA1, supE44 Stratagene .DELTA.(lac-ProAB)
[F'traD36, proAB lacI.sup.qZ.DELTA.M15] XL1-Blue recA1 endA1 gyrA96
thi-1 hsdR17 supE44 relA1 lac [F'proAB Stratagene
lacI.sup.qZ.DELTA.M15 Tn10 (Tet.sup.r)] Top10 F.sup.- mcrA
.DELTA.(mrr-hsdRMS-mcrBC) .PHI.80lacZ.DELTA.M15 .DELTA.lacX74
Invitrogen recA1 ara.DELTA.139 .DELTA.(ara-leu)7697 galU galK rpsL
(Str.sup.R) endA1 nupG Mach1 .DELTA.recA1398 endA1 tonA
.PHI.80.DELTA.lacM15 .DELTA.lacX74 hsdR(r.sub.k.sup.-m.sub.k.sup.+)
Invitrogen GT116 F.sup.- mcrA .DELTA.(mrr-hsdRMS-mcrBC)
.PHI.80lacZ.DELTA.M15 .DELTA.lacX74 Invivogen recA1 endA1
.DELTA.dcm .DELTA.sbcC-sbcD ECOS101 F.sup.- (.PHI.80 .DELTA.lacZ
.DELTA.M15).DELTA.(lacZYA-argF)U169 hsdR17(r.sub..kappa.-
m.sub..kappa.+) Yeastern recA1 endA1 relA1 deoR .lamda.- EC100
F.sup.- mcrA .DELTA.(mrr-hsdRMS-mcrBS) .PHI.80 .DELTA.lacZ
.DELTA.M15).DELTA.lacX74 Epicentre recA1 endA1 araD139(ara,
leu)7697, galU, galK, .lamda.- rpsL, nupG Sure e14- (McrA-) .DELTA.
(mcrCB-hsdSMR-mrr)171 endA1 supE44 thi-1 Stratagene gyrA96 relA1
lac recB recJ sbcC umuC::Tn5 (Kan.sup.r) uvrC [F' proAB
lacI.sup.qZ.quadrature.M15 Tn10 (Tet.sup.r)] Stbl2 F.sup.- mcrA
.DELTA.(mcrBC-hsdRMS-mrr) recA1 endA1 lon gyrA96 thi Invitrogen
supE44 relAl .lamda..sup.- .DELTA.(lac-proAB) Stbl4 mcrA
.DELTA.(mcrBC-hsdRMS-mrr) recA1 endA1 gyrA96 gal.sup.- thi-1
Invitrogen supE44 .lamda..sup.- relA1
.DELTA.(lac-proAB)/F'proAB.sup.+ lacI.sup.qZ.DELTA.M15 Tn10
Tet.sup.R
[0060] DH5.alpha., XL1-Blue, DH10B, JM109 and Top 10 have been well
established as plasmid production strains. Mach1, and ECOS101 have
been developed recently and may be desirable plasmid production
hosts. Stb12, GT116 and Sure cells have been utilized for the
production of unstable DNA containing plasmids. Unstable DNA
contains structures like direct (e.g. retroviral long terminal
repeats) or inverted repeats (e.g. shRNA palindromes), Z DNA, etc.
The deletion of the dcm gene in GT116 eliminates dam methylation
which is immuno-stimulatory. Therefore, production in GT116 reduces
the immunogenicity of plasmid DNA. Similar reductions in
immunogenicity are observed utilizing strains expressing CpG
methylase.
Production of Unstable Plasmids
[0061] We also contemplate use of the invention in the production
of plasmids containing unstable sequences. Palindrome sequences,
direct or inverted repeats, and Z DNA forming sequences are
unstable and are deleted or rearranged by E. coli hosts. In some
instances, plasmids for therapeutic use must contain unstable
sequences (inverted or direct repeats for viral vectors such as AAV
and HIV, Z DNA forming segments or triplet repeats for certain
therapeutic genes). Current strategies to maintain plasmids
containing unstable sequences are to use host cell lines with
stabilizing mutations. Several hosts are commercially available for
propagation of these plasmids, for example, Sure cells
(Stratagene), GT115 (Invivogen) or Stb12 and Stb14 (Invitrogen).
The Stb12 and Stb14 cell lines utilize an undisclosed mutation that
increases stability of direct repeat containing vectors such as
retroviral vectors; this effect is enhanced at reduced temperature,
presumably due to reduced copy number. Specific combinations of
repair mutations can stabilize plasmid propagation, especially at
low temperature. The Sure and Sure2 cell lines uses one such
combination, with homologous recombination deficiency (recB, recJ)
in conjunction with UV repair (uvrC) and SOS repair (umuC)
deficiency (to stabilize LTRs), and SbcC (and recJ) to stabilize Z
DNA. The GT116 cell line uses SbcC and SbcD to stabilize
palindromic sequences. These strains function to stabilize plasmids
only at low temperature (i.e. 30.degree. C.), presumably due to
reduced plasmid copy number. This strategy obviously increases
production cost. Use of the inducible fermentation process
described herein would allow propagation at 30.degree. C. of
unstable plasmids in stabilizing cell lines, prior to increasing
copy number only for a short duration prior to harvest. This should
maximize yield and stability (i.e. quality) of unstable
plasmids.
DNA and plasmid Production
[0062] The underlying mechanism for the observed increased yield of
plasmid DNA (>6 mg/L/OD.sub.600) in the inducible fed-batch
process is unknown. It is potentially due to induction of DNA
compaction agents (e.g. histone-like protein or other chromatin
binding proteins, such as the dps gene product) during biomass
production at slow growth and reduced temperature.
[0063] Altering DNA condensation during the induction phase may
increase plasmid yield by increasing tolerable plasmid levels or
copy number. The degree of compaction of a DNA is set by two
opposing factors; condensing chromatin proteins and decondensing
transcription complexes. Plasmid compaction may be affected by the
level of transcription from plasmid promoters. Less transcription
may be associated with higher compaction, and potentially higher
carrying capacity.
[0064] In E. coli, a number of chromatin proteins have been
identified that are involved in DNA compaction. These gene products
bind plasmid and genomic DNA. In the case of genomic DNA, they
compact the DNA into the nucleoid (reviewed in (Robinow C,
Kellenberger E. 1994 Microbiol Review 58: 211-232)). The major
components of the nucleoid are the histone like proteins HU, IHF,
and BN-S, StpA (related to HN-S, expressed at about 1/10 level) and
Dps, which are distributed uniformly in the nucleoid, while other
proteins, such as SeqA, CbpA, CbpB, Fis and IciA are in lower
amount, show non-uniform distribution in the nucleoid, and may have
regulatory functions. An isolated R plasmid protein complex
contained three major proteins, 23% HN-S, 23% RNA polymerase, and
5% HU. This would presumably change depending on growth phase since
chromatin associated gene products are differentially regulated in
different media, different cell densities and during growth and
stationary phases. F is, HU, BF-1 generally are more highly
expressed in log phase, while IHF and Dps are at higher levels in
stationary phase. Dps condenses DNA into liquid biocrystalline
complexes in stationary phase to improve stress resistance.
Over-expression of BN-S during the growth phase leads to DNA
condensation and viability loss. Cells may have higher plasmid
capacity when DNA is highly compacted. In the NTC inducible
fermentation process, growth phase cells have lower overall
capacity for plasmid DNA than induction phase cells. This may be
due to differences in the combinations of chromatin proteins
present in the induction phase which may allow higher levels of
tolerable plasmid than in the growth phase. Alternations to the
ratios of chromatin proteins during the induction phase may
increase plasmid compaction, and carrying capacity.
[0065] Alternations to the ratios of chromatin proteins during the
induction phase may also increase plasmid replication rates. For
example, expression from the p15A origin RNAII promoter, but not
the pMB1 (pBR322) RNAII promoter, is repressed by IHF; p15A RNAII
transcription is increased in IHF mutants. Dps and HU are
non-specific DNA binders, HN-S, CbpA and CbpB bind curved DNA. StpA
is related to HN-S, binds DNA with higher affinity, and also binds
curved DNA. Fis, IHF, IciA and seqA are sequence specific. HN-S
represses transcription from a number of promoters that contain
curved DNA. The RNAII promoter of pMB1 (pUC and pBR322) contains
polyA and poly T tracks; these sequences form curved DNA. The
decreased levels of curved DNA binding chromatin proteins that
repress transcription (e.g. HN-S) in stationary phase may be
associated with increased ratio of RNAII to RNAI transcription, and
the documented stationary phase increase in plasmid copy number.
Alterations to the composition of the chromatin proteins (e.g.
further decrease in BN-S) present during the production phase of
NTC fermentation process may lead to increased plasmid copy number
with pMB1 plasmids such as pUC.
[0066] Heterologous DNA compactors, for example, the acid soluble
spore proteins of Bacillus species, when expressed in E. coli, may
also be useful DNA compactors for increasing plasmid yield. For
example, expression of a B. subtilis small acid soluble protein in
E. coli causes DNA (Setlow B, Hand A R, and Setlow P. J Bacteriol.
173: 1642-1653).
[0067] Process alterations may also improve yields through effects
on DNA condensation. Dps is regulated by Magnesium (Mg.sup.++)
concentration; the presence of Dps does not result in DNA
condensation; tightly packed crystalline DNA:Dps complexes form
when Mg.sup.++ concentration falls below a threshold [reviewed in
(Frenkiel-Krispin D, Levin-Zaidman S, Shimoni E, Wolf S G, Wachtel
E J, Arad T, Finkel S E, Kolter R, Minsky A. 2001 EMBO J. 20:
1184-1191)]. Morphologically, the complex resembles that induced by
chloramphenicol addition during stationary phase. Addition of 0.2
mM spermidine to growing cultures accelerates DNA condensation in
the absence of Dps. Phosphate starvation has the same effect,
perhaps through enhanced degradation of threonine and arginine to
spermidine (Frenkiel-Krispin et al, Supra, 2001). Changes to
fermentation composition or conditions during the induction phase,
to alter the levels of divalent cations (e.g. Mg.sup.++, through
exogenous addition or depletion), or alter the level of positively
charged polyamines (e.g. spermidine, through exogenous addition or
control of bacterial synthesis) may increase plasmid yield and are
contemplated as alterations to the media.
[0068] We contemplate further yield increases may be obtained by
further compaction of plasmid DNA. This could be achieved by
addition of DNA compaction agents to the feed (e.g.
polyethyleneimine, spermidine, spermine) or strain modifications
that increase production of host strain DNA compaction agents such
as spermine production or dps protein production, during the
fermentation process. Such strain modifications could be
alterations that allow the relevant gene products to be induced
during the fermentation process.
[0069] In practicing the inducible processes, we contemplate using
alternative strategies to maintain plasmid copy number at a low
level during the growth phase. For example, in addition to growth
at a low temperature, other mechanisms exist to reduce copy number
that could be incorporated into the growth phase. For example,
reduced dissolved oxygen during fermentation has been shown to
reduce plasmid copy number (Games A E, 2005 BioProcess
International 3:9, in press).
Improvement to Final Product Purity
[0070] We contemplate utilizing plasmid enriched feed streams from
the described fermentation culture in exemplary plasmid
purification processes. Such processes are well known in the art.
The combination of high yield fermentation and exemplary
purification process may provide cost effective methodologies to
further reduce genomic DNA to acceptable levels for gene therapy
and DNA vaccination applications.
EXAMPLES
[0071] The method of the invention is further illustrated in the
following examples. These are provided by way of illustration and
are not intended in any way to limit the scope of the
invention.
Example 1
NTC3018 and NTC3019 Fermentation Media
[0072] The following criteria were established for evaluation of an
optimized fermentation process fo manufacturing plasmid DNA:
1) High specific yield of plasmid (mg plasmid DNA per g cell mass);
2) High biomass yield; 3) It will retain high degrees of
super-coiled plasmid; 4) It will cause minimal problems during
downstream processing; 5) It will meet regulatory requirements; and
6) It will retain plasmid structure (e.g. no deletions or other
rearrangements).
[0073] Culture media was formulated to support high specific
plasmid yield, high biomass yield, and high plasmid quality. The
batch fermentation medium was designed to reduce the specific
growth rate. The use of a reduced growth rate has been associated
with higher plasmid copy number and better plasmid stability.
During fed-batch fermentations the growth rate was controlled at
0.12 hr.sup.-1 by feeding of the limiting nutrient. The host
strain, DH5.alpha., has the endA1, recA, and relA mutations, all
important for plasmid production. Additionally, all components used
in the media were well characterized and certified animal product
free.
[0074] NTC3018 (batch) and NTC3019 (fed-batch) media are optimized
for many components of both batch and fed-batch process media. For
example glycerol is utilized as the carbon source rather than
glucose to reduce the growth rate. Yeast extract is used as the
nitrogen source. The trace metals and MgSO.sub.4 concentrations
have been optimized, based on determined requirements of E. coli
production strains.
Example 2
NTC3019 Media Fed-Batch Culture with pBR322-Derived Plasmids
[0075] Fed-batch fermentations were carried out in a New Brunswick
BioFlo 110 fermentor at 37.degree. C. pH was controlled by
automatic addition of 30% ammonium hydroxide or 10% phosphoric
acid. The dissolved oxygen probe was calibrated to 0% by nitrogen
gas sparging and 100% with air saturation. The vessel was aerated
at 1 VVM and dissolved oxygen was maintained at 30% by
proportional-integral control of agitation. At cell densities above
about 20 OD.sub.600, O.sub.2 supplementation was also required to
maintain 30% saturation.
[0076] Seed cultures were started from single isolated colonies
inoculated into LB plus 50 .mu.g/ml kanamycin and grown at
37.degree. C. At mid-exponential phase (0.5-1.5 OD.sub.600) the
seed cultures were used to provide 1% inoculums for the
fermentor.
[0077] During fed-batch cultures a semi-defined feed nutrient was
added according to a carbon limiting exponential feeding strategy.
Briefly, an initial amount of carbon substrate is consumed during
the batch phase at a specific growth rate of .mu..sub.max. Upon
exhaustion of the carbon substrate, the fed-batch phase begins and
feed nutrient is added automatically at the rate determined by the
following equation (Carnes, Supra, 2005):
F ( t ) = .mu. X B V B S f Y X / S .mu. t ##EQU00001##
Where
[0078] .mu.=desired specific growth rate during fed-batch phase,
[0079] X.sub.B=biomass concentration at the end of the batch phase,
g DCW/L, [0080] V.sub.B=initial liquid volume of culture, L, [0081]
S.sub.f=limiting substrate concentration in nutrient feed medium,
g/L, [0082] Y.sub.X/S=yield coefficient of biomass from substrate,
g/g, [0083] t=time since beginning of fed-batch phase.
[0084] Typically, fed-batch fermentations in NTC3019 media with
several independent kanamycin resistant pBR322-derived plasmids
reach a cell density of 100-120 OD.sub.600, or 55-65 g dry cell
weight per liter (FIG. 1). Plasmid yields average 260 mg/L and have
been as high as 430 mg/L. By comparison, published fermentation
yields with pBR322-derived plasmids are on the order of 3-4 mg/L
(Lahijani et al., Supra, 1996).
[0085] Importantly, the specific plasmid yields are very high,
typically between 2.5 and 3.8 mg/L/OD.sub.600, well exceeding
levels observed with other fermentation media/processes using much
higher copy pUC origin plasmids (Table 3). Expressing plasmid
yields in terms of specific yields mg/L/OD.sub.600 indicates the
amount of plasmid relative to the total cell mass. High specific
yields are very desirable since increased plasmid yield per gram of
bacteria leads directly to higher final product purities.
TABLE-US-00003 TABLE 3 Comparison of specific plasmid yields with
published high yield fermentation processes Specific plasmid yield,
Fermentation process mg/L/OD.sub.600 Friehs et al., Supra, 2003
(fed-batch) 1.3-2.1 Lahijani et al., Supra, 1996 (fed-batch) 2.8
NTC3019 pBR322-derived origin fed-batch 2.5-3.8 (Example 2) NTC3018
pUC origin batch (Example 3) 2.9-5.3 NTC3019 pUC origin fed-batch
(Example 4) 2.7 NTC3019 pUC origin inducible fed-batch 6.5-11
(Example 5)
[0086] This demonstrates that NTC3019 fermentation media
dramatically boosts the fermentation yields of moderate-copy number
plasmids (e.g. pBR322 with rop deletion) relative to media and
processes described in the art. This effect is not plasmid
specific.
[0087] The DNA purified from these processes is of a high quality,
being essentially 100% super-coiled with no detectable deletion or
other rearrangement. As well, DNA purifications at the 1 gram scale
have been performed utilizing the cells from this process. This
demonstrates fermentations performed in NTC3019 fed-batch media are
amenable to large scale downstream processing.
Example 3
NTC3018 Medium Batch Fermentation with High-Copy Gene Therapy
Plasmid
[0088] NTC3018 medium batch culture with pUC origin plasmids was
performed. The following pUC origin containing plasmids were
utilized:
1) pW2.0, a derivative of pUC19 that has an altered polylinker
sequence. 2) pMaxGFP 3) pEGFP-C1
[0089] Batch fermentations were carried out in a New Brunswick
BioFlo 110 fermentor at 37.degree. C. pH was controlled by
automatic addition of 30% ammonium hydroxide or 10% phosphoric
acid. The dissolved oxygen probe was calibrated to 0% by nitrogen
gas sparging and 100% with air saturation. The vessel was aerated
at 1 VVM and dissolved oxygen was maintained at 30% by
proportional-integral control of agitation. At cell densities above
about 20 OD.sub.600, O.sub.2 supplementation was also required to
maintain 30% saturation.
[0090] Seed cultures were started from single isolated colonies
inoculated into LB plus 50 .mu.g/ml kanamycin or 100 .mu.g/ml
ampicillin and grown at 37.degree. C. At mid-exponential phase
(0.5-1.5 OD.sub.600) the seed cultures were used to provide 1%
inoculums for the fermentor.
[0091] All fermentations were performed at 37.degree. C. For pW2.0,
plasmid copy number was induced by growth at 42.degree. C. late in
the fermentation. Batch fermentations with pUC plasmids reached
cell densities of only 16-57 OD.sub.600. However, specific plasmid
yield results are encouraging. Final yields for pEGFP-C1 were a
cell density of 56 OD.sub.600 and yielded 163 mg plasmid/L (2.9
mg/L/OD.sub.600), pMaxGFP a cell density of 16 OD.sub.600 and
yielded 84 mg plasmid/L (5.3 mg/L/OD.sub.600) and for pW2.0 a cell
density of 57 OD.sub.600 and yielded 230 mg plasmid/L (4.0
mg/L/OD.sub.600; FIG. 2).
[0092] The DNA purified from these processes is of a high quality,
being essentially 100% super-coiled with no detectable deletion or
other rearrangement. As well, DNA purifications at the 0.5 gram
scale have been performed utilizing the cells from this process.
This demonstrates fermentations performed in NTC3018 batch medium
are amenable to large scale downstream processing.
Example 4
NTC3019 Media Fed-Batch Fermentation with High-Copy Gene Therapy
Plasmids
[0093] The plasmid gWiz GFP (Gene Therapy Systems) which is a GFP
gene containing derivative of the Vical VR1012 vector was selected
for fed-batch fermentation evaluation. This is a widely used
kanamycin resistance (kanR) pUC origin containing DNA vaccine
plasmid with a size of 5757 bp. The plasmid gWiz GFP (Gene Therapy
Systems) was transformed into E. coli DH5.alpha.. pMaxGFP was also
tested in fed-batch cultures; similar results were obtained for
both plasmids.
[0094] Two problems were encountered when using NTC3019 media for
producing these plasmids. The first problem was discovered when
growing gWiz GFP plasmid cultures at 37.degree. C., as was done
successfully with the pBR322-derived plasmids. With the pUC plasmid
cultures, cell growth stopped around 15 OD.sub.600. Fluorescence
microscopy showed extensive filamentation, indicating inhibition of
cell division.
[0095] This is lethal, since the filaments eventually lyse (Arends
S J R, Weiss, D S. 2004 J Bacteriol 186: 880-884). For example,
FIG. 3(A) shows fed-batch fermentation with the plasmid gWiz GFP.
Cell growth had slowed and appeared to be entering stationary phase
prematurely at 15 OD.sub.600. Plasmid yield analysis indicated an
elevated specific plasmid yield of 2.7 mg/L/OD.sub.600 as the cell
growth began to stop. pUC plasmids contain a temperature sensitive
point mutation that can exhibit a 30-40 fold increase in copy
number at 42.degree. C. when compared to 30.degree. C. (Lin-Chao et
al, 1992): The temperature was then reduced to 33.degree. C. in an
attempt to reduce the plasmid copy number and thus alleviate the
metabolic burden on the cells, after which the plasmid dropped to
1.6 mg/L/OD.sub.600 and cell growth resumed. Interestingly, the
specific plasmid yield gradually rose again and growth entered
stationary phase at about 60 OD.sub.600 instead of growing to
>100 OD.sub.600 as expected, even though feed nutrient was still
being added.
[0096] FIG. 3(B) shows cell filamentation that had occurred at
37.degree. C. After the temperature was reduced to 33.degree. C., a
sample of growing cells showed much less filamentation.
[0097] A possible explanation was that the cell population never
fully recovered from the filamentation and loss of viability when
begun at 37.degree. C. To test this, two subsequent fed-batch
fermentations with the same plasmid were carried out entirely at
33.degree. C. In both fermentations, the culture peaked at cell
densities <60 OD.sub.600.
[0098] Biomass and plasmid DNA yield data from these fermentations
indicate a reduction in specific growth rate and a sharp rise in
specific plasmid yield before inhibition of cell growth. The sudden
rise in plasmid content to such a high level was unexpected, and
places a metabolic burden on the cell population, which may be the
cause of the reduced growth rate. However, it has also been shown
that reductions in growth rate often lead to an increase in plasmid
copy number (Satyagal V N, Agrawal P. 1989 Biotechnol. Bioeng. 33:
1135-1144), (Seo J H, Bailey J E. 1985 Biotechnol. Bioeng. 27:
1668-1674). It is unclear whether the unexpected increased specific
plasmid yield is causing the reduced growth rate, vice versa, or
whether each is causing the other in a compounded manner.
Example 5
Inducible Fed-Batch Process for High Yield Production of High Copy
Plasmids with NTC3019 Media
[0099] Based on the results from the 33.degree. C. and 37.degree.
C. fermentations (Example 5), a strategy was designed to overcome
the unexpected plasmid increase observed in fed-batch mode with pUC
origin plasmids. The plasmid gWiz GFP in DH5.alpha. was utilized in
an inducible fed-batch process. NTC3019 fed-batch fermentation was
performed as outlined in Example 5, except the culture was grown at
30.degree. C. until 60 OD.sub.600, at which time the temperature
was shifted to 37.degree. C. The surprising results are shown in
FIG. 4A. Growth at 30.degree. C. through 60 OD.sub.600 eliminated
the growth arrest problem, and the culture ultimately exceeded 100
OD.sub.600 with a total plasmid yield of 670 mg/L. The DNA purified
from samples from this process is of a high quality, being
essentially 100% super-coiled with no detectable deletion or other
rearrangement.
[0100] Plasmid yields prior to the temperature shift remained low
throughout the growth phase, remaining below 2 mg/L/OD.sub.600.
This is in contrast to the results from 33.degree. C. or 37.degree.
C. fermentations. Remarkably, the specific plasmid yields after
temperature shift are very high, up to 6.5 mg/L/OD.sub.600, well
exceeding levels observed with other fermentation media/processes
(Table 3). Fermentation at 30.degree. C. through the growth phase,
and shifting to 42.degree. C. resulted in productivity yields of
1.1 gm/L (11 mg/L/OD.sub.600) with gWiz GFP (FIG. 4B). Productivity
plateau is not associated with extensive cell death, as the
majority of the cells remain viable.
[0101] Modification of the NTC3019 media (four fold increase in
glycerol, yeast extract, and magnesium in the batched media) to
reduce the duration of the fed-batch phase (by extending the batch
phase to higher OD.sub.600) also produced similarly high plasmid
yields after induction at 42.degree. C., demonstrating that the
fed-batch phase can be started at higher OD.sub.600 without loss of
plasmid induction.
[0102] Multiple different plasmids with various pUC origin
backbones, including different antibiotic resistance genes and
orientations of prokaryotic elements, have been produced in yields
greater than 0.5 gm/L in NTC3019 media, using the 30.degree. C. to
42.degree. C. inducible process in DH5.alpha.. These results
demonstrate that the inducible process is not specific to a
particular plasmid.
[0103] The gWiz-GFP plasmid was also produced in yields greater
than 500 mg/L in NTC3019 media, using the 30.degree. C. to
42.degree. C. inducible process, in the DH1 cell line. This result
demonstrates that the inducible process is not specific to a
particular E. coli strain.
[0104] As well, DNA purifications at the 1 gram scale have been
performed utilizing the cells from this process. This demonstrates
inducible fermentations performed in NTC3019 fed-batch media are
amenable to large scale downstream processing.
[0105] Expressing plasmid yields in terms of specific yields
(mg/L/OD.sub.600) indicates the amount of plasmid relative to the
total cell mass. The inducible fed-batch process described herein
maintained low (<2 mg/L/OD.sub.600) plasmid levels throughout
the growth phase of the process, and facilitated unprecedented
ultra high plasmid production (6-11 mg/L/OD.sub.600) after biomass
production. High specific yields are very desirable since increased
plasmid yield per gram of bacteria leads directly to higher final
product purities.
[0106] These results demonstrate the general utility of the
fed-batch and batch fermentation processes of the invention to
improve plasmid DNA productivity and quality.
[0107] Thus, the reader will see that the production processes of
the invention provide methods for improved plasmid production.
[0108] While the above description contains many specificities,
these should not be construed as limitations on the invention, but
rather as an exemplification of one preferred embodiment thereof.
Many other variations are possible. For example, the inducible
fed-batch process can be integrated with the batch process, such
that fermentation is done in the NTC3018 batch media until nutrient
depletion, whereupon the fed-batch media from NTC3019 and induction
are simultaneously initiated. In this embodiment, with some
plasmids, the growth phase can be performed at up to 37.degree. C.
since plasmid copy number will be reduced with the higher growth
rate. The optimal temperature to allow cell division during the
growth phase, and retain plasmid inducibility during the fed-batch
phase, can be determined by one skilled in the art. Accordingly,
the scope of the invention should be determined not by the
embodiments illustrated, but by the appended claims and their legal
equivalents.
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