GB2552853A - Process of manufacture - Google Patents

Abstract

The invention claims a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions. Compositions comprising the purified AnxA5 and its medical uses are claimed.

Description

(71) Applicant(s):

Annexin Pharmaceuticals AB Box 56, Veberod SE 247 26, Sweden (72) Inventor(s):

Toomas Moks Jan Christoph Reich (74) Agent and/or Address for Service:

Potter Clarkson LLP

The Belgrave Centre, Talbot Street, NOTTINGHAM, NG1 5GG, United Kingdom (51) INT CL:

C07K 1/14 (2006.01) A61K 38/17 (2006.01)

C07K 14/47 (2006.01) (56) Documents Cited:

EP 0363176 A WO 2011/135071 A

WO 2005/099744 A

Preparative biochemistry & biotechnology, Vol 30, 2000, LN Zhang et al, Expression and purification of recombinant human annexin V in Escherichia coli, 305-312

BMC Biotechnology, Vol 14, 2014, LA Marder et al, Production of recombinant human annexin V by fedbatch cultivation, 33

Biochem. J., Vol 308,1995, PJ Trotter et al, Ca2+ concentration during binding determines the manner in which annexin V binds to membranes, 591-8 (58) Field of Search:

INT CL C07K

Other: ONLINE: EPODOC, WPI (54) Title of the Invention: Process of manufacture

Abstract Title: Purification of Annexin A5 from a composition that includes a calcium ion chelator (57) The invention claims a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions.

Compositions comprising the purified AnxA5 and its medical uses are claimed.

Fig 2

Cell disruption (High pressure homogenizer)
4
Clarification (Depth filtration)
4
Capture AX Chromatography (Q Sepharose XL)
4
Intermediate AF Chromatography (Heparin HyperD)
4
Polishing AX Chromatography (Source15 Q)
4
Ultra/Diafiltration (10 kDa)
4

Filtration / Filling

Fig 1

Met Ala Gin Val Leu

5

Glu Arg Ala Asp Ala 20

Thr Asp Glu Glu Ser 35

Gin Arg Gin Glu lie 50

Leu Leu Asp Asp Leu 65

He Val Ala Leu Met

Lys His Ala Leu Lys 100 lie He Ala Ser Arg 115

Tyr Glu Glu Glu Tyr 130

Thr Ser Gly Tyr Tyr 145

Arg Asp Pro Asp Ala 165

Gin Ala Leu Phe Gin

180

Lys Phe He Thr lie 195

Val Phe Asp Lys Tyr 210

Gin Arg Met Leu Val Val 150 155

Gly He Asp Glu Ala Gin 170

Ala Gly Glu Leu Lys Trp 185

Phe Gly Thr Arg Ser Val 200

Met Thr He Ser Gly Phe 215

Arg Gly Thr Val Thr Asp 10

Glu Thr Leu Arg Lys Ala 25

He Leu Thr Leu Leu Thr 40

Ser Ala Ala Phe Lys Thr 55

Lys Ser Glu Leu Thr Gly 70 75

Lys Pro Ser Arg Leu Tyr 90

Gly Ala Gly Thr Asn Glu 105

Thr Pro Glu Glu Leu Arg 120

Gly Ser Ser Leu Glu Asp 135

Phe Pro Gly Phe Asp 15

Met Lys Gly Leu Gly 30

Ser Arg Ser Asn Ala 45

Leu Phe Gly Arg Asp 60

Lys Phe Glu Lys Leu 80

Asp Ala Tyr Glu Leu 95

Lys Val Leu Thr Glu 110

Ala He Lys Gin Val 125

Asp Val Val Gly Asp 140

Leu Leu Gin Ala Asn

160

Val Glu Gin Asp Ala 175

Gly Thr Asp Glu Glu 190

Ser His Leu Arg Lys 205

Gin He Glu Glu Thr

220

1/8 lie Asp Arg Glu Thr Ser Gly Asn leu Glu Gin Leu Leu Leu Ala Val

225

Val Lys Ser He Arg 245

Tyr Ala Met Lys Gly 260

Met Val Ser Arg Ser 275

Arg Lys Asn Phe Ala 290

Ser Gly Asp Tyr Lys 305

230 235

Ser lie Pro Ala Tyr Leu 250

Ala Gly Thr Asp Asp His 265

Glu He Asp Leu Phe Asn 280

Thr Ser Leu Tyr Ser Met 295

Lys Ala Leu Leu Leu Leu 310 315

240

Ala Glu Thr Leu Tyr 255

Thr Leu He Arg Val 270 lie Arg Lys Glu Phe 285 lie Lys Gly Asp Thr 300

Cys Gly Glu Asp Asp 320

2/8

Fig 2

Cell disruption (High pressure homogenizer)

I

Clarification (Depth filtration)

4

Capture AX Chromatography (Q Sepharose XL)

I

Intermediate AF Chromatography (Heparin HyperD)

4

Polishing AX Chromatography (Source15 Q)

4

Ultra/Diafiltration (10 kDa)

4

Filtration / Filling

3/8

Fig 3

AX

▼

EQ

▼

Load

▼

Wash

▼

Step Elution

▼

Pooling

▼

CIP

▼

Storage

Process

Step

Parameter	3 L process	100 L process
Resin:	G Sepharose XL	Q Sepharose XL
Column:	XK 50	BPG 300
Column diameter (cm):	5	30
Bed height (cm):	13.5	13.5
Column volume (L):	0.265	9.5
Flow rate:	200 cm/h	170 cm/h
Buffer temperature: Pump:	Ambient temperature with WATSON-MARLOW Tubing pump 323S	Ambient temperature Bio Process system
Buffer A: Vol:	20 mM Tris pH 7.4, 0.1 % Tween80, 25 mM NaCI 2CV	20 mM Tris pH 7.4, 0.1 % Tween80, 25 mM NaCI 3CV

Online dilution (1 +1) with 1 % (v/v) Tween 80, 4 mM EDTA, pH 8.0

Buffer:	20 mMTris pH 7.4, 0.1 % Tween80, 25 mM NaCI	20 mMTris pH 7.4, 0.1 % Tween80, 25 mM NaCI
Vol:	10 CV	10 CV
100 % Buffer B:	20 mM Tris pH 7.4, 0.1 % Tween80, 300 mM NaCI	20 mM Tris pH 7.4, 0.1 % Tween80, 300 mM NaCI
Vol:	9CV	9CV
Criteria:	Main peak Pool (0.1 AU-0.2 AU)	Main peak Pool (target 0.2 AU-0.4 AU 5 mm light path) (within 3 weeks)
Step 1:	2 M NaCI	2 M NaCI
Vol:	3CV	3CV
Step 2:	1 M NaOH	1 M NaOH
Vol:	3CV	3CV
Incubation:	15 h	15 h
Storage:	20 mM NaOH	10 mM NaOH

4/8

Fig 4

Process Step

Parameter

3 L Process

AF	> Resin:	Heparin HyperD
	Column:	XK 50
	Column diameter (cm):	5
	Bed height (cm):	25
	Column volume (L):	0.491
	Flow rate:	60-100 cm/h
	Buffer temperature:	Ambient temperature
▼
EQ	Buffer A:	20 mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCb, 25 mM NaCI
▼	Vol:	2CV
Load	Flow rate:	100 cm/h
▼
Wash 1	Buffer: Vol:	20 mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCb, 25 mM NaCI 15 CV
	Flow rate:	100 cm/h
▼
Wash 2	Buffer:	20 mM Tris pH 7.4; 0.1 % Tween80, 25 mM NaCI
	Vol:	2 CV
▼	Flow rate:	100 cm/h
Step Elution	100% Buffer B:	20 mMTris pH 7.4; 0.1 % Tween80; 10 mM EDTA; 25 mM NaCI
	Vol:	2-3 CV
	Flow rate:	40-60 cm/h
▼
Pooling	Criteria:	Complete peak Pool (0.1 AU-0.1 AU)
▼
CIP	Step 1: Vol:	2 M NaCI 3CV
▼	Step 2: Vol: Incubation:	0.1 M NaOH 3CV 15 h
Storage	Storage:	1 M NaCI, 25% EtOH

100 L Process

Heparin HyperD

BPG300

17.7

60-100 cm/h Ambient temperature mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCh, 25 mM NaCI

3CV

60-100 cm/h; online 1:8 dilution of AX eluate with buffer A mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCl2, 25 mM NaCI

CV

60-100 cm/h mM Tris pH 7.4; 0.1 % Tween80, 25 mM NaCI 2 CV

60-100 cm/h mM Tris pH 7.4; 0.1 % Tween80; 10 mM EDTA; 25 mM NaCI

2-3 CV

40-60 cm/h

Complete peak

Pool (0.2 AU-0.2 AU ; 5 mm light path) (within 3 weeks)

M NaCI

3CV

0.1 M NaOH 3CV >15 h (contact time, no pumping)

M NaCI, 25% EtOH

5/8

Fig 5

AX

▼

EQ

▼

Load

▼

Wash

▼

Gradient Elution

▼

Pooling

▼

CIP

▼

Storage

Process

Step

Parameter	3 L process	100 L process
Resin:	Source15 Q	Source15 Q
Column:	-	Fineline200
Column diameter (cm):	-	20
Bed height (cm):	15	15
Column volume (L):	0.4	4.7
Flow rate:	100 cm/h	100 cm/h
Buffer temperature:	Ambient temperature	Ambient temperature
Buffer A:	20 mM Bis-Tris pH 7; 25 mM NaCI	20 mM Bis-Tris pH 7; 25 mM NaCI
Vol:	2CV	3CV
Flow rate:	100 cm/h	100 cm/h AF pool splitting (1/4-1/5)
Buffer:	20 mM Bis-Tris pH 7; 25 mM NaCI	20 mM Bis-Tris pH 7; 25 mM NaCI
Vol:	3CV	3CV
Flow rate:	100 cm/h	100 cm/h
Buffer B:	20 mM Bis-Tris pH 7; 180	20 mM Bis-Tris pH 7; 180
Gradient:	mM NaCI 0-100% B in 33 CV	mM NaCI 0-100% B in 33 CV
Criteria:	major peak starting at 0.05 AU to the valley between peak 1 and peak 2	major peak starting at 0.1 AU to the valley between peak 1 and peak 2 (5 mm light path) (within 3 weeks)
Step 1:	2 M NaCI	2 M NaCI
Vol:	3CV	3CV
Step 2:	1 M NaOH	1 M NaOH
Vol:	3CV	3CV
Incubation:	15 h	^15 h (contact time, no pumping)
Storage:	25 mM NaOH	10 mM NaOH

6/8

Fig 6

Process

Step

Parameter

L process

100 L process

Concentration cassette:

area:

Target concentration: Processing time: Parameter:

Concentration factor

Hydrosart 10 K 0.1 m² 5g/L ~2h

TMP 0.9-1.1 Entrance pressure 1 bar Retentate back pressure 0.8 bar

Hydrosart 10 K 2.4 m² 5 g/L

TMP 0.9-1.1

Entrance pressure 1 bar Retentate back pressure 0.8 bar

6-8

Buffer change

Dilution buffer:

Diafiitration volumes: Concentration factor Target concentration: Dilution mM Bis-Tris, 150 mM NaCI, 1mM CaCb pH 7 10 g/L

Addition of cassette wash mM Bis-Tris, 150 mM NaCI, 1mMCaCI₂ pH 7 10 g/L

Addition of cassette wash ▼

Addition of Tween80 ▼

Sterile filtration ▼

Storage of bulk

Buffer:

Target concentration Tween80:

Target concentration bulk:

Device:

Cut off:

Target concentration bulk:

Temperature:

mM Bis-Tris, 150 mM NaCI, 1mMCaCI2, 10% Tween80 pH 7 0.05 % g/L

Sartopore2 0.45-0.2 pm 10 g/L

2-8° C mM Bis-Tris, 150 mM NaCI, 1mM CaCI2,10% Tween80 pH 7 0.05 % g/L

Sartopore2

0.45-0.2 pm 10 g/L

2-8°C

7/8

Fig 7

A.

8/8

PROCESS OF MANUFACTURE

FIELD OF THE INVENTION

The present application relates to processes for the manufacture of protein comprising the sequence of Annexin A5 (AnxA5). More particularly, the process is for the recovery and/or purification of the AnxA5 protein, especially from a recombinant host cell, such as bacterial host cell. The processes described herein are highly efficient and cost effective, and can be used on a commercial scale (e.g. with recombinant host cell cultures having a culture volume of about 1000L or more) to rapidly and conveniently produce pharmaceutical grade AnxA5 protein product.

BACKGROUND OF THE INVENTION

The listing or discussion of an apparently prior-published document in this specification should not necessarily be taken as an acknowledgement that the document is part of the state of the art or is common general knowledge.

Atherothrombosis, formed on an underlying atherosclerotic plaque, is the key pathogenic mechanism behind the majority of clinically evident cardiovascular ischemic diseases including acute coronary artery disease, cerebrovascular and peripheral arterial occlusion. As discussed in Cederholm and Frostegard, 2007, Drug News Perspect., 20(5): 321-6, Annexin A5 (previously known as annexin V), a member of the annexin superfamily, is a protein with potent and unique antithrombotic properties. The antithrombotic effect exerted by Annexin A5 is thought to be mediated mainly by mechanical shielding of phospholipids, phosphatidylserine in particular, thereby reducing their availability for coagulation reactions. However, other intriguing properties of Annexin A5 potentially contributing to its antithrombotic function, especially downregulation of surface expressed tissue factor, or interaction with additional ligands involved in hemostasis such as sulfatide and heparin, as well as upregulation of urokinase-type plasminogen activator were reported. The biological significance of Annexin A5 as a member of endogenous antithrombotic system in vivo has also been suggested for the large vasculature and for placental microcirculation.

Indeed, it is known that Annexin A5 has a wide range of utilities in medicine, in providing direct therapeutic effects. Examples include the use of Annexin A5:

for prevention of atherothrombosis and/or plaque rupture as described in WO 2005/099744 (the contents of which are incorporated herein by reference);

for the treatment of vascular dysfunction, reducing ischemic pain and/or treatment of a vascular disease rupture as described in WO 2009/077764 (the contents of which are incorporated herein by reference);

for the prophylaxis or treatment of restenosis as described in WO 2009/103977 (the contents of which are incorporated herein by reference);

for use in inhibiting the activity of oxidised cardiolipin (oxCL) and for treating, preventing and/or reducing the risk of developing a cardiovascular disease, an autoimmune disease or inflammatory condition as described in WO 2010/069605 (the contents of which are incorporated herein by reference); and for the prevention and/or reduction of peri- or postoperative complications following surgical intervention, such as complications following vascular surgery, especially peripheral vascular surgery as described in WO 2012/136819 (the contents of which are incorporated herein by reference).

As such, Annexin A5 represents a protein of high therapeutic interest and potential. Therefore, there is a pressing need for an effective method to produce therapeutic grade Annexin A5 protein by an efficient and cost-effective process that can be scaled up and conveniently applied to commercial scale production (e.g. to collect Annexin A5 protein from recombinant host cell cultures having a culture volume of about WOOL or more).

A particular challenge, when recombinantly expressing Annexin A5 in standard bacterial host cells such as E. coli, is contamination with host cell derived components, and in particular with endotoxin. Endotoxin is a lipopolysaccharide (LPS), which is formed of a lipid and a polysaccharide composed of O-antigen, outer core and inner core joined by a covalent bond; LPS is found in the outer membrane of Gram-negative bacteria, and elicit strong immune responses in animals. Annexin A5 is characterised by its strong binding to biological membranes containing negatively charged phospholipids, and so has a particularly high affinity to endotoxin. This makes large, commercial scale, production of Annexin A5 from endotoxin-producing hosts even more challenging.

To date, no such process has been provided to produce therapeutic grade Annexin A5 protein by an efficient and cost-effective process that can be scaled up and conveniently applied to commercial scale production (e.g. to collect Annexin A5 protein from recombinant host cell cultures having a culture volume of about WOOL or more) at all, much less in a way that addresses endotoxin contamination.

In 1991, Kumar reported on the development of a process for the production and purification of Annexin A5 (An Undergraduate Honors College Thesis entitled “Expression, Purification, and Large-Scale Production ofthe Human Recombinant Annexin-V Protein as presented to Department of Chemical Engineering College of Engineering University of Arkansas , Fayetteville, AR, available online at https://uarkive.uark.edu/xmlui/handle/ 10826/981). Kumar’s process involved the expression of the Annexin A5 in recombinant E. coli host cells in 100 mL culture flasks, pelleting the cells, resuspending the cells in presence of a homogenisation/lysis buffer consisting of 50 mM Tris HCI, 10 mM CaCb at pH 7.2, and then breaking the cells via sonication to release the Annexin A5 protein. The added CaCb caused the Annexin A5 to bind, in a calcium-dependent manner, to the cell membranes in the debris, and then the mixture was subjected to a first purification centrifugation step of 20 minutes, after which the supernatant was discarded and the pellet containing the cell debris and the bound Annexin A5 was recovered. Annexin A5 was released from the pellet using EDTA, and this was followed by a second purification centrifugation step of 20 minutes and collection ofthe Annexin A5 in the supernatant. Then followed an overnight dialysis to change the buffer for Annexin A5 to Tris HCI at pH 8.0, before the further step of anion exchange on a DEAE-sepharose column, and elution of Annexin A5 using a salt gradient.

The present applicant has realised that there are numerous limitations and shortcomings in the method of Kumar. First, it is only demonstrated on a small scale, using 100 mL cultures, and requires two separate centrifugation steps during the purification process. This is not scalable to commercial processes that use high volume cultures (e.g. WOOL or greater) in an efficient way. As discussed further below, the centrifugation of such high volumes of fluid would be extremely time-consuming and costly. Yet, centrifugation is necessitated by Kumar’s approach which relies on using calcium-induced binding of Annexin A5 to the membranes in cell debris as a preliminary capture step. Second, the applicant has realised that the method of Kumar leads to high losses of Annexin A5 protein, for example, by disposing of soluble Annexin A5 that is unbound in the supernatant ofthe product of the first purification centrifugation step. Third, the method of Kumar is completely unable to remove endotoxin to a level suitable for a therapeutic use, and it is notable that there are no checks on endotoxin levels in the final product. As such, Kumar’s method is not scalable to commercial production in an efficient and time-effective manner, 3 leads to high losses of Annexin A5 protein (i.e. low yields) and results in a low grade of protein purification that is not suitable for therapeutic use.

In 2008, the Department of Laboratory Medicine at University of Washington Medical Center, Tait Research Laboratory published a document entitled “Production of Recombinant Annexin V from plasmid pET12a-PAPI”. It is available online at: https://depts.washington.edu/labweb/Faculty/Tait/108.pdf. The method described is highly similar to the methodology proposed by Kumar. The method expresses Annexin A5 in recombinant E. coli host cells in 1 L cultures, pelleting the cells, resuspending the cells in presence of a homogenisation/lysis buffer consisting of 50 mM Tris HCI, 10 mM CaCL at pH 7.2, and then breaking the cells via sonication to release the Annexin A5 protein. The added CaCL causes the Annexin A5 to bind, in a calcium-dependent manner, to the cell membranes in the debris, and then the mixture is subjected to a first purification centrifugation step of 20 minutes, after which the supernatant was discarded and the pellet containing the cell debris and the bound Annexin A5 was recovered. Annexin A5 was released from the pellet using EDTA, and followed by a second purification centrifugation step of 20 minutes and collection of the Annexin A5 in the supernatant. Then followed a dialysis step to change the buffer for Annexin A5 to Tris HCI at pH 8.0, before the further step of anion exchange on a Mono Q column, and elution of Annexin A5 using a salt gradient. The present applicant has realised that the numerous limitations and shortcomings in the method of Kumar also applies to this method.

In 2014, a further method for the purification of Annexin A5 was proposed in Marder et al., 2014, BMC Biotechnology, 14:33 entitled “Production of recombinant human annexin V by fed-batch cultivation”. Marder et al., reports that its method is a fed-batch method to produce recombinant human annexin V in large scale, and it is proposed that this method may expand the commercial utilities for recombinant human Annexin A5 to applications such as in vivo imaging studies.

Yet again, the method of Marder et al, is highly similar to the 1991 method of Kumar and the 2008 method of the Department of Laboratory Medicine at University of Washington Medical Center. Marder et al expresses Annexin A5 in recombinant E. coli host cells in 1 L cultures, held in 2 L tanks. As discussed (in the Purification section of the Methods of Marder ef al), the collected cells were resuspended in presence of a homogenisation/lysis buffer (buffer A) consisting of 50 mM Tris HCI, 10 mM CaCL at pH 7.2, and then the cells were broken via sonication to release the Annexin A5 protein. The added CaCb causes 4 the Annexin A5 to bind, in a calcium-dependent manner, to the cell membranes in the debris, and then the mixture is subjected to a first purification centrifugation step of 30 minutes, after which the supernatant was discarded and the pellet containing the cell debris and the bound Annexin A5 was recovered. Annexin A5 was released from the pellet using EDTA, and followed by a second purification centrifugation step of 30 minutes and collection of the Annexin A5 in the supernatant. Then followed a dialysis step to change the buffer for Annexin A5 to Tris HCI at pH 8.0, before a third purification centrifugation step of 20 minutes to remove residual precipitate and then the further step of anion exchange on a Mono Q column, and elution of Annexin A5 using a salt gradient. Again, the present applicant has realised that the numerous limitations and shortcomings in the method of Kumar also applies to this method.

The 1997 method of Kumar, the 2008 method of the Department of Laboratory Medicine at University of Washington Medical Center, and the 2014 method of Marder et al, clearly show that the art had developed and established an approach to the production and purification of Annexin A5 products for commercial purposes, although the limitation and shortcomings of these methods were unappreciated in the art, with no readily available alternative.

All of these prior art methods for Annexin A5 recovery have been demonstrated only at a lab-scale process and are incapable of being adopted for scale-up or taking into account industry standards or equipment available at larger scale. The processes have inherent drawbacks making them unsuitable for large scale manufacturing. In particular, a highly limiting features of these prior art processes are the two or (in the case of 2014 method of Marder et al.) the three high G-force centrifugations that the processes require where the Annexin A5 is alternatively in solution or as precipitate. Applying just two centrifugation steps to the processing of one 1000 L batch can be reasonably estimated to result in a process that would take about 12 weeks with 12 hour daily shift in any well-equipped biomanufacturing facility, resulting in unacceptably high production costs. See Comparative Example 1.

Accordingly, it is an object of the present invention to provide methodological steps for the purification and recovery of Annexin A5 that are efficient and cost-effective for the a manufacturing process that is operated on a commercial scale (e.g. recombinant host cell cultures having a culture volume of about WOOL or more), and further to overcome the drawback of loss of yield and low purity (including endotoxin contamination) suffered by the prior art processes.

It is also an object of the invention to provide pharmaceutical grade Annexin A5 products that are produced by methods of the present invention.

SUMMARY OF THE INVENTION

The applicant has made numerous developments and improvements to a process for the production of a protein comprising the sequence of Annexin A5 (AnxA5), and has devised several highly efficient purification steps, which may be used independently and/or used in combination to improve existing processes. Most preferably, the process for production of Annexin A5 contains all of the developed process steps.

In particular, the applicant’s developments provide the possibility of a highly efficient process for the recovery of the AnxA5 protein thorough a method in which the AnxA5 protein preferably remains in solution throughout the process (except when temporarily bound to chromatographic resins). That is to say, the applicant’s developments provide a process for the recovery of the AnxA5 protein that can be performed preferably without the requirement to apply any purification centrifugation steps to AnxA5 protein following the release of the AnxA5 protein from a host cell. Further, this means that the processes of the present invention can all be performed without relying on the ability of Annexin A5 to bind to membranes (e.g. host cells membranes and/or liposomes) which can often cause the Annexin A5 to co-purify with undesirable contaminants such as endotoxin.

Accordingly, the process can be applied to the processing of high volume (e.g. about 100L, 500L, 1,000L, 5,000L, 10.000L, 50,000L, 100.000L or higher) cultures of host cells in a highly time-efficient way without the bottleneck caused by one or more purification centrifugation steps. For example, it may be preferred that the purification process is conducted in, or in less than, 5, 4, 3, 2 weeks and most typically less than 1 weeks per 1.000L of host cell culture processed. Yet further, the process can be used, surprisingly, to provide improved yield and/or improved purity (including, for example, improved endotoxin removal) compared to the slower, less efficient, prior art processes.

Accordingly, a first aspect of the present invention provides an improved step of protein release from a host cell. More specifically, it provides a process for the recovery and/or 6 purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from an endotoxin-producing host cell with a cell wall, wherein the process comprises releasing the intracellular protein from the host cell, characterised in that the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising non-ionic detergent. Preferably, the non-ionic detergent is a polysorbate, more preferably a polysorbate selected from Tween20 and Tween80, and most preferably Tween80.

The applicant has also discovered (as discussed further in Example 2, below), contrary to conventional methods in which the successive addition of purification steps leads to an ever increasing loss of yield (as product is lost at each step), that the combination of an anion exchange step and a heparin affinity chromatography step has a surprising benefit of attaining the high purity achieved by the heparin affinity chromatography step alone, but with substantially increased yield (i.e. the recovery is increased from about 30-40% to about 70-90%). This is the direct opposite of what would normally be expected from the combination of purification steps.

Accordingly, a second aspect the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein; and subjecting the first anion exchange product, directly or indirectly, to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

Preferably, in accordance with the process of the second aspect of the present invention, the affinity chromatography step may comprise the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions and further optionally, the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

Additionally, as discussed in Example 3, the applicant has discovered that Tween80 has a particularly advantageous effect (compared to other non-ionic detergents, including other 7

Tweens, such as Tween20) on a heparin affinity chromatography step. The inclusion of Tween 80, for example at around 0.1% (w/v) in the buffers used in the heparin affinity chromatography step can assist in eluting the AnxA5 protein in a single peak, reduce pressure, and prevent precipitation.

Accordingly, a third aspect the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities (which may, or may not be the direct or indirect product of a first anion exchange chromatography capture step, as discussed herein) to a heparin affinity chromatography step in the presence of Tween80 (preferably in the presence of about 0.1% w/vTween80), thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

A fourth aspect of the present invention is based on the applicant’s realisation that calcium metal ion chelators (e.g. EDTA) can impact negatively on the efficacy of anion exchange steps. Free EDTA (or other chelator) can bind directly to the anion exchange functional groups, and thereby reduce the capacity and also the separation achieved by an anion exchange step. On the other hand, it is time consuming and therefore also increases costs, to attempt to remove calcium metal ion chelator before an anion exchange step. Therefore, prior art methods involving slow dialysis steps for buffer replacement are inefficient. Further, in the inclusion of the calcium metal ion chelator in the AnxA5 product during the anion exchange step can be an important component to prevent calciummediated binding of the AnxA5 protein to impurities, including endotoxin. It would therefore be convenient and efficacious to introduce an additive that blocks or reduces the binding of the calcium ion chelator to the anion exchange resin, which would allow the anion exchange step to be performed without inconvenience and cost associated with dialysis, and without preventing the beneficial effect of the calcium metal ion chelator during the anion exchange step.

The applicant has realised that this can be achieved by the inclusion in the AnxA5 protein product, prior to anion exchange, or one or more types of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions. The 8 selection of the appropriate additional metal ions will depend on the nature of the calcium ion chelator and the nature of the anion exchange resin. For example, in the case of using EDTA as a calcium ion chelator, Mg²⁺ ions are generally suitable to achieve the object of the present invention, and can be added to the AnxA5 protein product prior to an anion exchange step.

Accordingly, a fourth aspect of the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions.

A fifth aspect of the present invention provides a composition comprising an AnxA5 protein, wherein the composition is the direct, or indirect product of (or is directly or indirectly obtainable by) a process according to any of the first, second, third or fourth aspects of the present invention. Optionally, the composition is a pharmaceutically acceptable and/or veterinarily acceptable composition.

The sixth aspect of the present invention also provides the composition of the fifth aspect of the present invention for use in medicine. To put it another way, the sixth aspect of the present invention provides a method comprising administering to a human or animal in need thereof a therapeutically effective amount of a composition of the fifth aspect of the present invention.

It is contemplated that any method or composition described herein can be implemented with respect to any other method or composition described herein.

The use of the word “a” or “an” when used in conjunction with the term “comprising” in the claims and/or the specification may mean “one,” but it is also consistent with the meaning of “one or more,” “at least one,” and “one or more than one.”

These, and further, aspects of the present invention will be better appreciated and understood when considered in conjunction with the following description and the accompanying drawings. It should be understood, however, that the following description, while indicating various aspects and embodiments of the invention and numerous specific details thereof, is given by way of illustration and not of limitation. Many substitutions, modifications, additions and/or rearrangements may be made within the scope of the invention without departing from the spirit thereof, and the invention includes all such substitutions, modifications, additions and/or rearrangements.

DESCRIPTION OF THE FIGURES

Figure 1 shows the sequence SEQ ID NO: 1, which is the sequence of human Annexin A5.

Figure 2 shows a schematic flow chart of the exemplified complete manufacturing process for Annexin A5.

Figure 3 provides a process flow chart for the exemplified AX capture chromatography.

Figure 4 shows the process flow chart for the exemplified Intermediate Affinity Chromatography.

Figure 5 shows the process flow chart for the exemplified AX Polishing Chromatography step.

Figure 6 shows the process flow chart for exemplified ultra/diafiltration and formulation of Annexin A5.

Figure 7 shows the results of Example 3, which demonstrates the impact of Tween80 on heparin affinity chromatography purification of Annexin A5, wherein Fig 7A shows the results for Test 1 (without Tween80), and Fig 7B shows the results for Test 2 (with Tween 80).

DETAILED DESCRIPTION OF THE INVENTION

A. Annexin A5 protein

The present invention relates to methods for the purification and/or recovery of a protein comprising the sequence of Annexin A5 (AnxA5), and products and formulations thus produced comprising the AnxA5 protein.

In accordance with one embodiment of the present invention, the AnxA5 protein that is purified and/or recovered may comprise, consist essentially of, or consist of, a protein having the sequence of human Annexin A5 (SEQ ID NO:1, as shown in Fig 1), either with or without the N-terminal methionine.

In another embodiment, the AnxA5 protein that is purified and/or recovered may comprise, consist essentially of, or consist of, a variant or mutant of a protein having the sequence of human Annexin A5 (SEQ ID NO:1, as shown in Fig 1), either with or without the Nterminal methionine. For example, the variant or mutant may differ from SEQ ID NO: 1 (either with, or without, the N-terminal methionine) at any one or more positions, such as at, or up to, 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20, 25, 30, 35, 40, 45, 50, 55, 60, 65, 70, 75, 80, 85, 90, 95, 100, 110, 120, 130, 140, 150, 160 or more positions.

Thus, a variant or mutant of Annexin A5 may be a protein wherein at one or more positions there have been amino acid insertions, deletions, or substitutions, either conservative or nonconservative. Preferably, the changes result in a protein whose basic properties to function in an equivalent manner to Annexin A5 have not significantly been changed. “Significantly” in this context means that one skilled in the art would say that the properties of the variant may still be different but would not be unobvious over the ones of the original protein.

Preferably the isoelectric point (pi) of the variant or mutant is not altered, compared to the unmodified protein, or is not modified by more than 1, 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2 or 0.1 pH units.

In a preferred embodiment, the AnxA5 protein is capable of binding to phosphatidylserine on a biological membrane, preferably to a level that is at least 10%, 20%, 30%, 40%, 50%, 60%, 70%, 80%, 90%, 95%, 99% or about 100% of that displayed by human Annexin A5 (SEQ ID NO:1) under the same conditions. A suitable method for measuring Annexin A5 binding to phosphatidylserine on a biological membrane is known in the art (Vermes et al. (1995) J Immunol Methods, 184(1): p. 39-51).

By “conservative substitutions” is intended combinations such as Gly, Ala; Val, lie, Leu; Asp, Glu; Asn, Gin; Ser, Thr; Lys, Arg; and Phe, Tyr.

Variants and mutants may be made using the methods of protein engineering and sitedirected mutagenesis which are well known in the art.

In a further embodiment, the AnxA5 protein that is purified and/or recovered may be a dimer of a protein that comprises, consists essentially of, or consists of, a protein having 12 the sequence of human Annexin A5 (SEQ ID NO:1, as shown in Fig 1), either with or without the N-terminal methionine, or a variant or mutant thereof as described above.

In a further embodiment, the AnxA5 protein that is purified and/or recovered may be a fusion protein, which fusion protein comprises, consists essentially of, or consists of: (a) one or more protein sequences comprising the sequence of fusion partner that is/are fused to; (b) one or more protein sequences that comprises, consists essentially of, or consists of, a protein having the sequence of human Annexin A5 (SEQ ID NO:1, as shown in Fig 1), either with or without the N-terminal methionine, or a variant or mutant thereof, or dimer as described above. For example, without limitation, the fusion protein may have a general structure selected from:

- in the case of the fusion of two amino acid sequences, for example: H₂N-(a)-(b)COOH; or H₂N-(b)-(a)-COOH; or

- in the case of the fusion of three amino acid sequences, for example: H₂N-(a)-(b)-(a)COOH; or H₂N-(b)-(a)-(b)-COOH; or H₂N-(a)-(b)-(b)-COOH; or H₂N-(b)-(b)-(a)COOH; or H₂N-(a)-(a)-(b)-COOH; or H₂N-(b)-(a)-(a)-COOH; or in the case of the fusion of four amino acid sequences, for example: H₂N-(a)-(a)-(a)(b)-COOH; or H₂N-(a)-(a)-(b)-(a)-COOH; or H₂N-(a)-(b)-(a)-(a)-COOH; or H₂N-(b)-(a)(a)-(a)-COOH; or H₂N-(a)-(a)-(b)-(b)-COOH; or H₂N-(a)-(b)-(a)-(b)-COOH; or H₂N-(b)(a) -(a)-(b)-COOH; or H₂N-(a)-(b)-(b)-(a)-COOH; or H₂N-(b)-(a)-(b)-(a)-COOH; or H₂N(b) -(b)-(a)-(a)-COOH; or H₂N-(b)-(b)-(b)-(a)-COOH; or H₂N-(b)-(b)-(a)-(b)-COOH; or H₂N-(b)-(a)-(b)-(b)-COOH; or H₂N-(a)-(b)-(b)-(b)-COOH; or

- in the case of the fusion of five amino acid sequences, for example: or H2N-(a)-(a)(a) -(a)-(b)-COOH; or H₂N-(a)-(a)-(a)-(b)-(a)-COOH; or H₂N-(a)-(a)-(b)-(a)-(a)-COOH; or H₂N-(a)-(b)-(a)-(a)-(a)-COOH; or H₂N-(b)-(a)-(a)-(a)-(a)-COOH; or H₂N-(a)-(a)-(a)(b) -(b)-COOH; or H₂N-(a)-(a)-(b)-(a)-(b)-COOH; or H₂N-(a)-(b)-(a)-(a)-(b)-COOH; or H₂N-(b)-(a)-(a)-(a)-(b)-COOH; or H₂N-(a)-(a)-(b)-(b)-(a)-COOH; or H₂N-(a)-(b)-(a)(b)-(a)-COOH; or H₂N-(b)-(a)-(a)-(b)-(a)-COOH; or H₂N-(a)-(b)-(b)-(a)-(a)-COOH; or H₂N-(b)-(a)-(b)-(a)-(a)-COOH; or H₂N-(b)-(b)-(a)-(a)-(a)-COOH; or H₂N-(a)-(a)-(b)(b)-(b)-COOH; or H₂N-(a)-(b)-(a)-(b)-(b)-COOH; or H₂N-(b)-(a)-(a)-(b)-(b)-COOH; or H₂N-(a)-(b)-(b)-(a)-(b)-COOH; or H₂N-(b)-(a)-(b)-(a)-(b)-COOH; or H₂N-(b)-(b)-(a)(a) -(b)-COOH; or H₂N-(a)-(b)-(b)-(b)-(a)-COOH; or H₂N-(b)-(a)-(b)-(b)-(a)-COOH; or H₂N-(b)-(b)-(b)-(a)-(a)-COOH; or H₂N-(a)-(b)-(b)-(b)-(b)-COOH; or H₂N-(b)-(a)-(b)(b) -(b)-COOH; or H₂N-(b)-(b)-(a)-(b)-(b)-COOH; or H₂N-(b)-(b)-(b)-(a)-(b)-COOH; or H₂N-(b)-(b)-(b)-(b)-(a)-COOH, wherein (a) and (b) are as defined above in this paragraph. In the case of multiple fusion partner proteins, as defined by (a), the multiple fusion partners may be same or different. Any fusion partner of interest may be used. For example the fusion partner polypeptide sequence(s) may be suitable to extend the half-life of the molecule within a patient’s circulatory system and/or add further functionality to the molecule, such as to add additional therapeutic properties (e.g. anti-coagulant, cell inhibition and/or killing, etc.). In the case of fusion proteins comprising multiple protein sequences having the sequence of human Annexin A5 (SEQ ID NO:1, as shown in Fig 1), either with or without the N-terminal methionine, or a variant or mutant thereof, or dimer as described above, as defined by (b), those proteins may be the same or different.

In accordance with a further embodiment of the present invention, the AnxA5 protein that is purified and/or recovered may be a protein that comprises, consists essentially of, or consists of, the sequence of Annexin A5 or functional variant or mutant thereof as selected from:

a) human Annexin A5 (SEQ ID NO:1), with or without the N-terminal methionine;

b) a mammalian orthologue of human Annexin A5;

c) an allelic or genetic variant of a) or b);

d) a protein which is more than 50%, 60%, 70%, 75%, such as more than 80%, 85%, more than 90%, or even more preferably more than 95% or 99% identical to any of a), b) or c);

e) a dimer of any of a), b), c) or d); or

f) a fusion protein comprising one or more fusion partners fused to any of a), b), c), d) or e).

In particular embodiments, the AnxA5 protein is a functional variant or mutant of Annexin A5 that is more than 50%, 60%, 70%, 75%, such as more than 80%, 85%, more than 90%, or even more preferably more than 95% or 99% identical to human Annexin A5, SEQ ID NO:1, with or without the N-terminal methionine.

The percent identity between two amino acid sequences is determined as follows. First, an amino acid sequence is compared to, for example, SEQ ID NO:1 using the BLAST 2 Sequences (BI2seq) program from the stand-alone version of BLASTZ containing BLASTN version 2.0.14 and BLASTP version 2.0.14. This stand-alone version of BLASTZ can be obtained from the U.S. government’s National Center for Biotechnology Information web site at ncbi.nlm.nih.gov. Instructions explaining how to use the BI2seq program can 14 be found in the readme file accompanying BLASTZ. BI2seq performs a comparison between two amino acid sequences using the BLASTP algorithm. To compare two amino acid sequences, the options of BI2seq are set as follows: -i is set to a file containing the first amino acid sequence to be compared (e.g., C:\seq1.txt); -j is set to a file containing the second amino acid sequence to be compared (e.g., C:\seq2.txt); -p is set to blastp; -o is set to any desired file name (e.g., C:\output.txt); and all other options are left at their default setting. For example, the following command can be used to generate an output file containing a comparison between two amino acid sequences: C:\BI2seq -i c:\seq1.txt -j c:\seq2.txt -p blastp -o c:\output.txt. If the two compared sequences share homology, then the designated output file will present those regions of homology as aligned sequences. If the two compared sequences do not share homology, then the designated output file will not present aligned sequences. Once aligned, the number of matches is determined by counting the number of positions where an identical nucleotide or amino acid residue is presented in both sequences.

The percent identity is determined by dividing the number of matches by the length of the sequence set forth in an identified sequence followed by multiplying the resulting value by 100. For example, if a sequence is compared to the sequence set forth in SEQ ID NO:1 (the length of the sequence set forth in SEQ ID NO:1 is 320) and the number of matches is 288, then the sequence has a percent identity of 90 (i.e., 288 4- 320 * 100 = 90) to the sequence set forth in SEQ ID NO:1.

The AnxA5 protein may be a dimer of Annexin A5 (such as DiAnnexin) or a functional variant or mutant thereof. DiAnnexinA5 is disclosed in WO 02/067857.

B. Host cell culture

The AnxA5 protein can be expressed recombinantly in a host cell culture. Preferred host cell cultures that express AnxA5 protein, according to the present invention, are cultures that are on a commercial scale for AnxA5 protein production, such as cultures having a culture volume of about 100L, about 200L, about 300L, about 400L, about 500L, about 600L, about 700L, about 800L, about 900L, about 1,000L, about 2,000L, about 3,000L, about 4,000L, about 5,000L, about 6,000L, about 7.0000L, about 8,0000L, about 9,OOOOL, about 10.000L, about 20.000L, about 30.000L, about 40.000L, about 50.000L, about 60.000L, about 70,0000L, about 80,0000L, about 90.0000L, about 100.000L or higher.

The term “about” in that context can include the meaning of ± 50%, 40%, 30%, 20%, 10%, 5%, 4%, 3%, 2% or 1% of the stated volume.

Methods for the recombinant expression of a gene of interest are well known in the art.

Typically, a nucleotide sequence encoding an AnxA5 protein will be expressed recombinantly in a host cell culture. For example, the sequence encoding the AnxA5 protein may be introduced into a host cell by transformation of the host cell with a plasmid or other vector comprising the sequence encoding the AnxA5 protein and optionally, the sequence encoding the AnxA5 protein will be integrated into the host cell chromosome (or plastome) or maintained on an replicable extrachromosomal vector.

Accordingly, a host cell can be transformed with a polynucleotide vector construct comprising a sequence encoding the AnxA5 protein.

The host cell can be either prokaryotic or eukaryotic.

Bacterial cells are preferred prokaryotic host cells in the context of the present invention. Bacterial host cells may, for example, be gram-positive or gram-negative host cells (although gram-neutral and gram-variable bacteria may also be used). Examples of gramnegative bacteria include, but are not limited to, Escherichia coli, Salmonella, Shigella, Pseudomonas, Neisseria, Haemophilus influenzae, Bordetella pertussis and Vibrio cholera.

At least in the context of the first aspect of the present invention, and optionally in the context of all aspects of the present invention, the host cell is an endotoxin-producing host cell with a cell wall, and thus is typically a gram-negative bacteria, such as E. coli, for example, the E. coli strains DH5 available from Bethesda Research Laboratories Inc., Bethesda, MD, USA, and RR1 available from the American Type Culture Collection (ATCC) of Rockville, MD, USA (No ATCC 31343).

A further particularly-preferred endotoxin-producing strain of E. coli includes strain BL21 (DE3) (e.g. as is widely commercially-available, and as described in Marder et al., 2014, BMC Biotechnology, 14:33). However, the applicant has found that Annexin A5 expressed from strain BL21 (DE3) surprisingly displays unexpectedly high levels of undesirable posttranslational gluconoylation, such that about 40% of the Annexin A5 protein was 16 gluconoylated. This is much higher than the level of gluconoylation for most other recombinantly-expressed proteins in BL21 (DE3), which typically show levels of about only 5-10% gluconoylation. It is therefore even more preferred that the endotoxin-producing strain of E. coli is a strain of BL21 (DE3) that is engineered reduce the level of gluconoylation of the AnxA5 protein, for example by overexpressing phosphogluconolactonase (PGL), as described in Aon et al. (Appl. Env. Microbiol., 2008, 74(4): 950-958; the contents of which are incorporated herein by reference) and thereby suppress the post-translational gluconoylation of recombinantly-expressed protein, and so suppressing the formation of gluconoylated variants of AnxA5 protein to level below 40%, such as below 30%, 20%, 10%, 9%. 8%, 7%, 6%, 5%, 4%, 3%, 2%, or 1%, and preferably substantially 0%.

Typically, the bacterial host cell for use in the present invention is a bacterial host cell with a wall, and therefore preferably excludes cells lacking a cell wall and (in the case of gramnegative bacteria) the outer membrane, such as a spheropiast (such as described in Liu et al, 2006, J. Exp. Microbiol., 9: 81-85; the contents of which are incorporated herein by reference). Spheroplasts, within the context of the present application, are not endotoxinproducing host cells, and do not have a cell wall. Spheroplasts are entirely unsuitable for commercial scale production, in particularly due to their sensitivity and fragility in the absence of a cell wall which seriously restricts their ability to be productively grown in large volume cultures.

Optionally, the host cell is an endotoxin-producing host cell with a cell wall that is incapable of being lysed by osmotic shock and/or freeze/thaw treatments.

In a further option, the host cell culture is a culture wherein the host cell is not, or has not been, cultured in the presence of an antibiotic to which it has no resistance, and optionally not in the presence of any antibiotic. Specific antibiotics to be avoided, in one embodiment, are antibiotics that result in the formation of spheroblasts, such as ampiciilin.

Eukaryotic host cells may include yeast and mammalian cells, preferably vertebrate cells such as those from a mouse, rat, monkey or human fibroblastic cell line. Yeast host cells include YPH499, YPH500 and YPH501 which are generally available from Stratagene Cloning Systems, La Jolla, CA 92037, USA. Preferred mammalian host cells include Chinese hamster ovary (CHO) cells available from the ATCC as CCL61, NIH Swiss mouse embryo cells N1H/3T3 available from the ATCC as CRL 1658, and monkey kidney-derived 17

COS-1 cells available from the ATCC as CRL 1650. Preferred insect cells are Sf9 cells which can be transfected with baculovirus expression vectors.

Typical prokaryotic vector plasmids are: pl)C18, pUC19, pBR322 and pBR329 available from Biorad Laboratories (Richmond, CA, USA); p7?c99A, pKK223-3, pKK233-3, pDR540 and pR!T5 available from Pharmacia (Piscataway, NJ, USA); pBS vectors, Phagescript vectors, Bluescript vectors, pNH8A, pNH16A, pNH18A, pNH46A available from Stratagene Cloning Systems (La Jolla, CA 92037, USA).

A typical mammalian cell vector plasmid is pSVL available from Pharmacia (Piscataway, NJ, USA). This vector uses the SV40 late promoter to drive expression of cloned genes, the highest level of expression being found in T antigen-producing cells, such as COS-1 cells. An example of an inducible mammalian expression vector is pMSG, also available from Pharmacia (Piscataway, NJ, USA). This vector uses the glucocorticoid-inducible promoter of the mouse mammary tumour virus long terminal repeat to drive expression of the cloned gene.

Useful yeast plasmid vectors are pRS403-406 and pRS413-416 and are generally available from Stratagene Cloning Systems (La Jolla, CA 92037, USA). Plasmids pRS403, pRS404, pRS405 and pRS406 are Yeast Integrating plasmids (Yips) and incorporate the yeast selectable markers HIS3, TRP1, LEU2 and URA3. Plasmids pRS413-416 are Yeast Centromere plasmids (YCps).

Methods well known to those skilled in the art can be used to construct expression vectors containing the AnxA5 protein coding sequence and, for example appropriate transcriptional or translational controls. One such method involves ligation via homopolymer tails. Homopolymer polydA (or polydC) tails are added to exposed 3’ OH groups on the DNA fragment to be cloned by terminal deoxynucleotidyl transferases. The fragment is then capable of annealing to the polydT (or polydG) tails added to the ends of a linearised plasmid vector. Gaps left following annealing can be filled by DNA polymerase and the free ends joined by DNA ligase.

Another method involves ligation via cohesive ends. Compatible cohesive ends can be generated on the DNA fragment and vector by the action of suitable restriction enzymes. These ends will rapidly anneal through complementary base pairing and remaining nicks can be closed by the action of DNA ligase.

A further method uses synthetic molecules called linkers and adaptors. DNA fragments with blunt ends are generated by bacteriophage T4 DNA polymerase or E.coli DNA polymerase I which remove protruding 3’ termini and fill in recessed 3’ ends. Synthetic linkers, pieces of blunt-ended double-stranded DNA which contain recognition sequences for defined restriction enzymes, can be ligated to blunt-ended DNA fragments by T4 DNA ligase. They are subsequently digested with appropriate restriction enzymes to create cohesive ends and ligated to an expression vector with compatible termini. Adaptors are also chemically synthesised DNA fragments which contain one blunt end used for ligation but which also possess one preformed cohesive end.

Synthetic linkers containing a variety of restriction endonuclease sites are commercially available from a number of sources including International Biotechnologies Inc, New Haven, CN, USA.

A desirable way to modify the DNA encoding the AnxA5 protein is to use the polymerase chain reaction as disclosed by Saiki et al (1988) Science 239, 487-491. In this method the DNA to be enzymatically amplified is flanked by two specific oligonucleotide primers which themselves become incorporated into the amplified DNA. The said specific primers may contain restriction endonuclease recognition sites which can be used for cloning into expression vectors using methods known in the art.

Transformation of appropriate cell hosts with a DNA construct comprising a sequence encoding the AnxA5 protein is accomplished by well-known methods that typically depend on the type of vector used.

With regard to transformation of prokaryotic host cells, see, for example, Cohen et al (1972) Proc. Natl. Acad. Sci. USA 69, 2110 and Sambrook et al (2001) Molecular Cloning, A Laboratory Manual, 3^rd Ed. Cold Spring Harbor Laboratory, Cold Spring Harbor, NY. Transformation of yeast cells is described in Sherman et al (1986) Methods In Yeast Genetics, A Laboratory Manual, Cold Spring Harbor, NY. The method of Beggs (1978) Nature 275, 104-109 is also useful. With regard to vertebrate cells, reagents useful in transfecting such cells, for example calcium phosphate and DEAE-dextran or liposome formulations, are available from Stratagene Cloning Systems, or Life Technologies Inc., Gaithersburg, MD 20877, USA.

Electroporation is also useful for transforming cells and is well known in the art for transforming yeast cell, bacterial cells and vertebrate cells.

For example, many bacterial species may be transformed by the methods described in Luchansky et al (1988) Mol. Microbiol. 2, 637-646 incorporated herein by reference. The greatest number of transformants is consistently recovered following electroporation of the DNA-cell mixture suspended in 2.5X PEB using 6250V per cm at 25pFD.

Methods for transformation of yeast by electroporation are disclosed in Becker & Guarente (1990) Methods Enzymol. 194, 182.

Physical methods may be used for introducing DNA into animal and plant cells. For example, microinjection uses a very fine pipette to inject DNA molecules directly into the nucleus of the cells to be transformed. Another example involves bombardment of the cells with high-velocity microprojectiles, usually particles of gold or tungsten that have been coated with DNA.

Successfully transformed cells, i.e. cells that contain a DNA construct comprising a sequence encoding the AnxA5 protein, can be identified by well-known techniques. For example, one selection technique involves incorporating into the expression vector a DNA sequence (marker) that codes for a selectable trait in the transformed cell. These markers include dihydrofolate reductase, G418 or neomycin resistance for eukaryotic cell culture, and tetracyclin, kanamycin or ampicillin resistance genes for culturing in E.coli and other bacteria. Alternatively, the gene for such selectable trait can be on another vector, which is used to co-transform the desired host cell.

The marker gene can be used to identify transformants but it is desirable to determine which of the cells contain recombinant DNA molecules and which contain self-ligated vector molecules. This can be achieved by using a cloning vector where insertion of a DNA fragment destroys the integrity of one of the genes present on the molecule. Recombinants can therefore be identified because of loss of function of that gene.

Another method of identifying successfully transformed cells involves growing the cells resulting from the introduction of an expression construct comprising a sequence encoding the AnxA5 protein to produce the polypeptide of the invention. Cells can be harvested and lysed and their DNA content examined for the presence of the DNA using a method such 20 as that described by Southern (1975) J. Mol. Biol. 98, 503 or Berent et al (1985) Biotech. 3, 208. Alternatively, the presence of the protein in the supernatant can be detected using antibodies as described below.

In addition to directly assaying for the presence of recombinant DNA, successful transformation can be confirmed by well-known immunological methods when the recombinant DNA is capable of directing the expression of the protein. For example, cells successfully transformed with an expression vector produce proteins displaying appropriate antigenicity. Samples of cells suspected of being transformed are harvested and assayed for the protein using suitable antibodies.

Thus, the transformed host cells themselves can be cultured to provide a culture transformed host cells expressing the AnxA5 protein. The culture may be a monoclonal (clonally homogeneous) culture, or a culture derived from a monoclonal culture, in a nutrient medium.

The culture of transformed host cells expressing AnxA5 protein is grown under suitable growth conditions until a desired cell density is achieved, which is typically selected to balance productivity with time and cost associated with the culture phase, and then the cells are typically harvested. The optimal time for cell harvesting can be determined empirically for any given culture.

Harvesting may, for example, involve the collection of host cells (which are typically intact, and which typically retain substantially all (e.g. more than 80%, 90%, 95% o, 99% or 100%) of the AnxA5 protein intracellularly) from the culture medium. This can commonly be achieved by centrifugation or filtration, to collect the cultured host cells in the form of a biomass. In the case of centrifugation, the supernatant can be discarded, and cell pellets can be transferred directly or indirectly (e.g. following storage, such as by freezing) to the cell culture homogenisation stage.

C. Cell Culture Homogenisation

As discussed above, a first aspect of the present invention provides an improved step of protein release from a host cell. More specifically, it provides a process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from an endotoxin-producing host cell with a cell wall, 21 wherein the process comprises releasing the intracellular protein from the host cell, characterised in that the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising non-ionic detergent.

Preferably, the non-ionic detergent is a polysorbate, more preferably a polysorbate selected from Tween20 and Tween80, and most preferably Tween80. Alternatively, although less preferably, other non-ionic detergent may be used, although it is preferred to avoid (both in the cell culture homogenisation step, and also in any other steps of the process) the use of non-ionic detergents which have a UV absorption /._max similar to the absorption maxima of proteins, which is between 275 and 280 nm, as this can interfere with the ability of UV absorption to monitor the presence of protein during the recovery process. In that context, “similar” can include the meaning that the X_max is within 10mn, 9 nm, 8mn, 7 nm, 6 nm, 5 nm, 4 nm, 3 nm, 2 nm, or 1 nm of the absorption maxima of the AnxA5 protein being purified. Thus, for example, it may be preferred that the non-ionic detergent is not Triton X-100, which has k_max = 275 nm, and so it may be preferred that Triton X-100 is not used in the cell culture homogenisation step and/or any other step of the process of the present invention.

It is to be noted that the non-ionic detergent may be included in the homogenisation buffer that is added to the cells (e.g. the homogenisation buffer may be ‘pre-formed’ with the nonionic detergent present); or that the cells may be suspended in the homogenisation buffer without the non-ionic detergent, and then the non-ionic detergent can be added into, and mixed with, the suspended cells in the homogenisation buffer, prior to cell homogenisation to release the intracellular AnxA5 protein.

Preferably the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising an amount of non-ionic detergent that is effective to reduce (such as by 50%, 60%, 70%, 80%, 90%, 95%, 98%, 99% or more) or prevent the binding between Annexin A5 and endotoxin. Endotoxin levels may be measured by methods well known and established in the art, for example by the limulus amebocyte lysate (LAL) test.

For example the homogenisation buffer may comprise 0.01 to 10% (w/w) non-ionic detergent, such as 0.02 to 5% (w/w), 0.05 to 2% (w/w), or about 1% (w/w) non-ionic detergent. The term “about” in that context, can include the meaning of ± 0.5%, 0.4%, 0.3%, 0.2% or 0.1 % (w/w).

It is preferable that no calcium ions or ionisable calcium compounds (such as CaCb) are added or included in the homogenisation buffer. Accordingly, it is preferable that the free calcium ion concentration in the homogenisation buffer at the time of releasing the intracellular AnxA5 protein from the host cell is lower than 10 mM, preferably lower than 5 mM, 4 mM, 3 mM, 2 mM or 1 mM, more preferably lower than 500 μΜ, 400 μΜ, 300 μΜ, 200 μΜ, 100 μΜ, 50μΜ, 40 μΜ, 30 μΜ, 20 μΜ, 10 μΜ, 5 μΜ, 4 μΜ, 3 μΜ, 2 μΜ, 1 μίτΐ or substantially zero.

In one embodiment, the homogenisation buffer may comprise a calcium metal ion chelator. It may be preferred, in view of optional subsequent steps involving enzymatic treatment in which such enzymes use Mg²⁺ as a co-factor, to select a calcium ion chelator that does not strongly bind Mg²⁺, such as ethylene glycol tetraacetic acid (EGTA). Alternatively, the optional subsequent steps involving enzymatic treatment in which such enzymes use Mg²⁺ as a co-factor may be substituted with other steps not requiring Mg²⁺. In that case, any calcium ion chelator, such as EGTA or ethylenediaminetetraacetic acid (EDTA) may be included in the homogenisation buffer.

Optionally, the concentration of free calcium ions and/or the amount of calcium metal ion chelator in the homogenisation buffer is (or are) in an amount effective to reduce (such as by 50%, 60%, 70%, 80%, 90%, 95%, 98%, 99% or more) or prevent the binding between Annexin A5 and components of the cell membrane and/or wall of the host cell, such as compared to the level of binding that would be observed in the presence of a homogenisation buffer consisting of 50 mM Tris HCI, 10 mM CaCb at pH 7.2.

For example, the homogenisation buffer in accordance with the first aspect of the present invention may comprise 0.01 to 500 mM, such as 0.05 to 100 mM, 0.5 to 20 mM, 1 to 15 mM, 2 to 10 mM, or about 4 mM calcium metal ion chelator, and preferably wherein the calcium metal ion chelator is EDTA or EGTA.

As discussed above, the step of cell culture homogenisation in accordance with the first aspect of the present invention does not include a centrifugation step for purification and separation of the released AnxA5 protein from the host cell debris. Nevertheless, in order to establish a tolerance to free calcium ions and/or an effective amount of calcium metal ion chelator in the homogenisation buffer, a simple test can be conducted using a centrifugation step on an aliquot of lysed cells. Following cell homogenisation, the aliquot 23 (e.g. 100 mL) of lysed cells is subjected to centrifugation (e.g. at 38,900 g for 30 mins) and then the supernatant and pellet are separated. The amount of AnxA5 protein in the supernatant is determined to give the level of “free” AnxA5 protein. The pellet is resuspended in 50 mM Tris HCI, 20 mM EDTA, pH 7.2, with stirring for 30 mins at 4 °C, to release any bound AnxA5 protein, and then centrifuged at 38,900 g for 30 mins at 4 °C, and the amount of bound AnxA5 protein that is released into the supernatant is determined to give the level of “bound” AnxA5 protein. In that context, the percentage of binding of AnxA5 to components of the cell membrane and/or wall of the host cell = (level of “bound” AnxA5 protein / (level of “bound” AnxA5 protein + level of “free” AnxA5 protein)) x 100.

Preferably, as determined by the foregoing method, the percentage of bound AnxA5 in the resultant biomass homogenate is less than 50%, 40%, 30%, 25%, 24%, 23%, 22%, 21%, 20%, 19%, 18%, 17%, 16%, 15%, 14%, 13%, 12%, 11%, 10%, 9%, 8%, 7%, 6%, 5%, 4%, 3%, 2%, 1%, 0.5%, 0.1% or substantially 0%.

Although referred to herein as a “homogenisation buffer” it is not necessarily essential for the solution to be a pH buffer. However, optionally, the homogenisation buffer may further comprise additional components, including buffers (e.g. Tris) and may optionally be pH adjusted as required, for example to around pH 6-8, more preferably in the range of pH 78.5, such as about pH 7.0, 7.1, 7.2, 7.3, 7.4, 7.5, 7.6, 7.7, 7.8, 7.9, 8.0, 8.1, 8.2, 8.3, 8.4, or 8.5. In one embodiment, pH 7.4 may be selected for use.

As discussed above, it may also be preferable, in some options in which subsequent steps include enzymatic treatment with enzymes requiring co-factors such as Mg²⁺, to include the cofactor in the homogenisation buffer.

In one exemplary embodiment, the homogenisation buffer for use in accordance with the first aspect of the present invention comprises, consists essentially of, or consists of an aqueous solution of 50 mM Tris, pH 7.4, 1 mM MgCb and 1% (w/w) Tween80.

The process of the first aspect of the present invention may comprise the step of mixing biomass from a culture of host cells in the homogenisation buffer at a concentration of about 1g to 300g of biomass (wet weight) per Litre of homogenisation buffer, such as at a concentration of about 10g to 200g of biomass per Litre of homogenisation buffer. Exemplary concentrations may be about 10g/L, 20 g/L, 30 g/L, 40g/L, 50 g/L, 60 g/L, 70g/L, 80 g/L, 90 g/L, 100g/L, 110 g/L, 120 g/L, 130 g/L, 140g/L, 150 g/L, 160 g/L, 170g/L, 180 24 g/L, 190 g/L, or 200g/L. A resuspension ratio of about 100 g biomass per Litre of homogenisation buffer may be particularly preferred. In that context, the term “about” is intended to include ± 5 g/L, 4g/L, 3 g/L, 2 g/L, or 1 g/L of the stated value.

The mixing typically occurs around room temperature, i.e. typically around 18 °C to 28 °C, such at about 19 °C, 20°C, 21 °C, 22 °C, 23 °C, 24°C, 25 °C, 26 °C, or 27 °C. It may be preferred to control the temperature during the mixing process to maintain it at, or around (e.g. ± 5, 4, 3, 2, or 1 °C of) a temperature selected from the foregoing list, although active temperature control at this stage is usually not required.

Optionally, the homogenisation buffer may also include, or have added to it following mixing with the biomass but prior to host cell homogenisation, one or more enzymes useful in enzymatic treatment. For example, it may be suitable to include or add one or more nuclease enzymes to assist in the degradation of nucleic acids (including DNA and/or RNA) from the host cells, after homogenisation. This will reduce the viscosity of the subsequently-produced homogenate and thereby assist in downstream processing steps. Any suitable enzymes may be used. The enzyme may, for example, be a nuclease, such as a nuclease A, preferably a nuclease A from Serratia marescens. One such exemplary enzyme of interest is the Benzonase nuclease, an endonuclease from Serratia marcescens, which is available from numerous commercial sources including Merck/Novagen, Sigma Aldrich and the like, which can be used to degrade all forms of DNA and RNA while having no proteolytic activity. It is effective over a wide range of conditions and possesses a high specific activity. The enzyme completely digests nucleic acids to 5'-monophosphate terminated oligonucleotides 2 to 5 bases in length (below the hybridization limit), which is ideal for removal of nucleic acids from recombinant proteins, enabling compliance with FDA guidelines for nucleic acid contamination. The Benzonase enzyme requires 1-2 mM Mg²⁺ for activation, and remains active in the presence of ionic and non-ionic detergents, reducing agents, the protease inhibitor PMSF (1 mM), the chelator EDTA (1 mM) and urea (relative activity depends on specific conditions). The skilled person will be readily able to determine an effective concentration of such nuclease enzymes, although the applicant has identified that Benzonase is effective at least when used prediluted at about 3.3 U per L of host cell culture or at about 1.85 U per L of resuspended biomass. The term “about” in that context may include ± 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, or 10% of the stated number of units.

The step of releasing the intracellular AnxA5 protein from the host cell in the homogenisation buffer can involve any suitable approach to cell homogenisation or lysis. For example, it may comprises lysing, breaking or otherwise homogenising, sonicating, or pressure treating the host cell, such that the cell wall and cell membrane barrier of the host cell is disrupted and thereby releases the intracellular AnxA5 protein. In certain options of the first aspect of the present invention, this step does not include the use of osmotic shock and/or a freeze-thaw step.

In one preferred embodiment of the first aspect of the present invention, the step of releasing the intracellular AnxA5 protein from the host cell comprises high pressure homogenisation, such as one or more cycles of high pressure homogenisation between about 400 bar and about 2,500 bar, preferably three homogenisation cycles of about 600 bar, or two homogenisations cycles of about 800 bar. In that context, the term “about” can include ± 500, 400, 300, 200, 100, 50, 40, 30, 20, or 10 bar ofthe stated value.

Optionally, for example in situations in which no nuclease enzymes have been added to degrade nucleic acids (for example, where the concentrations of Mg²⁺ in the homogenisation buffer are too low, such as because of the inclusion of a Mg²⁺ chelator), then it may be beneficial to include multiple additional rounds of high pressure homogenisation (e.g. from 2 to 4 rounds, at a pressure within the range of from about 600 to 2500 bars) to degrade the nucleic acids and reduce the viscosity of the homogenate.

Accordingly, following the cell homogenisation the step of releasing the intracellular AnxA5 protein may create a biomass homogenate comprising the released AnxA5 protein. Preferably, the biomass homogenate is homogeneous, by which we include the meaning that at least 80%, preferably at least 90%, more preferably at least 95%, 96%, 97%, 98%, 99% or substantially 100% ofthe cells ofthe biomass are disintegrated.

Depending on the cell homogenisation approach applied, the technique may cause an increase in the temperature of the homogenate. It may be preferable to operate the cell homogenisation technique in such a way and/or apply temperature control, to prevent undesirable increases in temperature. However, for example, in the case that the homogenate contains an enzymatic treatment, such as Benzonase, then it may be advantageous to use the temperature increase to move closer to, and preferably within, the enzyme’s optimum temperature range. In the case of Benzonase, temperatures in the range of about 36 to 40 °C may be particularly suitable.

In the case that the cell homogenisation procedure includes enzymatic treatment with an enzyme requiring a metal ion co-factor (e.g. Mg²⁺), and further in the case that the homogenisation buffer excluded the calcium metal ion chelator, then in one option, the calcium ion chelator may be added after the completion of the enzymatic treatment. This may occur before or after a clarification step, as discussed below.

Following cell homogenisation, the biomass homogenate typically further comprises one or more (typically all) of the impurities selected from the group consisting of host cell proteins, host cell wall components, host cell membrane components, host cell nucleic acid, and endotoxin.

It is preferred that the viscosity of the homogenate is adequately low to assist in downstream processing steps.

D. Clarification of the Homogenate

Optionally, and in a preferred embodiment, then following the production of the biomass homogenate it is treated with a clarification step.

Accordingly, in a further embodiment of the first aspect of the present invention, the process further comprising the step of clarifying the biomass homogenate, and thereby producing a clarified product comprising the released AnxA5 protein. This step is conducted to reduce the content of nucleic acids and, additionally, to obtain a particlereduced solution which can be applied to subsequent purifications steps such as capture chromatography as discussed further below.

Any suitable clarification step or combination of steps can be performed. For example, the clarification process may comprise (preferably, subsequent to the nuclease treatment), the step of passing the biomass homogenate comprising the released AnxA5 protein through a filter, such as a cellulose or polypropylene filter, wherein the filter effluent is the clarified product comprising the released AnxA5 protein.

Preferably the filter is a depth filter, and/or preferably the filter has a cut off of less than 4 pm, such as a cut-off of less than 3pm, 2pm or 1pm, and most preferably a cut off within the range of 0.2 to 0.6pm. For example, the homogenate may be clarified by filtration 27 using a 0.6-0.2 pm cut off depth filter, examples of which are commercially available, e.g. such as available as the cellulose-based Cuno 60 SP depth filters. Other depth filters found to provide good performance (i.e. good filtration without product loss), albeit less so that the preferred cellulose Cuno 60 SP depth filters with 0.6-0.2 pm cut off, include a cellulose + kieselguhr filter with a 0.5 pm cut-off (e.g. PR12 UP available from Begerow); a polypropylene filter with a 1.2 pm cut off (e.g. Sartopure PP2 available from Sartorius); a cellulose filter with a 0.1 pm cut off (e.g. Sartoclear S9 available from Sartorius); a polypropylene filter with a 0.65 pm cut off (e.g. Sartopure PP2 available from Sartorius); and a cellulose filter with a 0.2-0.5 pm off (e.g. ΕΚ 1P or EKM-P both available from Pall, which were good but slow). Further tests showed that filters with larger cut offs (e.g. > 4 pm) achieved only moderate particle removal, and so are less preferred.

It has also been found by the applicant that positively charged cellulose based filters additionally reduce DNA content in the clarified homogenate, and therefore may represent a particularly preferred class of filters for use in the clarification step.

Moreover, it has been found that cellulose-based filters require a smaller filter area to provide effective clarification than do corresponding polypropylene filters. This may be a further reason to particularly prefer the cellulose-based class of filters for use in the clarification step.

The selection of filter area can also depend on the extent and nature of homogenisation used. For example, the applicant has found that in the case of cell homogenisation being performed by three homogenisation cycles of about 600 bar then a filter area of about 60 cm² per 1l_ of homogenate is suitable, whereas in the case of cell homogenisation being performed by two homogenisations cycles of about 800 bar then a filter area of about 180 cm² per 1L of homogenate is suitable. Accordingly, the depth filter may optionally be selected to have an area of from 10 to 500 cm² per L of homogenate clarified, such as from 30 to 400 cm²/L, from 40 to 250 cm²/L, from 50 to 200 cm²/L or from 60 to 180 cm²/L, such as from 50-100 cm²/L, or 60-80 cm²/L; or from 120-240 cm²/L, or 150-210 cm²/L.

After clarification, the clarified product may be further adjusted by the addition of one or more further additives in readiness for subsequent steps. For example, it may be suitable to condition the clarified product by the addition of one or both of: (a) a non-ionic detergent, such as polysorbate and most preferably Tween80; and (b) a calcium metal ion chelator, such as EDTA, unless the clarified product already contains adequate levels of the chelator 28 by virtue of its inclusion in the homogenisation buffer and/or by its addition after the enzymatic treatment step.

In one exemplary embodiment, the clarified product is diluted about 2-fold with 1% nonionic detergent (most preferably Tween80), and a calcium ion chelator (most preferably EDTA) is added to a final concentration of about 2 mM.

A further advantageous feature of the process of the present invention is the lack of need for any time-consuming dialysis steps in the clarified product prior to further chromatographic capture steps, such as anion exchange capture as discussed below. Accordingly, in an embodiment of the present invention, the clarified product is not subjected to dialysis prior to chromatographic capture ofthe AnxA5 protein.

E. Anion Exchange Capture

A process, in accordance with the first aspect of the present invention, may further comprise the step of subjecting the released AnxA5 protein to an anion exchange resin in order to perform a first anion exchange capture step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein.

Generally, protein capture by anion exchange chromatography from bacterial (e.g. E. coli) homogenate/lysate is not a first choice strategy since high quantities of host cell proteins (HCP) and DNA bind to the capture resin affecting the binding capacities for the target product and even stressing the resin performance. However, the applicant has determined that the foregoing cell homogenisation and clarification procedures according to the first aspect ofthe present invention are effective to provide an AnxA5 protein product that can be effectively further purified using anion exchange chromatography.

Accordingly, in one embodiment, the clarified product comprising the released AnxA5 protein as produced by the step of clarification of the homogenate/lysate and/or degradation of nucleic acids, as discussed above, is subjected to the first anion exchange capture step, thereby to produce a first anion exchange product which comprises the released AnxA5 protein.

Optionally, prior to the first anion exchange step, one or more parameters of the environment ofthe released AnxA5 protein, selected from the group consisting ofthe pH, 29 the conductivity, the level of calcium ion chelator and the level of non-ionic detergent, is or are adjusted. For example, the AnxA5 protein composition that is subjected to the anion exchange step may be formulated at a pH of about 6.9, optionally + 1, 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2 or 0.1 pH units (in one option, a preferred range is pH 6-8.5, more preferably pH 6.5-7.5, most preferably pH 6.9). The applicant has found that low pH values around this range (e.g. at pH 6) tend to cause the presence of detectable host cell proteins in the eluted product; whereas resolution is somewhat reduced at or above pH 8. The AnxA5 protein composition that is subjected to the anion exchange step may optionally be adjusted to have a conductivity of about 2.8 mS/cm, ± 1, 0.9, 0.8, 0.7, 0.6, 0.5, 0.4, 0.3, 0.2 or 0.1 mS/cm. After clarification, the clarified product may be further adjusted by the addition of one or more further additives in readiness for subsequent steps. As already discussed above, it may be suitable prior to the first anion exchange step to condition the AnxA5 protein composition that is subjected to the anion exchange step by the addition of one or both of: (a) a non-ionic detergent, such as polysorbate and most preferably Tween80; and (b) a calcium metal ion chelator, such as EDTA, unless the clarified product already contains adequate levels of the chelator by virtue of its inclusion in the homogenisation buffer and/or by its addition after the enzymatic treatment step. In one exemplary embodiment, the AnxA5 protein composition that is subjected to the anion exchange step is diluted about 2-fold with 1% non-ionic detergent (most preferably Tween80), and a calcium ion chelator (most preferably EDTA) is added to a final concentration of about 2 mM.

In this context, the use of non-ionic detergent and/or calcium metal ion chelator to condition the AnxA5 protein composition that is subjected to the first anion exchange capture step can be highly beneficial in enhancing the separation of the AnxA5 protein from host cellderived impurities (including cell wall components, cell membrane components, endotoxin, nucleic acids, etc.) by the first anion exchange capture step. For example, the applicant has demonstrated a highly efficient removal of endotoxin (around a 99% reduction) by the first capture anion exchange step when conducted in the presence of non-ionic detergent and calcium metal ion chelator.

Although primarily discussed below in the context of the second anion exchange polishing step, in the option in which a calcium metal ion chelator (e.g. EDTA) is present in the AnxA5 protein composition that is subjected to the first anion exchange capture step, it may also be beneficial to the operation of the first anion exchange capture step include one or more types of additional selected metal ions (not calcium), wherein the additional 30 selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions. One exemplary metal ion is Mg²⁺.

Typically, prior to the contacting of the anion exchange resin and the AnxA5 product, the anion exchange resin is equilibrated. Any suitable equilibration may be used. For example, the anion exchange resin may be equilibrated with a buffer (e.g. 20 mM Tris pH 7.4), a non-ionic detergent (e.g. 0.1% polysorbate, preferably Tween80) and salt (e.g. 25 mM NaCI). Any suitable equilibration volume may be used; without limitation, the applicant has found 3 column volumes (CV) to be a suitable volume in the exemplified embodiment.

Preferably, the first anion exchange capture step is run in the positive mode with respect to the AnxA5 protein, and so the AnxA5 protein is temporarily bound to the anion exchanger during the anion exchange step, typically a wash solution is passed over the column to remove impurities from the bound AnxA5 protein, and then the first anion exchange product which comprises the released AnxA5 protein is produced by applying an elution buffer to the anion exchange resin to release the bound AnxA5 protein.

Strong anion exchange resins are preferred, as the applicant has found that these provided acceptable capacities for AnxA5 protein capture, whereas the performance with weak anion exchange resins was less acceptable. Strong anion exchange resins are well known in the art, and examples include resins with a Quarternary Ammonium functional group, such as a Type I resin having trialkyl ammonium chloride or hydroxide, or Type II resins having dialkyl 2-hydroxyethyl ammonium chloride or hydroxide (e.g. Q Sepharose XL by GE Healthcare, Capto Q by GE Healthcare, Unosphere Q by Biorad, or Eshmuno Q by Merck). Weak anion exchange resins are not preferred, and examples include DEAE resin with a Diethylaminoethyl functional group. The Q Sepharose XL resin (e.g. as provided by GE Healthcare) may be most preferred.

After loading onto the anion exchange resin, under the positive mode, the AnxA5 protein temporarily binds to the resin, and can be washed to reduce/remove impurities. Any suitable wash conditions can be employed. For example, the wash solution may comprise, consist essentially of, or consist of an aqueous solution of a buffer (e.g. 20 mM Tris pH 7.4), a non-ionic detergent (e.g. 0.1% polysorbate, preferably Tween80) and salt (e.g. 25 mM NaCI). Any suitable wash volume may be used; without limitation, the applicant has found 10 column volumes (CV) to be a suitable volume in the exemplified embodiment.

The bound AnxA5 protein is then released from the anion exchange resin using an elution buffer. Any suitable elution buffer can be employed. For example, the elution buffer may comprise, consist essentially of, or consist of an aqueous solution of a buffer (e.g. 20 mM Tris pH 7.4), a non-ionic detergent (e.g. 0.01 to 1% (w/v) more preferably 0.1% (w/v) polysorbate, preferably Tween80) and salt at a concentration higher than the wash solution (e.g. 300 mM NaCI, optionally ± 100, 90, 80, 70, 60, 50, 40, 30, 20, 10, or 5 mM). Any suitable elution volume may be used; without limitation, the applicant has found 9 column volumes (CV) to be a suitable volume for elution in the exemplified embodiment.

Accordingly, the AnxA5 protein is captured in the elution buffer, and this provides the first anion exchange product.

The anion exchange resin may then be regenerated and cleaned. Suitable methods for the regeneration and cleaning are known in the art, and one such suitable protocol is discussed in the examples.

Typically the first anion exchange product which comprises the released AnxA5 protein contains substantially in excess of 50% of the AnxA5 protein that was released from the host cells. Preferably, the first anion exchange product comprises more than 60%, 70% or 80% of the AnxA5 protein that was from the host cells. By point of comparison with the process of Marder et al. (supra), it is apparent that the prior art processes demonstrated large product losses of approximately 50% or more. For example, the process of Marder et al. (supra) involves an initial purification centrifugation step which discards the supernatant and collects the Annexin A5 bound to the pellet. Relative amounts of Annexin A5 in the discarded supernatant and as recovered from the pellet are shown in Fig 3, lanes 2 and 3, respectively, of Marder et al (supra). From that figure it is apparent that about half of the released Annexin A5 is discarded in the process of Marder et al. (supra), leading to a low yield method.

As a further point of comparison, the applicant has found that the yield of the exemplified process provides a yield of about 5 g AnxA5 protein per litre of culture at the end of the first anion exchange chromatography capture step, which is much higher than the yield reported in Marder et al. (supra), (see “Conclusions”, second paragraph) of 0.983 g of purified Annexin A5 protein per litre of culture.

Accordingly, in accordance with the first aspect of the present invention, it is preferred that the first anion exchange product comprises more than 1 g, more than 2 g, more than 3 g, more than 4g, or about 5 g of AnxA5 protein per litre of culture.

Optionally, the first anion exchange product is subjected, directly or indirectly to a filtration step (such as a sterile filtration step). For example, without limitation, a 0.45 to 0.2 μΜ filtration step has been found to be suitable.

F. Affinity Chromatography

The applicant has also discovered (e.g. see Example 2, below), that contrary to conventional methods in which the successive addition of purification steps tends to lead to an ever increasing loss of yield (as product is lost at each step), that the combination of an anion exchange step and a heparin affinity chromatography step has a surprising benefit of attaining the high purity achieved by the heparin affinity chromatography step alone, but with substantially increased yield (i.e. the recovery is increased from about 3040% to about 70-90%). The large increase in yield associated with the addition of a purification step is the direct opposite of what would normally be expected from the combination of purification steps.

Accordingly, a second aspect the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities (which may, or may not, be a product of a clarification step as described above), the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities (which solution may, or may not, be the direct or indirect product of a cell homogenisation, clarification and/or first anion exchange chromatography capture step, as discussed above) to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the AnxA5 protein; and subjecting the first anion exchange product, directly or indirectly, to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

Preferably, in accordance with the process of the second aspect of the present invention, the affinity chromatography step may comprise the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions and further optionally, the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

Additionally, as discussed in Example 3, the applicant has discovered that Tween80 has a particularly advantageous effect (compared to other non-ionic detergents, including other Tweens, such as Tween20) on a heparin affinity chromatography step. The inclusion of Tween 80, for example at around 0.1% (w/v) in the buffers used in the heparin affinity chromatography step can assist in eluting the AnxA5 protein in a single peak, reduce pressure, and prevent precipitation.

Accordingly, a third aspect the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities (which solution may, or may not, be the direct or indirect product of a cell homogenisation, clarification and/or first anion exchange chromatography capture step, as discussed above) to a heparin affinity chromatography step in the presence of Tween80 (preferably in the presence of 0.1% Tween80), thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

Thus, both of the second and third aspects of the present invention, which can be operated either independently of each other or in combination (i.e. the heparin affinity chromatography step in the second aspect of the present invention can include Tween 80 (for example at around 0.1% (w/v)) in the buffers used in the heparin affinity chromatography step,

More generally, however, the first aspect of the present invention may comprise the step of subjecting the released AnxA5 protein to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein. It may be particularly preferred that the AnxA5 protein in the first anion exchange product, for example as produced by a method as described above, may be subjected directly or indirectly (e.g. after sterile filtration and/or the addition of further components) to the affinity chromatography step.

Accordingly, in one embodiment of the first aspect of the present invention (which may be combined with either or both of the features of the second and third aspects of the present invention), the process comprises steps wherein:

(a) a biomass homogenate comprising the released AnxA5 protein as described above is clarified by a clarification process as described above, and thereby produces a clarified product comprising the released AnxA5 protein, and (b) the AnxA5 protein in the clarified product is subjected to an anion exchange resin in order to perform a first anion exchange step as described above, and thereby produce a first anion exchange product which comprises the AnxA5 protein, and (c) wherein the AnxA5 protein in the first anion exchange product is subjected (directly or indirectly) to an affinity chromatography step.

Preferably, the affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and optionally the binding is promoted by the presence of calcium ions.

Accordingly, prior to the heparin affinity step, the AnxA5 product may be conditioned by the addition of any one or more of calcium ions (e.g. CaCb), non-ionic detergent (preferably Tween80), and optionally buffered (e.g. Tris buffer at pH 7.4). Without limitation, the applicant has demonstrated a beneficial effect when the filtered anion exchange product is diluted about 8-fold with a dilution buffer containing 20 mM Tris, pH 7.4, 0.1% Tween80 and 2 mM CaCb.

The dilution with calcium allows Annexin A5 to bind to the immobilized Heparin chromatography. This interaction is, by comparison with an ionic interaction, slow. The contact time is important, and therefore the chromatography is preferably performed with < 100 cm/h.

The conditions used in the loading of the affinity chromatography column (e.g. the heparin affinity chromatography column) permit binding of the AnxA5 protein to the heparin. That is, the affinity chromatography is typically run in the positive mode with respect to the AnxA5 protein.

After loading of the AnxA5 protein, the column is typically washed one or more times to remove impurities. Any suitable washing protocol may be used. The applicant had found, without limitation, that a suitable washing protocol includes a two stage wash. For example, in a first stage of washing, a wash may be performed using a first wash buffer containing calcium (e.g. 20 mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCy. The volume of first stage washing may be varied dependent in the desired result and the exact nature of the wash solution used. Without limitation, the applicant has found, for example, that the exemplary wash buffer noted above can be successfully used with 15 CV of washing. In a second stage wash, the wash buffer may contain calcium in an amount that is lower than the first wash, or preferably no calcium (e.g. 20 mM Tris pH 7.4; 0.1 % Tween80). The volume of second stage washing may be varied dependent in the desired result and the exact nature of the second stage wash solution used. Without limitation, the applicant has found, for example, that the exemplary second stage wash buffer noted above can be successfully used with 2 CV of washing.

Thereafter, the AnxA5 protein is eluted from the affinity chromatography column using an elution buffer, and thereby providing the first affinity chromatography product which comprises the released AnxA5 protein. In the case of using a heparin affinity chromatography column, it may be preferred to use an elution buffer comprising a calcium metal ion chelator, such as EDTA or EGTA.

For example, without limitation, the applicant has found that a suitable elution buffer is 20 mM Tris pH 7.4; 0.1 % Tween80; 10 mM EDTA; 25 mM NaCI, which chelates the calcium ions. The chelation reaction specifically elutes Annexin A5 which can only bind to Heparin in the presence of calcium.

It may be preferred to reduce the flow rate to less than 100 cm/h during elution to increase the concentration of the product. For example, without limitation, in the examples, the applicant allowed a concentrated elution by reducing the flow rate to < 60 cm/h in the elution. The complete elution peak may, for example, be collected starting from the rising of the UV signal at 0.05 AU to 0.05 AU in the descending peak representing approximately 7 CV. Preferably, the elution profile demonstrates a single peak, which is most ideally a sharp peak.

Accordingly, the first affinity chromatography product comprises the released AnxA5 protein and the calcium ion chelator, such as EDTA or EGTA, optionally wherein the calcium ion chelator is present in the range of from about 0.1 mM to 500 mM, such as from about 1 mM to about 100 mM, more typically in the range of from about 2 mM to about 50 mM, more preferably in the range of about 5 mM to about 15 mM, and most preferably about 10 mM. The term “about” in that context can include the meaning of ± 50%, 40%, 30%, 20%, 10%, 5% or 1% of the stated concentration(s).

The affinity chromatography step may be the most powerful purification step in the process scheme. The AnxA5 protein binds to calcium ions and, in this calcium bound state the product can form a highly specific bond with Heparin. Typically, only correctly folded AnxA5 protein forms that have the ability to complex with calcium can bind to Heparin. Thereby the affinity chromatographic step may be useful to assist in discriminating between correctly folded and misfolded product. Additionally the intermediate step reaches high depletion factors as the highly specific interaction is combined with a specific elution mode by the chelate reaction of calcium with EDTA. Therefore a strong reduction of endotoxin and HCP is observed combined with a moderate reduction of the DNA content. Endotoxin, typically already having been reduced (preferably by about 97%) during the preceding anion exchange capture step, is further reduced (preferably by about 99%), and this preferably takes the endotoxin levels to about 0.03% of the levels in the clarified product prior to the first anion exchange capture step.

G. Anion Exchange Polishing

In a further embodiment of the first, second and/or third aspects of the present invention, an AnxA5 product (for example, as produced by the affinity chromatography step) may, directly or indirectly, be further purified by an anion exchange polishing step.

In the case that the an AnxA5 product as produced by the affinity chromatography step is indirectly further purified by an anion exchange polishing step, then the steps of affinity chromatography and the anion exchange polishing step may be separated by the addition of one or more conditioning additives to the product of the affinity chromatography step.

Suitable additives can include, for example, diluent (e.g. water) to further dilute the AnxA5 protein in the product of the affinity chromatography product; buffer (e.g. Tris, for example 37 at 35 mM and pH 8); non-ionic detergent (e.g. polysorbate, more preferably Tween80, such as at a concentration of about 0.1% w/v); and/or one or more further additives based on the fourth aspect of the present invention, as discussed below.

That is, to say, a fourth aspect of the present invention is based on the applicant’s realisation that calcium metal ion chelators (e.g. EDTA) can impact negatively on the efficacy of anion exchange steps. Free EDTA (or other chelator) can bind directly to the anion exchange function groups, and thereby reduce the capacity and also the separation achieved by an anion exchange step. This is a particular issue in the case of performing an anion exchange on the product of a heparin affinity chromatography step, in which the AnxA5 protein is bound to heparin in the presence of calcium ions, and then a calcium metal ion chelator (e.g. EDTA) is used to elute the bound AnxA5 protein. As a consequence the eluted AnxA5 product of the heparin affinity chromatography step contains high levels of calcium ion chelator. It is generally desirable to be able to further purify the AnxA5 product with a further anion exchange step, but the calcium ion chelator is a problematic component during that further anion exchange step. On the other hand, it is time consuming and therefore also increases costs, to attempt to remove calcium metal ion chelator before an anion exchange step. Therefore, prior art methods involving, for example, dialysis steps for buffer replacement are slow and inefficient, and so increase production costs. Further, the inclusion of the calcium metal ion chelator in the AnxA5 product during the anion exchange step can be an important component to prevent calcium-mediated binding of the AnxA5 protein to impurities, including endotoxin. It would therefore be convenient and efficacious to introduce an additive that blocks or reduces the binding of the calcium ion chelator to the anion exchange resin, yet which would allow the anion exchange step to be performed without inconvenience and cost associated with dialysis, and without preventing the beneficial effect of the calcium metal ion chelator during the anion exchange step.

The applicant has realised that this can be achieved by the inclusion in the AnxA5 protein product, prior to anion exchange, or one or more types of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions. The selection of the appropriate additional metal ions will depend on the nature of the calcium ion chelator and the nature of the anion exchange resin. For example, in the case of using EDTA as a calcium ion chelator, Mg²⁺ ions are generally suitable to achieve the object of 38 the present invention, and can be added to the AnxA5 protein product prior to an anion exchange step.

Accordingly, a fourth aspect of the present invention provides a process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions.

Preferably, the additional selected metal ions are mixed with the composition that comprises the AnxA5 protein and a calcium metal ion chelator prior to being subjected to the composition to an anion exchange resin. Solutions used in subsequent anion exchange steps (e.g. wash solutions and/or elution buffers) may or may not also include the additional selected metal ions. Therefore, in one embodiment of this aspect of the invention, the step of conducting the anion exchange step in the presence of additional selected metal ions refers to the addition of the additional selected metal ions to the composition that comprises the AnxA5 protein and a calcium metal ion chelator prior to being subjected to the composition to an anion exchange resin.

In one embodiment of the fourth aspect of the present invention, the calcium metal ion chelator is selected from EDTA or salt thereof, EGTA or salt thereof, and most preferably EDTA.

The calcium metal ion chelator may be present in the composition in an excess and/or at a concentration in the range of from about 0.1 mM to 500 mM, such as from about 1 mM to about 100 mM, more typically in the range of from about 2 mM to about 50 mM, for example at a concentration of about, or at least, 0.1 mM, 0,5 mM, 1 mM, 2 mM, 3 mM, 4 mM, 5 mM, 6 mM, 7 mM, 8 mM, 9 mM, 10 mM, 11 mM, 12 mM, 13 mM, 14 mM, 15 mM, 16 mM, 17 mM, 18 mM, 19 mM, 20 mM or more. In that context, the term “about” can 39 include the meaning of ± 0.5, 0.4, 0.3, 0.2, or 0.1 mM of the stated value. In the foregoing context, the term “excess” can include the meaning that sufficient amount calcium metal ion chelator is present to remove any divalent ion that may contribute to the binding of the AnxA5 protein to an immobilized heparin on the column in a preceding affinity chromatography step, thereby allowing the AnxA5 protein to be released from the column to the solution, and then used directly or indirectly in the anion exchange polishing step.

In one exemplary embodiment of the fourth aspect of the present invention, the selected metal ions are divalent cations, such as Mg²⁺ ions.

It may be preferred that the selected metal ions are present during the anion exchange step in an amount effective to reduce (such as by about 50%, 60%, 70%, 80%, 90%, 95%, 98%, 99% or more) or prevent an interaction between the calcium ion chelator and the anion exchange resin during.

It may be preferred that the selected metal ions are present during the anion exchange step in an amount effective to increase binding ofthe AnxA5 protein to the anion exchange resin in the presence of the calcium ion chelator, and thereby reduce (such as by about 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45%, 50%, 60%, 70%, 80%, 90%, 95%, 98%, 99% or more) the loss of AnxA5 protein in the flow through of the anion exchange step, compared to the level of loss observed when no selected metal ions are present during the anion exchange step.

It may be preferred that the selected metal ions are present during the anion exchange step at a concentration of about 1 to about 100 mM, such as about 2 to about 50 mM, about 5 to about 25 mM, about 10 to about 15 mM or about 12.5 mM.

Further, it may be preferred that the calcium metal ion chelator is EDTA and the selected metal ions are Mg²⁺ ions, and more preferably the molar ratio of Mg²⁺ ions to EDTA is in the range of 0.5:1 to 2:1, most preferably at least 1:1 or >1:1.

In the context of the fourth aspect of the present invention, in a further embodiment, the composition that comprises the AnxA5 protein and a calcium metal ion chelator and which is subjected to the anion exchange resin may be the direct, or indirect, product of a preceding process that comprises the step of subjecting the AnxA5 protein to an affinity chromatography step and eluting the AnxA5 protein with a calcium ion chelator, thereby 40 producing an affinity chromatography product which is a composition that comprises the AnxA5 protein and a calcium metal ion chelator. For example, the preceding affinity chromatography step may comprises the binding of the AnxA5 protein to immobilised heparin, optionally wherein the binding is promoted by the presence of calcium ions, and further optionally wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

It may be further preferred that there is no dialysis step between the preceding affinity chromatography step and the anion exchange step and/or there is no removal of calcium ion chelator from the product of preceding affinity chromatography step prior to the application of the direct or indirect product to the anion exchange step.

In the context of the fourth aspect of the present invention, in a further embodiment the selected metal ions are added to the composition prior to, or during, the anion exchange step.

In a preferred embodiment, the product of an affinity chromatography step according to any of the first, second or third aspects of the present invention is treated with a further anion exchange step, such as an anion exchange step in accordance with the fourth aspect of the present invention.

Optionally, prior to the (second) polishing anion exchange step, one or more parameters of the environment of the released AnxA5 protein, selected from the group consisting of the concentration of the AnxA5 protein, the pH, the conductivity, the level of calcium ion chelator and the level of non-ionic detergent, or the level of selected additional metal ions (in accordance with the fourth aspect of the present invention) is, or are, adjusted.

Typically, prior to the contacting of the (second) anion exchange resin of the polishing step, and the AnxA5 product, the anion exchange resin is equilibrated. Any suitable equilibration may be used. For example, the anion exchange resin may be equilibrated with a buffer (e.g. 20 mM Tris pH 7.4), a non-ionic detergent (e.g. 0.1% polysorbate, preferably Tween80) and salt (e.g. 25 mM NaCI). Any suitable equilibration volume may be used; without limitation, the applicant has found 3 column volumes (CV) to be a suitable volume in the exemplified embodiment.

Preferably, the (second) anion exchange polishing step is run in the positive mode with respect to the AnxA5 protein, and so the AnxA5 protein is temporarily bound to the anion exchanger during the anion exchange step, typically a wash solution is passed over the column to remove impurities from the bound AnxA5 protein, and then the second anion exchange product which comprises the released AnxA5 protein is produced by applying an elution buffer to the anion exchange resin to release the bound AnxA5 protein.

Strong anion exchange resins are preferred. Strong anion exchange resins are well known in the art, and examples include resins with a Quarternary Ammonium functional group, such as a Type I resin having trialkyl ammonium chloride or hydroxide, or Type II resins having dialkyl 2-hydroxyethyl ammonium chloride or hydroxide. Without limitation, one example of a suitable anion exchange resin for the second polishing step includes Source15 Q.

After loading onto the (second) anion exchange resin for polishing, under the positive mode, the AnxA5 protein temporarily binds to the resin, and can be washed to reduce/remove impurities. Any suitable wash conditions can be employed. For example, the wash solution may comprise, consist essentially of, or consist of an aqueous solution of a buffer (e.g. 20 mM Bis-Tris, pH 7), and salt (e.g. 25 mM NaCI), and optionally a nonionic buffer (e.g. a polysorbate, preferably Tween80, such as at a level of about 0.1 w/v). Any suitable wash volume may be used; without limitation, the applicant has found 3 column volumes (CV) to be a suitable volume in the exemplified embodiment.

The bound AnxA5 protein is then released from the anion exchange resin using an elution buffer. Any suitable elution buffer can be employed. For example, the elution buffer may comprise, consist essentially of, or consist of an aqueous solution of a buffer (e.g. 20 mM Bis-Tris, pH 7), salt at a concentration higher than the wash solution (e.g. 180 mM NaCI, optionally + 100, 90, 80, 70, 60, 50, 40, 30, 20, 10, or 5 mM) and optionally a non-ionic buffer (e.g. a polysorbate, preferably Tween80, such as at a level of about 0.1 w/v). Any suitable elution volume may be used; without limitation, the applicant has found 33 column volumes (CV), increasing the concentration ofthe elution buffer from 0 to 100% in a linear gradient, to be a suitable for elution in the exemplified embodiment.

Accordingly, the AnxA5 protein is released into in the elution buffer, and this provides the (second) polished anion exchange product. As discussed in Example 1, a process conducted with 0.1 % Tween80 increased the product yield post intermediate by approximately 30%.

The (second) anion exchange resin may then be regenerated and cleaned. Suitable methods for the regeneration and cleaning are known in the art, and one such suitable protocol is discussed in the examples.

The polishing step is mainly implemented for the reduction of product related impurities e.g. the separation of different Annexin A5 isoforms. Additionally the polishing step reaches the highest depletion factor in the process for the residual DNA and strongly reduces HCP. Endotoxin, being already at a low level after the intermediate step, is further reduced by about 99%, which (when used in combination with the preceding cell homogenisation, nuclease treatment, clarification, capture anion exchange, filtration (such as a sterile filtration step), and heparin affinity steps) takes the endotoxin levels to about 0.0003% of the levels in the clarified product prior to the first AX step.

Accordingly, in a further embodiment of the first, second, third and/or fourth aspects of the present invention, there is provided a process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from a host cell with a cell wall, or a culture in accordance with the first aspect of the present invention and preferably wherein the process comprises recovery and/or purification of a recombinantly expressed intracellular AnxA5 protein from a culture of the host cells, and wherein the culture has a volume of at least about 100L, about 200L, about 300L, about 400L, about 500L, about 600L, about 700L, about 800L, about 900L, about 1.000L, about 2.000L, about 3.000L, about 4,0001., about 5.000L, about 6,000L, about 7.0000L, about 8,0000L, about 9,0000L, about 10.000L, about 20.000L, about 30.000L, about 40.000L, about 50.000L, about 60.000L, about 70.0000L, about 80.0000L, about 90.0000L, about 100.000L or higher, wherein:

(a) the process comprises releasing the intracellular protein from the host cell in the presence of a homogenisation buffer comprising non-ionic detergent in accordance with the first aspect of the present invention;

(b) optionally wherein the releasing step is in accordance with any one or more of the embodiments of the first aspect of the present invention as described above in subsection C;

(c) further optionally wherein the process comprises a step of clarifying the biomass homogenate according to any one or more of the embodiments of as described above in subsection D; and (d) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein in accordance with any of any one or more of the embodiments as described above in subsection E; and (e) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an affinity chromatography step, in accordance with any of the first, second and/or third aspects of the present invention as described above in section F, and (f) wherein the product of the affinity chromatography step is a composition that comprises the AnxA5 protein and a calcium metal ion chelator; and (g) wherein the direct, or indirect, product of the affinity chromatography step that comprises the AnxA5 protein and the calcium metal ion chelator is subjected to anion exchange step in accordance with any of the embodiments described above in this section (i.e. section G).

H. Product Formulation

The process of any of the first, second, third or fourth aspects of the present invention may further comprise, preferably at the end of the process, one or more further steps selected from the group consisting of concentration, buffer change, conditioning and filtration (such as a sterile filtration step), and optionally a final step of storing the AnxA5 proteincontaining product in a sterile container.

For example, one of the further steps used for product formulation may be ultrafiltration/diafiltration (UF/DF), optionally wherein the product of the UF/DF step contains the AnxA5 protein at a concentration of at least about 1 mg/mL, 2 mg/mL, 3 mg/mL, 4 mg/mL, 5 mg/mL, 6 mg/mL, 7 mg/mL, 8 mg/mL, 9 mg/mL, 10 mg/mL, 11 mg/mL, 12 mg/mL, 13 mg/mL, 14 mg/mL, 15 mg/mL, 16 mg/mL, 17 mg/mL, 18 mg/mL, 19 mg/mL, 20 mg/mL, 25 mg/mL, 30 mg/mL, 35 mg/mL, 40 mg/mL, 45 mg/mL, 50 mg/mL, 60 mg/mL, 70 mg/mL, 80 mg/mL, 90 mg/mL, 100 mg/mL, 125 mg/mL or greater.

In another example, one of the further steps used for product formulation may be the addition of a non-ionic surfactant, preferably a polysorbate, and more preferably Tween80. The non-ionic surfactant may be added in an amount desired forthe final product, such as to a final concentration of about 0.05% (w/w) (e.g. ± 0.05, 0.04. 0.03, 0.02 or 0.01 % w/v).

In another example, one of the further steps used for product formulation may be a filtration step (such as a sterile filtration step), for example using a 0.45-0.2 pm filter or a 0.22 pm filter.

As indicated above, the process of the first, second, third or fourth aspects of the present invention may conclude with the step of sterile filtration, and placing the sterile filtered AnxA5 protein-containing product in a sterile container.

The final concentration of the AnxA5 protein in the filled container may be adjusted as required. Without limitation, the applicant has exemplified a final concentration of 10 mg/mL. A suitable concentration may, for example, be 1-125 mg/mL, 2-100 mg/mL, 5-50 mg/mL, 7-30 mg/mL or about 10-20 mg/mL.

Optionally, the processes of the present invention may provide a final sterile AnxA5 protein product in a non-phosphate buffer (such as Bis-Tris or Tris buffer) at about pH 7.4 (e.g. ± 0.5, 0.4, 0.3, 0.2, or 0.1 pH units), comprising about 150 mM NaCI (e.g. + 50, 40, 30, 20 or 10 mM), about 1 mM CaCL (e.g. ± 500, 400, 300, 200, 100, or 50 pM), about 0.05% (w/w) (e.g. ± 0.05, 0.04. 0.03, 0.02 or 0.01 % w/v) polysorbate, such as Tween80 or other non-ionic detergent. A pH of about 7.4 is a typical target pH for formulations intended for use with humans (especially for intravenous delivery), as it matches the pH in human blood and provides a stable AnxA5 protein with good solubility. Below pH 7, and particularly down to around pH 6, the AnxA5 protein loses solubility and can start to precipitate.

NaCI can be useful to maintain the AnxA5 product in a monomeric form during storage. Accordingly, the processes of the present invention may provide a final sterile AnxA5 protein product, wherein the NaCI concentration present maintains AnxA5 protein in a form that is predominantly (that is, greater than about 50%, such as 60%, 70%, 80%, 85%, 90%, 95%, 96%, 97%, 98%, 99% or substantially 100%) monomeric. Percentage monomer levels can be readily determined using techniques well known in the art, such as gel permeation chromatography (GPC).

In one embodiment, the processes of the present invention provide a final sterile, therapeutically acceptable AnxA5 protein product with an overall yield of greater than 1 g of AnxA5 protein per L of host cell culture, more preferably at least about 1.5 g/L, even more preferably in the range of about 2 to about 4 g/L. In that context, the term “about” may include + 0.4, 0.3, 0.2 or 0.1 g/L of the stated value.

In another embodiment, the processes of the present invention provide a final sterile, therapeutically acceptable AnxA5 protein product with an overall recovery of AnxA5 protein of at least about 24 % by weight (e.g. ± 10, 9, 8, 7, 6, 5, 4, 3, 2, 1 %), or more, of the AnxA5 protein present in the from the host cell culture. This can be determined, for example, by measuring soluble AnxA5 protein in the initial homogenate (which can be captured and measured by centrifugation of an aliquot of the homogenate and testing the level of AnxA5 in the supernatant) and in the final purified product.

Additionally, at any point in the process (if relevant, prior to filling the sterile container), and typically after the final purification step as described above, the AnxA5 protein may be chemically modified. For example, the AnxA5 protein may be PEGylated. PEGylated AnnexinAS is disclosed in WO 02/067857. PEGylation is a method well known to those skilled in the art wherein a polypeptide or peptidomimetic compound (for the purposes of the present invention, the AnxA5 protein) is modified such that one or more polyethylene glycol (PEG) molecules are covalently attached to the side chain of one or more amino acids or derivatives thereof. It is one of the most important molecule altering structural chemistry techniques (MASC). Other MASC techniques may be used; such techniques may improve the pharmacodynamic properties of the molecule, for example extending its half-life in vivo. A PEG-protein conjugate is formed by first activating the PEG moiety so that it will react with, and couple to, the protein or peptidomimetic compound of the invention. PEG moieties vary considerably in molecular weight and conformation, with the early moieties (monofunctional PEGs; mPEGs) being linear with molecular weights of 12kDa or less, and later moieties being of increased molecular weights. PEG2, a recent innovation in PEG technology, involves the coupling of a 30kDa (or less) mPEG to a lysine amino acid (although PEGylation can be extended to the addition of PEG to other amino acids) that is further reacted to form a branched structure that behaves like a linear mPEG of much greater molecular weight (Kozlowski et al., 2001). Methods that may be used to covalently attach the PEG molecules to polypeptides are further described in Roberts et al. (2002) Adv Drug Deliv Rev, 54, 459 476; Bhadra et al. (2002) Pharmazie 57, 5 - 29; Kozlowski et al. (2001) J Control Release 72, 217 - 224; and Veronese (2001) Biomaterials 22, 405 - 417 and references referred to 46 therein. The advantages of PEGylation include reduced renal clearance which, for some products, results in a more sustained adsorption after administration as well as restricted distribution, possibly leading to a more constant and sustained plasma concentrations and hence an increase in clinical effectiveness (Harris et al. (2001) Clin Pharmacokinet 40, 539 551). Further advantages can include reduced immunogenicity of the therapeutic compound (Reddy (2001) Ann Pharmacother, 34,915 - 923), and lower toxicity (Kozlowski et al. (2001), Biodrugs 15, 419 - 429). In the event that the AnxA5 protein is chemically modified, it may be suitable to perform one or more additional purification steps, such as to reduce or remove unreacted components and/or to select a homogenous population of chemically modified AnxA5 protein for inclusion into the final product. Suitable technique for the purification of chemically-modified proteins from the reaction process are known to those skilled in the art.

The final product may be, or may be subsequent formulated to form, a pharmaceutical or veterinary composition.

The final product may be presented in a unit dosage form. For example, a unit dosage form may contain about 1,2,3, 4, 5, 6, 7, 8, 9, 10 mg of the AnxA5 protein (wherein the term “about” refers to + 0.5, 0.4, 0.3, 0.2 or 0.1 mg) or more, e.g. within the range of 0.1 to 1000 mg, or 1 to 100 mg.

A pharmaceutical or veterinary composition may comprise the AnxA5 protein in admixture with a pharmaceutically or veterinarily acceptable adjuvant, diluent or carrier, which will typically be selected with regard to the intended route of administration and standard pharmaceutical practice. The composition may be in the form of immediate-, delayed- or controlled-release applications. Preferably, the formulation is a unit dosage containing a daily dose or unit, daily sub-dose or an appropriate fraction thereof, of the active ingredient.

The phrases “pharmaceutical or veterinary acceptable” include reference to compositions that do not produce an adverse, allergic or other untoward reaction when administered to an animal or a human, as appropriate. The preparation of such pharmaceutical or veterinary compositions are known to those of skill in the art in light of the present disclosure, as exemplified by Remington's Pharmaceutical Sciences, 18th Ed. Mack Printing Company, 1990, incorporated herein by reference. Moreover, for animal or human administration, it will be understood that preparations should meet sterility, pyrogenicity, general safety and purity standards as required by FDA Office of Biological Standards.

As used herein, “pharmaceutically or veterinarily acceptable carrier” includes any and all solvents, dispersion media, coatings, surfactants, antioxidants, preservatives (e.g., antibacterial agents, antifungal agents), isotonic agents, salts, preservatives, drugs, drug stabilizers, excipients, disintegration agents, such like materials and combinations thereof, as would be known to one of ordinary skill in the art. Except insofar as any conventional carrier is incompatible with the active ingredient, its use in the therapeutic or pharmaceutical compositions is contemplated.

The pharmaceutical or veterinary compositions according to the invention may, or may not, be intended for, and, thus formulated in a manner suitable for, parenteral, intravenous, intra-arterial, intraperitoneal, intra-muscular or subcutaneous administration, or administration from a drug-eluting stent, or they may be administered by infusion techniques. Sterile injectable solutions may be prepared by incorporating the active compounds in the required amount in the appropriate solvent with various of the other ingredients enumerated above, as required, followed by sterilization. The pharmaceutical compositions may be best used in the form of a sterile aqueous solution which may contain other substances, for example, enough salts or glucose to make the solution isotonic with blood. The aqueous solutions may be suitably buffered (preferably to a pH of from 3 to 9), if necessary. The preparation of suitable pharmaceutical formulations under sterile conditions is readily accomplished by standard pharmaceutical techniques well-known to those skilled in the art.

A therapeutically effective amount of an AnxA5 protein for administration to a patient, such as a human patient, on the basis of a daily dosage level may be from 0.01 to 1000 mg of AnxA5 protein per adult (for example, from about 0.001 to 20 mg per kg of the patient’s body weight, such as 0.01 to 10 mg/kg, for example greater than 0.1 mg/kg and up to or less than 20, 10, 5, 4, 3 or 2 mg/kg, such as about 1 mg/kg), administered in single or divided doses.

The physician in any event will determine the actual dosage which will be most suitable for any individual patient and it will vary with the age, weight and response of the particular patient. The above dosages are exemplary of the average case. There can, of course, be individual instances where higher or lower dosage ranges are merited and such are within the scope of this invention.

For veterinary use, a compound of the invention is administered as a suitably acceptable formulation in accordance with normal veterinary practice and the veterinary surgeon will determine the dosing regimen and route of administration which will be most appropriate for a particular animal.

I. Product Characteristics

The processes of the present invention provide an AnxA5 product as defined above. As such, the product produced by the claimed process is also a further, fifth, aspect of the present invention.

In a further embodiment, the process of any of the aspects of the present invention may provide a product comprising the AnxA5 protein with a purity suitable for injectable pharmaceutical for use in humans. The process described herein typically removes process related impurities to well below acceptable levels like host cell protein below 20 ng per mg of AnxA5 protein, DNA below 10 pg per mg of AnxA5 protein, and Endotoxins below 1 EU per mg of AnxA5 protein.

In a further embodiment, the process of any of the aspects of the present invention may provide a product comprising host cell protein (other than the recombinantly expressed AnxA5 protein) at a level less than less than 100, 90, 80, 70, 60, 50, 40, 30, 20, 10, 5 ng or less per mg of AnxA5 protein. The FDA and EMA expect host cell protein less than 100 ng/mg and the applicant has demonstrated a host cell protein less than 20 ng/mg.

In a further embodiment, the process of any of the aspects of the present invention may provide a product comprising an endotoxin content of less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20,15, and preferably less than 10, 5 or 1 EU per mg AnxA5 protein, and/or preferably wherein the process provides a product in unit dosage form and the product contains less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20, 15, and preferably less than 10, 5 or 1 EU per unit dose. The FDA and EMA expect endotoxins to be less than 100 EU/dose (the maximum permitted is 350 EU/dose); the expected amount translates to less than 10EU/mg at 10 mg dose. Within these parameters, the unit dosage form may contain about 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 mg of the AnxA5 protein or more (e.g. within the range of 0.1 to 1000 mg, or 1 to 100 mg).

In a further embodiment, the process of any of the aspects of the present invention may provide a product comprising host cell nucleic acid levels of less than 1,000 pg per mg of AnxA5 protein, preferably less than 500 pg per mg of AnxA5 protein, less than 400 pg per mg of AnxA5 protein, less than 300 pg per mg of AnxA5 protein, less than 200 pg per mg of AnxA5 protein, less than 100 pg per mg of AnxA5 protein, less than 50 pg per mg of AnxA5 protein, less than 40 pg per mg of AnxA5 protein, less than 30 pg per mg of AnxA5 protein, less than 20 pg per mg of AnxA5 protein, less than 15 pg per mg of AnxA5 protein, less than 10 pg per mg of AnxA5 protein, less than 9 pg per mg of AnxA5 protein, less than 8 pg per mg of AnxA5 protein, less than 7 pg per mg of AnxA5 protein, less than 6 pg per mg of AnxA5 protein, less than 5 pg per mg of AnxA5 protein, such as about 4 pg per mg of AnxA5 protein.

In a particularly preferred embodiment, the process of any of the aspects of the present invention may provide a product having any one or more characteristics selected from the listed consisting of:

- a concentration of AnxA5 protein typically around 8-12 g/L;

- host cell protein levels at or below 100 ng/mg and more preferably 20 ng/mg(as detemined by ELISA);

host cell DNA levels at or below 100 pg/mg; and more preferably 10 pg/mg

- Endotoxin at or below 35 EU/mg and more preferably 1 EU/mg,

- a purity of > 95% as determined by size-exclusion chromatography;

- a bioburden of < 1 cfu/mL (as determined by Ph. Eur. 2.6.12);

- a clear, colourless appearance free of visible particles; and

- wherein the main band detected by western blot analysis corresponds to the Annexin A5 reference.

A further particularly-preferred embodiment, the AnxA5 protein in the product may have a low level of gluconoylation. “Low” in that context can include then meaning that the level of gluconoylation is less than (such as less than 90%, 80%, 70%, 60%, 50%, 40%, 30%, 20%, 10%, 9%, 8%, 7%, 6%, 5%, 4%, 3%, 2% or 1% of) the level of gluconoylation of an AnxA5 protein that is expressed in E. coli strain BL21 (DE3) (e.g. as is widely commercially-available, and as described in Marder et al., 2014, BMC Biotechnology, 14:33). For example, it maybe that the level of gluconoylated AnxA5 protein in the product is within the range of 0.5 to 30%, or 0.5 to 20%, or 0.5 to 15%, or 0.5 to 10% of the total content of AnxA5 protein in the product. To put it another way, it may be that the level of gluconoylated AnxA5 protein in the product is below 40%, such as below 30%, 20%, 10%, 9%. 8%, 7%, 6%, 5%, 4%, 3%, 2%, or 1%, and preferably substantially 0%.

Accordingly, a fifth aspect of the present invention provides a composition comprising an AnxA5 protein, wherein the composition is the direct, or indirect product of (or is directly or indirectly obtainable by) a process according to any of the first, second, third or fourth aspects of the present invention. Optionally, the composition is a pharmaceutically acceptable and/or veterinarily acceptable composition.

J. Medical and Veterinary Uses

The sixth aspect of the present invention also provides the composition of the fifth aspect of the present invention for use in medicine. To put it another way, the sixth aspect of the present invention provides a method comprising administering to a human or animal in need thereof a therapeutically effective amount of a composition of the fifth aspect of the present invention.

In certain embodiments of the sixth aspect of the present invention, the composition of the fifth aspect of the present invention may be used:

(a) for prevention or reduction of risk of thrombosis (such as atherothrombosis) and/or plaque rupture, or for administration to patients belonging to a risk group, including but not limited to systemic lupus erythematosus (SLE) patients and/or patients who have or have had (or are at risk of) a upper respiratory tract or other infection (including pneumococcal infection) that can cause increased levels of antiphospholipid related antibodies, or to treat (either actively or prophylactically) or reduce the risk of thromboembolism, hemorrhagic or vasculitic stroke, myocardial infarction, angina pectoris or intermittent claudication, unstable angina, other forms of severe angina, or transient ischemic attacks (TIA), for example as further described in WO 2005/099744 (the contents of which are incorporated herein by reference);

(b) for the treatment, prophylaxis or reduction of risk of vascular dysfunction, angina pectoris, ischaemic heart disease, peripheral artery disease, systolic hypertension, migraine, type 2 diabetes and erectile dysfunction, reducing ischemic pain and/or treatment of a vascular disease rupture, for example as described in WO 2009/077764 (the contents of which are incorporated herein by reference);

(c) for the prophylaxis or treatment of restenosis (in particular neointima formation or thickening), vascular inflammation, for example as described in WO 2009/103977 (the contents of which are incorporated herein by reference);

(d) for use in inhibiting the activity of oxidised cardiolipin (oxCL) and for treating, preventing and/or reducing the risk of developing a cardiovascular disease, an auto-immune disease or inflammatory condition, for example as described in WO 2010/069605 (the contents of which are incorporated herein by reference), including but not limited to the following diseases: cardiovascular disease (CVD), diabetes II, Alzheimer’s disease, dementia in general, rheumatic diseases, atherosclerosis, high blood pressure, acute and/or chronic inflammatory conditions, myocardial infarction, acute coronary syndrome, stroke, transient ischemic attack (TIA), claudiction, angina, type I diabetes, rheumatoid arthritis, psoriasis, psoriatic arthritis, ankylosing spondylitis, Reiter’s Syndrome, systemic lupus erythematosus, dermatomyositis, Sjogren’s syndrome, lupus erythematosus, multiple sclerosis, myasthenia gravis, asthma, encephalitis, inflammatory bowel disease, chronic obstructive pulmonary disease (COPD), arthritis including osteoarthritis, idiopathic inflammatory myopathies (IIM), dermatomyositis (DM), polymyositis (PM), inclusion body myositis, an allergic disorder and/or osteoarthritis in a mammal; and (e) for the prevention and/or reduction of peri- or postoperative complications following surgical intervention, such as complications following vascular surgery, especially peripheral vascular surgery, for example as described in WO 2012/136819 (the contents of which are incorporated herein by reference).

In a further embodiment of the sixth aspect of the present invention, the composition of the fifth aspect of the present invention may be used in a prophylactic or therapeutic method of treating, preventing or reducing the risk of haematological disorders, including but not limited to sickle cell anemia.

In a further embodiment of the sixth aspect of the present invention, the composition of the fifth aspect of the present invention may be used in a prophylactic or therapeutic method of (i) preventing, or reducing the rate of, the transmission of a viral infection; (ii) preventing, 52 or protecting against, a viral infection; or (iii) treating a viral infection, in a subject, wherein the viral infection is caused by a virus selected from the group consisting of(a) a virus capable of causing hemorrhagic fever (VHF), and (b) a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

Accordingly, in one further embodiment, the present invention provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method of preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

That is to say, the present invention provides a prophylactic or therapeutic method of preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or therapy by preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

In another embodiment, the present invention provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method of preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

That is to say, the present invention provides a prophylactic or therapeutic method of preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding, the method comprising the administration of a therapeutically effective amount the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or therapy by preventing, or reducing the rate of, the transmission of a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

In another embodiment, the present invention provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method of preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

That is to say, the present invention provides a prophylactic or therapeutic method of preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or therapy by preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

In another embodiment, the present invention provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method of preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

That is to say, the present invention provides a prophylactic or therapeutic method of preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding, the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or therapy by preventing, or protecting against, a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

In another embodiment, the present invention provides the composition ofthe fifth aspect of the present invention for use in a prophylactic or therapeutic method of treating a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

That is to say, the present invention provides a prophylactic or therapeutic method of treating a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or therapy by treating a viral infection, in a subject, wherein the viral infection is caused by a virus capable of causing hemorrhagic fever (VHF).

In another embodiment, the present invention provides the composition ofthe fifth aspect of the present invention for use in a prophylactic or therapeutic method of treating a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

That is to say, the present invention provides a prophylactic or therapeutic method of treating a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding, the method comprising the administration of a therapeutically effective amount ofthe composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for prophylaxis or 55 therapy by treating a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

According to a further embodiment of the present invention, there is provided the composition of the fifth aspect of the present invention for use in a method of treating a subject infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

To put it another way, this embodiment provides a method for treating a subject infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for treating a subject infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

According to another embodiment of the present invention, there is provided the composition of the fifth aspect of the present invention for use in a method of treating a subject that has been in contact with another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

To put it another way, this embodiment provides a method for treating a subject that has been in contact with another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for treating a subject that has been in contact with another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

According to a further embodiment of the present invention, there is provided the composition of the fifth aspect of the present invention for use in a method of treating a subject that has been in contact with biological material present in or produced by another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

To put it another way, this embodiment provides a method for treating a subject that has been in contact with biological material present in or produced by another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF), the method comprising the administration of a therapeutically effective amount of the composition of the fifth aspect of the present invention to the subject.

To put it yet another way, this embodiment provides the composition of the fifth aspect of the present invention for use in the manufacture of a medicament for treating a subject that has been in contact with biological material present in or produced by another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF).

In accordance with these foregoing embodiments of the present invention, the pathogen capable of causing hemorrhagic fever may be a VHF.

The viral hemorrhagic (or haemorrhagic) fevers (VHFs) are a diverse group of animal and human illnesses that may be caused by at least five distinct families of RNA viruses: the families Arenaviridae, Filoviridae, Bunyaviridae, Flaviviridae, and Rhabdoviridae. All types of VHF may be characterized by fever and bleeding disorders and all can progress to high fever, shock and death in many cases.

A subject who is suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a virus capable of causing hemorrhagic fever (VHF) or a bacteria capable of causing hemorrhagic fever (BHF) may be a subject with a history of coming into contact with the disease (e.g. by virtue of their employment as a health worker or due to the infection of a family member) and/or may be a subject that displays one or more signs or symptoms of being infected, prior to confirmatory diagnosis.

Signs and symptoms of VHFs characteristically include fever and increased susceptibility to bleeding (bleeding diathesis). Manifestations of VHF often also include flushing of the face and chest, small red or purple spots (petechiae), frank bleeding, swelling caused by edema, low blood pressure (hypotension), and shock. Malaise, muscle pain (myalgia), headache, vomiting, and diarrhea occur frequently. The severity of symptoms varies with the type of virus, with the “VHF syndrome” (capillary leak, bleeding diathesis, and circulatory compromise leading to shock) appearing in a majority of patients with filovirus hemorrhagic fevers (e.g., Ebola and Marburg), CCHF, and the South American hemorrhagic fevers, but in a small minority of patients with dengue, RVF, and Lassa fever.

In accordance with the sixth aspect of the present invention, the VHF may be Ebola, and subject may display one or more symptoms of Ebola, such as symptoms selected from initial clinical symptoms, such as excessive or profuse sweating, the onset of fever, myalgia, general malaise, and/or chills; and/or flu-like symptoms optionally accompanied by gastro-intestinal symptoms; maculo-papulary rash, petichae, conjunctival hemorrhage, epistaxis, melena, hematemesis, shock and/or encephalopathy; leukopenia (for example, associated with increased lymphoid cell apoptosis), thrombocytopenia, increased levels of aminotransferase, thrombin and/or partial thromboplastin times, fibrin split products detectable in the blood, and/or disseminated intravascular coagulation (DIC).

Definitive diagnosis is usually made at a reference laboratory with advanced biocontainment capabilities. The findings of laboratory investigation vary somewhat between the viruses but in general there is a decrease in the total white cell count (particularly the lymphocytes), a decrease in the platelet count, an increase in the blood serum liver enzymes, and reduced blood clotting ability measured as an increase in both the prothrombin (PT) and activated partial thromboplastin times (PTT). The hematocrit may 58 be elevated. The serum urea and creatine may be raised but this is dependent on the hydration status of the patient. The bleeding time tends to be prolonged.

For example, being a BSL-4 agent, confirmed clinical laboratory diagnosis of viremia during the acute phase of Ebola virus infection is possible with suitable laboratory facilities. The assays that can be utilized are based on the stage of the disease.

During acute disease the assays include a) virus isolation using Vero or Vero E6 cell lines, b) RT-PCR and real time quantitative PCR assays with appropriate false negative and false positive controls, c) antigen capture ELISA, and d) IgM ELISA.

Later during the course of disease the tests that can be utilized include a) IgM and IgG ELISA using authentic viral antigens, and in the case of death, autopsy tissues can be utilized fora) antigen detection using immunostaining techniques, b) immunohistochemical aided detection of Ebola antigen (Zaki etal, J Infect Dis, 1999;179(Suppl. 1):S36e47., the contents of which are incorporated herein by reference in its entirety), and c) in-situ hybridization techniques for the detection of viral RNA.

The details of each of these techniques have been summarized in Saijo et al, Clin Vaccine Immunol 2006;13:444e51, the contents of which are incorporated herein by reference in its entirety.

The ELISA based assay has been standardized by the CDC for the detection of Ebolavirus specific antibodies. The assay has high sensitivity and has been shown to be capable of detecting antibodies in the sera of humans exposed 10 years previously to Ebola. A cellbased plaque assay and an end point titration assay (TCID50) have also been developed to detect and quantitate filoviruses for use in pre-clinical studies (Shurtleff et al, Viruses 2012;4:3511e30; Smither et al, J Virol Methods 2013; 193: 565e71, the contents of which are incorporated herein by reference in their entirety).

For example, the VHF may be a virus in a family selected from Filoviridae, Arenaviridae, Bunyaviridae, Flaviviridae or Rhabdoviridae.

The family Arenaviridae includes the viruses responsible for Lassa fever, Lujo virus, Argentine, Bolivian, Brazilian and Venezuelan hemorrhagic fevers.

The family Bunyaviridae includes the members of the Hantavirus genus that cause hemorrhagic fever with renal syndrome (HFRS), the Crimean-Congo hemorrhagic fever (CCHF) virus from the Nairovirus genus, Garissa virus and llesha virus from the Orthobunyavirus and the Rift Valley fever (RVF) virus from the Phlebovirus genus.

The family Filoviridae includes Ebola virus and Marburg virus.

The family Flaviviridae includes dengue, yellow fever, and two viruses in the tick-borne encephalitis group that cause VHF: Omsk hemorrhagic fever virus and Kyasanur Forest disease virus.

The isolation of a member of the Rhabdoviridae responsible for 2 fatal and 2 non-fatal cases of hemorrhagic fever in the Bas-Congo district of the Democratic Republic of Congo has also been reported. The non-fatal cases occurred in healthcare workers involved in the treatment of the other two, suggesting the possibility of person-to-person transmission.

Accordingly, for example in one embodiment of particular interest, the present invention may be applied to viruses in the family Filoviridae, such as Ebola virus and Marburg virus. In another embodiment of particular interest, the present invention may be applied to viruses in the family Flaviviridae, such as dengue virus.

Accordingly, the present invention provides for the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method as described above, for (i) preventing, or reducing the rate of, the transmission of an Ebola infection; (ii) preventing, or protecting against, an Ebola infection; or (iii) treating an Ebola infection, in a subject infected or suspected of being infected with Ebola virus, or has been or is expected to be in contact with another subject who is infected or suspected of being infected with Ebola virus, or has been or is expected to be in contact with biological material present in or produced by another subject who is infected or suspected of being infected with Ebola virus.

Accordingly, the present invention provides for the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method as described above, for (i) preventing, or reducing the rate of, the transmission of an Marburg infection; (ii) preventing, or protecting against, an Marburg infection; or (iii) treating a Marburg infection, wherein the a subject is infected or suspected of being infected with Marburg virus, or has 60 been or is expected to be in contact with another subject who is infected or suspected of being infected with Marburg virus, or has been or is expected to be in contact with biological material present in or produced by another subject who is infected or suspected of being infected with Marburg virus.

Accordingly, the present invention provides for the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method as described above, for (i) preventing, or reducing the rate of, the transmission of an Dengue fever virus infection;

(ii) preventing, or protecting against, an Dengue fever virus infection; or (iii) treating a Dengue fever virus infection, wherein the subject is infected or suspected of being infected with Dengue fever virus, or has been or is expected to be in contact with another subject who is infected or suspected of being infected with Dengue fever virus, or has been or is expected to be in contact with biological material present in or produced by another subject who is infected or suspected of being infected with Dengue fever virus.

The present invention also provides the composition of the fifth aspect of the present invention for use in a method a described above, for treating, delaying the onset and/or delaying the progression of infection of the subject by the VHF or BHF.

The present invention also provides the composition of the fifth aspect of the present invention for use in a method a described above for preventing, reducing, delaying the onset of, or delaying the progression of, direct and/or indirect bacterial viral damage, as caused by the BHF or VHF, to the immune and/or vascular system in the subject.

For example, the present invention may be used for preventing, reducing, delaying the onset of, or delaying the progression of, direct and/or indirect bacterial or viral damage to the immune system in the subject, for example, in the context of an Ebola infection. For example, the bacterial or viral damage may be selected from damage to the innate immune response, damage to the acquired humoral response, damage to dendritic cells, damage to the regulation of the production of inflammatory factors such as interferon production (including IL1 production), damage to macrophages, and/or damage to monocytes.

The present invention may be used for preventing, reducing, delaying the onset of, or delaying the progression of, blood leakage (haemorrhage), hypotension, drop in blood pressure, shock or death in the subject.

The present invention may be used for preventing, reducing, delaying the onset of, or delaying the progression of, virally-induced nitric oxide damage to the vascular endothelium of the subject.

The present invention provides the composition of the fifth aspect of the present invention for use in a method of prevention, reduction, delaying the onset of, or delaying the progression of, damage, activation, death, and/or disruption to the integrity of, the vascular endothelium or endothelial cells thereof, in a subject infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a VHF or BHF. The integrity of the vascular endothelium or endothelial cells thereof may, for example, be determined by the extent of cellular or vascular epithelial leakage and/or by the detection of one or more haemorrhagic events, or the formation of oedema and/or dehydration of the subject.

The present invention provides the composition of the fifth aspect of the present invention for use in a method of prevention, reduction, delaying the onset of, or delaying the progression of, damage, activation, death, and/or disruption to the integrity of, the vascular endothelium or endothelial cells thereof, in a subject that has been or is expected to be in contact with another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a VHF or BHF.

The present invention provides the composition of the fifth aspect of the present invention for use in a method of prevention, reduction, delaying the onset of, or delaying the progression of, damage, activation, death, and/or disruption to the integrity of, the vascular endothelium or endothelial cells thereof, in a subject that has been or is expected to be in contact with biological material present in or produced by another subject who is infected or suspected of being infected with a pathogen capable of causing hemorrhagic fever, such as a VHF or BHF.

A further embodiment of the present invention provides for the composition of the fifth aspect of the present invention for use as described above by reference to the various embodiments of the present invention in a prophylactic or therapeutic method, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding. Alternatively, the viral infection may be caused by a virus that presents one or more other types of phospholipids that are bound by Annexin A5 and/or other moieties that are bound by Annexin A5.

Viruses that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding can particularly include enveloped viruses comprising phosphatidylserine (PS) in their envelope, especially in the outer layer. The presentation of PS by a virus can be determined by methods known in the art, for example, using an ELISA study to measure the binding of Annexin A5 to the virus. A suitable method can, for example, include the ELISA measurement of haemagglutinin (HA)-tagged Annexin A5 binding to anti-HA antisera, such as described in Moller-Tank, et al, 2013, J. Virol., 87(15), 8327-8341 (the contents of which are incorporated herein by reference).

A group of viruses of particular interest to the present invention includes those which mediate cell infection and/or internalisation through binding with a phosphatidylserinemediated virus entry enhancing receptor (PVEER). PVEERs are discussed in Moller Tank, et al, 2013, J. Virol., 87(15), 8327-8341, and one example thereof is the T-cell immunoglobulin and mucin 1 (TIM-1) receptor. Further examples may include TIM-4, Gas6 or Protein S/Axl, Mer, and Tyro3, and MFG-E8/integrin ανβ3 or ανβ5

Ebola is an example of one virus of particular interest that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding with TIM-1. Moller Tank, etal, 2013, J. Virol., 87(15), 8327-8341.

The present invention recognises that Annexin A5, and the composition of the fifth aspect of the present invention, may be used to inhibit or interrupt the PS-mediated cell infection and/or internalisation of viruses, such as Ebola virus, through PVEERs such as TIM-1, and thereby by can be useful in a prophylactic or therapeutic method of (i) preventing, or reducing the rate of, the transmission of a viral infection; (ii) preventing, or protecting against, a viral infection; or (iii) treating a viral infection, in a subject, wherein the viral infection is caused by a virus that presents phosphatidylserine (PS) and mediates cell infection and/or internalisation through PS binding.

Viruses that presents phosphatidylserine (PS) may, for example, be selected from the group consisting of a virus in the family Filoviridae (such as Ebola and Marburg); the family Flaviviridae', hepatitis A; alpha viruses; baculoviruses; and arena viruses. The viruses may be infectious in, or only in, humans. The viruses may be infectious in, or only in, nonhuman animals, such as any one or more of animals selected from the group consisting of dogs, cats, cattle, sheep, pigs, goats, rodents, camels, domesticated animals, and wild animals.

PVEERs such as TIM-1, can be involved in the internalisation of viruses into various cell types. In one embodiment, cell types of particular interest for protection and/or treatment in accordance with the present invention may include one or more cell types selected from the group consisting of epithelial cells (including vascular epithelial cells), mast cells, Bcells, and T-cells such as CD4+ cells or CD8+ cells and particularly activated CD4+ cells.

TIM-1, also known as HAVCR1 and KIM-1, has been identified as a susceptibility gene for human asthma (McIntire et al, 2003, Nature 425:576). One published amino acid sequence for human TIM-1 protein is shown as:

MHPQVVILSLILHLADSVAGSVKVGGEAGPSVTLPCHYSGAVTSMCWRGSC

SLFTCQNGIVWTNGTHVTYRKDTRYKLLGDLSRRDVSLTIENTAVSDSGVYC

CRVEHRGWFNDMKITVSLEIVPPKVTTTPIVTTVPTVTTVRTSTTVPTTTTVPM

TTVPTTTVPTTMSIPTTTTVLTTMTVSTTTSVPTTTSIPTTTSVPVTTTVSTFVPP MPLPRQNHEPVATSPSSPQPAETHPTTLQGAIRREPTSSPLYSYTTDGNDTVTE SSDGLWNNQTQLFLEHSLLTANTTKGIYAGVCISVLVLLALLGVIIAKKYFF KKEVQQLSVSFSSLQIKALQNAVEKEVQAEDNIYIENSLYATD (SEQ ID NO: 2).

TIM-1 is a type I membrane protein with an extracellular region containing an IgV domain, a mucin-rich domain, and a short membrane-proximal stalk containing N-linked glycosylation sites (Ichimura et al, 1998, J, Biol, Chem. 273(7):4135-42). The TIM-1 IgV domain has a disulfide-dependent conformation in which the CC' loop is folded onto the GFC β strands, resulting in a distinctive cleft formed by the CC' and FG loops (Santiago et al, 2007, Immunity 26(3):299-310). The cleft built by the CC' and FG loops is a binding site for phosphatidylserine (Kobayashi etal, 2007, Immunity27(6):927-40). Antibodies directed to the CC'/FG cleft of the TIM-1 IgV domain inhibit TIM-1 binding to phosphatidylserine and dendritic cells and exhibit therapeutic activity in vivo in a humanized mouse model of allergic asthma (Sonar ef al, 2010, J. Clin. Invest. 120: 2767-81).

A further embodiment of the present invention is based on the use of the composition of the fifth aspect of the present invention to prevent, inhibit or reduce the ability of the IgV domain of TIM-1, and other PVEERs, from binding to PS presented to it The AnxA5 protein in the composition of the fifth aspect of the present invention preferably also has 64 the ability to bind PS and, in accordance with this embodiment of the present invention, is capable of competing with the PVEER to bind to PS.

Accordingly, in one further embodiment, the composition of the fifth aspect of the present invention may be used in a method which inhibits phosphatidylserine binding to TIM-1 (or other PVEER).

For example, this may be prophylactically or therapeutically useful in the context of inhibiting, reducing or preventing the infection of cells with viruses that present phosphatidylserine (PS) and mediate cell infection and/or internalisation through PS.

Alternatively, this may be prophylactically or therapeutically useful in the context of addressing other medical conditions that involve the binding of PS to TIM-1 (or other PVEERs). TIM-1 associated disorders are discussed further below.

Therefore, in another embodiment, the present invention provides a method of inhibiting or reducing binding of TIM-1 or other PVEER, to phosphatidylserine, the method comprising contacting a first cell that expresses TIM-1 or other PVEER with an amount of the composition of the fifth aspect of the present invention effective to inhibit or reduce binding of the first cell to a second cell that contains phosphatidylserine on its cell surface or to a virus that present phosphatidylserine (PS) on its surface. The method may be an in vivo or in vitro method. In the case of an in vivo method, it may be to treat or prevent a condition that involves the binding of PS to TIM-1 or other PVEER.

In other words, this embodiment of the present invention also provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method for inhibiting or reducing the binding of TIM-1 or other PVEER, to phosphatidylserine, in a patient in need thereof.

In another embodiment, the present invention provides a method of inhibiting or reducing binding of PS to a TIM-1 or other PVEER on a dendritic cell, the method comprising contacting a dendritic cell that expresses TIM-1 or other PVEER with an amount of the composition of the fifth aspect of the present invention effective to inhibit or reduce binding of PS to the dendritic cell. The method may be an in vivo or in vitro method. In the case of an in vivo method, it may be to treat or prevent a condition that involves the binding of PS to TIM-1 or other PVEER on a dendritic cell.

In other words, this embodiment of the present invention also provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method for inhibiting or reducing the binding of PS to TIM-1 or other PVEER on a dendritic cell, in a patient in need thereof.

Also disclosed is a method of treating or preventing an inflammatory or autoimmune condition, the method comprising administering to a mammal having an inflammatory or autoimmune condition a pharmaceutical composition comprising a therapeutically effective amount of the composition of the fifth aspect of the present invention.

In other words, this embodiment of the present invention also provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method for preventing, treating or reducing inflammatory or autoimmune condition.

Also disclosed is a method of treating or preventing asthma, the method comprising administering to a mammal having asthma a pharmaceutical composition comprising the composition of the fifth aspect of the present invention.

In other words, this embodiment of the present invention also provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method for preventing, treating or reducing asthma.

Also disclosed is a method of treating or preventing an atopic disorder, the method comprising administering to a mammal having an atopic disorder a pharmaceutical composition comprising a therapeutically effective amount of the composition of the fifth aspect of the present invention. The atopic disorder can be, for example, atopic dermatitis, contact dermatitis, urticaria, allergic rhinitis, angioedema, latex allergy, or an allergic lung disorder (e.g., asthma, allergic bronchopulmonary aspergillosis, or hypersensitivity pneumonitis).

In other words, this embodiment of the present invention also provides the composition of the fifth aspect of the present invention for use in a prophylactic or therapeutic method for preventing, treating or reducing an atopic disorder.

The composition of the fifth aspect of the present invention be used as described herein to treat or prevent a variety of TIM-1 associated disorders, and other PVEER-associated disorders, including immunological disorders, such as inflammatory and autoimmune disorders.

The term treating includes the meaning of administering a substance or composition described herein in an amount, manner, and/or mode effective to improve a condition, symptom, or parameter associated with a disorder or to prevent progression or exacerbation of the disorder (including secondary damage caused by the disorder) to either a statistically significant degree or to a degree detectable to one skilled in the art.

A subject who is at risk for, diagnosed with, or who has one of these disorders can be administered the composition of the fifth aspect of the present invention in an amount and for a time to provide an overall therapeutic effect. The composition of the fifth aspect of the present invention can be administered alone (monotherapy) or in combination with other agents (combination therapy), either in admixture or by separate, simultaneous or sequential administration. In the case of a combination therapy, the amounts and times of administration can be those that provide, e.g., an additive or a synergistic therapeutic effect. Further, the administration of the composition of the fifth aspect of the present invention (with or without the second agent) can be used as a primary, e.g., first line treatment, or as a secondary treatment, e.g., for subjects who have an inadequate response to a previously administered therapy (i.e., a therapy other than one with an AnxA5 protein).

Diseases or conditions treatable with the composition of the fifth aspect of the present invention described herein include, e.g., ischemia-reperfusion injury (e.g., organ ischemiareperfusion injury such as liver or renal ischemia-reperfusion injury), allergy, asthma, inflammatory bowel disease (IBD), Crohn's disease, transplant rejection, pancreatitis, and delayed type hypersensitivity (DTH).

Additional diseases or conditions treatable with the composition of the fifth aspect of the present invention described herein include, e.g., autoimmune disorders.

Systematic lupus erythromatosis (SLE; lupus) is a TH-2 mediated autoimmune disorder characterized by high levels of autoantibodies directed against intracellular antigens such as double stranded DNA, single stranded DNA, and histones.

Examples of other organ-specific or systemic autoimmune diseases suitable for treatment with the composition of the fifth aspect of the present invention described herein include myasthenia gravis, autoimmune hemolytic anemia, Chagas' disease, Graves disease, idiopathic thrombocytopenia purpura (ITP), Wegener's Granulomatosis, poly-arteritis Nodosa and Rapidly Progressive Crescentic Glomerulonephritis. See, e.g., Benjamini et al.,1996, Immunology, A Short Course, Third Ed. (Wiley-Liss, New York). In addition, rheumatoid arthritis (RA) is suitable for treatment with Annexin A5 as described herein.

Additional TIM-1 associated diseases or conditions treatable with the composition of the fifth aspect of the present invention described herein include, e.g., Graft-Versus Host Disease (GVHD). GVHD exemplifies a T cell-mediated condition that can be treated using Annexin A5 described herein. GVHD is initiated when donor T cells recognize host antigens as foreign. GVHD, often a fatal consequence of bone marrow transplantation (BMT) in human patients, can be acute or chronic. Acute and chronic forms of GVHD exemplify the development of antigen specific Th1 and Th2 responses, respectively. Acute GVHD occurs within the first two months following BMT, and is characterized by donor cytotoxic T cell-mediated damage to skin, gut, liver, and other organs. Chronic GVHD appears later (over 100 days post-BMT) and is characterized by hyperproduction of immunoglobulin (Ig), including autoantibodies, and damage to the skin, kidney, and other organs caused by Ig-deposition. Nearly 90% of acute GVHD patients go on to develop chronic GVHD. Chronic GVHD appears to be a Th2 T cell mediated disease (De Wit et al, 1993, J. Immunol. 150:361-366). Acute GVHD is a Thl mediated disease (Krenger et al, 1996, Immunol. Res. 15:50-73; Williamson et al, 1996, J. Immunol. 157:689-699). T cell cytotoxicity is a characteristic of acute GVHD. The consequence of donor anti-host cytotoxicity can be seen in various ways. First, host lymphocytes are rapidly destroyed, such that mice experiencing acute GVHD are profoundly immunosuppressed. Second, donor lymphocytes become engrafted and expand in the host spleen, and their cytotoxic activity can be directly measured in vitro by taking advantage of cell lines that express the host antigens that can be recognized (as foreign) by the donor cells. Third, the disease becomes lethal as additional tissues and cell populations are destroyed.

Additional TIM-1 associated diseases or conditions treatable with the composition of the fifth aspect of the present invention described herein include, e.g., atopic disorders. Atopic disorders are characterized by the expression by immune system cells, including activated T cells and APC, of cytokines, chemokines, and other molecules which are characteristic 68 of Th2 responses, such as the IL-4, IL-5 and IL-13 cytokines, among others. Such atopic disorders therefore will be amenable to treatment with the composition of the fifth aspect of the present invention as described herein. Atopic disorders include airway hypersensitivity and distress syndromes, atopic dermatitis, contact dermatitis, urticaria, allergic rhinitis, angioedema, latex allergy, and an allergic lung disorder (e.g., asthma, allergic bronchopulmonary aspergillosis, and hypersensitivity pneumonitis).

Additional TIM-1 associated diseases or conditions treatable with the composition of the fifth aspect of the present invention as described herein include, e.g., numerous immune or inflammatory disorders. Immune or inflammatory disorders include, but are not limited to, allergic rhinitis, autoimmune hemolytic anemia; acanthosis nigricans; Addison's disease; alopecia areata; alopecia universalis; amyloidosis; anaphylactoid purpura; anaphylactoid reaction; aplastic anemia; ankylosing spondylitis; arteritis, cranial; arteritis, giant cell; arteritis, Takayasu's; arteritis, temporal; ataxia-telangiectasia; autoimmune oophoritis; autoimmune orchitis; autoimmune polyendocrine failure; Behcet's disease; Berger's disease; Buerger's disease; bronchitis; bullous pemphigus; candidiasis, chronic mucocutaneous; Caplan's syndrome; post-myocardial infarction syndrome; postpericardiotomy syndrome; carditis; celiac sprue; Chagas's disease; Chediak-Higashi syndrome; Churg-Strauss disease; Cogan's syndrome; cold agglutinin disease; CREST syndrome; Crohn's disease; cryoglobulinemia; cryptogenic fibrosing alveolitis; dermatitis herpetifomis; dermatomyositis; diabetes mellitus; Diamond-Blackfan syndrome; DiGeorge syndrome; discoid lupus erythematosus; eosinophilic fasciitis; episcleritis; drythema elevatum diutinum; erythema marginatum; erythema multiforme; erythema nodosum; Familial Mediterranean fever; Felty's syndrome; pulmonary fibrosis; glomerulonephritis, anaphylactoid; glomerulonephritis, autoimmune; glomerulonephritis, post-streptococcal; glomerulonephritis, posttransplantation; glomerulopathy, membranous; Goodpasture's syndrome; granulocytopenia, immune-mediated; granuloma annulare; granulomatosis, allergic; granulomatous myositis; Grave's disease; Hashimoto's thyroiditis; hemolytic disease of the newborn; hemochromatosis, idiopathic; Henoch- Schoenlein purpura; hepatitis, chronic active and chronic progressive; histiocytosis X; hypereosinophilic syndrome; idiopathic thrombocytopenic purpura; Job's syndrome; juvenile dermatomyositis; juvenile rheumatoid arthritis (Juvenile chronic arthritis); Kawasaki's disease; keratitis; keratoconjunctivitis sicca; Landry-Guillain-Barre-Strohl syndrome; leprosy, lepromatous; Loeffler's syndrome; lupus; Lyell’s syndrome; lyme disease; lymphomatoid granulomatosis; mastocytosis, systemic; mixed connective tissue disease; mononeuritis multiplex; Muckle-Wells syndrome; mucocutaneous lymph node syndrome; 69 mucocutaneous lymph node syndrome; multicentric reticulohistiocytosis; multiple sclerosis; myasthenia gravis; mycosis fungoides; necrotizing vasculitis, systemic; nephrotic syndrome; overlap syndrome; panniculitis; paroxysmal cold hemoglobinuria; paroxysmal nocturnal hemoglobinuria; pemphigoid; pemphigus; pemphigus erythematosus; pemphigus foliaceus; pemphigus vulgaris; pigeon breeder's disease; polyarteritis nodosa; polymyalgia rheumatic; polymyositis; polyneuritis, idiopathic; Portuguese familial polyneuropathies; pre-eclampsia/eclampsia; primary biliary cirrhosis; progressive systemic sclerosis (scleroderma); psoriasis; psoriatic arthritis; pulmonary alveolar proteinosis; pulmonary fibrosis, Raynaud's phenomenon/syndrome; Reidel's thyroiditis; Reiter's syndrome, relapsing polychrondritis; rheumatic fever; rheumatoid arthritis; sarcoidosis; scleritis; sclerosing cholangitis; serum sickness; Sezary syndrome; Sjogren's syndrome; Stevens- Johnson syndrome; Still's disease; subacute sclerosing panencephalitis; sympathetic ophthalmia; systemic lupus erythematosus; yransplant rejection; ulcerative colitis; undifferentiated connective tissue disease; urticaria, chronic; urticaria, cold; uveitis; vitiligo; Weber-Christian disease; Wegener's granulomatosis, or Wiskott-Aldrich syndrome.

The present invention will now be described with reference to one or more non-limiting examples.

EXAMPLES

The following examples are included to demonstrate particular embodiments of the invention. It should be appreciated by those of skill in the art that the techniques disclosed in the examples which follow represent techniques discovered by the inventor to function well in the practice of the invention, and thus can be considered to constitute preferred modes for its practice. However, those of skill in the art should, in light of the present disclosure, appreciate that many changes can be made in the specific embodiments which are disclosed and still obtain a like or similar result without departing from the spirit and scope of the invention.

Comparative Example 1

The process of Marder et al., 2014, BMC Biotechnology, 14:33 reports on the processing of 1L cultures and consists of two 38,900 g centrifugations of 30 minute duration, which in the first centrifugation step precipitate the Annexin A5 bound to cell debris, and in the 70 second centrifugation step precipitate the cell debris while keeping the Annexin A5 in solution.

The following analysis is provided to calculate the implications of scaling up the process of Marder et al., from 1L to the commercially-relevant culture volume of 1000L.

Based on a selection of the best centrifuges currently available with the best rotors for maximal throughput, they can take 6x250 ml = 1.5 liter and can achieve 30,200-38,400 g. Examples are expensive carbon fiber lightweight rotor (Fiberlite F14-6 x 250y Fixed-Angle Rotor) for use in Thermo Scientific™ Sorvall™ LYNX superspeed centrifuges or the JLA16.250 Rotor, Fixed Angle, Aluminum, Biosafety Lid, 6 x 250 mL, 38,400 x g for use in Beckmancoulters Avanti JXN-26. Using such high-end advanced centrifuges, to load the centrifuge, start and accelerate to the required speed, spend 30 minutes at maximum Gforce and then allowing for careful breaking to a standstill so as not to disturb the pellet, then emptying the rotor would take about 45 min.

That is, the best centrifuges currently available allow the processing of 1.5 liter per 45 min.

Marder et al. reports (in the section entitled “Purification) that 3 g of wet weight of the cells were suspending in 30 mL of buffer before sonication and centrifugation. Accordingly, the wet cell weight (WCW) concentration used by Marder etal., during the centrifugations was (3 gram into 30 ml buffer) = 9.1 % WCW.

Marder et al. (under the heading “Bioreactor cultivation” on second page) also reports a mean value of 27.48 g (DCW) L^_1 (SD = 1.96) for the biomass concentration. Therefore, the dry cell weight (DCW) concentration in Marder’s fermenter was 27.48 gr/L = 2.748 %. It is known that 1 gram DCW = about 4 gram Wet Cell Weight (WCW). Therefore, in the cell concentration fermenter there was a WCW concentration of 2.748 x 4 = 11.0 %. If one scales this up to a WOOL culture volume, and make a conservative assumption of 5 % cell loss during harvest from 1000 L, then the WCW in a WOOL tank using Marder’s method would = WOO x 11 % x 0.95 = 104.5 kg WCW.

Marder’s centrifugation method used a 9.1% WCW concentration during the centrifugation step. Therefore, 104.5 kg WCW from a WOOL culture would need to be diluted to a 9.1 % WCW concentration, which requires a total volume to be centrifuged of 1148 L.

Making the generous assumption that a bio-manufacturing facility has two high-end advanced centrifuges, so that one can be used for pelleting the Annexin with cell debris (first centrifugation), while the other can work in parallel with the second centrifugation when the Annexin is in solution and the cell debris is pelleted then:

Total time for centrifuging the 1148 L solution is, wherein the centrifuges can process 1.5 liter per 45 min = 1148/1.5 = 766 centrifugations at 45 min each = 34,470 min = 574,5 hours.

Assuming that the bio-manufacturing facility operated 12 hours per day, then the processing of the WCW from a WOOL tank using the method of Marder et al will take 48 days of work, or (assuming five working days per week) 10 weeks just for the centrifugations.

In total, approximately an additional two weeks would be needed for fermentation, downstream processing and other operations. This give 12 weeks in manufacturing plant to prepare and process the cells from a WOOL culture, assuming that the biomanufacturing facility is fully occupied with that one process, and so no other production can occur in the same facility meanwhile. This is despite the generous assumption that two centrifuges are available. If only one centrifuge is used, the manufacturing time would be 22 weeks for one WOOL batch.

In contrast, as discussed below, the methods of the present invention can process a WOOL culture in just two weeks, i.e. around 6-times quicker (and, also provide a far higher quality product, with a far higher yield, than the product of the Marder et al. process).

The manufacturing cost is direct proportional to the manufacturing time as the manufacturing plant will be occupied and no other production can occur in the same plant meanwhile.

The yield of Annexin A5 in the process of the present invention is calculated to be 2-3 times higher per batch than the product produced by Marder et al. This makes the manufacturing cost per gram Annexin A5 protein between (6x2-3 =) 12-18 times higher for the Marder process.

Furthermore, the purity of the protein from the Marder process would not be suitable for human use. Despite elaborate centrifugations, only one anion exchange chromatography step is used which is far below the requirements to reach sufficient purity with regards to both in-process related impurities (especially endotoxin) and product related variants.

Marder does not show any data on endotoxin levels or other impurities further indicating lack of suitability for pharmaceutical use.

In addition, the very slow centrifugation operations of the Marder process require the Annexin A5 protein to be in an unstable environment for long period of time. This is likely result in product degradation or product modification, and is a further drawback of long manufacturing operation time, with negative implications for product quality.

Example 1

Abbreviations:

AP	Aqua Purificata (purified water)	NF	national formulary
BV	Bovenau	NL	norm litre
clEF	capillary isoelectric focussing	NMWCO	Nominal molecular weight cut-off
CX	Cation Exchange Chromatography	n.p.	not performed
CFU	colony forming unit	n.s.	not specified
CR	Column Room	OD	optical density
CRG	Column Room Grade	PAGE	Poly Acrylamide Gel Electrophoresis
CV	Column Volume	PBS	Phosphate buffer saline
DF	Diafiltration	PC	polycarbonate
DP	Drug Product	PETG	polyethylene terephthalate copolyester, glycol modified
DSP	Downstream Process	PES	Polyethersulfone
DS	Drug Substance	Ph.Eur.	European Pharmacopoeia
EU	Endotoxin units	PP	polypropylene
EVA	ethylene vinyl acetate copolymer	PPG	polypropylene glycol
EVOH	Ethylene vinyl ethanol copolymer	PVDF	Polyvinylidene Fluoride
FF	forward flow test / diffusion test	QA	Quality Assurance Department
FIO	For Information Only	QC	Quality Control Department
g	gram	RHB	Richter-Helm BioLogics
h	hours	RPC	Reversed Phase Chromatography
H	Hanover	rpm	rotation per minute
HCP	Host Cell Protein	RT	Room Temperature (20 25 °C)

HH	Hamburg	SDS	Sodium Dodecyl Sulphate
ID	inner diameter	SEC	Size Exclusion Chromatography
IEX	Ion Exchange Chromatography	TFF	Tangential Flow Filtration
IPC	In-Process Control	TMP	Trans Membrane Pressure
L	Litre	UF	Ultrafiltration
LAF	Laminar Air Flow	USP	Upstream Process
LDPE	Low-density Polyethylene	LISP	US Pharmacopoeia
MCB	Master cell bank	v/v	Volume per Volume
min	minutes	WB	western blot
MRS	master reference standard	WCB	Working Cell Bank
n. a.	not applicable	WFI	Water for Injection

Introduction:

The 320 amino acid containing recombinant ~36 kDa protein Annexin A5 is expressed in the cytoplasm of the E. coli BL21/pHIP.ANXA5. Recombinant Annexin A5 is produced mainly in its soluble form. A heat inducible expression plasmid pHIP, carrying the coding sequence for Annexin A5, is used. Selective marker is a kanamycin resistance gene. A MCB of the respective clone has been established and extensively characterized.

The manufacturing process is scaled-up from lab scale equivalent to 3 L fermentation volume to large scale equivalent to 100 L fermentation volume.

The developed process includes an efficient anion exchange capture from crude lysate followed by an affinity step on immobilized heparin in the presence of calcium. This intermediate affinity step is highly specific for Annexin A5. As final polishing step a high resolution anion exchange chromatography is used. The polishing step allows a separation of product related impurities. Formulation is conducted by ultra-diafiltration using a 10 kDa NMWCO cassette.

This example describes and evaluates the planned adaptations/changes in the manufacturing process, determines operational parameters and necessary measures to assure a successful transfer and defines acceptance criteria to determine its success. A successful transfer is shown by the performance of a downstream process run implementing the adaptations to the lab scale procedure with respect to scale-up resulting in DS of comparable yield and quality.

The overall project objective is the development of a cGMP manufacturing process for Annexin A5.

Procedure - Process Comparison and Evaluation

In this section the process parameters, raw materials, consumables, buffers and equipment used are evaluated.

Figure 2 shows a schematic overview of the complete process for manufacturing of Annexin A5.

Table 1 compares and evaluates the raw materials used by the 3L and 100 L processes.

Table 1: Comparison of raw materials used by 3L and 100 L processes

	3 L process	100 L process
Raw material	Supplier	Quality	Supplier	Quality
Tris (hydroxymethyl) aminomethane (Tris)	Merck	Ph.Eur.	Merck	Ph.Eur.
Magnesium chloride heptahydrate	Merck	Ph.Eur.	Merck	Ph.Eur.
Sodium chloride	Merck	Ph.Eur.	Merck	Ph.Eur.
Tween-80 (polysorbate)	Merck	Ph.Eur.	Merck	Ph.Eur.
Sodium hydroxide	Merck	Ph.Eur.	Merck	Ph.Eur.
Benzonase Nuclease	Merck/Novagen	Purity > 90%	Merck	Purity > 90%
CaCI2x2H2O	Merck	Ph.Eur.	Merck	Ph.Eur.
Titriplex III	Merck	Ph.Eur.	Merck	Ph.Eur.
Bis-Tris 1,3- bi s [tri s( Hyd roxy m eth yl )methylaminojpropane	Merck	Ultrol grade	Sigma	BioUltra
Water	RHB HH	Bidest/Ampuv a (Fresenius)	Fresenius Biochrom	Ph.Eur.
Ethanol	Merck	Em prove	Merck	EMSURE® ACS, ISO
Hydrochloric acid	Merck	Emprove exp.Ph.Helv	Merck	p.A.
ortho-Phosphoric acid	Merck	Emprove exp.Ph.Eur	Merck	Ph.Eur.
Sodium hydroxide 33%	Reher&Ramsd en	n.a.	—	—

Table 2 compares and evaluates the consumables used by the 3L and 100L processes. The consumables (sampling devices, and tubing) should not have an impact on the product quality and yield of the DSP process. All materials used fulfil the required specification.

Table 2: List of consumables

	3 L process	100 L process
Consumable	Supplier	Quality	Supplier	Quality
Depth Filter Cuno SP 60	3M, CUNO	USP class VI	3M, CUNO	USP class VI
Q Sepharose XL (AX Resin)	GE Healthcare	Manufacturers monograph	GE Healthcare	Manufacturers monograph
Heparin HyperD M (AF Resin)	Pall	Manufacturers monograph	Pall	Manufacturers monograph
Sou reel 5 Q (AX Resin)	GE Healthcare	Manufacturers monograph	GE Healthcare	Manufacturers monograph
0.2 pm Filter Sarto pore 2 0.45-0.2 pm	Sartorius	USP class VI	Sartorius	USP class VI
0.2 pm Filter EKV, Supor	Pall	USP class VI	Pall	USP class VI
UF/DF cassette, Hydrosart, 10kDa Membrane	Sartorius	USP class VI	Sartorius	USP class VI

General remarks:

• All consumables used are single-use or product-dedicated materials.

· Bags used for buffer storage and as an intermediate product container are from

Sartorius with an PE/EVOH layer (CX5-14 film) throughout the process. Bags validated by the manufacturer with respect to e.g. sterility, low Endotoxin as well as leachables and extractables.

• All other consumables used including materials with product contact such as tubing, connectors, sampling systems or sample containers are fit for purpose at the respective step of the process. This includes usually a USP class VI certification, sterility and / or low Endotoxin if applicable. Platinum-cured silicone tubing is used throughout the DSP, except C-Flex tubing preassembled to the bags. All consumables used are animal derived component free ora TSE certificate is available.

Table 3 compares the equipment used by the 3L and 100 L processes for manufacturing of Annexin A5.

Table 3: List of equipment used

	3 L process	100 L process
Equipment	Type	Manufacturer	Type	Manufacturer
Thermometer	n.a.	Hanna	>0-100 °C	Amarell
Pipet	n.a.	Eppendorf	different	Eppendorf
Pump	n.a.	Watson Marlow	604 U/R	Watson Marlow
Pump	n.a.	Watson Marlow	505DU	Watson Marlow
Pump	n.a.	n.a.	1000S	QuattroFlow
LPLC-system 1	Akta 100	GE Healthcare	BioProcess	GE Healthcare
Capture Column	XK 50	GE Healthcare	BPG300	GE Healthcare
Intermediate Column	XK 50	GE Healthcare	BPG300	GE Healthcare
Polishing Column	FineLine 70	GE Healthcare	Fineline20 0	GE Healthcare
Ultrafiltration system	n.a.	n.a.	UFDF-H1	PALL
Photometer	Ultrospec 3100	GE Healthcare	Ultrospec x300	GE Healthcare
pH-/conductivity Meter+Printer	MPC227	Mettler-Toledo	CG HI 730P	Schott Hanna WTW
Laminar air flow cabinet (LAF)	n.a.	Herasafe	HS	Herasafe
Magnet Stirrer	n.a.	IKA	RET/REO	IKA
Vacuum Pump	n.a.	KNF	-	-

	3 L process	100 L process
Equipment	Type	Manufacturer	Type	Manufacturer
Filter integrity testing device	n.a.	n.a.	AquaWIT Exacta	PALL Millipore

Media, buffers and solutions as shown in Table 4. Specifications of buffers are adapted only with respect to conductivity and based on test buffer preparations. Buffers are prepared before the process, tested according their specification, microfiltrated (0.2 pm filter) and stored (holding time s 3 months at RT). Sampling of buffers (as reference; analysis; Endotoxin, Bioburden) are performed at the time point of use.

Table 4: List of Media and solutions

	3L process	100 L process
Buffer	Composition	Application	Composition
homogenisation buffer 1	50 mM Tris; pH 7.4,1 mM MgCl2; 1% Tween80	Homogenisation	50 mM Tris; pH 7.4, 1 mM MgCl2; 1% Tween80
Conditioning post homogenisation buffer 1	1% Tween80 (w/v)	Capture	1 % (v/v) Tween 80, 4 mM EDTA, pH 8,0
Conditioning post homogenisation buffer 2	0.5 M EDTA	Capture
AX buffer A	20mM Tris, 25mM NaCI, 0.1% Tween80, pH 7.4	Capture	20mM Tris, 25mM NaCI, 0.1% Tween80, pH 7.4
AX buffer B	20mM Tris, 300mM NaCI, 0.1%Tween80, pH 7.4	Capture	20mM Tris, 300mM NaCI, 0.1% Tween80, pH 7.4
AX CIP1	2M NaCI	Capture	2M NaCI
AX CIP2	1M NaOH	Capture	1M NaOH
AF buffer A	20mM Tris, 25mM NaCI, 2mM CaCl2, 0.1% Tween80, pH 7.4	Intermediate	20mM Tris, 25mM NaCI, 2mM CaCb, 0.1% Tween80, pH 7.4
AF buffer wash	20mM Tris, 25mM NaCI, 0.1% Tween80, pH 7.4	Intermediate	20mM Tris, 25mM NaCI, 0.1% Tween80, pH 7.4
AF buffer B	20mM Tris, 10mM EDTA, 25mM NaCI, 0.1% Tween80, pH 7.4	Intermediate	20mMTris, 10mM EDTA, 25mM NaCI, 0.1% Tween80, pH 7.4
AF CIP 1	50mM Tris, 2M NaCI, pH 7.4	Intermediate	50mM Tris, 2M NaCI, pH 7.4
AF	0,1 M NaOH	Intermediate	0,1 M NaOH

	3L process	100 L process
Buffer	Composition	Application	Composition
CIP2
AF Storage	25% EtOH, 1M NaCI	Intermediate	25% EtOH, 1M NaCI
AX 2 conditioning	35mM Tris, 0.1% Tween80, 12.5mM MgClz, pH 8.0	Polishing	35mM Tris, 0,1% Tween80, 12.5mM MgClz, pH 8.0
AX buffer A	20mM Bis-Tris, 25mM NaCI, pH 7.4	Polishing	20mM Bis-Tris, 25mM NaCI, pH 7.4
AX buffer B	20mM Bis-Tris, 180mM NaCI, pH 7.4	Polishing	20mM Bis-Tris, 180mM NaCI, pH 7.4
UF/DF buffer	20 mM Bis-Tris, 150 mM NaCI, 1 mM CaCL, pH 7.0	Formulation	20 mM Bis-Tris, 150 mM NaCI, 1 mM CaCL, pH 7.0
Conditioning post UF/DF	10% Tween80, 20 mM Bis- Tris, 150 mM NaCI, 1 mM CaCL, pH 7.0	Formulation	10% Tween80, 20 mM Bis- Tris, 150 mM NaCI, 1 mM CaCL, pH 7.0

A scalable fed batch fermentation process was developed and scaled-up in the production unit. The downstream purification process includes three chromatography steps. Post Benzonase treatment the filtered and diluted feed stream is applied to AX chromatography (Q Sepharose XL, GE Healthcare) as the first capture step. The eluate is conditioned by dilution to allow an intermediate purification by means of affinity chromatography (Heparin Hyper D M, Pall). The AF pool is diluted and applied to a final AX chromatography step (Source15 Q, GE Healthcare). Finally a concentration and buffer change is conducted by UF/DF.

A successful pilot run was carried out at DSP equivalent to 3 L fermentation volume to demonstrate adequate process performance for all process steps.

Target ranges were defined by the small scale process, and are used to evaluate the result of the scale up.

Comparison of Process

In the following sections the lab scale downstream process (DSP) is described in detail based on a pilot run performed at process scale equivalent to 3 L fermentation volume. Generally, besides the loading to the first capture, the chromatographic steps are performed at lab scale with an Aekta Explorer system. In large scale all chromatographic steps are conducted with a Bioprocess system. The up scaling factor for the DSP is 33 (from 3 Lusp to 100 Lusp).

1.1.1 Resuspension of biomass, Benzonase treatment and cell disruption

Post fermentation the biomass is harvested by centrifugation and stored at -20°C. Downstream processing starts with the thawing of the biomass and the resuspension in homogenisation buffer 1. Prior homogenization Benzonase, pre-diluted in homogenisation buffer (3.300 U/Lusp or 1.850 U/L_resus_Pended biomass), is added to the resuspended cells. The resuspension ratio is set to 1g biomass/10 mL. Homogenization is performed in three cycles with 600 bar to reach a high degree of homogeneity which is beneficial for the following capture step. No active cooling is needed within homogenization as an elevated temperature of up to 40°C is desired to allow an optimal digestion of nucleic acids with

Benzonase. In small scale temperatures ranging from 36-40°C were obtained.

A process flow chart for resuspension of biomass, Benzonase treatment and cell disruption is shown below:

Process Step

Parameter

3 L process

100 L process

Resuspension for homogenisation	Buffer:	50 mM Tris; pH 7.4, 1 mM MgCI2; 1% Tween80	50 mM Tris; pH 7.4, 1 mM MgCI2; 1%Tween80
	Buffer temperature:	RT	RT
▼	Ratio:	1g/10 mL	1g/8-10 mL
Addition of Benzonase	Benzonase (stock 25 U/pL):	1.850 U/Lres biomass	3.300 U/Lusp
▼	Pre-dilution in homogenisation buffer:	In 1/10 of the final resuspension volume	In 1 L resuspension buffer
High pressure homogenization	Pressure:	600 bar	600 bar
▼	Cycles:	3	3
Storage of	Conditions:	Ambient temperature	Ambient temperature

homogenate

1.1.2 Clarification, Conditioning and Capture Chromatography

Subsequent to homogenization the lysate is clarified by filtration using a Cuno 60 SP (0.60.2 pm) depth filter. This step is conducted to reduce the content of nucleic acids additionally and to obtain a particle reduced solution which can be applied to capture chromatography. The depth filter is pre-washed with water according to the manufacturer’s instructions.

Post filtration the lysate is diluted 2-fold with 1% Tween80. EDTA is added to a final concentration of 2 mM.

This conditioned pool is applied offline, with a peristaltic pump, to AX capture chromatography. The AX capture column is equilibrated with two column volumes (CV) (20 mM Tris pH 7.4, 0.1 % Tween80, 25 mM NaCI) at a linear pump rate of 200 cm/h.

Post loading the column is washed offline with equilibration buffer for 5 CV and subsequently transferred to the chromatography system to do additional 5 CV of washing. The Annexin A5 elution is conducted with a step elution for 9 CV using a higher salt concentration (20 mM Tris pH 7.4; 0.1 % Tween80; 300 mM NaCI). Fractionation is defined from the raising of the UV₂₈o_nm signal by 0.1 absorption unit (AU) to 0.2 AU in the descending peak. The whole elution peak is further processed.

A two-step CIP procedure is carried out to regenerate and clean the column (Step 1: 2 M NaCI for 3 CV 100 cm/h; upflow / Step 2: 1 M NaOH, 3 CV; incubation for >15 h, 40 cm/h upflow). The column is finally stored in 20 mM of NaOH.

Figure 3 provides a process flow chart for AX capture chromatography.

Generally the capture step can be considered as a conditioning step to enhance the performance of the intermediate step. It concentrates the product and significantly changes the matrix of the load. Moreover a strong reduction of endotoxin (by about 97%) and a moderate reduction of DNA and HCP was observed.

1.1.3 Intermediate - Affinity Chromatography

The obtained AX elution pool (250 mL/Lusp) is filtered (Sartopore2 0.45-0.2 pm) prior intermediate chromatography.

The filtered AX pool is subsequently 8-fold diluted (dilution buffer: 20 mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCb). The dilution with calcium allows Annexin A5 to bind to the immobilized Heparin chromatography. This interaction is, by comparison with an ionic interaction, slow. The contact time is critical and therefore the chromatography is performed with < 100 cm/h.

Two washing steps are conducted. Washing step 1 is conducted for 15 CV (20 mM Tris pH 7.4; 0.1 % Tween80; 2 mM CaCb) and is followed by a second washing step for 2 CV with buffer not containing calcium (20 mM Tris pH 7.4; 0.1 % Tween80).

The elution is performed with a step elution using a buffer containing EDTA (20 mM Tris pH 7.4; 0.1 % Tween80; 10 mM EDTA; 25 mM NaCI) which chelates the calcium ions. The chelating reaction specifically elutes Annexin A5 which can only bind to Heparin in the presence of calcium. To allow a concentrated elution the flow rate was reduced to < 60 cm/h in the elution. The complete elution peak is collecting starting from the rising of the UV signal at 0.05 AU to 0.05 AU in the descending peak representing approximately 7 CV. The elution profile demonstrates a single sharp peak.

A two-step CIP procedure is carried out to regenerate and clean the column (Step 1: 2 M NaCI for 3 CV 100 cm/h; upflow / Step 2: 0.1 M NaOH, 3 CV; incubation for >15 h, 40 cm/h upflow). The column is finally stored in 1 M NaCI in 25% EtOH.

Figure 1 shows the process flow chart for Intermediate Affinity Chromatography.

The intermediate step is the most powerful purification step in the process scheme. Annexin A5 binds to calcium ions. In this calcium bound state the product can form a highly specific bond with Heparin. Only correctly folded Annexin A5 forms that have the ability to complex with calcium can bind to Heparin. Thereby the chromatographic step can discriminate between correctly folded and misfolded product. Additionally the intermediate step reaches high depletion factors as the highly specific interaction is combined with a 84 specific elution mode by the chelate reaction of calcium with EDTA. Therefore a strong reduction of endotoxin (a further approximately 99% reduction) and HCP is observed combined with a moderate reduction of the DNA content.

The combined endotoxin reducing effect of the first AX capture step (about 97%) and the intermediate affinity chromatography step (about 99%) provides an Annexin A5 product in which endotoxin levels are reduced to about 0.03% of the levels in the clarified product prior to the first AX step.

1.1.4 Polishing - AX Chromatography

The obtained AF elution pool (300 mL/Lusp) is 2-fold diluted (35 mM Tris pH 8; 0.1 % Tween80; 12.5 mM MgCL) and filtered (Sartopore2 0.45-0.2 pm) prior polishing chromatography. The dilution reduces the conductivity of the AX load but also complexes free EDTA molecules with Mg-ions. Otherwise the free EDTA is bound to the column thereby reducing mainly capacity but also the separation in this step.

The polishing resin is Source15 Q with an average resin diameter of 15 pm. It is a high resolution polishing resin having the disadvantage of a high back pressure. Therefore the chromatography is performed with 100 cm/h. The loading should be <16 g/L resin to allow an appropriate resolution.

Washing after loading is conducted with buffer A (20 mM Bis-Tris pH 7; 25 mM NaCI) for 3 CV. The elution is performed using a linear gradient to 100 % B (20 mM Bis-Tris pH 7; 180 mM NaCI) in 33 CV. This chromatographic step is mainly designed for the removal of product related impurities. Different forms of Annexin A5 elute from 40-100% B starting with a main peak, a second reduced peak and several smaller peak which follow.

The first major peak starting at 0.05 AU to the valley between peak 1 and peak 2 representing approximately 7 CV is collected.

A two-step CIP procedure is carried out to regenerate and clean the column (Step 1: 2 M NaCI for 3 CV 100 cm/h; up-flow / Step 2: 1 M NaOH, 3 CV; incubation for >15 h, 40 cm/h up-flow). The column was finally stored in 25 mM NaCI.

Recent results obtained in small scale experiments indicated positive effects of Tween80. A process conducted with 0.1 % Tween80 increased the product yield post intermediate by approximately 30%. The loading on the polishing step is limited to 16 g/L resin to ensure an appropriate resolution. The improvement in yield has also an impact on the upscaling scenario. The calculated column dimension in the polishing step was planned with two cycles. The increased yield makes a 4-5 cycle scenario necessary, if total amount from 100 Lusp scale is processed.

Figure 2 shows the process flow chart for the AX Polishing Chromatography step.

The polishing step is mainly implemented for the reduction of product related impurities e. g. the separation of different Annexin A5 isoforms. Additionally the polishing step reaches the highest depletion factor in the process for the residual DNA and strongly reduces HCP. Endotoxin, being already at a low level after the intermediate step, is further reduced by about 99%, which takes the endotoxin levels to about 0.0003% of the levels in the clarified product prior to the first AX step.

1.1.5 Ultra/diafiltration and Formulation of Annexin A5

The AX pool is directly transferred to the UF/DF to elevate product concentration and perform a buffer change. Following buffer change Tween80 is added to a final concentration of 0.05 % and the drug substance is sterile filtered.

In a first process step the AX pool is 6-8 fold concentrated. Following this a buffer change is conducted with 8-10 diafiltration volumes in formulation buffer not containing Tween (20 mM Bis-Tris, 150 mM NaCI, 1 mM CaCb pH 7 or pH 7.4). Post buffer change a second concentration is conducted to achieve a final concentration of 12 g/L. This allows an addition of the first wash of the cassette and the addition of Tween80 to a final concentration of 0.05% to reach a final concentration post sterile filtration of 10 g/L. The

UF/DF step is conducted with a low TMP of 0.9-1.1 bar to minimize cover layer formation.

Figure 3 shows the process flow chart for ultra/diafiltration and formulation of Annexin A5.

Target Values and Acceptance Criteria

The following target values and acceptance criteria are defined to evaluate the process 5 performance and scale-up in comparison to small scale DSP runs. Target values are defined based on IPC / Bulk analysis of a pilot run. Key process parameters were characterized to specify key process steps and enhance reliability of process performance.

2.1 Main Process Parameters o

Table 5 shows the main process parameters. Attainment of target ranges during the process performance is indicative of successful process scale up.

Table 5: Process parameters of process steps and respective target values

Step	Parameter	Target range
Homogenization	Temperature post homogenization	34-40°C
pressure	600 bar
cycles	3
Resuspension ratio	1 g/10 mL
Capture Step AX chromatography (Q Sepharose XL)	load amount [g/L Resin] [10 Lusp /L Resin]]	30-50 10-12
Elution criteria Elution criteria [UV280, 2mm]	Main peak Pool (0.1 AU-0.2 AU)
Elution volume [CV]	5-10
Intermediate Step AF Chromatography (Heparin HyperD)	load amount [g/L Resin]	20-30
Elution criteria [UV280, 2mm]	Complete peak Pool (0.1 AU-0.1 AU)
Elution volume [CV]	2-3
Polishing Step AX Chromatography (Sou reel 5 Q)	load amount [g/L Resin]	10-23
Elution criteria [UV280, 2mm]	major peak starting at 0.05 AU to the valley between peak 1 and peak 2

Step	Parameter	Target range
	Elution volume [CV]	5-10
UF/DF - Hydrosart 10 KDa	Inlet Pressure [bar]	0.8-1.2

2.2 Key Process Parameters

A high degree of homogeneity of the suspension prior capture chromatography is important. The use of three homogenisation cycles is suitable to achieve this. Moreover a temperature increase within homogenization is suitable to obtain temperatures of the lysate in the range of 37°C. This is important for the activity of the Benzonase having an direct impact on the filtration step and capture performance.

The pooling from the polishing step is also important as this step is used for the separation of product related impurities. The UF/DF step is performed under moderate conditions with regard to TMP to minimize the formation of a cover layer.

Table 6: Important process parameters

Step	Parameter	Target range
homogenization	Temperature post homogenization	34-40°C
homogenization	Cycle times	3
Polishing	Loading	10-16 g/L Resin
Pooling after polishing	UV signal (2mm)	major peak starting at 0.05 AU to the valley between peak 1 and peak 2
UF/DF	TMP	0.9-1.1 bar

2.3 In-Process Controls

Table 7 shows the In-Process Controls. Target ranges achieved during the process performance show successful process scale up. Target ranges were set based on observations in previous small scale runs, which were performed with implemented changes, only.

Step Nomenclature: 3 L process 100 L process	Test	Laboratory	Target range
Resuspension for homogenisation IPC-D01	Resuspension for homogenisation IPC-03.1	Content: SDS-PAGE [g/L]	Bioanalytics HH	> 5 g/L USP
SDS-PAGE (soluble & insoluble fraction on red. Gel) [ratio in sol/insol in %]	Bioanalytics HH	< 40% insoluble
Ceil disruption (post cycle 3) IPC-D05	Cell disruption (post cycle 3) IPC-03	Content: SDS-PAGE [g/L]	Bioanalytics HH	> 5 g/L USP
SDS-PAGE (soluble & insoluble fraction on red. Gel) [ratio in sol/insol in %]	Bioanalytics HH	< 40% insoluble
Clarification IPC-D07	Clarification IPC-04	Content: SDS PAGE [g/L]	Bioanalytics HH	n.a.
Conditioning for Capture IPC-D07a	Online Dilution for Capture IPC-05.1	Content: SDS PAGE [g/L]	Bioanalytics HH	t.b.d.
Identity: SDS-PAGE Coomassie	Bioanalytics HH	tb.d.
Purity: HCP (WB)	Bioanalytics HH	band pattern
Purity: HCP (ELISA) [ng/mg]	Bioanalytics HH	t.b.d.
Purity: DNA (qPCR) [pg/mg]	Bioanalytics HH	t.b.d.
Purity: Endotoxin [EU/mg]; [EU/mL]	L+S	t.b.d.
AX capture FT IPC-D08	AX capture FT IPC-05.2	Identity: SDS-PAGE Coomassie	Bioanalytics HH	band pattern
AX capture elution pool	AX capture elution pool	Content. PANATecs AX-HPLC [g/L] ™HHiecs	n.a.

Step Nomenclature: 3 L process 100 L process	Test	Laboratory	Target range
IPC-D09	I PC-05	Content: SDS PAGE [g/L]	Bioanalytics HH	t.b.d.
Identity: SDS-PAGE Coomassie	Bioanalytics HH	band pattern
Identity: IEF	Bioanalytics HH	band pattern
Purity: HOP (WB)	Bioanalytics HH	band pattern
Purity: HCP (ELISA) [ng/mg]	Bioanalytics HH	t.b.d.
Purity: DNA (qPCR) [pg/mg]	Bioanalytics HH	Reduced compared to IPC-D07a
Purity: Endotoxin [EU/mg]; [EU/mL]	L+S	Reduced compared to IPC-D07a
Purity: AX-HPLC [%]	PAN AT ecs	t.b.d.
AX capture Salt CIP IPC-D10	AX capture Salt CIP IPC-05.3	Optional analytics	Bioanalytics HH	n. a.
0.2 pm filtration of capture pool IPC-D11	0.2 pm filtration of capture pool IPC-06.1	n.a.	Bioanalytics HH	n.a.
Conditioning for AF Intermediate IPC-D12	Conditioning for AF Intermediate IPC-06.2	Content: AX-HPLC [g/L]	PAN AT ecs	n.a.
AF intermediate FT+wash IPC-D13	AF intermediate FT IPC-06.3	Content: AX-HPLC [g/L]	PANATecs	n.a.
Identity: SDS-PAGE Coomassie	Bioanalytics HH	band pattern
AF intermediate Elution pool IPC-D14	AF intermediate Elution pool IPC-06	Content: AX-HPLC [g/L]	PANATecs	n.a.
Content: UV280 [g/L]	QCH	t.b.d.

Step Nomenclature: 3 L process 100 L process	Test	Laboratory	Target range
		Identity: SDS-PAGE Coomassie	Bioanalytics HH	band pattern
Identity: IEF	Bioanalytics HH	band pattern
Purity: HCP (WB)	Bioanalytics HH	band pattern
Purity: HCP (ELISA) [ng/mg]	Bioanalytics HH	Reduced compared to IPC-D09
Purity: DNA (qPCR) [pg/mg]	Bioanalytics HH	Reduced compared to IPC-D09
Purity: Endotoxin [EU/mg]; [EU/mL]	L+S	Reduced compared to IPC-D09
Purity: AX-HPLC [%]	PAN AT ecs	t.b.d.
Purity: SEC [%]	QC BV	t.b.d.
0.2 pm filtration of intermediate pool IPC-D17	0.2 pm filtration of intermediate pool IPC-07.1	Optional analytics	Bioanalytics HH	n.a.
AX polishing FT+wash IPC-D18	AX polishing FT IPC-07.2	Identity: SDS-PAGE Coomassie FQKA-HB005	Bioanalytics HH	band pattern
AX polishing Salt CIP IPC-D20	AX polishing Salt CIP IPC-07.3	Optional analytics	Bioanalytics HH	n. a.
-	AX polishing fraction IPC-07.4	Identity: IEF	Bioanalytics HH	band pattern
Purity: AX-HPLC [%]	PANATecs	t.b.d.
-	AX polishing fraction IPC-07.5	Identity: IEF	Bioanalytics HH	band pattern
Purity: AX-HPLC [%]	PANATecs	t.b.d.

Step Nomenclature: 3 L process 100 L process	Test	Laboratory	Target range
-	AX polishing fraction IPC-07.6	Identity: IEF	Bioanalytics HH	band pattern
Purity: AX-HPLC [%]	PAN AT ecs	t.b.d.
-	AX polishing fraction IPC-07.7	Identity: IEF	Bioanalytics HH	band pattern
Purity: AX-HPLC [%]	PAN AT ecs	t.b.d.
AX polishing Elution Pool IPC-D19	AX polishing Elution Pool IPC-07	Content: AX-HPLC [g/L]	PANATecs	t.b.d.
Content: UV280 [g/L]	QC H	t.b.d.
Identity: SDS-PAGE Coomassie	Bioanalytics HH	band pattern
Identity: IEF	Bioanalytics HH	band pattern
Purity: HCP (WB)	Bioanalytics HH	band pattern
Purity: HCP (ELISA) [ng/mg]	Bioanalytics HH	Reduced compared to IPC-D14
Purity: DNA (qPCR) [pg/mg]	Bioanalytics HH	Reduced compared to IPC-D14
Purity: Endotoxin [EU/mg]; [EU/mL]	L+S	Reduced compared to IPC-D14
Purity: AX-HPLC [%]	PANATecs	t.b.d.
Purity: SEC [%]	QC BV	t.b.d.
Post concentration IPC-D21	Post concentration IPC-08.1	Optional analytics	Bioanalytics HH	n. a.
Post diafiltration/conc. IPC-D22	Post diafiltration/conc. IPC-08.2	Content: UV280 [g/L]	QC H	t.b.d.
Post addition of cassette wash and addition of Tween80	Post addition of cassette wash	Content: UV280 [g/L]	QC H	t.b.d.

Step Nomenclature: 3 L process 100 L process	Test	Laboratory	Target range
IPC-D23	IPC-08.3
Bulk including Tween80 IPC-D24	Bulk including Tween80 IPC-08	Content: UV280 [g/L]	QC H	>10 g/L
Bulk Sterile filtered IPC-D25	Bulk Sterile filtered IPC-09	Identity: SDS PAGE red.	Bioanalytics HH	Confirms to reference
Identity: IEF	Bioanalytics HH	Main band corresponds to reference
Content: UV280 [g/L]	QC H	8-12 g/L band pattern
Purity: HCP (WB)	Bioanalytics HH
Purity: HCP (ELISA) [ng/mg]	Bioanalytics HH	100 ng/mg
Purity: DNA (qPCR) [pg/mg]	Bioanalytics HH	100 pg/mg
Purity: Endotoxin]	L+S	35 EU/mg
Purity: AX-HPLC [%]	PAN AT ecs	t.b.d.
Purity: SEC [%]	QC BV	> 95
Bio burden Ph. Eur. 2.6.12	L+S	< 1 cfu/mL
Potency	Bioassay HH	t.b.d.
pH	QC-Hannover	6.8-7.2
Appearance	QC-Hannover	Clear, colourless, free of visible particles
Purity: SDS PAGE nonred. Silver	QC BV	> 90 %
Content: AX-HPLC [g/L]	PANATecs	t.b.d.
Identity: Western Blot	Bioanalytics HH	Main band corresponds to reference
Osmolality	TECHPharm	t.b.d.

Conclusions

The foregoing manufacturing process is well adapted for large scale manufacturing with no bottlenecks for up-scale to and above 10,000 L scale, if needed.

Throughout the manufacturing process, the Annexin A5 protein is kept in solution in its active form when not temporarily bound to chromatography resins.

As applied to a 1,000 L culture, the overall process time in the manufacturing plant will be one week in fermentation, harvest, cell-disruption and processing prior chromatography and an consecutive week in downstream processing. The whole process in a GMP plant will be 2 weeks. This is independent of scale and perfectly adapted to industry standard and would fit into any CMO or pharmaceutical manufacturer.

As noted above, in comparison, the process of Marder et al. would take around 12 weeks to process a 1,000 L culture.

Moreover, the yield in the present process is 2-3 times higher per batch than that of Marder et al. This makes the manufacturing cost per gram Annexin A5 drug substance between (6-8 x 2-3 =) 12-24 times higher for the Marder process.

Furthermore, in addition to providing a purification process that is faster, and with higher yield than the process of Marder et al., the process of the present invention also provides a higher purity product. As discussed above in Comparative Example 1, the purity of the protein from the Marder process would not be suitable for human use. Despite elaborate centrifugations, only one anion exchange chromatography step is used in the Marder process which is far below the requirements to reach sufficient purity with regards to both in-process related impurities (especially endotoxin) and product related variants. Marder does not show any data on endotoxin levels or other impurities further indicating lack of suitability for pharmaceutical use.

In contrast, the process of the present application provides a highly pure Annexin A5 protein product, having the characteristics listed as follows:

- a concentration typically around 8-12 g/L;

- host cell protein levels at or below 100 ng/mg, more typically below 20 ng/mg (as determined by ELISA);

- host cell DNA levels at or below 100 pg/mg, more typically below 10 pg/mg; Endotoxin at or below 35 EU/mg, more typically below 1 EU/mg,

- a purity of > 95% as determined by size-exclusion chromatography;

- a bioburden of < 1 cfu/mL (as determined by Ph. Eur. 2.6.12);

- a clear, colourless appaearance free of visible particles; and

- wherein the main band detected by western blot analysis corresponds to the Annexin A5 reference.

Example 2

The example illustrated a comparison of anion exchange (AX) capture and affinity capture by heparin chromatography.

AX capture and heparin affinity capture chromatography were compared with respect to Annexin A5 step yield and purity in the capture eluate. Both strategies were compared in batch experiments under optimized conditions.

Test parameters:

AX chromatography:

Batch mode 500 pi resin (75% slurry)

Buffer AX A: 20 mM NaPhosphate pH 7, 5 mM EDTA, 250 mM NaCI Buffer AX B: 20 mM NaPhosphate pH 6.5, 5 mM EDTA AX chromatography: Load: 10 mL pre-filtered lysate CIP: 1 M NaOH

Heparin affinity chromatography:

Batch mode 500 pi resin (75% slurry)

Load: 10 mL pre-filtered lysate; +10 mM CaCb

Buffer AF A: 50 mM Tris pH 7.4, 5 mM CaCb

Buffer AF B: 50 mM Tris pH 7.4, 40 mM EGTA, 50 mM NaCI

CIP: 3 M NaCI

Table 7: Comparison of AX and Heparin affinity chromatography capture

	Resin	Recovery (%)	Purity (determined based on SDSPAGE-R&D) (%)
AX	Q Sepharose XL	70-90	10-20
Affinity	Heparin Hyper D	30-40	85-95
Affinity (after AX)	Heparin Hyper D (Q Sepharose XL)	70-80	85-95

These results demonstrate that performing an AX capture before the affinity chromatography does not significantly improve the purity but has a considerable influence on the Heparin step yield. Moreover the costly affinity resin might have a prolonged lifetime if used as an intermediate step. Yield is of major importance.

The capture by AX might be rated as a conditioning step which allows an effective use of the highly specific affinity step by Heparin chromatography.

Example 3

A partially purified Annexin A5 product was obtained using methods similar to Exaple 1, up to the first Anion exchange chromatography capture step.

Briefly, recombinant E. coli expressing Annexin A5 were resuspended in a homogenisation buffer (50 mM Tris, 1 mM MgCI, 1% Tween20 pH 7.5), with 3200 U of Bezonase and homogenised with three cycles of 600 bar pressure. Temperature post homogenisation was measured with 36°C. A clarifying step using Cuno 60 SP 0.6-0.2 pm was performed, and the clarified solution diluted 1:2 in 1% Tween20, with the addition of EDTA. Post conditioning for capture the solution had a pH 6.9 and a conductivity of 2.7 mS/cm. Anion exchange was performed sing Q Sepharose XL (GE), washed with Buffer A (20mM Tris,

25mM NaCI, 0,1% Tween20, pH 7.4), and then eluted with Buffer B (20mM Tris, 300mM NaCI, 0,1% Tween20, pH 7.4). The resultant product was then sterile filtered with a 0.2 pm filter.

The resultant sterile filtered anion exchange product was the purified using heparin affinity chromatography and different conditions tested.

The heparin affinity chromatography conditions used were as follows:

Heparin HyperD M	50 mL CV
Volume of diluted load (mL)	1173
Volume after load (mL)	5
Volume of flow through (mL)	1145
Volume of mock elution pool (A5-B6) 50 up to 50 mAU in the descending peak) (mL) -UV 2 mm-	150
Volume of IPC samples (mL)	-
Flow rate (cm/h)	100 (elution 60)

Sterile filtration of capture elution pool was performed with Sartopore 2 0.45-0.2 pm. This pool was 8 fold diluted with (1050 mL) buffer A from Heparin chromatography. The resulting pool had a pH of 7.4 and a conductivity of 6.8 mS. Elution was conducted using a reduced flow rate of 60 cm/h.

Tests 1 and 2 were performed to determine the impact of Tween80 using Buffer A for wash and Buffer B for elution, as follows:

Test 1:

Buffer A 20mM Tris, 25mM NaCI, 2mM CaCI2, 0.1% Tween20, pH 7.4 Buffer B 20mM Tris, 10mM EDTA, 25mM NaCI, 0.1% Tween20, pH 7.4

Test 2:

Buffer A 20mM Tris, 25 mM NaCI, 2mM CaCh, 0.1% Tween20, 0.1% Tween80 pH

7.4

Buffer B 20mM Tris, 10mM EDTA, 100mM NaCI, 0.1% Tween20, 0.1% Tween80 pH 7.4

The results for Test 1 are shown in Fig 7A, and the results for Test 2 are shown in Fig 7B.

The results show that the addition of Tween80 shifted the elution to a single peak, in contrast to the separated elution under standard conditions (Test 1). Tween80 appears to stabilize Annexin A5. A possible explanation for the change in the elution behavior is that a theoretical precipitation on the column is prevented. Two major positive effects can be described for the use of Tween80 in the heparin affinity chromatography step:

Reduced pressure: The pressure on the column, which increased in the loading from 0.5 to 2-3 bar, was clearly reduced to 0.5 bar. This is especially beneficial for the large scale. The slight precipitation that is seen after prolonged incubation might be the reason for the pressure increase.

- Prevention of precipitation: The second positive effect is seen in the elution.

Within fractionation of the elution the highly concentrated main peak fractions have a tendency to precipitate. After pooling of the fractions no precipitation is observed anymore assuming that this effect has to do with the very high concentration of Annexin A5 in the main peak: Moreover the precipitation seems to be reversible. The precipitation in the main peak could not be prevented by elevated salt concentration in the elution. In contrast to this the addition of Tween80 did also prevent the formation of precipitates in the main peak fractions.

Based on these results it seems advantageous to additionally add Tween80 in all intermediate chromatography buffers as it has a stabilizing effect on Annexin A5.

The present application provides embodiments as described by the following numbered paragraphs 1. A process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from an endotoxinproducing host cell with a cell wall, wherein the process comprises releasing the intracellular protein from the host cell, characterised in that the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising non-ionic detergent, and preferably wherein the process does not include any centrifugation steps for the recovery and/or purification of the AnxA5 protein after its release from the host cell.

2. The process of paragraph 1 wherein the non-ionic detergent is a polysorbate, preferably a polysorbate selected from Tween20 and Tween80, most preferably Tween80.

3. The process of paragraph 1 or 2 wherein the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising an amount of non-ionic detergent that is effective to reduce or prevent the binding between Annexin A5 and endotoxin.

4. The process of any preceding paragraph, wherein the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising 0.01 to 10% (w/w) non-ionic detergent, such as 0.02 to 5% (w/w), 0.05 to 2% (w/w), or about 1 % (w/w) non-ionic detergent.

5. The process of any preceding paragraph for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from a host cell having a cell wall, wherein the process comprises releasing the intracellular AnxA5 protein from the host cell, wherein the free calcium ion concentration in the homogenisation buffer at the time of releasing the intracellular AnxA5 protein from the host cell, or after releasing the intracellular AnxA5 protein from the host cell but before any further chromatographic purification occurs, is lower than 10 mM, preferably lower than 5 mM, 1 mM, more preferably lower than 500 μΜ, or substantially zero, and/or wherein the homogenisation buffer comprises, or is modified after releasing the intracellular AnxA5 protein to include, a calcium metal ion chelator.

6. The process of paragraph 5, wherein the calcium metal ion chelator is selected from EDTA or salt thereof, EGTA or sait thereof, and most preferably EDTA.

7. The process of paragraph 5 or 6 wherein the level of free calcium ions, and/or an amount of calcium metal ion chelator, is effective to reduce or prevent the binding between Annexin A5 and components of the cell wall of the host cell.

8. The process of any of paragraph 5 to 7, wherein the homogenisation buffer comprises, or is adjusted (before or after the release of the AnxA5 protein) to comprise, 0.01 to 500 mM, such as 0.05 to 100 mM, 0.5 to 20 mM, 1 to 15 mM, 2 to 10 mM, or about 4 mM calcium metal ion chelator, and preferably wherein the calcium metal ion chelator is EDTA.

9. The process of paragraph 5,6, 7 or 8 wherein the homogenisation buffer comprises a non-ionic detergent in accordance with the process of any of paragraphs 2, 3 or 4.

10. The process of paragraph 9, wherein the calcium metal ion chelator is EDTA.

11. The process of paragraph 9 or 10, wherein the non-ionic detergent is Tween80.

12. The process of any preceding paragraph, wherein the process comprises recovery and/or purification of a recombinantly expressed intracellular AnxA5 protein from a culture of the host cells, and wherein the culture has a volume of at least 100L, 500L, 1.000L, 5,000L, or10,000L.

13. The process of any preceding paragraph, comprising the step of mixing biomass from the culture of host cells in the homogenisation buffer at a concentration of about 10g of biomass per mL of homogenisation buffer.

14. The process of any preceding paragraph, wherein the step of releasing the intracellular AnxA5 protein from the host cell in the homogenisation buffer comprises lysing, breaking, homogenising, sonicating, or pressure treating the host cell, such that the cell wall and cell membrane barrier of the host cell is disrupted and thereby releases the intracellular AnxA5 protein, and optionally wherein this step does not include the use of osmotic shock and/or a freeze-thaw step.

100

15. The process according to paragraph 14, wherein the step of releasing the intracellular AnxA5 protein from the host cell comprises high pressure homogenisation, such as one or more cycles of high pressure homogenisation between about 400 bar and about 2,500 bar, preferably three homogenisation cycles of about 600 bar, or two homogenisations cycles of about 800 bar.

16. The process according to any preceding paragraph, wherein the step of releasing the intracellular AnxA5 protein creates a biomass homogenate comprising the released AnxA5 protein.

17. The process according to paragraph 16, wherein the biomass homogenate further comprises one or more (typically all) of the impurities selected from the group consisting of host cell proteins, host cell wall components, host cell membrane, host cell nucleic acid, and endotoxin.

18. The process according to paragraph 16 or 17 further comprising the step of clarifying the biomass homogenate, and thereby producing a clarified product comprising the released AnxA5 protein.

19. The process according to paragraph 18, wherein the step of clarifying the biomass homogenate comprises treatment of the homogenate with a nuclease, such as a nuclease A, preferably a nuclease A from Serratia marescens, and optionally wherein the nuclease is included in the homogenisation buffer prior to releasing the intracellular AnxA5 protein.

20. The process according to paragraph 18 or 19, wherein the step of clarifying the biomass homogenate comprises (preferably subsequent to the nuclease treatment of paragraph 18 or 19), the step of passing the biomass homogenate comprising the released AnxA5 protein through a filter (such as a cellulose or polypropylene filter, preferably wherein the filter is a depth filter, and/or preferably wherein the filter has a cut off of less than 4 pm), and wherein the filter effluent is the clarified product comprising the released AnxA5 protein.

21. The process of any preceding paragraph, further comprising the step of subjecting the released AnxA5 protein to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein.

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22. The process of paragraph 21, wherein the clarified product comprising the released AnxA5 protein as produced by the method of paragraph 20 is subjected to the first anion exchange step, thereby to produce a first anion exchange product which comprises the released AnxA5 protein.

23. The process of paragraph 21 or 22 wherein, prior to the first anion exchange step, one or more parameters of the environment of the released AnxA5 protein, selected from the group consisting of the pH, the conductivity, the level of calcium ion chelator and the level of non-ionic detergent, is or are adjusted.

24. The process of any of paragraphs 21 to 23 wherein the released AnxA5 protein that is subjected to the anion exchange step is formulated at a pH of about 6.9, a conductivity of about 2.8 mS/cm, a calcium ion chelator concentration of about 1mM and diluted using a non-ionic detergent, for example to obtain a final non-ionic detergent concentration of 0.01 to 1 % (w/v), more preferably about 0.1% (w/v).

25. The process of any of paragraphs 21 to 24 wherein the AnxA5 protein is bound during the anion exchange step, and the first anion exchange product which comprises the released AnxA5 protein is produced by applying a wash solution and/or an elution buffer to the anion exchange resin to release the bound AnxA5 protein, optionally wherein the elution buffer comprises NaCI, for example about 300 mM NaCI.

26. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein; and subjecting the first anion exchange product, directly or indirectly, to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

27. The process of paragraph 26 wherein the affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and wherein the binding is promoted by the presence of calcium ions.

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28. The process of paragraph 27 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA,

29. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities to a heparin affinity chromatography step in the presence of Tween80 (preferably in the presence of 0.1% Tween80), thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

30. The process of any paragraphs 1 to 25, further comprising the step of subjecting the released AnxA5 protein to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

31. The process of paragraph 30, wherein AnxA5 protein in the first anion exchange product, as produced by the method of any of paragraphs 21 to 25, is subjected to the affinity chromatography step.

32. The process of paragraph 31 comprising steps wherein:

(a) a biomass homogenate comprising the released AnxA5 protein according to paragraph 16 or 17 is clarified by the process of any of paragraphs 18, 19 or 20 and thereby produces a clarified product comprising the released AnxA5 protein, and (b) the AnxA5 protein in the clarified product is subjected to an anion exchange resin in order to perform a first anion exchange step in accordance with any of paragraphs 21 to 25, and thereby produce a first anion exchange product which comprises the AnxA5 protein, and (c) wherein the AnxA5 protein in the first anion exchange product is subjected to an affinity chromatography step in accordance with paragraph 30 or 31.

33. The process of any of paragraphs 30 to 32 wherein the affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions.

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34. The process of paragraph 33 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

35. The process of any of paragraphs 30 to 34, wherein the first affinity chromatography product comprises the released AnxA5 protein and a calcium ion chelator, such as EDTA or EGTA, optionally in the range of 0.1 to 500 mM, more preferably about 10 mM.

36. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions.

37. The process of paragraph 36, wherein the calcium metal ion chelator is selected from EDTA or salt thereof, EGTA or salt thereof, and most preferably EDTA.

38. The process of paragraph 36 or 37, wherein the calcium metal ion chelator is present in the composition in an excess and/or at a concentration of about, or at least, 0.1 mM, 0,5 mM, 1 mM, 5 mM, 10 mM, 15 mM, 20 mM or more.

39. The process of any of any of paragraphs 36 to 38 wherein the selected metal ions are divalent cations, such as Mg²⁺ ions.

40. The process of any of paragraphs 36 to 39 wherein the selected metal ions are present during the anion exchange step in an amount effective to reduce or prevent an interaction between the calcium ion chelator and the anion exchange resin during.

41. The process of any of paragraphs 36 to 40, wherein the selected metal ions are present during the anion exchange step in an amount effective to increase binding of the

AnxA5 protein to the anion exchange resin in the presence of the calcium ion chelator, and 104 thereby reduce the loss of AnxA5 protein in the flow through of the anion exchange step, compared to the level of loss observed when no selected metal ions are present during the anion exchange step.

42. The process of any of paragraphs 36 to 41 wherein the selected metal ions are present during the anion exchange step (for example, by addition to the composition that comprises the AnxA5 protein and a calcium metal ion chelator prior to subjecting the composition to the anion exchange resin) at a concentration of about 1 to about 100 mM, such as about 2 to about 50 mM, about 5 to about 25 mM, about 10 to about 15 mM or about 12.5 mM.

43. The process of any of paragraphs 36 to 42 wherein the calcium metal ion chelator is EDTA and the selected metal ions are Mg²⁺ ions, and preferably the molar ratio of Mg²⁺ ions to EDTA is in the range of 0.5:1 to 2:1, most preferably at least 1:1 or more.

44. The process of any of paragraphs 36 to 43, wherein the composition that comprises the AnxA5 protein and a calcium metal ion chelator and which is subjected to the anion exchange resin is the direct, or indirect, product of a preceding process that comprises the step of subjecting the AnxA5 protein to an affinity chromatography step and eluting the AnxA5 protein with a calcium ion chelator, thereby producing an affinity chromatography product which is a composition that comprises the AnxA5 protein and a calcium metal ion chelator.

45. The process of paragraph 44 wherein the preceding affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions.

46. The process of paragraph 45 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA or EGTA.

47. The process of any one of paragraphs 44 to 46, wherein there is no dialysis step between the preceding affinity chromatography step and the anion exchange step and/or there is no removal of calcium ion chelator from the product of preceding affinity chromatography step prior to the application of the direct or indirect product to the anion exchange step.

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48. The process of any one of paragraphs 36 to 47, wherein the selected metal ions are added to the composition prior to, or during, the anion exchange step.

49. The process of any one of paragraphs 1 to 35, wherein the process comprises an anion exchange step according to any one of paragraphs 36 to 48.

50. A process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from a host cell with a cell wall, or a culture thereof as defined by paragraph 12, wherein:

(a) the process comprises releasing the intracellular protein from the host cell in the presence of a homogenisation buffer comprising non-ionic detergent according to any one of paragraphs 1 to 4;

(b) optionally wherein the releasing step is in accordance with any of paragraphs 13 to 17;

(c) further optionally wherein the process comprises a step of clarifying the biomass homogenate according to any of paragraphs 18 to 20; and (d) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an anion exchange resin, optionally in the presence of a calcium ion chelator, in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein in accordance with any of paragraphs 21 to 25; and (e) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an affinity chromatography step, in accordance with any of paragraphs 26 to 35, and (f) wherein the product of the affinity chromatography step is a composition that comprises the AnxA5 protein and a calcium metal ion chelator; and (g) wherein the direct, or indirect, product of the affinity chromatography step that comprises the AnxA5 protein and the calcium metal ion chelator is subjected to anion exchange step in accordance with any of paragraphs 36 to 49;

and preferably wherein none of steps (a) to (g) include, or are intervened by, one or more steps selected from centrifugation or dialysis, and more preferably wherein the AnxA5 protein remains soluble (except for temporarily binding to anion exchange and affinity chromatography solid phases) throughout the process.

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51. The process of any preceding paragraph wherein the process comprises, preferably at the end of the process as defined by any preceding paragraph, one or more further steps selected from the group consisting of concentration, buffer change, conditioning and filtration (such as sterile filtration), and optionally a final step of storing the AnxA5 protein-containing product in a sterile container.

52. The process of paragraph 51 wherein one of the further steps is diafiltration, optionally wherein the product of the diafiltration step contains the AnxA5 protein at a concentration of at least about 1 mg/mL, 5 mg/mL, 10 mg/mL, 15 mg/ml_, 20 mg/ml_, 50 100 mg/mL or greater.

53. The process of paragraph 51 or 52 wherein the filtration uses a 0.45-0.2 Lim filter or a 0.22 pm filter, and is preferably a sterile filtration step.

54. The process of any of paragraphs 51 to 53 wherein sterile filtration is the final purification step, prior to storing the AnxA5 protein-containing product in a sterile container.

55. The process of any preceding paragraph, wherein the process comprises steps required to provide a final sterile AnxA5 protein product in a non-phosphate buffer (such as Bis-Tris or Tris-buffer) at about pH 7.4, comprising about 150 mM NaCI, about 1 mM CaCb, about 0.05% (w/w) polysorbate (such as Tween80) or other non-ionic detergent, and optionally wherein the concentration of the AnxA5 protein in the final sterile AnxA5 protein product is about 10 mg/mL.

56. The process of any preceding paragraph wherein the process provides a final sterile AnxA5 protein product, wherein the NaCI concentration present maintains AnxA5 protein in a form that is predominantly monomeric.

57. The process of any preceding paragraph wherein the process provides an overall yield of greater than 1 g of AnxA5 protein per L of host cell culture, more preferably at least about 1.5 g/L, even more preferably in the range of about 2 to about 4 g/L.

58. The process of any preceding paragraph wherein the process provides an overall recovery of AnxA5 protein of about 24 % by weight of the AnxA5 protein present in the from the host cell culture.

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59. The process of any preceding paragraph wherein the process provides a product comprising host cell protein (other than the recombinantly expressed AnxA5 protein) at a level less than 100, 90, 80, 70, 60, 50, 40, 30, 20 ng or less per mg of AnxA5 protein.

60. The process of any preceding paragraph wherein the process provides a product comprising an endotoxin content of less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20, 15, and preferably less than 10, 5 or 1 EU per mg AnxA5 protein, and/or preferably wherein the process provides a product in unit dosage form and the product contains less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20, 15, and preferably less than 10, 5 or 1 EU per unit dose.

61. The process of any preceding paragraph wherein the process provides a product comprising host cell nucleic acid levels of less than 1,000 pg per mg of AnxA5 protein, preferably less than 100 pg per mg of AnxA5 protein, more preferably less than 10 pg per mg of AnxA5 protein.

62. A composition comprising an AnxA5 protein, wherein the composition is the direct, or indirect product of (or is directly or indirectly obtainable by) the process of any preceding paragraph.

63. The composition of paragraph 62, wherein the composition is a pharmaceutically acceptable and/or veterinarily acceptable composition.

64. A composition according to paragraph 62 or 63 for use in medicine.

65. A method of treating a human or animal subject in need thereof, comprising administering a composition according to paragraph 62 or 63 thereto.

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Claims (64)

1. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5) from a composition that comprises the AnxA5 protein and a calcium metal ion chelator, characterised in that the process comprises subjecting the composition to an anion exchange resin in order to perform an anion exchange step and thereby recover and/or purify the AnxA5 protein from the composition, and further characterised in that the anion exchange step is conducted in the presence of additional selected metal ions, wherein the additional selected metal ions are selected such that the calcium metal ion chelator has a binding affinity for the selected metal ions that is greater than its binding affinity for the anion exchange resin, but less than its binding affinity for calcium ions.

2. The process of Claim 1, wherein the calcium metal ion chelator is selected from EDTA or salt thereof, EGTA or salt thereof, and most preferably EDTA.

3. The process of Claim 1 or 2, wherein the calcium metal ion chelator is present in the composition in an excess and/or at a concentration of about, or at least, 0.1 mM, 0,5 mM, 1 mM, 5 mM, 10 mM, 15 mM, 20 mM or more.

4. The process of any preceding claim, wherein the selected metal ions are divalent cations, such as Mg2+ ions.

5. The process of any preceding claim, wherein the selected metal ions are present during the anion exchange step in an amount effective to reduce or prevent an interaction between the calcium ion chelator and the anion exchange resin during.

6. The process of any preceding claim, wherein the selected metal ions are present during the anion exchange step in an amount effective to increase binding of the AnxA5 protein to the anion exchange resin in the presence of the calcium ion chelator, and thereby reduce the loss of AnxA5 protein in the flow through of the anion exchange step, compared to the level of loss observed when no selected metal ions are present during the anion exchange step.

7. The process of any preceding claim, wherein the selected metal ions are present during the anion exchange step (for example, by addition to the composition that comprises the AnxA5 protein and a calcium metal ion chelator prior to subjecting the 109 composition to the anion exchange resin) at a concentration of about 1 to about 100 mM, such as about 2 to about 50 mM, about 5 to about 25 mM, about 10 to about 15 mM or about 12.5 mM.

8. The process of any preceding claim, wherein the calcium metal ion chelator is EDTA and the selected metal ions are Mg2+ ions, and preferably the molar ratio of Mg2+ ions to EDTA is in the range of 0.5:1 to 2:1, most preferably at least 1:1 or more.

9. The process of any of preceding claim, wherein the composition that comprises the AnxA5 protein and a calcium metal ion chelator and which is subjected to the anion exchange resin is the direct, or indirect, product of a preceding process that comprises the step of subjecting the AnxA5 protein to an affinity chromatography step and eluting the AnxA5 protein with a calcium ion chelator, thereby producing an affinity chromatography product which is a composition that comprises the AnxA5 protein and a calcium metal ion chelator.

10. The process of Claim 8 wherein the preceding affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions.

11. The process of Claim 9 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA or EGTA.

12. The process of any one of Claims 8 to 10, wherein there is no dialysis step between the preceding affinity chromatography step and the anion exchange step and/or there is no removal of calcium ion chelator from the product of preceding affinity chromatography step prior to the application of the direct or indirect product to the anion exchange step.

13. The process of any preceding claim, wherein the selected metal ions are added to the composition prior to, or during, the anion exchange step.

14. A process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from an endotoxinproducing host cell with a cell wall, wherein the process comprises releasing the intracellular protein from the host cell, characterised in that the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising non-ionic detergent, and

110 further characterised in that the process comprises an anion exchange step according to any preceding claim, preferably wherein the process does not include any centrifugation steps for the recovery and/or purification of the AnxA5 protein after its release from the host cell.

15. The process of Claim 14 wherein the non-ionic detergent is a poiysorbate, preferably a polysorbate selected from Tween20 and Tween80, most preferably Tween80.

16. The process of Claim 14 or 15 wherein the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising an amount of non-ionic detergent that is effective to reduce or prevent the binding between Annexin A5 and endotoxin.

17. The process of any of Claims 14 to 16, wherein the step of releasing the intracellular AnxA5 protein is conducted in the presence of a homogenisation buffer comprising 0.01 to 10% (w/w) non-ionic detergent, such as 0.02 to 5% (w/w), 0.05 to 2% (w/w), or about 1% (w/w) non-ionic detergent.

18. The process of any of Claims 14 to 17, for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from a host cell having a cell wall, wherein the process comprises releasing the intracellular AnxA5 protein from the host cell, wherein the free calcium ion concentration in the homogenisation buffer at the time of releasing the intracellular AnxA5 protein from the host cell, or after releasing the intracellular AnxA5 protein from the host cell but before any further chromatographic purification occurs, is lower than 10 mM, preferably lower than 5 mM, 1 mM, more preferably lower than 500 μΜ, or substantially zero, and/or wherein the homogenisation buffer comprises, or is modified after releasing the intracellular AnxA5 protein to include, a calcium metal ion chelator.

19. The process of Claim 18, wherein the calcium metal ion chelator is selected from EDTA or salt thereof, EGTA or salt thereof, and most preferably EDTA.

20. The process of Claim 18 or 19 wherein the level of free calcium ions, and/or an amount of calcium metal ion chelator, is effective to reduce or prevent the binding between Annexin A5 and components of the cell wall of the host cell.

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21. The process of any of Claim 18 to 20, wherein the homogenisation buffer comprises, or is adjusted (before or after the release of the AnxA5 protein) to comprise, 0.01 to 500 mM, such as 0.05 to 100 mM, 0.5 to 20 mM, 1 to 15 mM, 2 to 10 mM, or about 4 mM calcium metal ion chelator, and preferably wherein the calcium metal ion chelator is EDTA.

22. The process of Claim 18, 19, 20 or 21 wherein the homogenisation buffer comprises a non-ionic detergent in accordance with the process of any of Claims 15, 16 or 17.

23. The process of Claim 22, wherein the calcium metal ion chelator is EDTA.

24. The process of Claim 22 or 23, wherein the non-ionic detergent is Tween80.

25. The process of any of claims 18 to 24, wherein the process comprises recovery and/or purification of a recombinantly expressed intracellular AnxA5 protein from a culture of the host cells, and wherein the culture has a volume of at least 100L, 500L, 1,000L, 5.000L, or10,000L.

26. The process of any of Claims 18 to 25, comprising the step of mixing biomass from the culture of host cells in the homogenisation buffer at a concentration of about 10g of biomass per mL of homogenisation buffer.

27. The process of any of Claims 18 to 26, wherein the step of releasing the intracellular AnxA5 protein from the host cell in the homogenisation buffer comprises lysing, breaking, homogenising, sonicating, or pressure treating the host cell, such that the cell wall and cell membrane barrier of the host cell is disrupted and thereby releases the intracellular AnxA5 protein, and optionally wherein this step does not include the use of osmotic shock and/or a freeze-thaw step.

28. The process according to Claim 27, wherein the step of releasing the intracellular AnxA5 protein from the host cell comprises high pressure homogenisation, such as one or more cycles of high pressure homogenisation between about 400 bar and about 2,500 bar, preferably three homogenisation cycles of about 600 bar, or two homogenisations cycles of about 800 bar.

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29. The process according to any of Claims 18 to 28, wherein the step of releasing the intracellular AnxA5 protein creates a biomass homogenate comprising the released AnxA5 protein.

30. The process according to Claim 29, wherein the biomass homogenate further comprises one or more (typically all) of the impurities selected from the group consisting of host cell proteins, host cell wall components, host cell membrane, host cell nucleic acid, and endotoxin.

31. The process according to Claims 29 or 30 further comprising the step of clarifying the biomass homogenate, and thereby producing a clarified product comprising the released AnxA5 protein.

32. The process according to Claim 31, wherein the step of clarifying the biomass homogenate comprises treatment of the homogenate with a nuclease, such as a nuclease A, preferably a nuclease A from Serratia marescens, and optionally wherein the nuclease is included in the homogenisation buffer prior to releasing the intracellular AnxA5 protein.

33. The process according to Claim 31 or 32, wherein the step of clarifying the biomass homogenate comprises (preferably subsequent to the nuclease treatment of Claim 17 or 18), the step of passing the biomass homogenate comprising the released AnxA5 protein through a filter (such as a cellulose or polypropylene filter, preferably wherein the filter is a depth filter, and/or preferably wherein the filter has a cut off of less than 4 pm), and wherein the filter effluent is the clarified product comprising the released AnxA5 protein.

34. The process of any of Claims 18 to 33, further comprising the step of subjecting the released AnxA5 protein to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein.

35. The process of Claim 34, wherein the clarified product comprising the released AnxA5 protein as produced by the method of Claim 33 is subjected to the first anion exchange step, thereby to produce a first anion exchange product which comprises the released AnxA5 protein.

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36. The process of Claim 34 or 35 wherein, prior to the first anion exchange step, one or more parameters of the environment of the released AnxA5 protein, selected from the group consisting of the pH, the conductivity, the level of calcium ion chelator and the level of non-ionic detergent, is or are adjusted.

37. The process of any of Claims 34 to 36 wherein the released AnxA5 protein that is subjected to the anion exchange step is formulated at a pH of about 6.9, a conductivity of about 2.8 mS/cm, a calcium ion chelator concentration of about 1mM and diluted using a non-ionic detergent, for example to obtain a final non-ionic detergent concentration of 0.01 to 1 % (w/v), more preferably about 0.1% (w/v).

38. The process of any of Claims 34 to 37 wherein the AnxA5 protein is bound during the anion exchange step, and the first anion exchange product which comprises the released AnxA5 protein is produced by applying a wash solution and/or an elution buffer to the anion exchange resin to release the bound AnxA5 protein, optionally wherein the elution buffer comprises NaCI, for example about 300 mM NaCI.

39. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities to an anion exchange resin in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein; and subjecting the first anion exchange product, directly or indirectly, to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein;

characterised in that the process comprises an anion exchange step according to any of Claims 1 to 14.

40. The process of Claim 39 wherein the affinity chromatography step comprises the binding ofthe AnxA5 protein to immobilised heparin, and wherein the binding is promoted by the presence of calcium ions.

41. The process of Claim 40 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

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42. A process for the recovery and/or purification of a protein comprising the sequence of Annexin A5 (AnxA5), from a solution comprising the AnxA5 protein and one or more impurities, the method comprising subjecting the solution comprising the AnxA5 protein and one or more impurities to a heparin affinity chromatography step in the presence of Tween80 (preferably in the presence of 0.1% Tween80), thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein characterised in that the process further comprises an anion exchange step according to any of Claims 1 to 14.

43. The process of any Claims 14 to 38, further comprising the step of subjecting the released AnxA5 protein to an affinity chromatography step, thereby to produce a first affinity chromatography product which comprises the released AnxA5 protein.

44. The process of Claim 43, wherein AnxA5 protein in the first anion exchange product, as produced by the method of any of Claims 34 to 38, is subjected to the affinity chromatography step.

45. The process of Claim 44 comprising steps wherein:

(d) a biomass homogenate comprising the released AnxA5 protein according to Claim 29 or 30 is clarified by the process of any of Claims 31, 32 or 33 and thereby produces a clarified product comprising the released AnxA5 protein, and (e) the AnxA5 protein in the clarified product is subjected to an anion exchange resin in order to perform a first anion exchange step in accordance with any of Claims 34 to 38, and thereby produce a first anion exchange product which comprises the AnxA5 protein, and (f) wherein the AnxA5 protein in the first anion exchange product is subjected to an affinity chromatography step in accordance with Claim 43 or 44.

46. The process of any of Claims 43 to 45 wherein the affinity chromatography step comprises the binding of the AnxA5 protein to immobilised heparin, and optionally wherein the binding is promoted by the presence of calcium ions.

47. The process of Claim 46 wherein the AnxA5 protein is eluted from the immobilised heparin using an elution buffer containing a calcium ion chelator, such as EDTA.

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48. The process of any of Claims 43 to 47, wherein the first affinity chromatography product comprises the released AnxA5 protein and a calcium ion chelator, such as EDTA or EGTA, optionally in the range of 0.1 to 500 mM, more preferably about 10 mM.

49. A process for the recovery and/or purification of a recombinantly expressed intracellular protein comprising the sequence of Annexin A5 (AnxA5) from a host cell with a cell wall, or a culture thereof as defined by Claim 25, wherein:

(h) the process comprises releasing the intracellular protein from the host cell in the presence of a homogenisation buffer comprising non-ionic detergent according to any one of Claims 14 to 17;

(i) optionally wherein the releasing step is in accordance with any of Claims 26 to 30;

(j) further optionally wherein the process comprises a step of clarifying the biomass homogenate according to any of Claims 31 to 33; and (k) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an anion exchange resin, optionally in the presence of a calcium ion chelator, in order to perform a first anion exchange step, and thereby produce a first anion exchange product which comprises the released AnxA5 protein in accordance with any of Claims 34 to 38; and (l) wherein the process further comprises the step of subjecting the released AnxA5 protein directly or indirectly to an affinity chromatography step, in accordance with any of Claims 39 to 48, and (m) wherein the product of the affinity chromatography step is a composition that comprises the AnxA5 protein and a calcium metal ion chelator; and (n) wherein the direct, or indirect, product of the affinity chromatography step that comprises the AnxA5 protein and the calcium metal ion chelator is subjected to anion exchange step in accordance with any of Claims 1 to 38;

and preferably wherein none of steps (a) to (g) include, or are intervened by, one or more steps selected from centrifugation or dialysis, and more preferably wherein the AnxA5 protein remains soluble (except for temporarily binding to anion exchange and affinity chromatography solid phases) throughout the process.

50. The process of any preceding claim wherein the process comprises, preferably at the end of the process as defined by any preceding claim, one or more further steps

116 selected from the group consisting of concentration, buffer change, conditioning and filtration (such as sterile filtration), and optionally a final step of storing the AnxA5 proteincontaining product in a sterile container.

51. The process of Claim 50 wherein one of the further steps is diafiltration, optionally wherein the product of the diafiltration step contains the AnxA5 protein at a concentration of at least about 1 mg/ml_, 5 mg/mL, 10 mg/ml_, 15 mg/mL, 20 mg/ml_, 50 100 mg/mL or greater.

52. The process of Claim 50 or 51 wherein the filtration uses a 0.45-0.2 pm filter or a 0.22 pm filter, and is preferably a sterile filtration step.

53. The process of any of Claims 50 to 52 wherein sterile filtration is the final purification step, prior to storing the AnxA5 protein-containing product in a sterile container.

54. The process of any preceding claim, wherein the process comprises steps required to provide a final sterile AnxA5 protein product in a non-phosphate buffer (such as Bis-Tris or Tris-buffer) at about pH 7.4, comprising about 150 mM NaCI, about 1 mM CaCb, about 0.05% (w/w) polysorbate (such as Tween80) or other non-ionic detergent, and optionally wherein the concentration of the AnxA5 protein in the final sterile AnxA5 protein product is about 10 mg/mL.

55. The process of any preceding claim wherein the process provides a final sterile AnxA5 protein product, wherein the NaCI concentration present maintains AnxA5 protein in a form that is predominantly monomeric.

56. The process of any preceding claim wherein the process provides an overall yield of greater than 1 g of AnxA5 protein per L of host cell culture, more preferably at least about 1.5 g/L, even more preferably in the range of about 2 to about 4 g/L.

57. The process of any preceding claim wherein the process provides an overall recovery of AnxA5 protein of about 24 % by weight of the AnxA5 protein present in the from the host cell culture.

58. The process of any preceding claim wherein the process provides a product comprising host cell protein (other than the recombinantly expressed AnxA5 protein) at a level less than 100, 90, 80, 70, 60, 50, 40, 30, 20 ng or less per mg of AnxA5 protein.

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59. The process of any preceding claim wherein the process provides a product comprising an endotoxin content of less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20, 15, and preferably less than 10, 5 or 1 EU per mg AnxA5 protein, and/or preferably wherein the process provides a product in unit dosage form and the product contains less than 100, 90, 80, 70, 60, 50 45, 40, 35, 30, 35, 20, 15, and preferably less than 10, 5 or 1 EU per unit dose.

60. The process of any preceding claim wherein the process provides a product comprising host cell nucleic acid levels of less than 1,000 pg per mg of AnxA5 protein, preferably less than 100 pg per mg of AnxA5 protein, more preferably less than 10 pg per mg of AnxA5 protein.

61. A composition comprising an AnxA5 protein, wherein the composition is the direct, or indirect product of (or is directly or indirectly obtainable by) the process of any preceding claim.

62. The composition of Claim 61, wherein the composition is a pharmaceutically acceptable and/or veterinarily acceptable composition.

63. A composition according to Claim 61 or 62 for use in medicine.

64. A method of treating a human or animal subject in need thereof, comprising administering a composition according to Claim 61 or 62 thereto.

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Intellectual

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Office

Application No: Claims searched:

GB 1700978.8 1-64