minimizing the environmental footprint of … bioprocess international oc t o b e r 2010 b i op r o...

36 BioProcess International OctOber 2010

B i o P r o c e s s Technical

Minimizing the Environmental Footprint of BioprocessesPart 2: Evaluation of Wastewater, Electricity, and Air Emissions

Beth Junker

Product Focus: All biologics

Process Focus: UpstreAm And downstreAm

Who should read: process development And mAnUfActUring

KeyWords: single-Use, disposAbles, sUstAinAbility, environmentAl impAct

level: intermediAte

Part 1 of this two-part article introduced the need to reduce the environmental footprint of bioprocesses and evaluated the

impact of solid-waste disposal. Part 2 continues by describing the effects of the remaining elements of the bioprocess footprint: wastewater, electricity, and air emissions.

WasteWater

Process Waste Streams: Generally, raw materials to produce and purify biopharmaceuticals fall into one of the following categories: inorganic/organic salts, sugars/polyols, trace elements, vitamins, amino acids, surface active agents, or complex (undefined) ingredients (Table 1). Most bioreactor media components are either life-supporting or life-promoting and thus likely to have a low intrinsic toxicity. However, when used at concentrations necessary to achieve commercially viable processes, these compounds can be toxic to aquatic life. Overall guidance for fermentation broth and downstream isolation component selection during early process development is best based on each component’s concentration and

potential hazard. Bioprocess scientists benefit from understanding acceptable limits for raw material components (most specifically trace metals) acceptable for sewering discharges as processes are improved. Although these boundaries in turn depend on local waste flow conditions and wastewater permit limits, several general considerations can be assembled to guide the selection and use of raw materials for culture media and buffers.

Production Operations: Table 1 shows typical concentrations for initial fermentation growth media components. Trace elements, including metals, are either added directly to media or are indirectly present in complex nutrients or multicomponent media powders. When total initial media concentrations of trace elements are compared for various host systems, Escherichia coli and Saccharomyces system values are notably higher than Chinese hamster ovary (CHO) and Pichia system values (Table 2). For E. coli, totals reach ~25 mg/L of which >75% is Fe and therefore can be an environmental concern (Table 3). Feed solutions can contain either whole media or only limiting nutrients, but in either

case they often contain trace metals either directly or indirectly. For intensified processes, accumulated component feed amounts and the eventual location of component accumulation must be considered. For example, small amounts of carbon, nitrogen, and oxygen components are incorporated into the desired biopharmaceutical products, but larger amounts are emitted as by-products, biomass, and off-gas.

During fed-batch operation for process intensification, trace metals accumulate intracellularly but also can accumulate extracellularly if the nutrient feed composition is unbalanced. Fed-batch additions to Pichia fermentations include glucose (500–600 g/L), glycerol (500–750 g/L), and salt solutions containing Cu, I, Mn, B, Fe, Zn, Co, Mo, B, or I and other nonelement items (1). Table 4 shows unbalance for a Pichia fermentation, in which extracellular trace metal increases relative to uninoculated medium are significant: Mo (threefold), Fe (twofold), and Cu (>30-fold). The accumulation of Cu to 3.7 ppm (mg/L) at harvest exceeds the toxicity limit by at least one order of magnitude, becoming a more serious problem than the initial uninoculated levels (Table 3).

Toxicity testing data are highly dependent on the organism required for the acute toxicity evaluation, which differs depending on a biopharmaceutical facility’s physical location. These differences are important to understand for companies executing processes in multiple locations including outsourcing vendors. At one Merck location (Rahway, NJ), for example,

Asif AkbAr (www.sxc.hu)


toxicity tests use mysid shrimp (Americamysis bahia) to indicate effects on the nearby salt-water discharge environment. At a second Merck location (West Point, PA), toxicity tests use Daphnia magna to indicate effects on the nearby fresh-water discharge environment. Differences in toxicity are evident depending on the organism used, with the fresh-water organism (Daphnia) often being 10-fold more sensitive to trace metals (Table 3). Regardless of location, some minimal toxicity assessment before sewering is prudent, which may require actual aquatic tests if previous data do not exist.

Relative and combined toxicities of toxic components, particularly trace metals, also are important considerations. Table 3 values are based on individual component testing and should be supplemented by testing a composite sample of the entire stream under evaluation. Combined (synergistic) toxicities of metals are evaluated, but not necessarily for commonly observed bioprocess concentrations and elements, which typically do not use Hg, Cd, Pb, and Ni (2). For each treatment plant, daily municipal sewering limits for certain metals and other components (e.g., CN) are established based on concentration, stream volume, and expected dilution/augmentation when mixed with other facility or site wastes flowing to the treatment plant. (It is not permissible to dilute waste upon disposal to achieve sewering limits.)

Generally trace minerals are present at a level of 10–4 M (0.1 mM) in uninoculated medium (3). Calculated concentrations of uninoculated BMGY medium show a greater than threefold higher NOEC levels of Cu and greater than 10-fold higher NOEC levels of Zn (Tables 3 and 4). In addition, trace metals may be present in media, buffer, and excipient ingredients, especially complex (undefined) nutrients and composite blends such as yeast nitrogen base. For an example dry ingredient with a measured trace metal value of 100 ppm, a 10-g/L solution of this component results in 1 ppm (1 mg/L) of trace metals in solution (Table 5), an amount similar in magnitude to the trace elements expressly added to the fermentation medium. Furthermore, trace metal composition in common raw materials can vary considerably by

vendor and grade, even for inorganic salts and sugars.

High extracellular concentrations of media components, such as trace metals, often inhibit cell growth. In one E. coli study, growth was inhibited at levels >8.7 g/L Mg, >0.8 g/L Mo, >44 mg/L B, >4.2 mg/L Cu, >68 mg/L Mn, >0.5 mg/L Co, >38 mg/L Zn, and >1.15 g/L Fe (4). In another E. coli study, levels of 1 mm/L Fe+3 and 0.5 mm/L Fe+2 reduced growth, and 1 mm/L Fe+2 inhibited growth (5). Compared with the NOEC/LC50 limits in Table 3, however, growth inhibition of the culture may not be evident before waste

stream concentrations exceed acceptable limits. The reliability of cultivation performance as a toxicity indicator depends on the specific culture and process as well as the calculation and other desired safety factors assumed when evaluating potential discharge toxicity. For comparison purposes, process concentrations are directly compared with toxic concentrations to provide a worst-case assessment without discharge safety factors that are commonly used (Table 2).

Interestingly, there is a certain desirable level of trace elements for industrial wastewater treatment plants.

Table 1: Typical media concentration ranges (not all ingredients are present in each medium)

Component

Concentration Range

E. coli (per liter)

S. cerevisiae (per liter)

P. pastoris (per liter) (1, 35, 36)

CHO (per liter)

Salts

Sodium chloride 0.5 g

Ammonium chloride/sulfate 1–20 g 5–40 g 15–20 g

Sodium/potassium phosphate 1–10 g 1–10 g 9–15 g 0.1 mg

Sodium bicarbonate 3.7 g

Magnesium sulfate heptahydrate 0.1–0.5 g 0.1–0.5 g 2–5 g

YNB with ammonium sulfate without amino acids

13.4 g (2 g ammonium

sulfate)

Calcium salts (excluding carbonate) 0.25–1 g 0.25–1 g

Ferrous salts 1–10 mg 1–10 mg

Other metal salts (~5) 0.02–2 mg

0.02–2 mg

Organic salts (alpha keto acid salts) 0.2 mg 0.1–0.4 g

Monosodium glutamate 10–30 g 10–30 g

l-glutamine 0.6 g

l-histidine 0.04 g

Other essential amino acids (~15–20) 0.015–0.15 mg

Vitamins (~1–3) 0.1–3 mg each

0.1–150 mg each

Insulin 5 mg

Albumin 10 g

Lipid mixture 30 mg

SugarsGlucose 10–50 g 10–100 g 20–25 g 1–5 g

Glycerol 40–100 g

Sorbitol 18 g

Silicone antifoam 0.1 mL

Pluronic F68 0.1 mL

UCON/P2000 antifoam 0.1–3 mL 0.1–3 mL

Complex IngredientsMeat extract 3 g

Yeast extract 10–30 g 5–25 g 10 g

Tryptone 10–16 g

Soy peptone 5 g 20 g

Casamino acids 5–10 g 5–10 g

Corn syrup 10–80 g 10–60 g

Bovine/calf fetal serum 0.5–10%

Trace metals (e.g., Co, Ni, Fe, Cu, Zn, Mn) are rarely if ever added to ensure adequate micronutrient concentrations. Chemical speciation affects trace metal bioavailability because relative uptake rates differ for different chemical species and relative concentrations of chemical species differ based on exposure conditions (6). For example, free Co concentration has been shown to correlate with Co toxicity to methylotrophic methanogenesis in anaerobic granular sludge (7). Consequently, the desirability of specific trace element discharges may

vary according to municipal discharge location.

The Department of Environmental Protection (DEP) in at least one state is considering regulating total dissolved solids (TDS) in new or expanded discharges to surface water and publicly owned treatment works (POTWs) to achieve tighter drinking-water quality standards (8). High TDS discharges are those >2,000 mg/L, and proposed regulations limit them to <500 mg/L TDS, <250 mg/L chlorides, and <250 mg/L sulfates (8). Dissolved solids can be introduced directly from inorganic

Table 2: Typical levels of trace element compositions in initial batched medium for various types of cultures (not all elements present in each media for each host system)

Element

Salt

E. coli mg/L

Comp

Saccha-romyces

mg/L

(38)

Comp

Pichia

(36, 37)

Comp

CHO per liter

Comp

Fe Ferric chloride hexa-hydrate;Ferric ammonium sulfate; Ferric sulfate

20.0 > 9.2 > 1.52 mg

<

Zn Zinc chloride

1.5 > 9.6 > 637 μg

> 1 mg >

Mn Manganous sulfate

6.6 < 96 μg <

Co Cobalt chloride

1.5 > 7.9 > 6 μg <

Mo Disodium molybdate

1.5 < 8.0 < 61 μg <

Cu Cupric chloride

1.0 > 2.7 > 72 μg > 2.5 μg

<

Total trace metals 25.5 44 2.35 mg

1.00 mg

* “Comp” is the level present compared with toxicity level indicated by Table 3 with “< “ less than NOEC or LC50; “~” about the same order of magnitude, and “>” greater than NOEC or LC50. Additional trace elements commonly included in fed-batch salt additions for Pichia fermentations.

Table 3: Toxicity data from literature

Chemical

Daphnia magna americamysis bahia

LC50 (μg/L) NOEC (μg/L) LC50 (μg/L) NOEC (μg/L)

CuSO4 15 1 111 10

NaI 150 10 1,235 120

CoCl2 110 12 1,066 148

ZnCl2 1,100 68 14,000 1,000

FeSO4 57,000 4,000 113,000 10,000

Na2MoO4 97,000 8,800 295,000 180,000

B(OH)3 185,000 18,000 288,000 220,000

MnSO4 >1,000,000 900,000 >1,000,000 >1,000,000

* Data are from USEPA ECOTOX, Micromedex Haz Subst DB, and TDS Numerica ECOTOX databases. 96 h LC50 for Cu LC50 of 181 μg/L and Zn LC50 of 499 μg/L for americamysis bahia at 30% salinity (2).

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components (such as potassium phosphate) or indirectly from complex media ingredients (Table 5).

Table 6 shows dissolved solids levels (Mg, K, Na, and Ca) for supernatant from a Pichia fermentation. Extracellular levels of Mg consistently are about 5–10× below the 500-mg/L target level and decrease further ~5- to 15-fold during the fermentation. Ca exhibits similar behavior, starting low and generally decreasing (even when increases occurred, levels remained below the target). K patterns are notably different, starting at up to 15-fold above the target, in the best case decreasing to 0.85 g/L and in the worst case increasing to 4.1 g/L potential due to midcycle additions. Na exhibits another dramatically different behavior, typically starting at about 0.25–0.8 g/L, but at its worst case increasing well above the target to 2.9 g/L (potentially as a result of NaI present in the salt feeding solution). Measured levels for chlorides and sulfates are not available to compare with targets; however, these levels could be expected to increase because trace elements present in salt feeding solutions often possess chloride or sulfate anions (1). Consequently, the impact of process intensification on accumulated extracellular TDS levels also should be considered when examining nutrient-feeding compositions.

Downstream Process Operations: Components of higher volume downstream processing and formulation buffers should be examined as suggested for fermentation-media components. Many buffers comprise relatively dilute inorganic or organic salts (6–50 mM sodium phosphate, sodium acetate, or Tris HCl) or dilute bases (50 mM sodium hydroxide). High-salt buffers are commonly used for ion-

exchange (1–5 M NaCl) and hydrophobic-interaction chromatography (2 M ammonium sulfate), potentially affecting TDS discharge levels if used in large volume. Packed column sanitization or storage buffers may contain solvents (18% ethanol). Formulation buffers generally are low in volume and contain salt (25 mM sodium phosphate), amino acids (25 mM arganine), or sucrose (up to 5 wt%). Chelators, such as 1 mM ethylenediaminetetraacetic acid (EDTA) present in some buffers, potentially interfere with trace metal bioavailability in toxicity tests, reducing levels below LC50 and NOEC before waste-stream dilution and subsequent metal release in the environment.

Denaturants such as 7.5 M urea solutions are used to solubilize inclusion bodies (9). Cyanate concentrations can reach 3–4 mM over 14 days at ambient temperature in aqueous buffered 8 M urea solutions and up to 20 mM at equilibrium above pH 6.0 (10). Cyanate is substantially less toxic than cyanide (which can have discharge limits as low as <10 mg/L), and it cannot be converted to cyanide. Acceptable cyanate levels must consider the acute 48 h LC50 for Daphnia magna of 18 mg/L or 0.4 mM (11), suggesting that large-volume discharges of aged urea solutions should be carefully evaluated. Alternatives to chemical denaturation include 0.5% Sarkosyl surfactant solutions to solubilize inclusion bodies. Refolding is then achieved with 0.08 mM copper sulfate in 14 mM Tris HCl buffer, about an order of magnitude less copper than is contained in typical initial fermentation medium.

Very high and low pH streams used in bioprocesses often can be appropriately neutralized by pH control

systems at site wastewater collection points. These streams include ammonium hydroxide, sodium/potassium hydroxide, phosphoric acid, sulfuric acid (usually industrial fermentations) for pH adjustments during cultivation as well as for cleaning of bioprocess equipment (12). They also include acidic concentrated sugar solutions (e.g., 200–300 g/L glucose, pH 3.0–3.5) for fed-batch carbon additions (13). Low and high pH excursions impair wastewater plants by dispersing flocs or inhibiting microbial populations (14). Furthermore, a combination of high pH and fats or fatty acids (particularly antifoams, detergents, and surfactants) can cause foaming in wastewater systems (e.g., aeration tanks) (14, 15).

Other biopharmaceutical waste streams arise from sanitization solutions (usually diluted bleach) and wipe-down solutions (often quaternary disinfectants). These can be potential sources of chlorides but generally are diluted to a few percent and typically used at low volumes for wipe-downs. Higher volumes associated with process equipment sanitization are limited because several facilities are moving from chemical to steam sanitization procedures because of regulatory preferences. This shift puts additional pressure on companies to reduce steam energy consumption to avoid offsetting the benefits of reduced rinsewater from chemical sanitization.

Special additives such as inhibitors are often added to harvested broth to stabilize protein quality before isolation. The peptide protease inhibitors pepstatin A and chymostatin are added to Pichia broth, achieving final concentrations of 0.05–1 mg/L. An O-glycosylation inhibitor, protein

Table 4: Trace element distribution for bMGY fed-batch Pichia pastoris process at various stages

Element

Batch Medium (uninoculated) End of Batch Growth Phase At Harvest

Calculated, Not Including Complex Component (mg/L)

Measured (ppm, mg/L)

Supernatant (ppm, mg/L)

Pellet (ppm, mg/kg)

Partition (pellet/

supernatant)Supernatant (ppm, mg/L)

Pellet (ppm, mg/L)

Partition (pellet/supernatant)

(ppm, mg/kg)

Mo 0.159 0.2 0.2 0.1 0.5 0.6 0.2 0.33

B 0.177 0.6 0.7 0.3 0.43 0.5 0.4 0.8

Mn 0.260 0.3 <0.1 2.6 2.6 0.0 12.9 129

Fe 0.890 1.1 0.2 8.1 40.5 2.0 171.2 85.6

Co 0.000 <0.1 <0.1 <0.1 1 <0.1 1.5 15

Cu 0.032 <0.1 <0.1 0.4 4 3.7 10.2 2.8

Zn 1.480 1.2 0.2 8.6 43 0.9 72.7 80.8Assays performed by atomic spectroscopy. Similar results published from a Picha pastoris fermentation broth at harvest (pellet and supernatant combined) containing 100 g/L dcw (39) are 20 mg/L Mn, 140 mg/L Fe, 16 mg/L Cu, and 100 mg/L Zn.

O-mannosyl transferase inhibitor (PMT), is also added to Pichia broth, achieving a final concentration of ~15 mg/L. None of them show aquatic toxicity when tested at projected discharge broth concentrations.

Sewering of high–biological-oxygen-demand (BOD) broth can choke wastewater systems designed to treat wastewater of BOD 250 mg/L. Reported measured BODs for

secondary metabolite broths range from 15,000 to 35,000 g/L (14). Based on relative cell mass concentrations, BODs for high–cell- density bacterial and yeast broths are expected to be similar or perhaps higher, suggesting prospective examination of sewering of high volumes of high–cell-mass broth. BODs for cell culture broths are likely to be at least 10-fold lower, creating less strain on the wastewater system.

Table 5: reported values of trace elements in common media, buffer and formulation ingredients.

Ingredient

Level (ppm, mg/1,000 g)

Mn Cr Fe Cu Zn K/P Cl/SO4

Dicalcium phosphate

9.4 10.9 180 5.9 Merck data

Yeast extract

10 Not available

60 3 130 17 g/ 34 g

Not available

Tastone 254Red Star

Bioproducts/Universal Foods (Milwaukee, WI)

Soy peptone

Not available 30 g/ 4 g

27 g/4 g Hy-soySheffield

Products/Kraft (Norwich, NY)

Table 6: Dissolved soft elements assayed in Pichia broth (Merck data).

Strain/protein

Media

Element

Initial (0 h)

per Liter

Comp

91 h

per Liter

Comp

Change ratio (final/

initial)

Pichia 1 A Ca 87 mg < 52 mg < -1.67

Mg 170 mg < 20 mg < -8.5

K 4 g > 1.7 g > -2.35

Na 0.8 g > 0.6 g > -1.3

B Ca 42 mg < 37 mg < -1.14

Mg 183 mg < 77 mg < -2.4

K 3.3 g > 0.85 g > -3.9

Na 0.25 g < 2.9 g > +11.6

Pichia 2 A Ca 87 mg < 50 mg < -1.7

Mg 170 mg < 10 mg < -17

K 6.9 g > 5.3 g > -1.3

Na 0.8 g > 1.9 g > +2.4

B Ca 42 mg < 30 mg < -1.4

Mg 183 mg < 29 mg < -6.3

K 3.2 g > 2.8 g > -1.1

Na 0.25 g < 2.4 g > +9.6

Pichia 3 A Ca 87 mg < 18 mg < -4.8

Mg 170 mg < 39 mg < -4.4

K 6.9 g > 1.35 g > +5.1

Na 0.8 g > 0.2 g < -4.0

B Ca 42 mg < 61 mg < +1.4

Mg 183 mg < 23 mg < -8.0

K 3.25 g > 4.1 g > +1.3

Na 0.3 g < 0.65 g > +2.2

* Comparison with target TDS levels (8): 500 mg/L TDS, 250 mg/L chlorides and sulfates. Complementary results published from a Picha pastoris fermentation broth at harvest (pellet and supernatant combined) contained 100 g/L dcw (38) are 1.6 g/L Ca, 3 g/L Mg, 20 g/L K, and 8 g/L S.

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utility Waste streams

Low dilution of wastewater also is problematic because large volumes of BOD 30-mg/L wastewater sent to a system designed to treat BOD 250-mg/L wastewater disrupt treatment by over dilution. In biopharmaceutical facilities, large water discharges are caused by

• water-for-injection (WFI) and purified-water system flushing to reduce bioburden (typically ~3 min/day/use point) generating 5,000–15,000 L daily for a single system of 30 use points ranging from 1 to 1.5 in)

• rejection of water from reverse osmosis water purification systems

• extensive rinsing and flushing to achieve clean-in-place (CIP) acceptance limits.

In addition to treatment system disruption, large water discharges related to processing simply waste water. High water volumes used during biopharmaceutical production can be recovered by blending rejected water into incoming city water or using it as make-up water for chilled or tower water systems (if it can be appropriately segregated). Wastewater generation itself also can be reduced. When shorter water systems use point flushing times or frequencies are evaluated, they often do not adversely affect water quality but require extensive revalidation testing to implement. Procedurally specified flush times may already have overage incorporated (safety factors based on the validated testing times), so users can be trained to target the standard operating procedure (SOP) time exactly. Automated flush valves with shut-off timers also can help reduce wasted water, although their implementation is less frequent because of higher installation and maintenance expense. Extra rinsing or flushing during CIP procedures can be reduced by removing equipment from service to perform modifications to reduce excessive hold-up volumes and deadlegs from inadequate tube or pipe lengths or altering vessel designs to improve cleanability (16). Volumes of low-quality water used for lubrication or condensate cooling primarily in older facilities can be reduced by increasing condensate quenching temperatures to 60 °C (generally the highest value considered safe for equipment and people) and

installing flowmeters and accurate valves to regulate pump seal and quench flowrates (which if unregulated can amount to as much as 2 L/min per site).

WFI costs can be a surprisingly large portion of biopharmaceutical production costs (17), generating another driver for water use reduction. Specifically, 140,000 L of buffer or cleaning solutions are required to isolate a 20,000-L fermentation (17), a sevenfold volume ratio. Buffer consumption for a protein A chromatography step is substantially reduced by lowering column volumes (CVs) (e.g., from five to three CVs for equilibration and from three to two CVs for wash steps) by 4,480 L for a 140-L column using eight cycles to purify one cell culture batch of titer of ~5 g/L (18). Higher resin loading reduces buffer and thus WFI consumption (19).

In-line buffer dilution reduces the sizes of nondisposable buffer holding tank about 10-fold (from 25,000 L to 2,500 L), which in turn reduces CIP, steam-in-place (SIP), and WFI consumption as well as physical

transport of solutions within or to a facility from a vendor (18, 20).Optimizing control of buffer distribution line switching is critical to minimize the line pressure disturbances that potentially alter chemical composition and generate large quantities of off-specification waste buffer (18–21).

electricity

HVAC: The number and size of HVAC units, dictated by a biopharmaceutical facility design, can be minimized by reducing classified operating space and using the least stringent permitted levels of classification for a retained space. The large number of dedicated HVAC units in a facility is expected to remain running constantly to preserve desired cleanliness and pressurizations even when not in use. Because regulatory airflow rate standards cannot be changed readily, improvements can instead be gained by using more energy-efficient filters, air handlers, and lighting (22–23). HVAC “setbacks” in operating areas not heavily operating

Table 7: Typical sources of excess water discharge in a biopharmaceutical facility, along with potential mitigation ideas and associated drawbacks

Source Typical Amount Mitigation Drawback

WFI system use point flushes

3 min/use point1.5 inch line/150 L/min flow1.0 inch line/50 L/min flow30 use points5,000–15,000 L/day

Revalidation to lengthen maximum times between flushes and reduce flush time before use and sampling;Automated flush valves with timers

Additional validation costs and resources Additional maintenance

CIP additional rinses

1,000 L/weakness25% skids with weaknessFour skids uses per day1,000 L/month

Redesign inadequate equipment installations to correct weaknesses

Additional installation costs and equipment-downtime delays

Direct cooling of hot streams prior to sewering

Up to 1 L/min/point10 points/facility10 h use6,000 L/day

Utilize heat exchanger and closed loop, install sensitive valve and flowmeter to minimize cooling volume

Additional installation costs and equipment maintenance.

Water purification

30% purified water rejected during reverse osmosis step10,000 L purified water used/day3,000 L/day

Recycling of water into city water-fed systems (chilled water, cooling tower)

Additional installation costs

HVAC air handler condensate from numerous dedicated HVAC units

10 HVAC units200 L/unit daily average over entire year2,000 L/day

Condensate return collection into city water-fed systems (chilled water, cooling tower)

Additional installation costs

Total 17,000–27,000 L/day

* Biopharmaceutical facility assumed to have six suites at operating scale of 2000 L running at full capacity

(because people and equipment are not frequently moving in and out) have particular impact in bioprocess facilities operating under capacity. These setbacks might be as minimal as decreasing air-handler temperatures by 3–5 °F (10% improvement) or reducing air changes from 20 to 15 for a Class 100,000 area. Such changes need to balance the additional monitoring level required to ensure the proper air quality is available when processing resumes.

Controlled Temperature Units (CTUs): Refrigerants are by far the largest burden on greenhouse gasses. In addition to large numbers of dedicated HVAC units, even larger numbers of primary and backup CTUs exist in biopharmaceutical facilities, primarily in the form of cold and frozen storage. Operators can shut off these units when they are not in use and ensure CTUs are mostly full rather than mostly empty to reduce the number of units and to minimize cycling to maintain target temperatures when doors are opened. A reduction in the amount of inventory, particularly inventory requiring controlled temperature storage such as intermediate hold streams, would further reduce CTU demands.

air emissions

In the United States, hazardous air pollutants (HAPs) are regulated by maximum available control technology (MACT). This standard affects methanol (MeOH) addition in methylotropic Pichia processes but excludes ethanol by-product production in Saccharomyces bioprocesses. Often MeOH emissions are limited because of subsurface addition lines and low extracellular levels required for high productivity. However, as fermentation scale increases >2,000–5,000 L, care must be taken to calculate emissions for facilities with site air-emission permit limits, particularly if a MeOH bolus of 0.5–1 vol% is used to start induction.

Entrained particles (in the form of cells) are not usually problematic for biopharmaceutical processes because of the use of 0.2-µm vent filters on bioreactor exhaust lines. If no dust collector is present, then nuisance dust emissions during charging of raw materials at the large scale may reach levels of concern. Often, large-scale commodity nonbiopharmaceutical

fermentations use liquid raw materials to prevent such dust.

Only one example is evident in which process development is applied to reduce carbon dioxide, a greenhouse gas. Synthetic media are used to optimize very large–scale penicillin and cephalosporin production fermentations with the added benefit of reducing greenhouse gas emissions by 26% (24). Carbon dioxide levels in fermenter off-gas streams can range from one to 10 vol%, depending on the process and the process phase. For a Pichia fermentation with a peak oxygen update rate (OUR) of 150 mmol/L-h and a respiratory quotient (RQ ) of 0.6, peak carbon evolution rates (CER) are 90 mmol/L-h (1). This translates into 2,100 mol carbon emitted per 1,000 L/day or 100 kg (220 lbs) carbon dioxide emitted per 1,000 L/day. This amount is significant but not substantial — it is about the same as driving 500 miles in a 2008 Toyota Prius (www.terrapass.com/carbon-footprint-calculator).

Energy use by employees commuting to and from a biopharmaceutical facility is a dominant influence on air emissions. Consequently, labor-saving technologies such as single-use equipment offer a collateral emission reduction benefit (25, 26). When burned, one gallon of gasoline creates 20 lbs of carbon dioxide, or ~10% of the fermentation level described above. Thus, staffing requirements are an important consideration when evaluating disposable or fixed process equipment options as well as for overall process design. Of course, substantial telecommuting (e.g., up to three days/week) often is impractical for most employees working directly on bioprocesses. It is potentially possible for some desk-based support staff, with whom it has been demonstrated to increase productivity by 10–20% and raise job satisfaction (27).

Powder formulations for basal and feed media and buffers, save energy because transport and storage are more convenient (16). Preparing solutions on site reduces transportation to the site. Furthermore, using concentrated buffers reduces transport and storage within a site (18, 20). Reconstitution or dilution methods are important to evaluate for ensuring that manpower, along with cleaning fixed equipment or disposable usage, is minimized as well.

© 2010 Pall Corporation. Pall, , and Mustang are trademarks of Pall Corporation. ® indicates a trademark registered in the USA. GN10.3516

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)

Buffer Use Capacity

Process Q Sorbent ColumnMustang Q XT Membrane Capsule

Comparison of buffer usage between MustangQ XT5000 membrane capsule and a 220 Lprocess chromatography column, single useat 50 L/min volumetric flow.


© 2010 Pall Corporation. Pall, , and Mustang are trademarks of Pall Corporation. ® indicates a trademark registered in the USA. GN10.3516

Innovative designs

improveprocess economics

Mustang Q XT ion exchange capsules provide a compact footprint and patentedmembrane technology to improve process economics. Scalable capsules can reduce buffer consumption, increasethroughput and lower capital, reagent, andlabor costs – all without compromisingcontaminant removal performance.

Mustang® IEX Capsules



Achieve High Performance and High Flow Rates with Lower Costs

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1009080706050403020100

DBC

BSA

(mg/

mL)

Buffe

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Buffer Use Capacity

Process Q Sorbent ColumnMustang Q XT Membrane Capsule

Comparison of buffer usage between MustangQ XT5000 membrane capsule and a 220 Lprocess chromatography column, single useat 50 L/min volumetric flow.



the Path ForWard For BioPharmaceutical Processes Current facility design and equipment selection for approved biopharmaceutical products are already largely fixed. Because of license restrictions, operations are likely to be altered only if validation requirements are relatively low and subsequent control procedures are relatively simple. Consequently, proposed changes to reduce the environmental footprint of existing biopharmaceutical processes also must be evaluated for their associated quality risk. In-line preparation of process solutions, adjustment of intermediate composition, and removal of process stops (hold points) are all examples of changes that improve fixed and sometimes variable costs (28) as well as environmental footprints.

Process intensification not only improves productivity but also clearly results in greener facilities with reduced carbon dioxide footprints (29) and reduced cost of goods. Volumetric productivities of recombinant proteins are improved by better cell strains, raising cell concentrations, or optimizing feeding strategies (30, 31). For example, bioreactor sizes have been reduced from 20 kL to 4 kL (32) or even 2 kL (29) as a result of higher

antibody titers of at least 2–4 g/L (32) and high cell density fed-batch cultivations. Equipment size, number of units, and process volumes can be minimized particularly for upstream processes (16), resulting in smaller facility sizes (29, 30) or larger facilities running under capacity. Smaller bioreactors have smaller harvest volumes, which also may permit use of ready-made media and buffers, thereby eliminating or reducing media and buffer preparation suite sizes (29). In addition, smaller bioreactors can lead to single-floor production facilities (and thus less structural steel) because smaller vessels do not protrude through multiple levels (29).

Purification operations are the typical processing bottleneck (12) with as many as three to five purification batches required for each harvested bioreactor. Titer increases lead to a linear increase in downstream equipment sizes and capacity, but this linear increase is not sustainable for very high titers. New chromatography resin technology, such as twofold higher dynamic binding capacity resins, is applied to maintain column sizes and thus proportionally sized buffer volumes constant (18). Buffer use, often another facility bottleneck, prompts process development efforts

and unit operation selection to reduce buffer consumption (18). New combined cation- and anion-exchange membrane chromatography technology decreases buffer volume requirements (and buffer storage requirements) by as much as 95% because hold-up volumes are lower and regeneration buffers are not required (16, 33). Other technologies that increase surface-to-volume ratios serve to decrease equipment linear dimensions and thus result in smaller equipment sizes (34).

Recent focus has shifted from product capture to contaminant removal, which has significant implications (12). For example, extra column flushes and diafiltration volumes often are added to increase process robustness for removing host cell impurities. A focus on lower cost of goods drives process development to reduce the number of process steps and eliminate unnecessary steps using improved process designs or new technology. Examples include reducing chromatography steps from three to two and omitting buffer exchange steps by designing subsequent steps to directly accept the eluate of a prior step (35). Eluates of a previous chromatography step are often diluted 1.7-fold to lower their conductivity for optimal performance in a subsequent

Table 8: Typical sources of excess water discharge in a biopharmaceutical facility, along with potential mitigation ideas and associated drawbacks.

Technology Improvement

Impact

Power (Electricity and Steam

Solid-Waste Disposal

Wastewater

Off-Gas Emissions

Commuter/Delivery

Interaction

Disposables equipment

Less fixed equipment

Avoid SIP and CIP

Increases solid waste

Decreases CIP chemical/aqueous waste

Similar Decreases employee operations

Opposing

High dynamic binding capacity disposable membranes

No columns, smaller hold-up volume

Similar Increases solid waste

Reduce buffer due to no cleaning, equilibration and/or storage

Similar Similar Opposing

High dynamic binding capacity resins

Smaller columns

Similar Reduce solid waste (less resin discard)

Reduce buffer for cleaning, equilibration and/or storage

Similar Similar Re-enforcing

High cell density cultivations (higher productivity)

Smaller vessels

Similar/increase compressor (aeration) and power (mixing)

Increased cell mass disposal

Similar Increase carbon dioxide emissions

Similar Opposing

Higher productivity cultivation (same cell mass)

Smaller vessels

Decrease compressor (aeration) and power mixing) since smaller tank volume

Similar Decrease CIP chemical/aqueous waste

Similar Similar Re-enforcing

* Biopharmaceutical facility is assumed to have six suites at operating scale of 2,000 L running at full capacity.


chromatography step. This dilution necessitates large tank volumes and might be avoided by changing column order or elution conditions (18).

Moving forward, evaluation of biopharmaceutical processes early in the development phase is critical to reducing resource use and achieving target environmental measures. Prospective environmental footprints can be developed for various discharge sources, along with proposed mitigations and their drawbacks (Table 7). Proposed technology improvements also can be evaluated for their footprint impact, with opposing and supporting effects identified for different footprint areas (Table 8). Formal tracking of environmental measures (E-factors or process mass index) quantitatively demonstrates progress in environmental footprint reduction as process development advances for the same product or as platform development evolves for successive products. Such tracking can surface conflicting process design alternatives. Existing milestone reviews by internal governance committees can be leveraged and linkage to quality by design (QbD), and process analytical technology (PAT) initiatives can be explored. The evaluation framework then can be transferred to internal or contract manufacturing organizations to develop and monitor processes for future sustainability.

acKnoWledgmentsThe contributions of the following colleagues are acknowledged: Ralph Magliette, Tiebang Wang, Thomas Potgieter, Andre Walker, Mary Buzby, Richard Williams, David Craign.

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Beth Junker is senior scientific director at Merck and company, RY804-130, PO Box 2000, Rahway, nJ 07065; [email protected].

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