NZ619583B2 - Method and apparatus for syngas fermentation with high co mass transfer coefficient - Google Patents

Abstract

Disclosed herein is a process and an apparatus which are effective for improving carbon monoxide (CO) mass transfer. The process comprises: introducing syngas into a reactor vessel (100) containing a liquid fermentation nutrient medium effective for permitting growth of acetogenic bacteria, wherein the gas is introduced through a gas sparger (120) located below a liquid level (110 and 115) in the reactor vessel (100), the syngas being introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, wherein the syngas has a CO/C02 molar ratio of at least about 0.75; and providing agitation energy input to the reactor vessel of about 0.01 to about 12 kWatts/m3 medium; wherein the process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour. the gas is introduced through a gas sparger (120) located below a liquid level (110 and 115) in the reactor vessel (100), the syngas being introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, wherein the syngas has a CO/C02 molar ratio of at least about 0.75; and providing agitation energy input to the reactor vessel of about 0.01 to about 12 kWatts/m3 medium; wherein the process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

Description

METHOD AND APPARATUS FOR SYNGAS FERMEN’I'A’I‘ION WITH HIGH MASS ER COEFFICIENT This application ciaims the benefit of US. Provisional ation Nos. 61/571,564 and 61/571,565, both filed June 30, 2011 and ,845, filed ber 13, 201 i, all of which are incorporated in their entirety herein by reference.

A process and apparatus is provided which are effective for ing carbon monoxide (CO) mass transfer. More specifically, factors including syngas quality, syngas sparging, reactor pressure and mixing are balanced to provide an improved volumetric CO mass transfer coefficient during syngas fermentation.” BACKGROUND Anaerobic microorganisms can produce ethanol from carbon monoxide (CO) through fermentation of gaseous ates. tations using anaerobic microorganisms from the genus Clostridium produce ethanol and other useful products.

For example, US. Patent No. 5,173,429 describes Closzridi‘um ljzmgdahlz‘z‘ ATCC No. 49587, an anaerobic microorganism that produces ethanol and e fiom synthesis gas.

U.S. Patent No. 5,807,722 describes a method and apparatus for converting waste gases into organic acids and alcohols using Clostrtdi'um ljwzga’ahlii ATCC No. 55380. US.

Patent No. 6,136,577 describes a method and apparatus for converting waste gases into ethanol using CIOSt/‘idium ljunga’a/tlit‘ A'I‘CC No. 55988 and 55989.

The CO is often provided to the fermentation as part of a gaseous substrate in the form of a syngas. Gasifica’ticn of carbonaceous materials to produce producer gas or synthesis gas or syngas that includes carbon monoxide and hydrogen is well known in the art. Typically, such a gasification process involves a partial ion or starved-air oxidation of carbonaceous material in which a subustoichiometric amormt of oxygen is supplied to the gasification process to promote production of carbon monoxide as described in .

Fermentation of s substrates can be challenging because at least a portion of the gaseous substrate must dissolve in an aqueous fermentation broth before the substrate can be metabolized by the microbial e. Fermentations where the gaseous substrate provides the carbon and energy source for the microorganism are particularly challenging due to the large amount of ate needed to be solubilized in the fermentation broth before metabolism can take place. ates such as CO which have a low solubility in an aqueOus fermentation broth require a highly efficient mass transfer into an aqueous fermentation broth as the CO provides a carbon source for the bic fermentation. ts to improve CO mass transfer are bed in U.S. Patent Nos. 5,972,661 and 7,201,884 and in SUMMARY In a first aspect, the t invention provides a process for fermentation of syngas, the s comprising: mixing the syngas with acetogenic ia in a liquid nutrient medium in a reactor vessel, wherein the syngas is introduced into the reactor vessel through a gas sparger, the gas sparger located below the liquid nutrient medium level in the reactor vessel, wherein the gas sparger includes holes having a diameter of 10 mm or less, the syngas being introduced such that the syngas pressure drop across the sparger is 3.4 to 17.2 kPa (0.5 to 2.5 psi) and at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least 6.9 kPag (1 psig), wherein the syngas has a CO/CO2 molar ratio of at least 0.75; and providing an agitation energy input to the reactor vessel of 0.01 to 12 kWatts/m3 medium, n the process is effective for providing a volumetric CO mass er coefficient of 100 to 1500 per hour and a STY (space time yield) of at least 10g ethanol/(L·day).

In a second aspect, the present invetion provides syngas fermented according to the process of the first aspect.

Methods and apparatus are provided which are effective for ing a tric CO mass transfer coefficient during syngas fermentation. In one , a process for fermentation of syngas is provided that includes introducing the syngas into a reactor vessel through a gas sparger or a gas distributor. The gas sparger is located below a liquid level in the reactor vessel and the syngas is introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, and in another aspect, at least about 10 psig. The syngas has a CO/CO2 molar ratio of at least about 0.75. An agitation energy is provided to the reactor vessel in an amount of about 0.01 to about 12 kWatts/m3 medium. The process is ive for providing a STY of at least about 10 g ethanol/(L·day) and a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

In another aspect, a process for fermentation of syngas is provided that includes introducing the syngas into a reactor vessel through a gas sparger. The gas sparger is located below a liquid level in the reactor vessel and the syngas is introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, and in r aspect, 10836282_1 at least about 10 psig. The syngas has a CO/CO2 molar ratio of at least about 0.75, and in another aspect, the syngas has a CO content of at least about 20 mole %. The syngas is contacted with at least one gas dispersion impeller d above the gas sparger and the sygas is mixed with acetogenic bacteria with at least one mixing impeller located above the gas dispersion impeller.

The gas dispersion impeller and mixing impeller are operably connected to an agitator h a drive shaft. The agitator provides an agitation energy input of about 0.3 to about 12 kWatts/m3, in another , about 0.7 to about 12 /m3, and in another aspect, about 0.9 to about 12 kWatts/m3 medium. The process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

In one aspect, the gas sparger includes holes having a diameter of 10 mm or less, and in another aspect, the holes have a diameter of 2.5 mm or less. Syngas may also be introduced at a flow rate effective for providing a gas ty of 25 m/sec or greater at an exit of the holes and/or a pressure drop across the sparger holes of about 0.5 to about 2.5 psi. 10836282_1 In another aspect, a process is provided for improving a volumetric CO mass transfer coefficient. The process includes introducing the syngas into a reactor vessel through a gas sparger. The gas sparger is d below a liquid level in the reactor vessel and the syngas is introduced at a flow rate ive for maintaining a pressure inside of the reactor vessel of at least about 1 psig, and in another aspect, at least about 10 psig. 'I’he syngas has a CO/COz molar ratio of at least about 0.75, and in another aspect, the syngas has a CO t of at least about 20 mole %. 'l‘he syngas is contacted with at least one gas dispersion impeller and one mixing impeller. The gas dispersion impeller and mixing impeller are typically operably connected to an agitator through a drive shaft. The agitator provides an agitation energy input of about 0.3 to about 12 kWatts/m3, in another aspect, about 0.7 to about 12 kWatts/m3, and in another , about 0.9 to about 12 kWatts/m3 medium. The process is effective for providing a volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

A bioreactor is provided that es a housing defining a reactor vessel, the reactor vessel effective for maintaining a pressure of at least about 1 psig, and in another aspect, at least about 10 psig. An agitator is disposed at least lly in the reactor vessel and at least partially below a liquid level in the reactor vessel. The agitator is operably connected to a drive shaft, the agitator effective for providing an agitation energy input of about 0.3 to about 12 kWatts/mj, in another aspect, about 0.7 to about 12 kWatts/mjg and in r , about 0.9 to about 22 lleatts/m3 medium. At least one mixing impeller ly is connected to the drive shaft and disposed below the liquid level of the medium and at least one gas dispersion impeller is operably connected to the drive shaft and disposed below the mixing impeller. A gas sparger is disposed below the gas dispersion er, the gas sparger including holes having a diameter of about 10 mm or less which are effective for providing a gas velocity of about 25 m/sec or greater at the exit of the holes. The bioreactor may further include a boot disposed at a lower end of the reactor vessel.

In another aspect, a bioreactor is provided that includes a g defining a reactor vessel, the reactor vessel effective for maintaining a pressure of at least about I Psig, and in another aspect, at least about 10 psig. An agitator is diSposed at least partially in the reactor vessel and at least partially below a liquid level in the reactor vessel. The or is operably connected to a drive shaft, the agitator effective for providing an agitation energy input of about 0.3 to about 12 kWatts/m3, in another , about 0.7 to about 12 kWatts/m3, and in r aspect, about 0.9 to about 12 kWa’tts/m3 medium. At least one mixing impeller operably is connected to the drive shaft and disposed below the liquid level of the medium and at least one gas dispersion impeller is operably connected to the drive shaft and disposed below the mixing impeller. A gas sparger is disposed below the gas dispersion impeller, the gas sparger including holes having a er of about 10 mm or less which are effective for previding a gas velocity of about 25 m/sec or greater at the exit of the holes. The ctor further es a boot disposed at a lower end of reactor vessel, the boot ing a boot sparger and boot mixer.

In another aspect, a process for fermentation of syngas is provided that includes inoculating acetogenic ia into a medium contained in a boot n of a reactor vessel, the medium fills at least about 75% of a total volume of the boot. The acetogenlc bacteria are contacted with syngas for a time effective for providing a cell density of at least about 5 grams per liter. Medium is added to the r vessel to provide a liquid level in the reactor vessel. Syngas is introduced into the reactor vessel through a gas sparger. The gas r is located below a liquid level in the reactor vessel. Syngas is introduced at a flow rate effective for maintaining a re inside of the reactor vessel of at least about I psig, and in another aspect about 10 psig. The syngas has a CO/COz molar ratio of at least about 0.75 and is contacted with at least one gas dispersion impeller located above the gas sparger. Syngas and acetogenic bacteria are mixed with at least one mixing impeller located above the gas dispersion impeller. The gas dispersion impeller and mixing impeller are typically operably ted to an agitator through a drive shaft.

The agitation energy input is aborit 0.3 to about 12 kWatts/m3 medium. The process is effective for providing volumetric CO mass transfer coefficient of about 100 to about lSOO per hour.

In another aspect, a process for fermentation of syngas is provided that includes inoculating acetogenic bacteria into a medium contained in a boot portion of a reactor vessel, the medium effective for filling at least about 75% of a total volume of the boot.

The acetogenic bacteria are contacted with syngas for a time effective for providing a cell y of at least about 3 grams per liter. Medium is added to the reactor vessel and cell density is maintained at about 3 grams per liter. Medium is added until a liquid level in the reactor vessel is obtained. Syngas is introduced into the reactor vessel through a gas sparger. The gas r is located below a liquid level in the reactor vessel. Syngas is introduced at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least about 1 psig, and in another aspect about 10 psig. The syngas has a CO/COZ molar ratio of at least about 0.75 and is contacted with at least one gas sion impeller located above the gas sparger. Syngas and acetogenic bacteria are mixed with at least mixing impeller located above the gas diSpersion er. The gas dispersion impeller and mixing impeller are Operably connected to an agitator h a drive shaft, the agitator providing an energy input of about 0.3 to about 12 l<\Rl/atts/m3 medium. The process is effective for providing volumetric CO mass transfer coefficient of about 100 to about 1500 per hour.

BRIEF DESCRIPTION OF S The above and other aspects, features and advantages of several aspects of the process will be more apparent from the following drawings.

Figure 1 is a perspective view of a bioreactor.

Figure 2A and ZB iliustrate a bottom view of a gas inlet/sparger.

Figure 3 is a cross sectional view of a gas sparger.

Figure 4A and 4B are top cross sectional views of a reactor vessel showing different impeller assemblies.

Figure 5 illustrates an alternative configuration of the bioreactor boot.

Corresponding reference characters indicate corresponding components throughout the several views of the drawings. Skilled ns will appreciate that elements in the figures are illustrated for simplicity and clarity and have not necessarily been drawn to scale. For example, the dimensions of some of the elements in the figures may be exaggerated relative to other elements to help to improve understanding of various aspects of the present process and apparatus. Also, common but well~understood elements that are useful or necessary in cially feasible aspects are often not depicted in order to facilitate a less obstructed view of these various aspects.

DETAILED DESCRIPTION The following description is not to be taken in a limiting sense, but is made merely for the purpose of describing the l ples of exemplary embodiments. The scope of the invention should be determined with reference to the claims.

Syngas fermentation ncy is ed by enhancing conditions for increasing the volumetric CO mass transfer coefficient. Methods and apparatus are provided that are ive for providing a volumetric C0 mass transfer coefficient of about 100 to about i500 per hour, in r aspect, about 200 to about 1100 per hour, in r aspect, about 200 to about 900 per hour, in another aspect, about 300 to about 800 per hour, in another aspect, about 400 to about 700 per hour, and in another aspect about 500 to about 600 per hour, Variables which affect the CO mass transfer coefficient include syngas sparging, reactor vessel pressure, syngas quality, and gas dispersion and mixing.

The processes described herein are effective for providing a high level of productivity. In this aspect, the s is effective for providing a S‘l‘Y (space time yield) of at least about 10 g ethanol/(L-day), Possible STY values include about 10 g ethanol/(L-day) to about 200 g ethanol/(L-day), in another , about 10 g ethanol/(L'day) to about 160 g ethanol/(L-day), in another aspect, about l0 ethanol/(L-day) to about 120 g ethanol/(lxday), in another aspect, about 10 ethanol/(L-day) to about 80 g ethanol/(L-daY), in another aspeC’t, about 20 W030: ct‘nanol/(L-day) to about 140 g cthanol/(L-day), in another aspect, about 20 l/(deay) to about 100 g ethanol/(1.xday), in another aspect, about 40 (NOW ethanol/(L-day) to about 140 g ethanol/(L-day), and in another aspect, about 40 (1")‘ ethanol/(L-day) to about 100 g ethanol/(L-day).

De_tln_i.tio_.n._s_ Unless otherwise defined, the following terms as used throughOut this specification for the present disclosure are defined as follows and can include either the singular or plural forms of definitions below defined: The tcnn “about” modifying any amount refers to the variation in that amount encountered in real world conditions, e.g., in the lab, pilot plant, or production ty. For e, an amount of an ingredient or ement employed in a e or quantity when modified by “about” includes the variation and degree of care typically employed in measaring in an experimental condition in production plant or lab. For example, the amount of a component of a product when modified by ” includes the variation between batches in a multiple experiments in the plant or lab and the ion nt in the analytical method, Whether or not modified by “about," the amounts include equivalents to those amounts. Any quantity Stated herein and modified by " can also be employed in the present disclosure as the amount not modified by “about”.

“Carbonaceous material” as used herein refers to carbon rich material such as coal, and petrochemicals. However, in this specification, carbonaceous material includes any carbon material whether in solid, liquid, gas, or plasma state. Among the numerous items that can be considered carbonaceous material, the present sure contemplates: carbonaceous material, carbonaceous liquid product, carbonaceous industrial liquid recycle, carbonaceous municipal solid waste (MSW or msw), carbonaceous urban waste, carbonaceous agricultural material, carbonaceous forestry material, carbonaceous wood waste, carbonaceous construction material, carbonaceous tive material, carbonaceous industrial waste, aceous fermentation waste, carbonaceous petrochemical co ts, carbonaceous alcohol production co~products, carbonaceous coal, tires, plastics, waste plastic, coke oven tar, fibersott, lignin, black liquor, polymers, waste polymers, polyethylene terephthalate (PETA), polystyrene (PS), sewage sludge, animal waste, crop residues, energy crops, forest processing residues, wood processing es, livestock wastes, poultry wastes, food processing residues, fcrmentative process wastes, ethanol co—products, spent grain, spent microorganisms, or their combinations.

The term “ilbcrsoft” or “Fibersofi” or “fibrosoft” or “fibrousoft” means a type of carbonaceous material that is produced as a result of softening and tration of various nces; in an example carbonaceous al is produced via steam autoclaving of various substances. In r e, the fibersoft can include steam autoclaving of municipal, rial, commercial, and medical waste resulting in a fibrous mushy material.

The term “municipal solid waste” or “MSW" or “msw” means waste that may include household, commercial, industrial and/or residual waste.

The term “syngas” or “synthesis gas” means synthesis gas which is the name given to a gas mixture that contains g amorurts of carbon monoxide and hydrogen.

Examples of production methods include steam reforming of natural gas or hydrocarbons to produce hydrogen, the gasification of coal and in some types of waste—to-energy 2O gasiiication facilities. The name comes from their use as intermediates in creating synthetic natural gas (SNG) and for producing ammonia or methanol. Syngas comprises use as an intermediate in producing tic petroleum for use as a fuel or lubricant via Fischer-’I‘ropsch synthesis and previously the Mobil methanol to gasoline s. Syngas consists primarily of hydrogen, carbon monoxide, and some carbon dioxide, and has less than half the energy density (i.e., B'l‘U t) of natural gas. Syngas is combustible and is often used as a fuel source or as an intermediate for the production of other chemicals.

The terms “fermentation”, fermentation process” or “fermentation reaction” and the like are intended to encompass both the growth phase and product biosynthcsis phase of the process. In one aspect, tation refers to conversion ofCO to alcohol. 3O The term “mass transfer" as used herein relates to the transfer of atoms or molecules, particularly ate atoms or molecules from a gaseous phase into an s solution. A mass transfer ient may be calculated in accordance with the equations described in Younesi et al. (Iranian Journal of Biotechnology, Vol. 4, No. 1, January 2006), which is incorporated herein by reference. The foliowing equation represents CO bioconversion (Xco) and the tric mass transfer coefficient: Zen.....~ Mill—(L3) l - Xco 75va kLa: volumetric mass transfer coefficient Xco: % CO bioconversion R: constant T: temperature V1,: liquid volume H: Henry’s constant (CO = 1.226 liter-atm-mmol‘l) to vg: gas volume The term “increasing the efficiency", “increased ncy” and the like, when used in rotation to a tation process includes increasing one or more of the rate of" growth of microorganisms in the fermentation, the volume or mass of desired product (such as alcohols) produced per volume or mass of substrate (such as carbon monoxide) consumed, the rate of production or level of tion of the desired product, and the relative proportion of the desired product produced compared with other by-products of fermentation.

Bioreactor Design Figure l is a perspective view of a bioreactor tus. The bioreactor apparatus includes a housing 105 defining a reactor vessel 100. The reactor vessel 100 may be substantially cylindrical and a cross section of the reactor vessel may be shaped in the form of a circle, substantially circular, or other shapes that are effective for ing mixing and mass transfer. The housing 105 may be formed of any materials know to withstand operating pressures of at least about 1 psig and up to pressures of at least about 250 psig and which is compatible with medium. In various aspects, the foliowing pressures may be utilized, about 5 to about 200 psig, abOut S to about 100 psig, about 5 to about 50 psig, about 5 to about 25 psig, about 10 to about 200 psig, about 10 to about 100 psig, about 10 to about 50 psig, about 10 to about 25 psig, about 15 to about 200 psig, 3O about 15 to about 100 psig, about 15 to about 50 psig, about 15 to about 25 psig, about 20 to about 200 psig, about 20 to about 100 psig, about 20 to about 50 psig, and about 20 to about 25 psig, Some examples of suitable materials e stainless steel, steel with a suitable inner liner and glass.

As further shown in Figure l, syngas enters the reactor vessel 100 through a gas inlet/distributor/sparger 120. Dispersion of the syngas and further mixing is accomplished with at least one gas dispersion impeller 225 and at least one mixing impeller 220 which are coupled to a drive shaft 200. The drive shaft 200 is supported by an or support plate 210. Gas is exhausted from the r vessel 100 through exhaust valve 170. The reactor vessel 100 may also include baffles 300 to further enhance mixing. in this aspect, the baffles 300 may be extended about 25% above an ed liquid level 1 25 to allow fora higher operating liquid level if the system is found to have low foaming.

In r aspect, the reactor vessel 100 may include addition ports 230. The if) addition ports 230 may include for example, one or more acidic addition ports, one or more alkaline addition ports, and one or more nutrient additiou ports. In this aspect, the addition ports may be equally spaced apart around a circumference of the reaction .

The ports may be on the same or different horizontal plane. in one aspect, the reactor vessel 100 es at least 4 equally spaced medium addition ports adjacent to a mixing impeller 220. The poits may be spaced around a circumference of the reactor vessel [00 at angles of 45° apart.

A gassed liquid level 110 and an ed liquid level 115 are maintained in the reactor vessel 100. Maintaining an ungassed liquid level 115 in the reactor vessel 100 allows for more efficient mass transfer and helps in maintaining control of foaming. In this aspect, an ungassed liquid level 115 is maintained in the reactor vessel 100 which is effective for providing a head space of at least about 1% of a total volume of the reactor vessel 100. In another aspect, the ungassed liquid level i 15 provides a head space of about 1 to about 75% of a total volume of the reactor vessel 100. in various aspects, the head space may include the following percentages of the total volume of the reactor: about 5 to about 50%, about 10 to about 50%, about 15 to about 50%, about 20 to about 50%, about to about 50%, about 30 to about 50%, about 30 to about 40% and about 30 to about %. The reactor vessel 100 may also include at least one liquid inlet 130 which aids in controlling foaming and allows for adjustment in r liquid volume. The liquid inlet 130 may be in the form of a spray nozzle. The reactor vessel 100 may also include additional ports 190‘ As further illustrated in Figure l, the r vessel 100 may also include a boot 400 and a vortex breaker 410 disposed within the boot and over a medium outlet 420, The boot 400 and vortex breaker 4'10 are effective for ting gas from being drawn out through the medium outlet 420. Medium drawn out through medium outlet 420 may be sent to a medium to recycle loop 450 or to a medium filter loop 460. Medium from the medium recycle loop 450 may be sent to a cooler/heat exchanger 500 and cooled medium 5l0 may be cycled back to the r vessel 100.

The boot 400 is effective for allowing gas bubbles to rise from the boot 400 back into the reactor vessel 100. In this aspect, liquid in the boot 400 should be as undisturbed as le, and gas bubbles must rise out of the boot 400 faster than liquid is drawn down the boot. In this aspect, less than about 2% gas is drawn through the medium outlet 420 to a‘pump.

Medium from the medium filter loop 460 may be sent to a recycle filter 600.

Concentrated cells 6l0 are returned to the reactor vessel 100 and te 620 is sent for further processing. Further sing may include separation of desired product such as for example ethanol, acetic acid and butane].

In another aspect, the biereacter may be configured without impellers. For example, the bioreactor may be configured as a gas lift type reactor or a bubble column l5 type reactor. In these reactor configurations, an agitation energy of about 0.01 to about £2 kWatts/mJ medium is provided.

Syngas and Syugas Sparging Syngas is introduced into the bioreactor 100 through a gas inlet/sparger l20.

Syngas may be provided from any know source. In one aspect, syngas may be sourced from gasification cf carbonaceous materials. Gasiflcation involves partial combustion of biomass in a restricted supply of oxygen. The resultant gas mainly includes CO and H2. In this aSpect, syngas will contain at least about 20 mole % CO, in one , about 20 to about 100 mole % CO, in another aspect, about 30 to about 90 mole % CO, in another , about 40 to about 80 mole % CO, and in another aspect, about 50 to about 70 mole % CO. The syngas will have a (IO/CO; molar ratio of at least about 0.75. Some examples of suitable ation methods and apparatus are provided in U.S Serial Numbers 6i/5l6,667, 61/516,704 and 61/516,646, all of which were filed on April 6, 2011, and all of which are incorporated herein by reference.

The bioreactor may include a CO concentration gradient where the CO concentration near the sparger is higher than the CO concentration at a higher level of the bioreactor. In this aspect, the bioreactor includes a ratio of CO tration at a bottom level (sparger level) of the bioreactor to CO concentration at a top level of the bioreactor ofabout 100:1 to about 10:1.

One factor that may affect the mass transfer rate of the CO into the aqueous medium is the partial pressure of the gaseous substrate that includes the CO. In this aSpect, the mass er rate can be increased by increasing the proportion of CO in a gas stream by enrichment or removal of unwanted components. In this aspect, the gas stream will have less than about 10 ppm oxygenated or non-oxygenated aromatics.

Figure 2A and 2B illustrate a bottom view of a gas iniet/sparger l20. In this aspect, the gas inlet/sparger 120 may include an inlet conduit 530 which is continuous with a sparger assembly 540. The sparger assembly 540 may be generally annular or circular as shown, or may be any other shape, such as for example, a straight, rectangular or free form. In the aspect where the sparger assembly 540 is annular in shape, the r assembly 540 has a diameter that is about 30 to about 100 % of a diameter formed by the gas sion impellers 225, in s other aspects, about 40 to about 90%, about 40 to about 80%, and about 50 to about 70%.

The bottom portion of the gas sparger assembly 540 may include a ity of holes 550. The holes 550 are of a diameter effective for providing a gas velocity of about m/sec or greater at an exit of the holes, in another aspect, a gas velocity of about 25 m/sec to about 75 m/sec at an exit of the holes. In various s, the gas velocity may include the following ranges: about 25 to about 75 m/sec, about 25 to about 50 m/sec, about 25 to about 40 m/sec, about 25 to about 30 m/sec, about 30 to about 75 m/sec, about 30 to about 50 m/scc, about 30 to about 40 misec, about 35 to about 75 m/sec, about 35 to about 50 111/300, about 35 to about 40 m/sec, about 40 to about 75 m/sec, about 40 to about 50 m/sec, and about 50 to about 75 m/sec. In this aspect, the holes will have a diameter of about 10 mm or less and in another aspect, a diameter of about 2.5 mm to about 1.0 mm.

Figure 3 illustrates a cross sectional view of a sparger assembly 540. In this aspect, dotted arrow lines show the flow of gas through hole 550. An angle of 120° is shown with lines drawn to a midpoint of the sparger assembly (shown as a). Holes may be located at any angle along the sparger assembly. in one , the sparger assembly 540 includes about 1 to about 5 rows of parallel holes 550. Holes 550 are spaced apart and point in a downward direction. As shown in Figure 3, the sparger ly 540 includes 5 el rows of holes 550 and a total number of 790 holes spaced 30° apart. The downward pointing ion of the holes is effective for preventing fouling or clogging of the holes and helps to minimize back flow into the sparger assembly 540.

Gas Dispersion and Mixing Referring again to Figure l, the reactor vessel 100 r includes a mixing assembly that includes a drive shaft 200, at least one mixing impeller 220, and at least one gas dispersion impeller 225. The mixing er 220 will generally be located below the liquid level 110. In one aspect, the reactor vessel too es two or mere mixing impellers 220. A gas dispersion impeller 225 is located below the mixing impeller 220.

The reactor vessel 100 may include one or two or more gas dispersion impellers 2255, Referring now to Figure 4A, each mixing and gas dispersion impeller assembly includes a hub 500 and a group of impellers ed around the drive shaft 200. Each impeller includes an arm 510 ed to the hub 500 and holding one or more blades 520.

The blades may be either mixing impeller or gas dispersion impellers. The mixing impeller assembly includes at least 2 blades and may include up to 6 blades. Examples of mixing impeller include low energy impellers such as marine impellers or marine propellers. In another aspect, the gas dispersion impeller assembly includes at least 2 blades and may include up to 6 blades. Examples of gas dispersion impellers include high energy impellers such as Rushton impellers or concave impellers Figure 4B is similar to Figure 4A except that the blades 520 are attached directly to a hub 500.

Upon rotation of the drive shaft 200, syngas introduced through the gas inlet/sparger is entrained in small bubbles in the medium and travels around the lly circular cross section of the r vessel 100. The drive shall: is operably connected to and may be rotated with any suitable agitator, such as for example, an electric motor, a motor and gearbox, or a hydraulic motor. In this , the agitator provides an energy input of about 0.3 to about 12 kWatts/In3, in another aspect, about 0.7 kWa'tts/m3 to about 12 kWatts/m3, and in an important aspect, 0.9 kWatts/m3 to about 12 kWatts/m3 medium.

Bioreactor Operation In accordance with one aspect, the fermentation process is started by addition of a suitable medium to the reactor vessel. The liquid contained in the reactor vessel may include any type of suitable nutrient medium or tation broth. The nutrient medium will include vitamins and minerals effective for permitting growth of the microorganism being used. bic medium suitable for the fermentation of l using CO as a carbon source are known. One example of a suitable fermentation medium is described in US. Patent No. 7,285,402, which is orated herein by reference.

The medium is sterilized to remove undesirable microorganisms and the reactor is inoculated with the d microorganisms. In one aspect, the rganisms utilized include acetogenic bacteria. Examples of useful acetogenic bacteria e those of genus Clostria'ium, such as strains of Closzridz'unz ljzmgdahliz’, including those described in WC 2000/68407, EP £17309, US Patent Nos. 5,173,429, 5,593,886 and 6,368,819, 1998/00558 and , strains of Closzrz'dz'um autoethanogenum (DSM 10061 and DSM 19630 of DSMZ, Germany) including those described in and W0 2009/151342 and Clostridium ragsdalei (PI 1, ATCC BAA-622) and Alkalibacalzcm bacclzi (CPI 1, ATCC BAA—1772) including those described respectively in US. Patent No. 7,704,723 and “Biofuels and Bioproducts from Biomass-Generated Synthesis Gas”, Hasan Atiyeh, presented in ma EPSCOR Annual State ence, April 29, 2010 and Clostrz'dium carboxz'divorans (ATCC PTA-7827) described in U .8. Patent Application No. 2007/0276447. Other suitable microorganisms includes those of the genus Moorella, including Moorella Sp. 2-l, and those of the genus Carboxydothermus. Each of these references is incorporated herein by nce. Mixed cultures of two or more microorganisms may be used.

Some es of useful bacteria include Acetogem‘um kz'vui, naerobium noterae, Acerobacterz'um i, Alkalibaculum bacchi CPll (ATCC BAA-1772), Blautfa producta, Butyribaclen’um methylotrophicum, Caldanaerobacter subterraneous, 'Caldanaerobacter subterraneous pacificus, Carboxydothermus Itydrogcnoformans, Clostridz’um aceticum, Clostrz'dz'um acetobutylz‘cum, Clostridz‘um acetobutylicum P262 (DSM 19630 of DSMZ Germany), Clostridt‘um autoethanogemmz (DSM 19630 of DSMZ y), idz'um autoethanogerzzun (DSM 10061 of DSMZ Germany), Clostrz‘ditmz autoethanogenum (DSM 23693 of DSMZ Germany), Closm'dz‘um autoethanogen-mn (DSM 24138 of DSMZ Germany), Clostridium carboxia’ivorans P7 (ATCC PTA-7827), Clostridz'zmz cos/catiz’ (ATCC PTA~10522), Clostl'z'dium dra/cez‘, Clostridium ahliz‘ PETC (ATCC 49587), Clostridz‘um ljngdahliz' ERIZ (ATCC , Clostrz‘dz'um ljwzgdahlii C—OI (ATCC 55988), Clostridz'um ljungdahlz‘r' 0—52 (ATCC 55889), Closlrz‘dz'um magnum, Clostrz'dium pasteurianum (DSM 525 of DSMZ Germany), z'dium ragsdalz‘ P1} (ATCC BAA—622), Clostrz‘dz'um scatologenes, Clostridium aceticum, Clostr'idz'mn ultuuerzse, Desalfotomaculum kuznetsovz'z‘, Eubacierium limosum, Geobacter sulfirreducens, Mezhanosarci/za acetivorans, Methaflosarcz’na bar/ceri, Morrel’la thermoacetz‘ca, Morrella tlzermoamotrophz‘ca, Oxobacter git’, Peptoslreptococcus productus, Ruminococcus productus, Thermoanaerobacter lcz’vm‘, and mixtures thereof.

Upon inoculation, an initial feed gas supply rate is established effective for supplying the l population of microorganisms. Effluent gas is ed to determine the content of the effluent gas. Results of gas analysis are used to control feed gas rates.

Upon reaching desired levels, liquid phase and cellular material is withdrawn from the r and ished with medium. In this aspect, the bioreactor is operated to maintain a cell density of at least about 2 grams/liter, and in another aspect, about 2 to about 50 grams/liter, in various other aSpccts, about 5 to about 40 grams/liter, about 5 to about 30 grams/liter, about 5 to about 20 grams/liter, about 5 to about 15 grains/liter, about 10 to about 40 grams/liter, about 10 to about 30 grams/liter, about 10 to about 20 grams/liter, and about 10 to about 15 grams/liter. Cell density may be controlled through the recycle filter 600. In a related aspect, the bioreactor is operated to provide a liquid retention time of about 10 to about 400 hours, and in s aspect, about 10 to about 300 hours, about to about 200 hours, about 10 to about 100 hours, about 10 to about 75 hours, about 10 to about 60 hours, about it) to about 50 hours, about 10 to about 40 hours, about 10 to about 30 hours, and about 10 to about 20 hours. In this aspect, liquid retention time ) may be calculated as follows: LRT = liquid volume net liquid volume flow rate (in or out) Syngas is introduced into the bioreactor at a rate effective for maintaining a pressure in the bioreactor of at least about 1 psig, and in another , a pressure of about 10 to about 250 psig. In various other aspect, the pressure may be about 10 to about 200 psig, about 10 to about 100 psig, about 10 to about 75 psig, about 10 to about 50 psig, about ll) to about 25 psig, about 20 to about 250 psig, about 20 to about 200 psig, about 20 to about 100 psig, about 20 to about 75 psig, about 20 to about 50 psig, about 20 to about psig, about 30 to about 250 psig, about 30 to about 200 psig, about 30 to about 100 psig, about 30 to about 75 psig, about 30 to about 50 psig, about 40 to about 250 psig, about 40 to about 200 psig, about 40 to about 100 psig, about 40 to about 75 psig, about 40 to about 50 psig, about 50 to abOut 250 psig, about 50 to about 200 psig, about 50 to about 200 psig, and about 50 to about ’75 psig.

In one aspect, in certain size fermentors, syngas is introduced into the gas inlet/sparger 120 at a rate of about 10 to about 50 {13/360, and in another aspect, a rate of about 25 to about 35 ec. Pressure is controlled h controlling the rate at which syngas is introduced in combinatiori with controlling the rate at which gas is exhausted from the reaction vessel. Pressure may be measured in the reactor headspace or at the bottom of the reactor vessel.

In one aSpect, sparger holes 550 and a pressure drop across the hole is important for improving the tric mass transfer rate of CO. A pressure drop across sparger holes 550 needs to be high enough to ensure bution of gas bubble around the sparger assembly 540. in this aspect, ng is effective to e a pressure drop across the sparger holes 550 of about 0.5 psi to about 2.5 psi, and in another aspect about 1 psi to about 2 psi. The sparger holes 550 provide advantages over other forms of spargingr exampie, sparger holes 550 are effective for avoiding fouling, as may occur with sintered metal spargers. Further, the sparger holes 550 are effective for providing consistent gas bubble sizes which contribute towards improved mass transfer.

Another factor that may affect the mass transfer rate is gas retention time. In this aspect, the hioreactor is effective for providing a gas retention time of at least about 2 minutes, and in another aspect, a gas retention time of about 2 minutes to about 15 l5 minutes, in and in another aspect about 5 to about 10 minutes. Gas retention time (GRT) may be determined ing to the following formula: GRT = liguid volume gas flow rate (in or out) 'l'emperature and ionic strength may also have an affect on the mass er rate.

In this aspect, the temperature of the bioreactor is about 30 to about 50 °C.

An alternative ration of the boot 400 is shown in Figure 5. In this aspect, the boot 400 is utilized as a growth reactor during startup. The boot is configured to include a boot r 600. The boot also includes a hoot mixer. The boot mixer may be configured with any known mixing apparatus. For example, gas mixing may be ed with impellers (not shown) or with a gas lift type fermentor equipped with a draft tube 620. As shown in Figure 5, the gas lift fementor is effective for ating bubbles 610 and cells around the boot 400. Other reactor designs including a bubble type r, and external gas loop or jet type reactor may be utilized.

The alternative boot configuration is utilized by inoculating acetogenic bacteria into a medium contained in a boot portion of a reactor vessel. The medium in the boot fills at least about 75% of a total volume of the boot, in another aspect at least about 80%, in another aspect at least about 85%, in another aspect at least about 90%, and in another aspect at least about 95%. The boot is sparged with syngas and mixed for a time effective to provide a target cell density. In this aspect, the target cell density will be about 5 to about 40 grams/liter, and in various other aspects, about 5 to about 30 grams/liter, about to about 20 grams/liter, about 5 to about 15 grams/liter, about 10 to about 40 grams/liter, about 10 to about 30 grains/liter, about 10 to about 20 grams/liter, and about 10 to about grams/liter. Upon reaching a target cell density, medium levels are allowed to rise out the boot and into the reactor vessel to previously indicated levels. Sparging and mixing in the boot is stopped and the fermentation proceeds as previously described.

In another , the cell y in the boot be brought to a level oi‘at least about 3 grams per liter or any of the cell densities described . Upon reaching a cell density of at least about 3 grams per liter, medium is added at a rate effective to allow the cell density level to remain at a level of at least about 3 grams per liter. Upon reaching a desired medium level, sparging and mixing in the boot is stopped and the fermentation proceeds as previously described EXAMPLE Pilot plant scale tations were conducted to determine km. The kLa was measured around 60 g ethanol/(L-day) STY (space time yield). An estimation of ion was done by forcing the reaction under mass transfer limitation condition, or zero dissolved CO concentration. This was lished by effecting a temporary reduction in either flowrate or agitation rate so that there were an excess of cells for the gas available. Under these conditions, CO is reacted away as soon as it is ved so that the reaction is was transfer limited. The CO dissolved into the solution is the same as the ence between the CO in the fcodgas and the CO in the product. In a mass transfer limited system, this difference is the mass transfer rate at a given ion.

The basic equation utilized was [on m (jkia(l’3/VI)“vbsg where kha = volumetric mass transfer coefficient (m3 gas/s/m3 liquid) Cm = Constant for a given system Pg = gassed agitator power consumption (W) V; :4 Liquid volume (m3) vsg == icial gas velocity (in/s) a = scale up constant '0 — scale up constant Runs were conducted at 6' psig (head pressure) and measurements were made at 60 g ethanol/(L'day) S’I‘Y. Results were as follows: Celi co féion % Concentration (grams/liter) 90.3 While the invention herein disclosed has been described by means of specific embodiments, examples and applications thereof, numerous modifications and variations could be made thereto by those skilled in the art without ing from the scope of the invention set forth in the claims.

Claims (15)

1. A process for fermentation of syngas, the process comprising: mixing the syngas with acetogenic bacteria in a liquid nutrient medium in a reactor vessel, wherein the syngas is introduced into the reactor vessel through a gas r, the gas sparger located below the liquid nutrient medium level in the reactor vessel, wherein the gas sparger es holes having a diameter of 10 mm or less, the syngas being introduced such that the syngas pressure drop across the sparger is 3.4 to 17.2 kPa (0.5 to 2.5 psi) and at a flow rate effective for maintaining a pressure inside of the reactor vessel of at least 6.9 kPag (1 psig), wherein the syngas has a CO/CO2 molar ratio of at least 0.75; and providing an agitation energy input to the reactor vessel of 0.01 to 12 kWatts/m3 medium, wherein the process is ive for ing a volumetric CO mass transfer coefficient of 100 to 1500 per hour and a STY (space time yield) of at least 10 g ethanol/(L·day).

2. The process of claim 1 wherein agitation in the reactor vessel is provided by one or more of a mechanical agitator, gas ion, liquid injection, and liquid recirculation (pump around).

3. The process of claim 1 which further comprises: ting the syngas with at least one gas dispersion er located above the gas sparger; and mixing the syngas with acetogenic bacteria with at least one mixing impeller located above the gas dispersion impeller, wherein the gas dispersion impeller and mixing impeller are operably connected to an agitator through a drive shaft, the agitator providing an agitation energy input of 0.3 to 12 kWatts/m3 medium.

4. The process of claim 1 or claim 3 wherein the gas sparger es holes having a diameter of 2.5 mm or less.

5. The process of claim 1 or claim 3 wherein the syngas is introduced into the 10836282_1 reactor vessel at a gas ty of 25 m/sec or greater at an exit of the holes.

6. The process of claim 1 or claim 3 wherein the holes in the sparger are spaced apart and point in a downward direction.

7. The process of claim 1 or claim 3 wherein the agitation energy is 0.9 to 12 kWatts/m3.

8. The process of claim 1 or claim 3 wherein syngas is introduced at a flow rate effective for maintaining a pressure inside of the r vessel of at least 69 kPag (10 psig).

9. The process of claim 1 or claim 3 wherein the process is effective for providing a volumetric CO mass transfer coefficient of 200 to 1100 per hour.

10. The process of claim 1 wherein the reactor vessel includes a CO concentration gradient where the CO concentration near the gas sparger is higher than at a higher than at a higher level of the reactor vessel and/or wherein the ratio of CO tration at a bottom portion of the reactor to the concentration at an upper n of the reactor is 100:1 to 10:1.

11. The process of claim 3 wherein the process is effective for providing an acetogenic cell density of at least 2 grams per liter.

12. The process of claim 3 wherein the process is effective for providing a liquid retention time of 10 to 400 hours and/or wherein the process is ive for providing a gas retention time of 2 to 15 minutes.

13. The process of claim 3 wherein the syngas has a CO t of at least 20 mole % and/or wherein the syngas includes less than 10 ppm oxygenated or non-oxygenated aromatics.

14. The process of claim 3 wherein the acetogenic bacteria is selected from the group consisting of enium kivui, Acetoanaerobium noterae, Acetobacterium woodii, 10836282_1 Alkalibaculum bacchi CP11 (ATCC 72), Blautia producta, Butyribacterium methylotrophicum, Caldanaerobacter subterraneous, Caldanaerobacter subterraneous pacificus, Carboxydothermus hydrogenoformans, Clostridium aceticum, Clostridium acetobutylicum, Clostridium acetobutylicum P262 (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 19630 of DSMZ Germany), Clostridium autoethanogenum (DSM 10061 of DSMZ Germany), Clostridium autoethanogenum (DSM 23693 of DSMZ Germany), Clostridium autoethanogenum (DSM 24138 of DSMZ Germany), Clostridium carboxidivorans P7 (ATCC PTA-7827), Clostridium coskatii (ATCC PTA-10522), Clostridium drakei, Clostridium ljungdahlii PETC (ATCC 49587), Clostridium ljungdahlii ERI2 (ATCC 55380), Clostridium ljungdahlii C-01 (ATCC , Clostridium ljungdahlii O-52 (ATCC 55889), Clostridium magnum, idium pasteurianum (DSM 525 of DSMZ y), Clostridium ragsdali P11 (ATCC BAA-622), Clostridium scatologenes, idium thermoaceticum, Clostridium ultunense, Desulfotomaculum kuznetsovii, Eubacterium limosum, Geobacter reducens, Methanosarcina acetivorans, Methanosarcina i, la thermoacetica, Morrella thermoautotrophica, Oxobacter pfennigii, Peptostreptococcus productus, coccus productus, Thermoanaerobacter kivui, and mixtures thereof.

15. Syngas fermented according to the process of any one of claims 1 to 14. INEOS Bio SA By the Attorneys for the Applicant SPRUSON & FERGUSON Per: 10836282