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This invention provides an activated sludge process for treating wastewater containing ammonia as a contaminant and further for treating wastewater containing ammonia as a contaminant and other contaminants which may possibly be present including cyanide, thiocyanate, sulfide and/or organics, wherein the process involves treating wastewater in the presence of an appropriate microorganism population acclimated to the wastewater contaminants and their levels in the wastewater, this microorganism population including (1) nitrifying microorganisms capable of converting ammonia to nitrite, (2) optionally, nitrifying microorganisms capable of converting nitrite to nitrate, and (3) facultative microorganisms capable of denitrifying nitrite and/or nitrate by oxidizing organic material and converting nitrite and/or nitrate to free nitrogen, with the process being operated under a series of controlled conditions to ultimately achieve in the activated sludge process a microbial conversion of ammonia to nitrite and/or nitrate and then to free nitrogen. The conditions controlled in the process of this invention include control of the sludge wastage rate, hydraulic residence time, dissolved oxygen level (DO), sludge mixing rate, biological oxygen demand (BOD), pH and temperature, as described hereinafter. Optionally, (4) other microorganisms capable of converting other contaminants such as cyanide and thiocyanate to ammonia and sulfide to sulfate can also be present.
FIELD OF THE INVENTION This invention relates to an activated sludge process for treating wastewater. More particularly, this invention relates to an activated sludge process for treating wastewater containing ammonia as a contaminant and further for treating wastewater containing ammonia as a contaminant and other contaminants which may possibly be present including cyanide, thiocyanate, sulfide and/or organics. The activated sludge process of this invention involves treating wastewater in the presence of an appropriate microorganism population acclimated to the wastewater contaminants and their levels in the wastewater. The microorganism population includes (1) nitrifying microorganisms capable of converting ammonia to nitrite, (2) optionally nitrifying microorganisms capable of converting nitrite to nitrate, and (3) facultative microorganisms capable of denitrifying nitrite and/or nitrate by oxidizing organic material and converting nitrite and/or nitrate to free nitrogen. The process is operated under a series of controlled conditions to ultimately achieve in the activated sludge process a microbial conversion of ammonia to nitrite and/or nitrate and then to free nitrogen. Conditions controlled in the process of this invention include control of the sludge wastage rate, hydraulic residence time, dissolved oxygen level (DO), sludge mixing rate, biological oxygen demand (BOD), pH and temperature, as described hereinafter. Optionally, (4) other microorganisms capable of converting other contaminants such as cyanide and thiocyanate to ammonia and sulfide to sulfate can also be present in the microorganism population. This invention also relates to a process for producing an appropriate microorganism population, including (1) nitrifying microorganisms capable of converting ammonia to nitrite, (2) optionally nitrifying microorganisms capable of converting nitrite to nitrate and (3) facultative microorganisms capable of denitrifying nitrite and/or nitrate by oxidizing organic material and converting nitrite and/or nitrate to free nitrogen, by a controlled development and acclimation of the microorganism population to the nature of the wastewater containing ammonia as a contaminant, particularly at high levels. BACKGROUND OF THE INVENTION A large amount of interest has arisen as a result of environmental pollution concerns on treatment of municipal and industrial wastewaters. As a result of federal, state and local regulations as well as concerns on protecting the environment, a large amount of research and development effort has gone into the treatment of wastewater from various sources and particularly wastewater arising from industrial facilities. Often in treatment of wastewater from industrial and municipal sources, the activated sludge process has been employed conventionally for treatment and purification to the extent that the treated water can be reused or returned to the environment. Where wastewater arises from industrial operations, the wastewater can contain problem contaminants, in general not normally found in wastewater from municipal sources, and these include industrial wastewaters containing as contaminants, ammonia, cyanide, thiocyanate, sulfide and organic materials, even of a complex nature. Further, industrial wastewaters can contain contaminants at concentrations which significantly exceed those found in wastewaters from municipal sources. In particular, wastewaters which contain ammonia as a contaminant are produced in a wide variety of industrial operations and problems presently exist in appropriately treating wastewaters where the wastewater contains a high concentration of ammonia. It is economically advantageous therefore to develop treatment procedures for wastewaters which, in raw form, contain not only ammonia in high concentrations, but typically a wide variety of contaminants other than ammonia. In fact, where wastewaters contain high concentrations of ammonia, state-of-the-art systems conventionally employed to treat these wastewaters to render them environmentally acceptable for discharge into the ecosphere are complex and extremely expensive. To illustrate this further, raw wastewater containing high concentrations of ammonia can arise in industrial processing in coke plants, petroleum refineries, oil shale retorting, coal gasification processes and coal liquefaction processes. Ammmonia-containing wastewaters can also arise from pharmaceutical processing, munitions manufacture, food processing and fertilizer manufacture. Typical compositions of contaminants present in one illustrative subset of typical wastewaters containing high concentrations of ammonia are shown in Table 1 below.
Typical Wastewater Composition (mg/l)
Wastewater Phen-
Source NH.sub.3 COD olic CN.sup.-
1,800 2,500 400 10 100 200
Coking to to to to to to
6,500 10,000 3,000 100 1,500 600
Refining to to to
7,000 1,000 11,000
Oil Shale
1,000 8,100 .about.45
0 .about.55
to to to to
7,300 10,800 21 220
Slagging 2,000 7,000 1,400 4 15 100
Lurgi Process
to to to to to to
17,000 21,000 4,000 15 300 500
Hygas 2,600 3,000 560 0.1 17 60
Process to to to to to to
4,600 5,000 900 0.7 45 220
Grand Forks
4,000 21,000 3,500 1 80 60
Energy Tech.
to to to to to to
Center 7,500 30,000 6,000 50 200 300
Solvent Ref.
N.A. N.A. .about.5,000
Biodegradable Organic N (TKN)
100's to 1000's
NH.sub.3 --N
COD Not Limited
S.sup.= 10's to 1000's
SCN.sup.- 100's
CN.sup.-, FREE 1's to 100's
CN.sup.-, TOTAL 1's to 10's
SUSPENDED SOLIDS <1000's
Alkalinity Not limited
TKN = Total Kjeldahl Nitrogen
The maximum allowable sludge wastage rate (e.g., in lbs/day) will vary with the total quantity of sludge involved, but in all cases the maximum allowable rate is based upon the replenishment rates for various types of microorganisms (e.g., nitrifying microorganisms, facultative microorganisms in lbs/day) and the percentage of the bulk sludge represented by each type of microorganism, respectively, in accordance with the following: ##EQU1## where the Maximum Sludge Wastage Rate is determined as the smallest of the Sludge Wastage Rates, calculated for each type microorganism present. The minimum sludge wastage rates necessary to avoid solids buildup in the sludge is determined by establishing (a) the net rate of inert solids input (i.e., arising from feed wastewater and sludge production) and (b) the steady state concentration of inert solids in the sludge which is desired in accordance with the following: ##EQU2## The above equations are exemplified in the English system of units but it is clear that using the principles described, sludge wastage rate calculations in other than the English system of units can be made. It should be noted that the minimum sludge wastage rate can be decreased by increasing the steady state fraction of the sludge which is inert solids. Within the limits described above, operation at as low an actual sludge wastage rate as is possible is generally preferred, with a substantially zero actual sludge wastage rate being especially preferred, unless enhanced reaction kinetics associated with microorganism growth are desired. Whether a steady state is achieved can be determined by determining the amount of sludge present and the amount of sludge lost or affirmatively described from the system to the extent that sludge increase as a result of microorganism population increase due to sludge growth and inert solids level increase are substantially equal to the amount of microorganisms and inert solids lost or affirmatively discharged as sludge with effluent from the system. Optimally, the system will be operated at substantially a zero actual sludge wastage rate such that (i) the growth of the microorganism population in terms of increase in number of microorganism cells is substantially equal to the loss of microorganism cells which inherently occur as a result of wastewater passed through the system during treatment and any microorganism cells affirmatively discharged and (ii) the inert solids level which arises as a result of input in the wastewater and production in situ in the sludge remains the same as a result of selecting increasing sludge concentration in the effluent discharged from the system. The actual sludge wastage rate can be determined by monitoring various variables such as total suspended solids in the inflow of raw wastewater to the system and in the outflow of treated water effluent from the system. The actual sludge wastage rate can be controlled by (1) measuring the suspended solids level in the wastewater feed and in discharge water from the sludge, (2) determining the average production rate of inert solids within the sludge, and (3) controlling the actual sludge wastage rate to between the Maximum and Minimum Sludge Rate as determined by equations (A) and (D) above. The replenishment rate of various types of microorganisms can be measured (directly or indirectly) from the quantity of nitrifying microorganisms and the knowledge gained after establishing their growth rate per unit weight of wastewater fed. Monitoring of suspended solids levels in the wastewater feed and discharge water from the sludge and measurement of the inert solids production rate per unit of sludge provides the necessary data to determine the inert solids flow in the sludge system. For example with a wastewater feed flow of 200 gpm, an ammonia concentration of 2500 mg/l and an effluent suspended solids concentration of 50 mg/l, (an input of 6048 lb/N/day and 121 lb inert solids/day), the sludge population required for the conversion of ammonia to nitrogen is (a) 2520 lb VSS (volatile suspended solids) of Nitrosomonas (if Nitrosomonas specific oxidation rate is 2.4 lb N/lb VSS/day), (b) 864 lb VSS of Nitrobacter (if Nitrobacter specific oxidation rate is 7.0 lb N/lb VSS/day and (c) 100,800 lbs VSS of heterotrophic facultative/denitrifying microorganisms (if specific denitrification rate is 0.06 lb N/lb VSS/day) for a total mass population of 104,184 lb VSS. The growth rate of Nitrosomonas is 0.10 to 0.20 lb VSS per lb of existing Nitrosomonas VSS per day. Thus, the replenishment rate of Nitrosomonas for a population of 2520 lb VSS is about 378 lbs of Nitrosomonas VSS per day, and the corresponding Maximum Sludge Wastage Rate based upon Nitrosomas replenishment rate would be 15,628 lb VSS per day (as calculated and using Equation (A) above), and the Minimum Sludge Wastage Rate would be 173 lb per day (at a steady state inert solids loading of 0.7) calculated using the above Equations (B) to (D). This calculation set forth herein, of course, is for exemplification and is not to be construed as limiting this invention in any way. As described above, the actual sludge wastage rate is an important parameter to be controlled. More specifically, above a critical sludge wastage rate, the rate of loss of one or more types of microorganisms, e.g., the slow growing nitrifying organisms, will exceed both their growth rate during sludge development and their replenishment rate in fully developed sludge. For successful sludge development and stable maintenance of sludge, this critical sludge wastage rate must not be exceeded. Critical sludge wastage rates will vary with the specific nature of the wastewater to be treated by the process of this invention since sludge pH, temperature and dissolved oxygen level all will influence the sludge growth rates. Sludge development is achieved most quickly and sludge maintenance is accomplished most smoothly by operating as closely as possible to the preferred zero actual sludge wastage rate described above. The most preferred system operation is to utilize a substantially zero actual sludge wastage rate. The term "zero actual sludge wastage rate" as used herein defines a rate at which sludge is wasted from the system, i.e., lost or affirmatively discarded, as a result of system operation and wastewater pass through, such that a steady state of microorganisms capable of converting ammonia to nitrite and/or nitrate is achieved and a steady level of inert solids exists. However, the process of this invention can be operated successfully, advantageously and economically by operating within the Minimum and Maximum Sludge Wastage Rates as set forth above. Preferably operation is within about 20% above the minimum rate to about 20% below the maximum rate, more preferably within about 40% above the minimum rate to about 40% below the maximum rate and most preferably at an actual sludge wastage rate of substantially zero. Thus, in the manner described above, the sludge wastage rate for operation of the process of this invention can be controlled to achieve a steady state of microorganisms capable of converting ammonia to nitrite and/or nitrate with this steady level being not only achieved but also maintained. (2) Hydraulic Residence Time Given a natural economic incentive to operate the process of the present invention at low hydraulic residence times (HRT), the HRT must be controlled to be (i) long enough to preserve full specified performance of the sludge given the sludge quantities and reaction rates established during microorganism population acclimation, and (ii) long enough to yield a sludge concentration with acceptable sludge/wastewater separation characteristics in relation to control of sludge wastage rates. Decreases from the HRT of initial sludge acclimation must be managed with additional sludge acclimation over that initially achieved, with this sludge acclimation being subject to all of the parameters outlined hereinbefore for sludge microorganism population acclimation. HRT describes the contact time allowed for reaction of feed wastewater with the sludge. Given a specific wastewater feed load, dissolved oxygen level, pH and temperature, HRT is interrelated to the steady state quantity and concentration of a sludge required to accomplish the specified treatment. This relationship is illustrated schematically in FIG. 3. Although the relationship is similar for different combinations of treatment conditions, a discrete relationship exists for each specific combination of feasible values of wastewater feed load, system dissolved oxygen level, and system pH and temperature. As HRT is reduced, FIG. 3 shows for one specific example that the steady state sludge concentration must increase to complete the desired reactions in the alotted time. Increasing sludge concentration involves growing all microorganisms in the sludge, in particular slow growing nitrifying microorganisms. Growth of microorganism populations constitutes sludge acclimation and must be conducted considering the procedures described hereinbefore for sludge microorganism population acclimation. With proper attention to incremental sludge acclimation requirements, HRT can be reduced and sludge concentration correspondingly increased until the point is reached where effective sludge/wastewater separation cannot be achieved to comply with the maximum allowable sludge wastage requirement described hereinbefore. This maximum sludge concentration and associated minimum HRT is a function of the settleability characteristics (natural or induced e.g., using coagulating or flocculating agents such as polyelectrolytes and other agents which might be used for sludge conditioning (e.g., Ca.sup.++) to include settling of the sludge) and can be expected to vary with the specific application of the process of this invention. In general, it has been found experimentally that hydraulic residence times of about 5 days to about 35 days, preferably 5 to 20 days, preferably 5 to 10 days and most preferably 5 days or less can be suitably used in the process of this invention. To the extent that denitrification remains rate limiting in sludge performance, denitrification to an extent less than complete provides the ability to use lower hydraulic residence times. (3) Dissolved Oxygen Level A further parameter which needs to be controlled when operating this embodiment of the process of this invention is the dissolved oxygen level. Dissolved oxygen levels must be controlled to be sufficiently high that microbial conversion of ammonia to nitrite and nitrite and/or nitrate in accordance with reaction schematic (I) and (II) above occurs but lower than the dissolved oxygen level at which microbial conversion of nitrite and/or nitrate to free nitrogen in accordance with reaction schematic (III) above ceases to occur. An important aspect of this embodiment of the process of this invention is the ability concomitantly to provide essentially complete aerobic nitrification and controllable amounts of anoxic denitrification from zero to essentially 100 percent using a single sludge under ostensibly aerobic conditions. Facultative heterotrophic microorganisms are known to form what appears to be microbial cell "agglomerates". In conventional activated sludge practice, efforts are made to ensure that sufficient dissolved oxygen levels are present in the sludge to ensure that the whole of these agglomerates acts aerobically by oxygen permeation thereinto. However, as have others, the inventor of the invention described and claimed herein postulated in 1977 as described hereinbefore that at low enough dissolved oxygen levels and high enough bulk sludge concentrations, these agglomerates may exhibit anaerobic, or anoxic, behavior. It has now been found experimentally that agglomerates of some form do exist in the sludge and that agglomerates begin to form at very low bulk sludge concentrations, for example, at least as low as about 1800 mg/l. These agglomerates may grow somewhat in size and number as the bulk sludge concentration in the system increases. Experimentally, it has further been demonstrated that these agglomerates exhibit variable degrees of anoxic behavior in the form of bulk denitrification reaction rate (e.g., in pounds of nitrite/nitrate consumption per day per pound of denitrifying microorganisms) as a function of bulk sludge concentration and sludge dissolved oxygen levels. However, in contrast to the speculation in 1977 by the inventor of the invention described and claimed herein, denitrification has been shown to occur at low sludge concentrations, at least as low as 1800 mg/l. Further, although there may be some effect of sludge concentration on sludge denitrification kinetics, experimental evidence suggests that this effect is minor. In further contrast to the inventor's 1977 observations and speculations, it has now been demonstrated experimentally that depending upon the specific sludge involved, dissolved oxygen levels substantially different from 1 mg/l may be used to achieve anoxic regions and denitrification in the sludge. Some sludges have achieved substantially complete denitrification at 1 mg/l with indications that they could sustain denitrification at higher dissolved oxygen levels, e.g., as high as 1.5 to 2.0 mg/l. Other sludges have achieved relatively low denitrification (e.g., less than 20%) even at dissolved oxygen levels as low as 0.2 to 0.3 mg/l. Thus, in contrast to conventional approaches using sufficiently high dissolved oxygen levels that agglomerate permeation by oxygen is achieved, in the process of this invention, the dissolved oxygen level is controlled to ensure anoxic regions in the agglomerates. For those sludges which develop substantial anoxic regions and therefore substantial denitrification capacity per weight of sludge, at dissolved oxygen levels which are high enough to support effective performance of nitrifying microorganisms, continuous supply of oxygen at a controlled low level is preferred in the operation of the invention. Example 1 below illustrates this mode of operation. Where sludges achieve relatively small anoxic regions and therefore relatively low denitrification capacity per weight of sludge even at dissolved oxygen levels below which effective performance of nitrifying microorganisms is achievable, intermittent supply of oxygen at controlled levels can be used to achieve desired levels of denitrification without interference of nitrification reactions. Example 5 illustrates this mode of operation. In this mode of operation of the invention, dissolved oxygen levels are first set at the level at which the anoxic region and corresponding "aerobic" denitrification capacity of the sludge is maximized subject to the constraint that effective nitrifying microorganism activity is maintained. This will typically occur at dissolved oxygen levels of between 0.3 and 0.75 mg/l. Using the same sludge and in the same reactor, the anoxic region and corresponding denitrification capacity of the sludge is then expanded by intermittently dropping the dissolved oxygen level to zero by interrupting oxygen flow to the sludge. The number and duration of the interruptions of oxygen flow can be varied according to the level of denitrification desired subject to the constraint that substantially complete nitrification is achieved and pH control is maintained. One example of an intermittent aeration cycle involves alternating periods of oxygen on and oxygen off. The above can be considered as producing a denitrification reaction rate per weight of sludge, which depends upon the sludge involved, the dissolved oxygen concentration imposed, and the frequency and duration of cycling of the sludge oxygen supply. Below a critical dissolved oxygen concentration, inhibition of facultative microorganism aerobic reactions within the sludge begins to develop. Correspondingly, denitrification begins to occur, with bulk denitrification rates per unit weight of sludge increasing thereafter with decreasing dissolved oxygen level as the percentage of facultative microorganisms in the sludge available for denitrification increases. In the limit which occurs during interruptions of sludge air supply, denitrification rates increase to the rate of denitrification consistent with utilization of all the facultative microorganism population in the sludge for denitrification reactions. At dissolved oxygen levels of zero, denitrification rates of 0.17 to about 0.9 mg of nitrogen per day per mg of sludge have been reported (see R. P. Michael, "Optimization of Biological Denitification Reactors in Treating High Strength Nitrate Wastewaters" Master of Science Thesis, Department of Civil Engineering, University of Vermont, Burlington, Vt., May 1973 and R. J. Cummings, "Comparison of the Capabilities of Denitification in Anaerobic Activated Sludge and Packed Column Reactors" Master of Science Thesis, Department of Civil Engineering, University of Vermont, Burlington, Vt., 1973). At dissolved oxygen levels of about 0.3 to 0.75 mg/l needed for effective performance of nitrifying microorganisms, bulk sludge denitrification reaction rates experimentally measured are less than 0.17 to 0.9 mg/day/mg reported in Cummings, supra, and Michaels, supra. Where sludges achieve substantially complete denitrification without resort to cycling of the sludge aeration supply, denitrification rates of 0.02 to 0.06 mg of nitrogen per day per mg of sludge have been measured. For sludges that require cycling to achieve desired levels of denitrification, "aerobic" denitrification rates are less than those above. In the cycling mode of operation, combined "aerobic" and anaerobic denitrification rates can be equal to or greater than 0.02 to 0.06. Suitable cycling periods can include cycling every hour, every two hours, every four hours, etc. These cycling periods are not to be construed as limiting, however. Thus, the present invention provides a "window" of dissolved oxygen concentration within which substantive amounts of concomitant nitrification and "aerobic" denitrification can occur in the same sludge, i.e., anoxic and aerobic reactions concomitantly occurring. Where levels of "aerobic" denitrification and/or the "aerobic" denitrification reaction rates achieved when operating effectively at strictly continuous dissolved oxygen levels are below those desired, they can be supplemented with anaerobic denitrification through on/off cycling of the oxygen supply to the sludge. This has the effect of producing a weighted average dissolved oxygen level in the sludge mixture which is low enough to accomplish additional denitrification and yet still intermittently high enough to maintain effective performance of nitrifying microorganisms. The lower limit of the "window" is the minimum oxygen level at which aerobic nitrification occurs, i.e., about 0.1 to 0.3 mg/l, while the upper limit of this "window" basically is the maximum oxygen level at which "aerobic" denitrification occurs, i.e., experimentally determined in some sludges to be at or below about 1 mg/l and more probably up to about 1.5 to 2 mg/l. Thus, the process of this invention can be operated at a dissolved oxygen level of about 0.1 mg/l to about 2 mg/l, preferably about 0.1 mg/l to about 1.5 mg/l and most preferably about 0.1 mg/l to about 1 mg/l in all cases achieved either as a dissolved oxygen level achieved on a continuous basis or as the weighted average dissolved oxygen level which results from on/off cycling of the oxygen to the sludge. It will be clear to one skilled in the art that the dissolved oxygen concentration for the sludge and its schedule of supply will thus vary with the specific system and wastewater to be treated, to the point where the autotrophic microbial reaction rate for nitrification is severely reduced. Lower dissolved oxygen levels favor increased denitrification kinetics and correspondingly reduce the sludge requirements for denitrification. In order to explain further the ability in this embodiment of the process of this invention controllably to achieve nitrification/denitrification or, said in another way, to achieve aerobic and anaerobic reactions concomitantly within the same bulk sludge, this aspect of the invention is described by example by way of FIG. 4. FIG. 4 shows schematically a cross sectional view of an idealized sludge agglomerate, where in FIG. 4, A represents the sludge agglomerate, B represents an aerobic region therein, i.e., a region where the dissolved oxygen concentration is sufficiently high that aerobic reactions such as nitrification can occur, and C represents an anoxic region within the agglomerate where anoxic reactions, i.e., denitrification (or conversion of nitrite and/or nitrate to free nitrogen), occur. The vertical arrow and the horizontal arrow superimposed on the agglomerate correspond to the dissolved oxygen concentration and distance from the agglomerate center, respectively. From the plot of dissolved oxygen concentration as a function of distance into the agglomerate, it can be seen that the dissolved oxygen concentration within the agglomerate decreases as the distance from the agglomerate surface increases, falling from the dissolved oxygen concentration in the bulk liquid at the agglomerate surface to a dissolved oxygen concentration of zero at some point within the agglomerate. The point at which the dissolved oxygen level falls to zero defines the beginning of the anoxic region of the agglomerate. Thus, in order to achieve concomitant nitrification/denitrification in accordance with this embodiment of the process of this invention, the dissolved oxygen concentration is controlled at a level to permit both nitrification and denitrification reactions to occur. The bulk dissolved oxygen level and the frequency and duration of any on/off cycling of the oxygen supply can be easily accomplished and measured using conventional techniques and the necessary oxygen to achieve an appropriate dissolved oxygen level can be added to the system simply by pumping air, oxygen enriched air, or oxygen into the system by any of a number of conventional means now employed in activated sludge processes for introduction of oxygen in a dissolved form into the system. The dissolved oxygen level and any schedule of on/off cycling of the oxygen supply can be continuously monitored and appropriately controlled within the levels described above in order to ensure desired nitrification/denitrification reactions do occur. To explain this dissolved oxygen effect even further, attention is directed to FIGS. 5 and 6. FIG. 5 schematically illustrates the relationship between hydraulic residence time and sludge concentration for concomitant and complete nitrification and denitrification of any specified wastewater load, viz., pounds per day of nitrogen load to be treated. It shows the "window" which exists at a lower limit of bulk dissolved oxygen of about 0.1 mg/l to achieve nitrification and an upper limit to concomitantly achieve denitrification. Further, FIG. 6 schematically outlines the relationship between hydraulic residence time and sludge concentration for complete nitrification with various levels of denitrification, i.e., conversion of nitrite and/or nitrate into free nitrogen, from zero to essentially complete or 100% denitrification. The process of the present invention is applicable to all levels of denitrification in combination with substantially complete nitrification. (4) Degree of Sludge Mixing An additional variable which must be controlled in order to achieve the objects of this embodiment of the process of this invention is the degree of sludge mixing. The degree of sludge mixing is controlled so that (i) the degree of mixing is large enough to achieve a substantially complete contacting of sludge with fresh wastewater thereby ensuring the utilization of all sludge while avoiding stimulation of undesired incremental sludge growth to such an extent that the maximum allowable sludge wastage rate is exceeded, (ii) the degree of mixing is large enough to reduce gradients in levels of dissolved oxygen in the sludge mixture to levels consistent with desired levels of sludge denitrification, and (iii) the degree of mixing is not high enough that disruption of sludge agglomerates occurs resulting in loss of denitrification capacity due to break up of sludge agglomerates, and/or microbial cell rupture occurs resulting in deterioration of all reaction kinetics and/or significant deterioration of sludge/water settleability characteristics occur. Basically, since slow growing nitrifying microorganisms are present in fully acclimated sludge used in this embodiment of the present invention in quantities just sufficient for feed nitrogen consumption, the feed wastewater and sludge must be continuously and completely mixed or incomplete nitrification of feed wastewater will occur. Incomplete wastewater/sludge mixing will also result in a stimulation of sludge growth. This creates a situation which forces increased sludge wastage rates, and at some point of incremental sludge production and wastage, results in a net decline in nitrifying microorganism population and the corresponding failure of sludge performance. Various types of conventional agitators or mixing devices can be used to achieve necessary levels of sludge/wastewater mixing. Nitrification performance is a direct measure of the adequacy of mixing of a fully acclimated sludge. The degree of mixing is therefore increased until, by measurement of ammonia levels in feed wastewater to and discharge water from the sludge, nitrification is essentially complete. Further, since techniques for dissolution of oxygen into the wastewater/sludge mixture all result in a gradient in dissolved oxygen levels between levels which can rise to saturation at the point of air or oxygen addition and targeted dissolved oxygen levels in the surrounding bulk mixture, the proportion of the sludge/wastewater mixture experiencing this gradient to the total amount of sludge/wastewater present is controlled by the degree of mixing of sludge and wastewater. Techniques for oxygen addition include use of surface aerators which create dissolved oxygen gradients from the surface downward into the mixture and submerged diffusers which create dissolved oxygen gradients in the region surrounding each diffuser. Techniques for mixing include mechanical agitators and devices which use the buoyancy effects of the injected air or oxygen. In general, the degree of mixing required to control dissolved oxygen gradients decreases as the number of point sources of oxygen addition increases and the degree of mixing increases as the proportion of the sludge/wastewater mixture to the total mixture present permitted to experience a gradient decreases. Both nitrification and denitrification performance serve as individual measures of the adequacy of mixing. Direct monitoring of dissolved oxygen levels throughout the sludge and wastewater mixture provides another source of measurement. Assuming that bulk dissolved oxygen concentrations achieved are both high enough to sustain complete nitrification yet low enough to establish anoxic regions in the sludge (and therefore the capacity for denitrification by the sludge), overall sludge denitrification rates will vary as the proportion of sludge exposed to dissolved oxygen gradients varies. Decreasing the proportion of the sludge exposed to oxygen gradients (through increases in sludge/wastewater mixing) will result in higher overall sludge denitrification rates and therefore improved overall sludge denitrification performance. Further, since mixing exposes the sludge to shearing forces, the severity of mixing, i.e., total induced shearing forces, must be controlled to avoid both excessive breakup of sludge agglomerates and the irreversible rupturing of microbial cell structures. Denitrification performance of the sludge serves as one measure of the onset of excessive shear mixing forces. As discussed hereinbefore with respect to the dissolved oxygen level, in order to achieve concomitant nitrification and denitrification, the bulk dissolved oxygen concentration is appropriately controlled to the extent that, within sludge agglomerates which are formed in the system and are present in the system, aerobic and anoxic regions in the agglomerates exist. As a result, extensive break up of sludge agglomerates can result in a destruction of anoxic regions in the sludge agglomerates. It has been found during the operation of this embodiment of the process of this invention, that as a result of mixing and shear forces arising, sludge agglomerates do break up but these breakups are not irreversible, i.e., it has been found that even with sludge mixing rates sufficiently high that on a microscopic scale, break up of the sludge agglomerate occurs, these particles of the agglomerates substantially immediately reform into agglomerates with basically no substantial effect on the anoxic behavior arising from the sludge agglomerate. As long as the degree of mixing does not cause excessively frequent break up of the agglomerates and a break up of the sludge agglomerates to the extent that reformation of the agglomerates is markedly delayed or is not possible, in a relatively short period of time, then this is an acceptable sludge mixing rate from this standpoint. To the extent that irreversible breakdown of the structure of sludge agglomerates occurs, it will result in loss of activity of the sludge and therefore loss of the denitrification capacity of the sludge. Mixing shearing forces can be increased until measurement indicates the onset of a distinct decline in sludge denitrification performance, all other conditions being equal. Nitrification performance of the sludge also serves as one measure of the onset of destructive shearing forces, since nitrifying as well as denitrifying microorganisms can be expected to be ruptured. Mixing shearing forces can be increased until measurement indicates the onset of a distinct decline in sludge nitrification performance, all other things being equal. A suitable sludge mixing rate can generally range from a mixing rate which achieves compliance with the maximum sludge wastage rate to one allowing about 80% of the maximum sludge wastage rate to the maximum sludge wastage rate, about 60% to less than 80% of the maximum sludge wastage rate, and 40% to less than 60% of the maximum sludge wastage rate to even one of substantially zero sludge wastage rate in the process of this invention. (5) Biological Oxygen Demand Also, in this embodiment of the process of this invention, the biological oxygen demand (BOD), which is biodegradable, is controlled during treatment. Basically, the biological oxygen demand during treatment is controlled such that at least the stoichiometric amount of biological oxygen demand required to achieve a specified level of denitrification conversion of nitrite and/or nitrate to nitrogen during treatment at a particular ammonia concentration of wastewater fed for treatment is present. BOD can be supplied as either or both aqueous BOD and the BOD represented by the microorganisms and available for reaction through endogenous respiration. As can be seen from an examination of reaction schematic (III) above, organics (expressed in the form of biological oxygen demand) are required for denitrification of the nitrified feed wastewater, more specifically, for the conversion of nitrite and/or nitrate to free nitrogen. In this conversion, microbial action on the biological oxygen demand occurs, where nitrite and/or nitrate serve as the terminal electron acceptor in the metabolic reactions involving the BOD with the resulting formation of free nitrogen. Reduced biological oxygen demand requirements for denitrification are favored by high sludge concentration and low dissolved oxygen levels because the lower dissolved oxygen levels will establish greater anoxic regions for BOD metabolism. The appropriate biological oxygen demand for conversion of nitrite and/or nitrate to free nitrogen microbially can arise in the system basically in two ways. The wastewater feed may have sufficiently high levels of biological oxygen demand in the form of dissolved organics and system microorganisms that, at the desired system reaction rate, at least a stoichiometric quantity of the biological oxygen demand in relation to the nitrite and/or nitrate to be converted is present. Alternatively, supplemental biological oxygen demand can be provided by affirmatively adding appropriate quantities of essentially any watersoluble organic material at concentrations up to the limit of their water solubility. For example, aliphatic alcohols such as methanol, aromatic alcohols such as phenols and cresols, aromatics such as benzene, toluene, and xylenes, carbohydrates such as molasses, and the like can be used. These specific examples of organic materials are given solely for exemplification and are in no way to be construed as limiting. Denitrification reaction rates can be expected to vary as a function of the type of organic comprising the biological oxygen demand. Basically, in the conversion of nitrite and/or nitrate to free nitrogen, the biological oxygen demand is believed to be provided by a combination of endogenous respiration of microorganisms in the anoxic region of sludge agglomerates and by permeation of organic material into the anoxic region of sludge agglomerates where, due to the lack of oxygen present, the oxidation of the organic material in a microbial manner occurs as a result of the utilization of the nitrite and/or nitrate ion as a terminal electron acceptor. This thereby results in a microbial consumption of a combination of microbial and aqueous BOD with conversion of the nitrite and/or nitrate to free nitrogen. Bulk sludge BOD reaction rates with nitrite and/or nitrate will vary as a function of the nature of the organic material comprising the BOD, due to a combination of differing organic material diffusion rates and microbial reactivities with types of organic material and the degree of endogenous respiration taking place since this rate is inherently much slower than aqueous organic rates. Although the process of this invention can be operated basically at the stoichiometric level of biological oxygen demand consistent with the amounts of nitrite and nitrate present for total conversion of nitrite and/or nitrate to free nitrogen, preferably it is desirable to have an excess biological oxygen demand to ensure that the desired conversion of nitrite and nitrate to free nitrogen, by the facultative microorganisms is achieved. Another reason for a preference of excess biological oxygen demand in this system over that stoichiometrically required for conversion of nitrite and/or nitrate to free nitrogen is that other microorganisms may well be, and generally are, present to oxidize the biological oxygen demand to produce carbon dioxide and water as an aerobic reaction. Since to some extent oxidation of the BOD with dissolved oxygen will occur in the aerobic region of the sludge agglomerate, this represents a competing reaction to that which occurs in the anoxic region. Thus, the BOD present must be at least large enough to satisfy simultaneously denitrification requirements and competing demands for BOD consumption through reaction with dissolved oxygen. It is preferred that the BOD be present in net excess of demand in the feed up to but not exceeding the point of inducing incremental sludge quantities which cannot be adequately separated from wastewater and therefore result in sludge wastage rates in excess of the maximum allowable rate. For complete denitrification, stoichiometric ratios of BOD to nitrogen must be controlled to be at least between about 1.7:1 for nitrite nitrogen and about 2.8:1 for nitrate nitrogen. The specific level is dependent upon the form of the nitrogen involved in the denitrification, nitrite or nitrate, respectively. If any BOD is consumed through oxidation with dissolved oxygen, rather than with nitrite or nitrate present, then correspondingly additional BOD must be added and the above BOD/N ratios may well be larger as a result. Biologically reactive quantities of BOD present in the wastewater above those required for denitrification are converted to CO.sub.2 and H.sub.2 O through direct oxidation with dissolved oxygen. As described hereinbefore, BOD is required for the reduction of nitrification products, produced from ammonia in the wastewater, to free nitrogen. The amount of BOD required for denitrification depends upon the form of the nitrogen to be denitrified, viz., nitrite or nitrate. Nitrogen in nitrite is in a lower oxidation state than that in nitrate and therefore less reducing agent in the form of BOD is required for conversion of nitrite to free nitrogen. Approximately 1.7 mg of BOD are required for the reduction of one mg of nitrite nitrogen while about 2.8 mg of BOD are required for the reduction of one mg of nitrate nitrogen. Thus, in practice, the required BOD/N ratios for complete denitrification can be expected to vary between 1.7:1 and 2.8:1 depending upon the ratio of nitrite nitrogen to nitrate nitrogen present in the system. Fractional amounts of denitrification, i.e., where less than complete denitrification results, require correspondingly lower ratios than 1.7:1 to 2.8:1 BOD/N. To the extent that direct oxidation of BOD with dissolved oxygen occurs in the system, it can be seen that total BOD/N requirements are increased. As set forth above, the preferred source of BOD for denitrification is dissolved organic material present directly in the ammonia-containing wastewater to be treated. If this source is insufficient for the desired level of denitrification, additional BOD can be affirmatively added in the form of any organic material having sufficient solubility in water to insure its availability to the microorganisms in the anoxic regions of the sludge. In the actual practice of this invention, BOD/N requirements are established basically experimentally. Sludge is acclimated and initially operated on feed wastewater having a BOD/N ratio at least high enough to achieve desired levels of denitrification assuming that all the nitrogen to be denitrified is present in the form of nitrite rather than nitrate and that at least about the first 1.7:1 units of BOD per unit of nitrogen react with nitrite rather than dissolved oxygen. Thus, if 50 percent denitrification is desired, a BOD/N ratio of at least about 0.85:1 is required in the initial feed wastewater. If less than this amount is present naturally in the wastewater feed, additional BOD must be added to bring the ratio to a value of about 0.85:1 to achieve 50 percent denitrification. In actual operation, this BOD/N requirement (e.g., 0.85:1 for 50 percent denitrification) may prove insufficient for two reasons. First, a portion of the nitrite may be converted by Nitrobacter microorganisms before denitrification occurs, thus increasing the BOD demand per unit of nitrogen conversion from 1.7:1 to 2.8:1. Secondly, a portion of the feed BOD may be microbially oxidized in the presence of dissolved oxygen in the wastewater rather than due to nitrite and nitrate, thereby increasing total wastewater feed BOD/N requirements for any desired level of denitrification. The extent to which these two factors will vary is dependent on the actual operation of the process of this invention, but can be easily and routinely determined using the above principles. Thus for complete denitrification, the stoichiometric amount of BOD to N will be at least about 1.7:1 to 2.8:1 and more preferably above about 2.8:1 to ensure sufficient BOD for denitrification of both nitrate as well as nitrite species present. Appropriate ratios will be proportionally less where less than complete denitrification is desired, i.e., about 75% thereof for 75% denitrification, about 50% thereof for 50% denitrification, and about 25% thereof for 25% denitrification. Where no denitrification is desired the BOD needed is not interrelated to nitrite/nitrate nitrogen. (6) pH An even further parameter of the process of this invention which is controlled is the pH. Specifically, pH and its range of variation in operation is controlled to provide preferred reaction kinetics within the constraints that (i) the pH lies within a range hospitable to growth and reaction of all the microorganisms involved, (ii) the pH does not induce free ammonia levels in the system which are inhibitory to microorganism activity, (iii) the pH does not result in nitrous acid levels in the system inhibitory to microorganism activity and (iv) sludge microorganism activity is preserved at a sufficiently high level that significant amounts of contaminant species do not build up and leave the sludge unreacted, particularly at levels which are high enough to induce inhibitions to microorganism activity. As to free ammonia (NH.sub.3) level, beyond certain concentration limits, it has been found experimentally that free ammonia in solution, as opposed to NH.sub.4.sup.+ in solution, significantly affects autotrophic microorganism reaction rates (see Anthonisen et al "Inhibition of Nitification by Ammonia or Nitrous Acid"Vour. Water Pollution Control Federation, 48, 835-852, (1976)). The free ammonia concentration levels in sludge are thermodynamically determined by a combination of total ammonia concentration (NH.sub.3 and NH.sub.4.sup.+) in the sludge, sludge pH and sludge temperature. Inhibition of microorganism activity by nitrous acid is also seen experimentally. FIG. 7 shows schematically Nitrosomonas microorganism inhibition by free ammonia and Nitrobacter microorganism inhibition by free ammonia and nitrous acid as a function of pH at a specified temperature. In FIG. 7, the abscissa shows increasing pH while the left-hand ordinate shows the logarithm of nitrite-nitrogen concentration (NO.sub.2.sup.- concentration) while the right-hand ordinate shows the logarithm of total ammonia (NH.sub.3 plus NH.sub.4.sup.+) nitrogen. Zone 1 shows the area in which free ammonia inhibits Nitrobacter and Nitrosomonas microorganisms. Zone 2 shows free ammonia inhibition to Nitrobacter. Zone 4 shows free nitrous acid inhibition to Nitrobacter while Zone 3 is an area in which complete nitrification can occur. Conventionally, it has been thought that microbial inhibition is prevented by maintaining sludge conditions within Zone 3 as shown in FIG. 7. Further, as to facultative microorganisms capable of converting nitrite and/or nitrate to free nitrogen present, it has been experimentally found that the level of free nitrous acid also needs to be controlled since levels greater than about 0.13 to 0.2 mg/l of nitrous acid inhibit the activity of facultative microorganisms. As a result control of the level of nitrous acid by use of pH and temperature, as described below, will avoid inhibition of this type as well as inhibition of Nitrobacter and Nitrosomonas. Specific sludge maintenance actions to avoid levels of free ammonia and nitrous acid which result in inhibition, for example, pH adjustment through controlled additions of alkali, will vary, based upon the nature of the wastewater to be treated and the applications to which the process of this invention is directed. Control of free ammonia and nitrous acid to levels below which nitrifying microorganism growth and/or treatment of waste is inhibited can be achieved by any conventional means wherein free dissolved ammonia and nitrous acid in an aqueous system can be controlled. For example, ammonia concentration can be appropriately controlled by adding water for dilution, the pH can be appropriately controlled by the addition of an amount of acid necessary to reduce the free ammonia concentration below the inhibitory level, or the temperature can be changed. By using either of these approaches for controlling the free ammonia level, the equilibrium between the free ammonia in the system and the ammonia as ammonium ion can thereby directed. The free ammonia concentration should, for a particular pH and temperature be controlled to be no greater than that as shown within the limits of Zone 3 in FIG. 7. From the limits of Zone 3 of FIG. 7 and based on the fraction of free ammonia present in solution as shown in Table 3 below, the concentration of free ammonia can be calculated at the system pH and temperature with knowledge of the total amount of ammonia present. Similarly, adjustments can be made to control the nitrous acid level. The nitrous acid level should, for a particular pH and temperature, also be controlled to be no greater than that as shown within the limits of Zone 3 in FIG. 7. From the limits of Zone 3 of FIG. 7 and based on the fraction of nitrous acid shown in Table 3 below, the concentration of nitrous acid can be calculated at the system pH and temperature with knowledge of the amount of nitrite present. To avoid inhibition the limits of Zone 3 of FIG. 7 for free ammonia and nitrous acid must be met.
6.0 6.5 7.0 7.5 8.0
10 0.0002 0.0007 0.002 0.007 0.022
15 0.0003 0.0010 0.003 0.010 0.032
20 0.0005 0.0015 0.0048 0.015 0.048
25 0.0007 0.0022 0.0068 0.021 0.068
30 0.0010 0.0031 0.0097 0.030 0.091
35 0.0014 0.0043 0.0136 0.042 0.124
10 0.011 0.0035 0.0011 0.00035
15 0.010 0.0031 0.0010 0.00031
20 0.008 0.0027 0.0008 0.00027
25 0.007 0.0023 0.0007 0.00023
30 0.0065 0.0021 0.00065
35 0.0057 0.0018 0.0006 0.00018
Component (ppm)
NH.sub.3 --N 2912
NO.sub.x --N 0
Phenolics 971
Free HCN 5.6
Total HCN 8.2
Sulfide 6.3
Thiocyanate 255
Suspended Solids
Alkalinity 7520
Concentration, ppm
Component Influent Effluent % Removal
NH.sub.3 -- N
2912 <5 99.8
NO.sub.x -- N
-- .about.14
Phenolics 971 <0.05 >99.9
CN.sup.- FREE
5.6 0.24 95.7
CN.sup.- TOTAL
8.2 3.7 54.9
S.sup.= 6.3 0.9 85.7
SCN.sup.- 255 1.7 99.3
pH 9.6 7.0 --
TSS = total suspended solids
Concentrations, mg/l
Component Influent Effluent % Removal
NH.sub.3 --N
1000 <10 >99
COD 3000 .about.300
SCN.sup.- 125 <1 >99
NO.sup.-.sub.3 --N
0 450 .about.55%*
TSS 0 .about.40
Concentrations, mg/l
Component Influent Effluent % Removal
NH.sub.3 --N
3000 15 99.5
Sulfide 3000 .about.1 99.9
SCN.sup.- 150 <1 99.3
NO.sup.-.sub.3 --N
0 1500 to 1800
40 to 50
Concentrations, mg/l
Component Influent Effluent % Removal
NH.sub.3 --N
2900 10 99.7
SCN.sup.- 255 <1.0 99.6
NO.sup.-.sub.3 --N
0 .about.17


text:
237 Young Road Baldivis WA 6171
- Acreage/Semi-Rural
- 3
- 1
- 1
Bob McPherson
- 0417 974 532
- 0417 974 532
Open for Inspection Times
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Contact the agent to arrange an appointment.
237 Young Road Baldivis
Invest In Your Future
Set on 17 Acres of rural land, fully fenced, good cattle & hay country. Attractive 3 bedroom home with combustion fire heating, solar workshop, 4 horse stables, bore. Heaps of potential, invest in your future.
Property No. 115549683
Page Visits: 2,261
- General Features
- Property Type:Acreage/Semi-Rural
- Bedrooms:3
- Bathrooms:1
- Land Size:6.90ha (17.06 acres) (approx)
- Price per acre:$50,352
- Indoor Features
- Toilets:1
- Air Conditioning
- Outdoor Features
- Carport Spaces:1
- Fully Fenced
- Other Features
- powered shed, 4 stables
Floorplans & Interactive Tours
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© Western Australian Land Information Authority (2014) trading as Landgate.

subset: commoncrawl


text:
Red Letter Days is always around to guide you through your gifting decisions be it for your dear ones, loves ones, spouses or for corporate gifting. As you browse through the Red Letter Day, you will be wonder stuck at the gift experience and unique gift ideas at your disposal, tempting you to purchase one for yourself !! And it will come as no surprise if you do so as they are simply irresistible.
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About Advising
All students should meet with an academic advisor each term to review curriculum requirements, to discuss career and educational goals (including transfer) and to discuss problems that may interfere with your academic success. It is your responsibility to meet all curriculum and college requirements.
As a full-time student, you are assigned a faculty advisor, usually from your academic program. Full-time faculty maintain a regular schedule of office hours. It is your responsibility to make appointments with your advisor. Names of advisors for full-time students are available through WebAdvisor in CampusCruiser, the Academic Advising Center, and the Office of the Registrar. Full-time students are strongly encouraged and generally prefer to meet with their assigned faculty advisors. Please click here to obtain faculty members' office hours. However, you are also welcome to seek assistance from the Academic Advising Center.
All part-time students are welcome to meet with an advisor in the Academic Advising Center or to meet with the Chairperson of their curriculum.
If you would like to print a map of the Edison Campus in order to locate Johnson Learning Center, click here. You can also find a list of directions to campus or print a map of the area leading to our campus.


text:
I have SO many of these fantastic custom photo bags – I'm always handing out my cards because people stop me and ask me where they can get them.
We carry GORGEOUS Luxury Leather bags as seen below:
And – the Photo Lunch Bag and Photographer's Tote are available ONLY from CanvasRox!!
Here's the Large Classic Tote
…and one side that I made for it. Collages are easy – just upload it as a jpeg! If you need help, we'd be happy to create a custom collage for you.
You must have your order in by November 30th to receive the free ground shipping. All orders for Christmas delivery must be received by December 10th.
Questions? Send emails to firstname.lastname@example.com or post them here!
Loving the blog Roxanne. I added you to my feed and look forward to all the wisdom you have to share
Love your new blog Roxanne – and those bags are awesome!!! jen
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Panch Phoron Recipe
Panch phoron is a five-seed mixture from Bengal, India, a region famous for its distinctive cuisine. Panch phoron is most common in northern India, where the majority of seed spices are grown. Grind coarsely and use as a coating on roasted meat, or sprinkle on Indian breads, potato dishes, and vegetables, especially eggplant and cauliflower.
- 2 tablespoons whole black mustard seeds
- 2 tablespoons whole nigella seeds
- 2 tablespoons cumin seeds
- 2 tablespoons whole fenugreek seeds
- 2 tablespoon whole fennel seeds
- Combine 2 tablespoons each whole black mustard seeds, whole nigella seeds, whole cumin seeds, whole fenugreek seeds, and whole fennel seeds.
This recipe, while from a trusted source, may not have been tested by the CHOW food team.


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Teens Get Cash to Not Get Pregnant
Girls in the program attend 90-minute meetings every week at which they receive lessons in abstinence and the use of contraceptives -- and they receive $7 every week they do not get pregnant. The money is deposited into a fund that's collectible when they enroll in college.
But not everyone thinks paying kids to stay childless is the right way to lower the teen pregnancy rate. They say the program sends mixed messages, specifically to parents, that incentivizing good behavior is the way to go.
"It makes me a bit uneasy," said Bill Albert, chief program officer at the National Campaign to Prevent Teen and Unplanned Pregnancy. "I do have mixed feelings. It's hard to pay people to do something that we think they should be doing regardless. It would be like if you didn't want young people to experiment with marijuana, you'd pay them not to do it."
Despite what he called his "gut-level queasiness" about paying girls not to get pregnant, Albert acknowledged that creative ways are needed to address the "very challenging social issue" of teen pregnancy.
The nation's teen birth rate, after declining for 14 consecutive years, has increased over the last two years and now stands at 7.2 pregnancies per 1,000 teenage girls, Albert said. Furthermore, he said, three out of 10 young women become pregnant by age 20, and costs associated with teen pregnancies exceed $9 billion annually.
With those figures in mind, paying girls $365 a year to stay childless seems like a "modest investment" -- especially if the program works, Albert said.
Dr. Hazel Brown, co-director of the program, said six girls of the 125 who have been enrolled for six months or longer have gotten pregnant or otherwise dropped out since it began in 1997. Funded by a grant from the state's Department of Health and Human Services, Brown said it costs about $75,000 a year to operate the program.
"We talk about abstinence, but it's not a requirement," Brown told FOXNews.com. "We teach decision-making, being responsible and avoiding pregnancy. The meetings are very interactive."
Enrollment in the program -- which meets separately twice a week for two groups, ages 12-14 and 15-18 -- is at capacity with 24 young women. To participate, girls must have never been pregnant, be enrolled in school, have a desire to attend college and have had a sister who gave birth before age 18.
Recent graduates have left the program with up to $3,000 saved up for college, including four young women who are set to begin their higher education in the fall.
Brown said the program is successful, and said its critics should consider the "cost of a teen getting pregnant," Brown said.
"When you can prevent one of those, you've more than paid for a program like this," she said. "We want to give them something to work toward. And without exception, our girls have come from homes that did not have someone with a college education ...
"If somebody believes in you, there's no end to what a lot of people can accomplish."
Read more hot stories Moms Are Talking About.
I have read some of the messages left about this program and I am truely disappointed! I was apart of this program some years ago and I did not finish the program because I did become a teen parent but I know alot of my friends who were in the program with me and they finished all the way through. The thing that most people don't realize is that alot of us girls grow up with these things already happening in our homes. This program is a GREAT program for teen girls to get a chance to learn alot that we don't get to learn in school. They teach the girls all about STD's and everything there is to know about STD's. Things that they never tought us in school and things that alot of people I know don't know! They also had people from different colleges come in to talk to us, and taught us alot about going to college and how we could better ourselves by not having a child and by finishing a school and going to college. This program is one of the greatest programs I've ever heard of! They paid the teen every week for going, one payment was giving to them right then for gas so that whom ever brought them to the classes can have that and the other payment was made to their college account. The girls in this program NEED this program! It helped me even though I did get prengant it still helped me learn alot about life and what I'm capable of doing with myself if I put my mind to it.


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The second shooting victim in last week's deadly shooting and resultant crash has been identified.
According to shooting suspect Ammar Harris' criminal complaint, Harris is alleged to have shot victim Freddy Walters, for which Harris is charged with attempted murder. The District Attorney's office provided FOX5 the report on Thursday afternoon.
Walters was the passenger in the Maserati driven by victim Ken Cherry, Jr. Cherry was shot before accelerating along Las Vegas Boulevard and striking a cab containing victims Michael Boldon and Sandra Sutton-Wasmund. Cherry was killed as well.
Harris was arrested in Los Angeles at noon on Thursday by officers and FBI agents. Metro police have scheduled a press conference for 4 p.m. on Thursday to discuss Harris' arrest.
Copyright 2013 KVVU (KVVU Broadcasting Corporation). All rights reserved.


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The month number and year number will be converted so that January and February are considered months 13 and 14 rather than months 1 and 2. January and February of year Y are converted so that they occur in the year Y - 1. In other words, a system is used where the first month of the year is March (designated as month 3) and the last month of the year is February of the following year and designated as month 14. The purpose of this scheme is to cause the extra day in a leap year to occur at the end of the "year." As will be seen, this simplifies the calculation of the number of leap years from year zero to a particular date and it simplifies the function which relates month number to the number of days in the preceding months.
Since the base year is March 1 of year 0, the Julian day number is determined relative to that date. From table 2, it can be seen that March 1.0 of year 0 is JD 1721119.5, assuming the date is in the Gregorian calendar. Thus March 1.5 of year 0 is JD 1721120.0 and is the Julian Day Number if a date of March 1 of year 0 is specified. Thus 1721118.5 must be added to the day number (of one) to get the correct JD. Note, however, that dates in the Gregorian calendar are assumed even though the base date is before the Gregorian calendar was invented. This works fine as long as the dates input to the algorithm are Gregorian calendar dates or dates in the Gregorian proleptic calendar.
Next, the days in the year are accounted for. This is easily done using the following function:
This expression directly encodes the rule that there are 365 days in a year plus an extra day for leap years, where leap years occur every 4 years except for century years unless they are also divisible by 400. Here [x] is the greatest integer function, that is, [x] is the greatest integer that is not greater than x. Thus [2]=2, [2.5]=2, [0]=0, [-1.5]=-2, and [-3]=-3. For positive numbers, the greatest integer is the same as a function which truncates any fractional part of a number.
Note that although 0 is a leap year, the number of days relative to March 1 of the year zero are being considered. Relative to March 1 of the year zero, the first leap year is year 4 and February 29, 4, is part of the year beginning March 1, 3. The expression - [Y/100] eliminates all century years as leap years while [Y/400] adds back century years that are divisible by 400.
Finally, the number of days in the months prior to the specified month are accounted for. The following gives the range and domain of the function explicitly:
|days in previous months
Since, all the months except February are either 30 or 31 days long, one might suspect that a linear approximation can be used and the fractional part of the value removed to generate a convenient form of the function. One can not be certain that this will work on a particular function before it is examined in more detail, but, as will be shown, the function given in the table can be successfully generated in this way.
The function will take the form:
X = month number,
M = the slope of the line,
B= the Y intercept of the line, and
FIX() is the truncation function.
Now since FIX() removes the fraction, the values of MX+B that produce the same FIX function value are values of MX + B from some integer, say Y, up to, but not including, the value Y+1. The values for each Y can be graphed, but because of the scale, it is difficult to see precisely how the line might fit through all the function values or whether or not it is even possible to do so. However, it isn't difficult to write a computer program that determines what equations can pass through these intervals. Doing so shows that the line with maximum slope goes from point (4,31) to (12,276), has slope= 30.625 and Y intercept=-91.5. The line with minimum slope goes from point (14,337) to (7,123), has a slope= 30.57142857142857 and Y intercept=-91.0000000000000. These two lines cross at (9.333333333333067,194.3333333333252) and I call this the pivot point, since there will be lines within the specified intervals that go through this point and take on any of the slopes from 30.57142857142857 to 30.625. Given slope M, the values 194.3333333333252 - M * 9.333333333333067 can be used as the Y intercept. However, there will usually be many other Y intercept values that work as well.
From a computational point of view, one probably notices that a slope of 30.6 contains a minimum number of digits and shouldn't be too difficult to produce using integer arithmetic. If for slope = 30.6, the line goes through the pivot, the Y intercept is -91.26666666666669 but there are lots of other Y intercept values that work as well. These Y intercept values can range from -91.4 to -91.2, although the value of -91.2 can not actually be taken since the line would go through a couple of points that are integers and the truncation function would not produce the desired result. Thus the function
can be used to produce our desired function values. The function can also be converted to other forms for convenience. For example
FIX(30.6*X-91.4) is equivalent to (153*m-457)\5 since 153/5=30.6 and -457/5=-91.4.
Other coefficients for our generating function are also possible, and they can be searched for using the bounds described above. Suppose, for example, that the function is to have the form (A*X+B)\32 so that shifts can be used in the binary representation to implement integer division. Since the slope must range from 30.57142857142857 to 30.625, A/32 must also be in this range. This implies that A must range from 30.57142857142857 * 32 = 978.28571428571424 to 30.625*32= 980.0. The integer 979 is an obvious choice. This means the slope is 979.0/32=30.59375. This slope implies that the Y intercept is in the range -91.15625 to -91.3125. Thus B must be in the range of -91.15625*32= -2,917.0 to -91.3125*32=-2,922, where the larger of the intercepts (-2,917) is excluded as before. Thus the range choice for B is -2,922 through -2918 inclusive. Thus the alternative formula: (979*m-2918)\32 can be used to generate the required function. Here "\" is a shift which implements integer division with truncation rather than the greatest integer function. This is possible because variable "m" has a value of 3 or greater so that the numerator is always positive.


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Deadpan video
2013-01-19 09:09:17.53107-08 by Dan Lyke 0 comments
It's deadpan video day.
2013-01-19 09:09:17.53107-08 by Dan Lyke 0 comments
It's deadpan video day.
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Click here to print the obituary below
In Memory of
Rita V. Moore
June 15, 1935 - August 11, 2013
Rita V. Moore (nee Lapenta), 78, of Dewitt, passed away Sunday at the Jewish Home. Born in Syracuse, she was the youngest daughter of the late Nicholas V. and Assunta Lapenta, Italian immigrants. Rita was a graduate of New York University's Bellevue School of Nursing. She worked over the course of a long and distinguished career as an Emergency Room charge nurse in Ogden, Utah, and Washington, D.C. She was also a dedicated leader on the Emergency Room team at Crouse Hospital in Syracuse, N.Y., where she was one of the last nurses who wore a white uniform and hat. She was a decorated veteran, and proud of her service in the United States Air Force; she retired as a Lt. Colonel in the USAF Reserve Nurse Corps. Rita was activated during the 1991 Gulf War and was recognized for her outstanding service in setting up and administering a temporary hospital at the former Griffiss Air Force Base in Rome, N.Y. She was married for a time to the late Robert Moore, also an Air Force officer. In the course of her career she traveled extensively, including volunteering as a nurse in post-colonial Algeria. She was a dedicated Parishioner of Holy Cross Church in DeWitt. Rita was predeceased by her sister Irene Sutphin and brother Nicholas Lapenta, both of Syracuse, N.Y.
Survivors include her sister Frances Neer of N.J., as well as beloved nieces and nephews, including Paul R. (Catherine) Sutphin of Alexandria, VA, Lisa (Nicholas) Petosa of Syracuse, Michael Lapenta of Syracuse, Richard (Vickie) Neer of N.C., John (Jeannie) Neer of NJ, Dan (Rose) Neer of NJ, and Susan (Victor) Csirip, of NJ.
Funeral services will be held on Friday, August 16 at 10:15 a.m. at FARONE & SON FUNERAL HOME and 11 a.m. at Holy Cross Church where a Mass of Christian Burial will be celebrated. Entombment will follow in St. Mary's Cemetery Mausoleum, Dewitt. Calling hours will be held on Thursday, August 15 from 5-8 p.m. at the funeral home, 1500 Park Street, Syracuse.
Condolences may be offered at
Thursday, August 15, 2013 | 5:00p.m. - 8:00p.m.
Farone & Son Funeral Home
1500 Park Street, Syracuse, NY 13208 | (315) 422-1911
Funeral Service
Friday, August 16, 2013 | 10:15a.m.
Farone & Son Funeral Home
1500 Park Street, Syracuse, NY 13208
Mass of Christian Burial
Friday, August 16, 2013 | 11:00a.m.
Holy Cross Church
4112 E. Genesee Street, Dewitt, NY 13214 | (315) 446-0473


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lord of starkness This blackmail shot appeared on the front cover of the FRCC Newsletter in '87
© Ron Kenyon
Route: Brown Slabs Direct


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PHILADELPHIA (AP) — Philadelphia Mayor Michael Nutter and Pennsylvania Attorney General Kathleen Kane are joining top prosecutors in San Francisco and New York in a nationwide initiative to thwart smartphone thefts.
The initiative called Secure Our Smartphones brought New York Attorney General Eric Schneiderman to Philadelphia on Monday to make the announcement with Nutter and Kane.
The idea is to pressure the smartphone the industry to develop a technological solution, such as a "kill switch" for stolen phones, that would make smartphones inoperable after they are stolen.
They say that such a safety switch would stop the robberies that are feeding a massive and lucrative secondary market for stolen devices.
The group was begun in June by Schneiderman (SHNEYE'-dur-muhn) and San Francisco District Attorney George Gascon.


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Photo reblogged from say a prayer for surf boy, wherever he is with 7 notes
i want this pair of osu toms
gotta represent
Photoset reblogged from Swoosh Spotter with 3 notes
Who is wearing Ohio State apparel today? Go Buckeyes! Central Florida doesn't stand a chance!
Ohio State True Rivalry Collection
Photo reblogged from fyeah Spirit Squads with 16 notes
Go Buckeyes!
Ohio State cheer
Photo reblogged from SI Photo Blog with 240 notes
Only one month until Ohio State faces off against Nebraska under the lights! Will you be wearing Ohio State Apparel or Nebraska Apparel? I hope you answered Ohio State!
Ohio State receiver Devin Smith makes the play of the weekend with this one-handed touchdown catch against Miami (Ohio) cornerback Dayonne Nunley during the second quarter of Saturday's game. Ohio State won, 56-10. (Kyle Robertson/MCT/ZUMAPRESS.com)
MANDEL: Urban Meyer wins OSU debut and other college football notes
ANDERSON: The best and worst of college football's opening weekend
GALLERY: Top 25 review: Week 1 | The scene at Penn State
Photo reblogged from Talan with 25 notes
No place like the O state!!!
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I like this Ohio State cup!
My new tervis tumbler (: go buckeyes!
Photo reblogged from Columbus, Ohio with 69 notes
devin smith
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osu basketball & synchronized swimming team
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These boys make me very proud of Ohio State!
ohio state football
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Junction City (WQOW) - Bear hunting season is slowly coming
to a close in Wisconsin,
and one young girl took advantage of it, killing a 335-pound bear.
11 year old Kaitlynn Bessette was
diagnosed with a congenital heart disease when she was born, causing her to
need a heart and liver transplant. She's still waiting for that. But that
hasn't stopped her from doing what she loves most, hunting and fishing. A wish
of hers was granted last Saturday when Kaitlynn went out on a bear hunt in Junction City. She says
she was expecting to go home empty handed, but that wasn't the case. With one
shot to the heart, Kaitlynn got this 335 pound black bear.
"When I looked
through that scope I didn't see it as a bear. I saw it as a 300 pound lion
that's about to attack you so I held the gun as steady as I could, I turned my
head and then I shot," says Bessette.
The hunt was made possible by the United
Special Sportsman Alliance. It's a program that helps children with
disabilities do the things they've always wanted to do.


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Welcome to the Nagoya Friends Party site!!
Find Japanese pen pals and pen pals from around the world.
International Parties in Nagoya! Please join us for the next Nagoya Friends Party.
Around 125+ people attend each month. Many Japanese and non-Japanese will be participating.
It's a good opportunity to make new friends, find your language exchange partners, or even find your girlfriends/boyfriends. Increase your network of friends and contacts in the Aichi, Gifu and Mie areas at Nagoya Friends Come alone or bring your friends. Everybody is WELCOME! Just come and be ready to make new friends with everybody.
Nagoya Friends Party @ Red Rock Sepember 27th, Saturday
Date: Saturday September 27th, 2014
- Time: 18:00 – 21:00
- Drinks will be served between 6:00pm-8:45pm.
- Place: The Red Rock (2F Aster Plaza Building, 4-14-6 Sakae, Nagoya (very close to Sakae Station)
Fee: 3500 Yen
Dress code: Anything (Casual, etc)
- Reservations: Not necessary but recommended and appreciated. Just show up to the party!
- Over 25,000 Yen worth of exciting prize giveaways each month!
- A special menu featuring: A special Australia menu from the chefs at Red Rock
There will be free food along with free drinks (beers, wine, cocktail drinks and juices).
Our party is not a dinner party, but we will have light food & snacks.
Quantities are limited, so please come early! Please free to come alone or bring your friends.
EVERYBODY is welcome to join regardless of nationality/gender. Reservation is greatly appreciated.
About 125-150+ people are expected to attend. Approximately 55% female and 45% male, 70% Japanese and 30% non-Japanese.
Pictures from previous Nagoya Friends Parties.
Contact: 080-3648-1666(Japanese) 080-5469-6317(English)
Get off at Sakae Station [Exit #13]
The Red Rock (2F Aster Plaza Building,
The Red Rock is located behind the Chunichi Building in the Sakae business/shopping district.
Subway access from Sakae Station (serving the yellow and purple lines) Exit 13. It's a big station connected to a huge underground shopping mall so you'll need to do a little underground walking.
We're also just a couple of minutes' walk from the Tokyu and Precede hotels, and a 10 minute walk up Hirokoji Street from the Hilton Hotel in Fushimi.
Nagoya International Speed Dating in December
Will Santa bring you a sweetie!
Over 85% of couples get at least 1 match!
3 couples have gotten married!!!
◉ Date: SUNDAY JDecember 6th, 2014
◉ Time: 5-8pm registration from 5:00 to 5:30pm
◉ Place: The Red Rock (2F Aster Plaza Building, 4-14-6 Sakae, Nagoya (very close to Sakae Station)
◉ PREPAY FEE: Men 2500 yen, Women 2000 yen
◉ Dress code: Anything (Casual, etc)◉ Reservations: Pre Paid spots are Gauranteed! only 30 men and 30 women. Reserve and prepay to secure your spot.


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Stanley Zlotkin
Chief, Global Child Health, Hospital for Sick Children, Canada
Stanley Zlotkin MD, PhD is a professor of Paediatrics, Public Health Sciences and Nutritional Sciences at the University of Toronto. He graduated from the University of Toronto with an undergraduate degree in Ecology in 1971 and received his MD degree from McMaster University in Hamilton, Ontario in 1974. He completed his paediatric training at the Montreal Children's Hospital and received his paediatric Fellowship (FRCPC) in Paediatrics from McGill University in 1978. He moved from Montreal back to Toronto and completed his PhD in Nutritional Sciences at the University of Toronto in 1981. He joined the Division of Clinical Nutrition at the Hospital for Sick Children in 1980 and became Division Head of the combined Division of Gastroenterology, Hepatology and Nutrition in 1998. He remained Division Head until June 2008. In 1980 he was appointed to the Research Institute at the Hospital for Sick Children as a Senior Scientist and continues to hold that position today. Dr. Zlotkin and his Program, the Sprinkles Global Health Initiative has focused on research and advocacy to control micronutrient malnutrition in children. Micronutrient malnutrition was ranked as the second highest priority, after HIV/AIDS, by the Copenhagen Consensus in 2004, and the highest priority in 2008. UNICEF and the World Health Organization (WHO) had a goal to reduce micronutrient malnutrition by one third by 2010. It is estimated that as many as 750 million in developing countries suffer from micronutrient malnutrition. Challenged by UNICEF to come up with a viable and reproducible solution to the problem of micronutrient malnutrition, Zlotkin and his research team developed the concept of micronutrient powders for 'home-fortification' of complementary foods. With support from USAID, CIHR (Canadian Institutes of Health Research) and private foundations, he has completed stable isotope studies and RCTs in more than 8 developing countries to 'prove' the efficacy and effectiveness of 'home-fortification' to control micronutrient deficiencies. He has advocated for and helped implement national and international guidelines to combat micronutrient deficiencies in some of the world's most needy countries; facilitated replication of its model; and, forged strong, sustainable partnerships to facilitate sustainability at the national level. Dr. Zlotkin is past Chair of the Canadian Paediatric Society Nutrition Committee, participated in the Institute of Medicine's DRI process for establishing RDAs for minerals and vitamins, and is a frequent consultant to governments and United Nations agencies on issues related to paediatric nutrition. His advocacy work was recognized by the Canadian Institutes of Health Research (CIHR) in 2006 with his receipt of the prestigious 'CIHR National Knowledge Translation Award' for "outstanding contributions to the health of children worldwide". He was awarded the HJ Heinz Humanitarian Award in 2001 for his international contribution to the health of children globally, and he was recently awarded the Order of Canada, the highest civilian honour in Canada, for his contributions to improving the lives of children globally. He is known internationally as a successful social entrepreneur for his work on home fortification and was awarded an International Ashoka Fellowship in 2007. Today, Dr. Zlotkin continues to head the Sprinkles Global Health Initiative at the Hospital for Sick Children, is a physician nutritionist in the Division of Gastroenterology, Hepatology and Nutrition and is an active researcher with support from the NIH and other granting agencies. He was appointed to the position of VP Medical and Academic Affairs in July 2010.


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March 2014
The Issue:
The specter of workplace violence in healthcare settings is a growing phenomenon that healthcare facilities have not addressed adequately. In 2002, the World Health Organization defined workplace violence (WPV) as "the use of physical force with or without bodily contact." The National Institute for Occupational Safety and Health (NIOSH) defines workplace violence as any physical assault, threatening behavior or verbal abuse occurring in the workplace. Violence includes overt and covert behaviors ranging in aggressiveness from verbal harassment and threatening gestures to kicking, hitting, biting, punching, stabbing, sexual assault, shooting and murder. The rates of work-related assaults and injuries appear to be trending upward, according to limited data gathered by some federal, state and healthcare associations. Yet, few healthcare facilities have adopted comprehensive workplace violence prevention programs and security systems.
Unfortunately, many healthcare workers consider WPV to be "just part of the job," and many don't report assaults and injuries. WPV and related injuries should neither be expected nor accepted as part of anyone's work.
How Widespread Is Physical Workplace Violence In Healthcare?
- Healthcare workers are at greatest risk when working with patients who have impaired thinking and judgment secondary to psychiatric problems, when substance abuse is an issue, or when the person is cognitively impaired (delirium and/or dementia).
- Settings where workplace violence is most likely to occur include: emergency departments and psych/mental health units in acute-care hospitals, long-term care facilities (including mental health and developmental disability care), skilled nursing facilities (particularly on dementia units), home healthcare and penal institutions.
- There currently is no consistent tracking protocol across states and agencies for the incidence of violence in healthcare settings. As a result, measuring the extent is difficult. Limited data are captured form various sources.
- The Emergency Nurses Association annual survey of Emergency Department Violence shows that in 2011, more than 12 percent of nurses experienced physical violence within the previous seven-day period, and more than 42 percent experienced only verbal abuse in that same time period.In data from 2007, the Bureau of Labor Statistics reports that nearly 60 percent of all nonfatal assaults and violent acts by persons occurred in the healthcare and social assistance industry, but nearly three-quarters of these were assaults by healthcare patients or residents of a healthcare facility.
- The Joint Commission identifies workplace violence as a sentinel event in healthcare facilities, yet it notes that incidents are significantly unreported. Of note, the Joint Commission identifies assault, rape, and homicide as consistently among the top 10 types of sentinel events.
- From 2003 to 2009, four registered nurses were shot and killed at work (Bureau of Labor Statistics, 2011).
- A 2002 NIOSH study reported that healthcare workers are four times more likely to face workplace violence than other private sector workers.
- From 1993 to 1999, approximately 765,000 healthcare workers were assaulted resulting in days away from work (Bureau of Labor Statistics, 2001; BLS, 2006).
- Nineteen states have taken the initiative to create or strengthen felony assault laws to criminalize assaults of healthcare workers in the line of duty (AL, AZ, CA, CO, CT, DE, HI, IL, NE, NV, NJ, NM, NY, NC, RI, OK, VT, VA and WV).
- Legislation requiring employers to provide worker training and protections and/or studies of WPV is in place in nine states (CA, CT, IL, ME, NJ, NY, OR, WA and WV).
- HI has a resolution encouraging employers to develop and implement standards of conduct and policies for manager and employers.
The AFT has educational programs and training available for members. AFT can work with locals to file complaints with OSHA when injuries have occurred.
AFT Positions:
1996: Prevention of Workplace Violence
1996: Public Employee Safety and Health Resolutions
2010: Workplace Violence In Healthcare Facilities and Settings
2010: In Support Of A Healthy Workplace And Against Workplace Bullying
2012: Preventing Workplace Violence In All Healthcare Settings
What Do Healthcare Workers Need?
Healthcare workers need the protection afforded by an OSHA regulation on workplace violence prevention which would guide the development of comprehensive and effective prevention programs in healthcare settings, and provide a more concrete measure by which facilities would be held accountable. To make a more objective case for an OSHA standard, healthcare workers need a congressional request for a U.S. Government Accountability Office study to assess:
1. The adequacy of federal and state surveillance data to accurately capture the rates of injuries and assaults associated with work-related violence among healthcare workers in a wide variety of healthcare settings;
2. The impact of comprehensive workplace violence prevention programs in both the Veterans Administration system and selected states (Connecticut, New York or other states as examples ) in reducing rates of assaults and injuries associated with work-related violence in healthcare settings; and
3. Recommendations that weigh the need for further research:
- On the surveillance of workplace assaults and violence on healthcare workers in private and public healthcare facilities; and
- On the relative impact of current state and federal healthcare workplace violence-prevention guidelines and/or laws on the incidence of work-related assaults and injuries.


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November 10, 2009
why do I get tired when I begin to study?
Everytime I start studying, I will get tired within 5 minutes. (even if I find what I study interesting) The only time I'm able to study is by using coffee or caffeine pills. By using the stimulants I am able to focus and be more productive. Why does this happen and can it be done without stimulants? I have good health, but I think its psychological perhaps..
Filed under Uncategorized by admin
Spread the Word!
Comments on why do I get tired when I begin to study?
5:32 am@
you are overwhealmed. I am the same way.
11:39 pm@
The fact is youre not interested in it you may need to find another method of study such as group.
6:40 am@
The night set myself up for falling asleep everytime would read do believe though that studying early in the day when was young had habit of reading till got tired and put down the night set myself up for the book to study early in the day might help you.
For falling asleep everytime would read do believe though that studying early in the day might help you.
12:59 am@
For stimulants change your mouth and esophagus something to do.
7:58 am@
For short walk first get your vision checked eye strain from trying to bedtime try going for short walk first energetic music and little fresh air always noticeable.
For short walk first get your adreneline pumping first energetic music that has energy in location add some music that is very relaxing it can do this even under direct light you tired.


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Category Archives: Culinary Arts
Easter is almost here!
Written on March 21, 2013 at 4:54 pm, by foundryparkinn
Easter is almost here, and that means it's almost time for our annual Easter brunch at the Foundry Park Inn & Spa! Click here for complete info and to download our entire menu!
Taste of Athens '13!
Written on February 21, 2013 at 2:59 pm, by foundryparkinn
This past weekend, our culinary team (lead by ACF Chef of the Year Steve Vining) participated in the always excellent Taste of Athens. Among Athens' finest chefs and restaurants, our team perfectly represented the Melting Point and served up Continue Reading »
Ah… Romance at the Melting Point!
Written on January 23, 2013 at 5:30 pm, by foundryparkinn
Can you feel it? Valentine's Day is once again tapping us on the shoulder and asking the immortal question, "What in the world are you going to do to show that special someone that you care?!!" Let's face it; no Continue Reading »
The Hoyt House is #1 in Athens on TripAdvisor!
Written on January 8, 2013 at 10:30 am, by foundryparkinn
We did it! Our historic Hoyt House Restaurant here at the Foundry Park Inn & Spa is now ranked Number #1 on TripAdvisor for restaurants in Athens! Check it out —> http://www.tripadvisor.com/Restaurant_Review-g29209-d2058410-Reviews-The_Hoyt_House_Restaraunt-Athens_Georgia.html#REVIEWS
Announcing the 7th Annual Valentine's Dinner & Evening with Francine Reed
Written on January 7, 2013 at 6:26 pm, by foundryparkinn
We are pleased to officially announce the 7th Annual Valentine's Dinner & Evening with legend Francine Reed with Java Monkey on Friday, February 15th, 2013! Join us for a romance-filled, "one night only" performance with, Francine Reed. Known for her Continue Reading »
Choose Your Own Adventure this New Year's Eve!
Written on November 19, 2012 at 4:39 pm, by foundryparkinn
This year, New Year's Eve at the Foundry Park Inn is a little bit country, a little bit rock & roll… and a whole lot of awesome! Get on your boots and kick off 2013 properly with a one-night, year-end bash Continue Reading »
Announcing New Year's Eve 2012 with Kinchafoonee Cowboys!
Written on October 16, 2012 at 2:30 pm, by foundryparkinn
This year, New Year's Eve at the Foundry Park Inn is a little bit country, a little bit rock & roll… and a whole lot of awesome! Get on your boots and kick off 2013 properly with a one-night, year-end Continue Reading »
Chef Steve Vining visits Oconee County High
Written on October 15, 2012 at 9:13 pm, by foundryparkinn
Our Executive Chef Steve Vining recently visited Oconee County High School as part of the American Culinary Federation's "Chef 2 Kids" program. Chef spoke with Consumer Science students about the importance of making healthy food choices for long term health, Continue Reading »
Soup Fest is Almost Here!
Written on October 2, 2012 at 6:22 pm, by foundryparkinn
The 3rd Annual Classic City Soup Fest is here! Brought to you by the Classic City Chefs (American Culinary Federation, Athens Chapter), Soup Fest is a city-wide soup cook-off to raise money for the United Way and Project Safe! From Continue Reading »
Work Smarter (Not Harder) This Thanksgiving!
Written on October 1, 2012 at 3:37 pm, by foundryparkinn
Why stress out over Thanksgiving? This year, work smarter – not harder – and let us take the stress away from your Thanksgiving dining plans! Our "Thanksgiving To-Go" Menu offers both package and à la carte dishes, desserts, and of Continue Reading »


text: The Jumeirah Lake Towers is a huge development in Dubai, United Arab Emirates which consists of a 79 towers being constructed along the edges of four artificial lakes as well as the JLT Embankment of 8 tower facing Jumeirah Islands. The lakes will be completely filled by end of 2009. The total area covered by the lakes, waterways and landscaping will be 730,000-square-meter '7,900,000 sq ft'. The towers will range from having 35 floors to having 45, except for the centerpiece, which is 66 floors. The tallest tower and the centerpiece of the entire complex is Almas Tower which will be situated on its own island between Lake Almas West and Lake Almas East. All residential towers will be placed in clusters of three. This therefore makes the areas easier to navigate when mail is distributed.