text: the following definitions are intended to be clarifying and are not intended to be limiting . “ alkyl ” refers to a monovalent group derived from a straight or branched chain saturated hydrocarbon by the removal of a single hydrogen atom . representative alkyl groups include methyl ; ethyl ; n - and iso - propyl ; n -, sec -, iso -, and tert - butyl ; c 5 to c 12 groups ; eicosanyl ( c 20 ); heneicosanyl ( c 21 ); docosyl ( behenyl , c 22 ); tricosanyl ( c 23 ); tetracosanyl ( c 24 ); pentacosyl ( c 25 ), 3 -, 7 -, and 13 - methylhexadecanyl ; and the like . preferred alkyls include methyl , ethyl , propyl , isopropyl , butyl , and isobutyl . “ aliphatic amine ” and / or “ aminoalkyl ” refers to an alkyl group having one or more amino substitutions or an amino group having multiple alkyl substitutions . representative aminoalkyls include aminomethyl , dimethylaminomethyl , diethylaminomethyl , 2 - aminoethyl , 2 - dimethylaminoethyl , 2 - ethylaminoethyl , and the like . “ amino ” or “ amine ” refers to a group having the structure — nr ′ r ″, wherein r ′ and r ″ are independently selected from h and alkyl , as previously defined . additionally , r ′ and r ″ taken together may optionally be —( ch 2 ) k — where k is an integer of from 2 to 6 . representative amino groups include , amino (— nh 2 ), methylamino , ethylamino , n - and iso - propylamino , dimethylamino , methylethylamino , piperidino , and the like . “ depth of removal ” refers to the amount of co 2 that escapes the absorbent solution during peak performance ( i . e ., co 2 slip ), and is an approximation of the efficiency of co 2 absorption . “ heterocyclic amine ” refers to a substituted carbocyclic structure containing at least one nitrogen member in the ring . “ working capacity ” refers to the difference between rich loading and lean loading . this invention has application in a wide array of industrial processes including gas fields ( e . g ., marginal , stranded , and sour gas fields ), liquefied natural gas ( lng ) liquefaction developments , gas - to - liquids ( gtl ) developments , synthesis gas , and for the removal of co 2 from combustion gases . the disclosed composition may be used in any industrial process , such as single or multi - injection , known in the art or in any specialized high - pressure processes , such as those described in u . s . pat . no . 6 , 497 , 852 , “ carbon dioxide recovery at high pressure ” and u . s . pat . no . 7 , 481 , 988 , “ method for obtaining a high pressure acid gas stream by removal of the acid gases from a fluid stream ,” and in pct patent application no . wo2007077323a1 , “ method for deacidifying a gas with a fractionally - regenerated absorbent solution with control of the water content of the solution .” referring to fig1 , an exemplary production process ( typically found in natural gas processing ) where this invention has utility is shown . production process 100 includes raw gas inlet 105 where gas is contacted counter currently ( typically at pressures greater than atmospheric ) with a lean solvent solution ( i . e ., containing very low concentrations of acidic contaminants ) in absorber column 110 . the rich solvent solution ( i . e ., containing high concentrations of acidic contaminant ( s ) absorbed from the feed gas ) drains out of absorber column 110 and passes via a pressure reduction valve ( not shown ) to rich amine flash drum 115 where co - absorbed volatile hydrocarbons and a portion of the absorbed acid gas contaminate is flashed from the solvent and removed into a vapor discharge stream from the drum . treated gas outlet 120 contains gas exiting the top of absorber column 110 , treated and freed of acid gas contaminant ( s ). the rich amine solvent exits rich amine flash drum 115 and proceeds through rich / lean amine exchanger 125 , where it is heated , and then into the top of regenerator column 130 , where the acid gas contaminant ( s ) is separated from the rich solution at low pressure and high temperature as the solvent flows down the column . the rich solvent is stripped in the column by a countercurrent steam flow produced in amine reboiler 135 at the base of the column . the hot regenerated solvent accumulates at the base of the column and the stripped contaminant ( s ) gasses exit the top of the column with the stripping steam . steam and solvent vapor exiting the top of regenerator column 130 enters acid gas condenser 140 . resulting liquids are collected in reflux drum 145 for circulation back to the top of the regenerator column through reflux , circulation pump 165 . the regenerated hot lean solvent is pumped from the base of regenerator column 130 via rich / lean exchanger 125 ( through lean amine circulation pump 160 ) and lean amine cooler 150 back into the top of absorber column 110 ( through lean amine pressure pump 170 ), where the cycle is repeated . filtration of lean solvent at lean amine filter 155 keeps it clear of solids and contaminants including degradation products caused by adverse components of the raw feed gas stream . it should be appreciated that filtration could take place in multiple and various locations in the process . in one embodiment , the composition of this invention includes at least one substituted cyclic diamine component ( as shown in structure ( i ) above ). in a preferred embodiment , the composition of this invention includes substituted piperazine moieties with substitution at the 1 and / or 4 nitrogen positions of the piperazine ring as well as substitution at the 2 , 3 , 5 , and / or 6 positions . in other embodiments , the composition includes substituted cyclic diamines having a 4 - to 12 - membered ring . exemplary structures of typical n - mono - or n - bi - substituted piperazines of the invention are shown as structure ( iii ) below , where r 18 is h , alkyl , aminoalkyl , or structure ( iv ); r is structure ( ii ) shown below , and r 19 , r 20 , r 21 , r 22 , r 23 , r 24 , r 25 , and r 26 are independently h , alkyl , or aminoalkyl . r 27 , r 28 , r 29 , r 30 , r 14 , r 15 , r 16 , and r 17 are independently h , alkyl , or aminoalkyl , and each m , n , o , x , y and z is independently 0 , 1 , or 2 . in a preferred embodiment , if r 18 is h at least one of r 14 , r 15 , r 16 , or r 17 is not h , and if r 18 is structure ( ii ) at least one of r 27 , r 28 , r 29 , r 30 , r 14 , r 15 , r 16 , or r 17 is not h . in a further embodiment , the composition of the invention includes n - mono - and n - bisubstituted aminopiperazines , which may be substituted in the 2 , 3 , 5 , and / or 6 positions of the piperazine ring . the substitutions are typically methyl , ethyl , propyl , isopropyl , or dimethyl . it should be appreciated that although the 2 , 3 , 5 , and 6 unsubstituted piperazines are proficient co 2 absorbents , significant advantages exist in utilizing the 2 , 3 , 5 , and 6 substituted variants . particularly reductions in process viscosity and improved regenerability are observed . structure ( v ) below illustrates a representative structure for the bisubstituted piperazine embodiment of the invention . r 31 , r 32 , r 33 , r 34 , r 35 , r 36 , r 37 , r 38 , r 39 , r 40 , r 41 , r 42 , r 43 , r 44 , r 45 and r 46 are independently h , alkyl , or aminoalkyl . preferred alkyls include methyl , ethyl , propyl , isopropyl , butyl , and isobutyl . preferred aminoalkyls include 2 - aminopropyl , 2 - aminobutyl , aminoethyl , and aminopropyl . in a preferred embodiment , at least one of r 31 , r 32 , r 33 , r 34 , r 35 , r 36 , r 37 , or r 38 is not h and at least one of r 39 , r 40 , r 41 , r 42 , r 43 , r 44 , r 45 , or r 46 is not h . the value of each s , t , and u are independently 0 , 1 , or 2 . representative monosubstituted piperazines include 2 - aminopropyl - piperazine , 2 - aminobutyl - piperazine , 1 - acetylpiperazine , and 1 - formylpiperazine . representative examples of typical bisubstituted piperazines include 1 , 4 - bis -( 2 - aminopropyl )- piperazine ; 1 , 4 - bis -( 2 - aminobutyl )- piperazine ; 1 , 4 - bis -( 3 - aminobutyl )- piperazone ; 1 , 4 - bis -( n - methyl - aminoethyl )- piperazine ; 1 -( 2 - aminobutyl )- 4 - methylpiperazine ; 1 -( 2 - aminopropyl )- 4 - methylpiperazine ; and 1 -( 2 - aminopropyl )- 4 - ethylpiperazine ; 1 - aminoethyl - 4 -( 2 - aminobutyl )- piperazine ; 1 - aminoethyl - 4 -( 2 - aminopropyl )- piperazine ; 1 - aminopropyl - 4 -( 3 - aminobutyl )- piperazine ; 1 - aminoethyl - 4 -( n - methyl - aminoethyl )- piperazine ; the like ; and combinations thereof . in one embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 1 - 14 ) where r = h , or more preferably r is selected from methyl , ethyl , propyl , isopropyl , and combinations thereof . in another embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 15 - 21 ). in an additional embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 22 - 35 ). in yet another embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 36 - 42 ). in another embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 43 - 49 ), where r = h , or more preferably r is selected from methyl , ethyl , propyl , isopropyl , and combinations thereof . in another embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 50 - 56 ). in a further embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 57 - 63 ). in one embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 64 - 77 ). in a further embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 78 - 84 ). in another embodiment , the composition of the invention includes at least one n absorbent component of the formulas illustrated in structures ( 85 - 91 ). in another embodiment , the composition of the invention includes at least one absorbent component of the formulas illustrated in structures ( 91 - 97 ). the composition of the invention may also include derivatives and / or salts of the disclosed structures . representative derivatives include carbonates , bicarbonates , carbamates , ureas , and amides . representative salts include all inorganic , mineral , and organic salts . it is the intent of this invention to use the disclosed structures in a multitude of compositions including single or multiple component solutions in water or as combined with other acid gas solvent components such as tetramethylene sulfone ( i . e ., sulfolane ), mdea , dea , mea , and the like in water and / or other mutual solvents . for example , single and multiple component solutions range from about 0 . 01 to about 100 wt % actives or from about 1 to about 75 wt % actives and include the use of solvents , such as water , alcohols , polyols , other acid gas solvents , and organic solvents . in a preferred embodiment , the composition includes about 10 to about 75 wt % or from about 40 to about 50 wt % actives . additionally , the composition generally includes an amount of solvent in the range of 0 to 99 . 09 wt %, depending upon the amount of actives . the scrubbing liquid used in the composition of the invention may also include , for example , one or more of the following components : aminoethyl - piperazine ; 2 - aminoethyl - piperazine ; 2 - aminopropyl - piperazine ; 2 - aminobutyl - piperazine ; 1 - acetylpiperazine ; 1 - formylpiperazine ; 1 , 4 - bis - aminoethyl - piperazine ; 1 , 4 - bis - aminopropyl - piperazine ; 1 , 4 - bisaminobutyl - piperazine ; 1 , 4 - bis -( 2 - aminopropyl )- piperazine ; 1 , 4 - bis -( 2 - aminobutyl )- piperazine ; 1 , 4 - bis -( n - methyl - aminoethyl )- piperazine ; 1 -( 2 - aminobutyl )- 4 - methylpiperazine ; 1 -( 2 - aminopropyl )- 4 - methylpiperazine ; 1 -( 2 - aminopropyl )- 4 - ethylpiperazine ; 1 - aminoethyl - 4 -( 2 - aminobutyl )- piperazine ; 1 - aminoethyl - 4 -( 2 - aminopropyl )- piperazine ; 1 - aminoethyl - 4 -( n - methyl - aminoethyl )- piperazine ; 2 - morpholinoethanamine ; 2 - aminopropyl - morpholine ; 2 -( 1h - imidazol - 1 - yl ) ethanamine ; 2 - aminopropyl - piperidine ; 2 - aminopropyl - pyrrolidine ; n1 -( 2 - aminopropyl ) butane - 1 , 4 - diamine ; n1 -( 3 - aminopropyl ) propane - 1 , 2 - diamine ; water ; sulfolane , n - methylpyrrolidone ; n - alkylated pyrrolidones , piperidones and morpholines corresponding to the foregoing ; methanol ; mixtures of dialkyl ethers of polyethylene glycols ; c 1 to c 4 dialkylether monoethylene glycols ; c 1 to c 4 monoether monoethylene glycols ; c 1 to c 4 dialkylether poly ethylene glycols ; c 1 to c 4 monoether polyethylene ethylene glycols ; c 1 to c 4 ; ethylene glycol ; diethylene glycol ; triethylene glycol ; n , n - dimethyl formamide ; n - acetyl morpholine ; n - formyl morpholine ; n , n - dimethyl imidazolidin - 2 - one ; n - methyl imidazole ; and the like . in another embodiment , the composition of the invention may also include other components . representative other components include blends of amines , activators , promoters , antifoaming agents , co - absorbents , corrosion inhibitors , solvents , coloring agents , the like , and combinations thereof . representative examples include alkanolamines ; cyclotetramethylene sulfone and its derivatives ; aliphatic acid amines such as acetyl morpholine or n - formyl morpholine ; alkali metal compounds which provide alkaline hydrolysis products , such as alkali metal hydrolysis and hydrocarbonates ; aliphatic and cycloaliphatic mono - and diamines , such as triethylene diamine , dicyclohexyl amine , n - ethyl - cyclohexylamine , and n , n - diemthylcyclohexylamine ; the like ; and combinations thereof . in various embodiments , the absorbent of the invention may include coabsorbents as disclosed in , for example , u . s . patent application ser . no . 12 / 494 , 521 , “ acid gas scrubbing composition ,” filed jun . 30 , 2009 , 12 / 494 , 533 , “ acid gas scrubbing composition ,” filed jun . 30 , 2009 , and ser . no . 12 / 761 , 939 , “ composition for treating acid gas ,” filed apr . 6 , 2010 , each of which is currently pending . in another embodiment , coabsorbents include one or more components selected from calcium oxide , calcium lignosulfonate , calcium silicate hydrates , calcium hydroxide , calcium carbonate , calcium bicarbonate , sodium carbonate , sodium bicarbonate , trona , sodium sesquicarbonate , soda ash , nacholite , sodium aluminate , metal oxides , and the like . activators and coabsorbents are preferably present in the composition of the invention from about 0 . 01 to about 90 wt %, more preferably from about 1 to about 50 wt %, and most preferably from about 1 to about 25 wt % ( wt % based on the weight of total actives ). in a further embodiment , the invention is a process for reducing acidic contaminants in an industrial fluid stream . the fluid stream is contacted with the disclosed composition to form a washed fluid stream and a rich acid gas scrubbing liquid . typically , the composition is contacted with the gas stream at a temperature ranging from about 0 to about 200 ° c . in certain cases , this temperature range may be from about 0 to about 100 ° c . or from about 20 to about 65 ° c . industrial processes generally run at a pressure ranging from about 0 to about 200 atm , from about 0 to about 100 atm , from about 0 to about 70 atm , from about 0 to about 50 atm , from about 0 to about 25 atm , from about 0 to about 10 atm , or from about 1 to about 5 atm during the time when the composition is contacted with the fluid stream . u . s . pat . no . 4 , 556 , “ bis tertiary amino alkyl derivatives as solvents for acid gas removal from gas streams ” discloses pressure ranges from 4 to 70 atm . canadian patent application no . 2 , 651 , 888 , “ carbon dioxide absorbent requiring less regeneration energy ” discloses pressures from 1 to 120 atm . it should be appreciated that this invention is operable in any of these or other pressure ranges encountered in the relevant art . the rich acid gas scrubbing liquid is further processed through a regeneration system where at least a portion of the composition including at least a portion of the absorbent compound ( s ) contacted with the fluid stream are regenerated . the regeneration step normally takes place at a higher temperature than absorption ( depending on the particular industrial process ), usually at a temperature ranging from about 0 to about 500 ° c ., from about 20 to about 250 ° c , or from about 50 to about 150 ° c . the pressure range for the regeneration step is normally from about 0 to about 10 atm or from about 1 to about 5 atm . in certain cases , the regeneration step may be carried out via a steam - assisted reboiler . regeneration may also be carried out via a fractional regeneration process ( e . g ., wo 2007 / 077323 , “ method for deacidifying a gas with a fractionally - regenerated absorbent solution with control of the water content of the solution ”). the foregoing may be better understood by reference to the following examples , which are intended for illustrative purposes and are not intended to limit the scope of the invention . the testing in this example was used as a means of screening potential acidic contaminant scavengers and also to confirm the performance of existing commercially available scavengers . the test was designed to determine the maximum capacity of an amine solvent in absorbing acidic gases . different amine solvents were compared . the amine solvents were saturated with acidic gases at a constant pressure and temperature until no more gas was able to be absorbed . the difference between the rich and lean loadings was used to determine the working capacity . the test was designed to regenerate the solvent by boiling to remove the acidic gases so that the lean loading of co 2 in an amine solvent could be determined . solvent performance was characterized by liquid loading at equilibrium with defined composition gas mixtures at simulated amine contactor and regenerator conditions relative to industry benchmarks . to highlight the advantages of the disclosed novel amines , several specific samples were benchmarked against common commercial co 2 absorbents ( such as 33 . 8 / 6 . 2 wt . %) methyldiethanolamine / piperazine ( dmdea , a derivative of mdea ), monoethanolamine ( mea ), and illustrated in fig2 ) using a laboratory - scale fixed bed absorption cell and a batch reboiler . the “ sorbent ” numbers indicated in table 1 correspond to the structure numbers above and those indicated in fig2 . the equilibrium saturation test to determine the rich loading ( weight % co 2 absorbed by fresh sorbent ) was run by exposing an aqueous solution of the absorbent at 40 ° c . to 30 psig of co 2 until saturation was reached . the lean loading ( weight % co 2 remaining associated with the absorbent after regeneration ) was determined by refluxing the aqueous solution of the absorbents for two hours at atmospheric pressure . the working capacity is defined as the rich loading minus the lean loading . it is the working capacity that most accurately reflects the capacity of the chemical to absorb co 2 under process conditions . the results of this evaluation are reported in table 1 . to determine rich loading , the equipment consisted of a high pressure gas panel that was capable of receiving supplies of 100 % co 2 , co 2 / n 2 mixtures and co 2 / h 2 s / n 2 mixtures . the chosen gas was fed via a mass flow controller ( sierra series 100 mass flow controller , available from sierra instruments , inc . in monterey , calif .) to the reaction vessel . a gas totalizer ( a sierra compod ) attached to the mass flow controller measured the volume of gas used . once the appropriate gas cylinder valve and regulators were opened , the recirculating bath was set to a temperature of 40 ° c . a 200 ml glass reaction vessel was attached to the head of a buchi picoclave . the inlet and outlet valves to the reaction vessel were closed and the inlet pressure regulator was set to 30 psig . the gas mixture was set to 100 % co 2 and the flow rate was set to 0 . 5 liters / min . after allowing the gas pressure to build to 30 psig at the reactor inlet , the amine solution was prepared at the concentration indicated in table 1 and , after being brought to the same temperature as the reaction vessel , was added to the reaction vessel and stirred at 1 , 000 rpm . the inlet valve was opened and the reactor pressure was allowed to equilibrate to 30 psig . when the pressure in the reactor reached 30 psig , the inlet valve was closed and the gas flow was shut off . the volume in the reactor vessel was recorded . gas flow was resumed after 5 minutes and continued until the pressure equalized to 30 psig . this procedure was repeated until no additional co 2 was absorbed as measured by the final volume . the wt % rich loading of the amine was calculated from the final volume of co 2 absorbed . to determine lean loading , the amine composition to be regenerated was poured into a 250 ml 3 - neck flask equipped with mechanical stirring and a chilled condenser ( 8 ° c ). the amine solution was slowly heated to reflux ( about 100 to 104 ° c ) to help avoid a sudden release of gas which would have caused the solution to foam . the solution was refluxed for 2 hours and then cooled to room temperature . the lean loading of the amine was determined via a standard barium chloride back titration . to determine depth of removal , a mass flow controller ( sierra series 100 mass flow controller ) was used to control the flow of gas through the reactor vessel . the chosen gas was fed via the mass flow controller to the saturation vessel ( which contained deionized water ) and then into the reaction vessel . from the reaction vessel , the gas was fed via a backpressure regulator through a dreschel bottle containing ethylene glycol and a drying tube containing silica gel to the co 2 analyzer . the co 2 analyzer ( signal 7000 fm co 2 analyzer ) recorded the concentration of co 2 flowing through it . the recirculating bath was set to the required temperature of 40 ° c . the 200 ml glass reaction vessel was fitted to the head of a buchi picoclave . a dreschel bottle containing ethylene glycol and a drying tube containing silica gel was connected to the gas line prior to the co 2 analyzer , and the backpressure regulator was set to 90 psig . the gas mixture ( 25 % co 2 / 75 % n 2 ) and the flow rate ( 0 . 45 liters / min ) were then set and allowed to stabilize for 30 minutes . the amine solution was prepared at the concentrations indicated in table 1 and heated as above . the amine was then added to the reaction vessel and the stirrer was set to 1 , 000 rpm . the downstream regulator was closed and the data recording began . the gas flow was allowed to continue until equilibrium was reached ˜ 3 hrs . at the end of the run , the gas flow was stopped , the inlet valve to the reaction vessel was closed , and the data recording was stopped . the tested amines on average absorbed about 1 . 36 moles of co 2 per mole of absorbent compared to less than 0 . 83 mole of co 2 per mole of the common absorbents . although 97 only slightly outperformed the common absorbents sorbent 1 ( r = methyl ) showed a significant increase in working capacity ( 13 % increase based on mea ; 22 % increase based on dmdea ). these novel amines also have a significantly lower lean loading than mea . the boiling points of the disclosed amines range from about 200 to about 280 ° c at 1 atm ( compared to mea at 170 ° c and 1 atm ). such higher boiling points help significantly reduce the losses and potential environmental releases currently associated with the volatility of mea and also help to prevent co 2 contamination during solvent regeneration . initial laboratory stability testing has indicated that unlike mea , which is known to degrade rapidly under process condition , the disclosed amines are highly robust at simulated process conditions showing no signs of degradation . to further highlight the utility of the tested amines for carbon capture , a 25 % co 2 gas stream at 90 psig was passed through the absorbents at 40 ° c until they reached saturation and the depth of removal was recorded . importantly , the depth of removal for many of the tested amines approached 0 %, an indication that they are highly efficient at co 2 capture as shown in table 1 . although a reduction in the lean loading of branched compounds over linear compounds would have been expected , the select group of molecules tested also showed a unique increase in the rich mole ratio of the branched targets ( table 1 )). this unusual reactivity is particularly evident when comparing the linear aep , a promoter known in the industry , to the branched sorbents 97 and 1 ( r = methyl ), this increase in molar capacity is thought to occur via a change in the mechanism by which the amine reacts with co 2 . thus , the reactions between co 2 and the branched amines are of greater efficiency . this example compared the absorption sorbents 97 and 1 ( r = methyl ). the two molecules are identical in molecular weight and were tested under identical conditions ; however , sorbent 1 ( r = methyl ) shows a 7 . 6 % increase in working capacity , and significantly improved in process viscosity and improved process regenerability . this effect has been attributed to the substitution of the piperazine ring carbon . the rate of transfer of a solute between a gas and a liquid is proportional to the liquid film area which is the contact surface between the two phases . this contact area will be beneficially greater in a liquid which has a lower viscosity as compared against a benchmark liquid of greater viscosity due to the decrease in mean gas bubble diameter in the lower viscosity liquid and resulting increase in contact surface area as compared against the liquid of greater viscosity . this benefit is realized in both absorption and desorption of the solute into and out of a liquid phase . in an absorption column the increase in surface contact area proportionally increases the volumetric mass transfer coefficient k 1 a therefore reducing the amount of contact time required to achieve a required solute transfer fraction from gas to liquid phase . in a desorption column , the increase in surface area again benefits the mass transfer , but this time out of the liquid phase and into the stripping gas phase resulting in a reduction in contact time required to achieve the required reduction in liquid phase concentration of the solute as compared to the more viscous benchmark . all of the compositions and methods disclosed and claimed herein can be made and executed without undue experimentation in light of the present disclosure . while this invention may be embodied in many different forms , there are described in detail herein specific preferred embodiments of the invention . the present disclosure is an exemplification of the principles of the invention and is not intended to limit the invention to the particular embodiments illustrated . in addition , unless expressly stated to the contrary , use of the term “ a ” is intended to include “ at least one ” or “ one or more .” for example , “ a device ” is intended to include “ at least one device ” or “ one or more devices .” any ranges given either in absolute terms or in approximate terms are intended to encompass both , and any definitions used herein are intended to be clarifying and not limiting . notwithstanding that the numerical ranges and parameters setting forth the broad scope of the invention are approximations , the numerical values set forth in the specific examples are reported as precisely as possible . any numerical value , however , inherently contains certain errors necessarily resulting from the standard deviation found in their respective testing measurements . moreover , all ranges disclosed herein are to be understood to encompass any and all subranges ( including all fractional and whole values ) subsumed therein . furthermore , the invention encompasses any and all possible combinations of some or all of the various embodiments described herein . any and all patents , patent applications , scientific papers , and other references cited in this application , as well as any references cited therein , are hereby incorporated by reference in their entirety . it should also be understood that various changes and modifications to the presently preferred embodiments described herein will be apparent to those skilled in the art . such changes and modifications can be made without departing from the spirit and scope of the invention and without diminishing its intended advantages . it is therefore intended that such changes and modifications be covered by the appended claims .