Abstract:
An off gas extraction system provides superior results to other systems for cleaning polluted soil. Off gas is extracted, followed by compression and condensation. Compression and condensation produce an off gas that must be further treated to produce pollutant-free exhaust. A regenerative adsorber cleans the influent gas/air by adsorbing residual chemical vapor and concentrates the removed chemical vapor and reprocesses them. Conventional scrubbers are used on the back end of the system to produce a final exhaust as prescribed by environmental regulation. Methods of accomplishing the same are similarly provided, including unique business methods for conforming extraction plans with current environmental regulations and compliance impact generation based on an evolved knowledge base.

Description:
RELATED APPLICATIONS 
   This application claims the Paris Convention Priority of U.S. Utility application Ser. No. 11/611,773, entitled “OFF GAS EXTRACTION AND CHEMICAL RECOVERY SYSTEM AND RELATED METHODS” filed on 19 Dec. 2006, the contents of which are incorporated by reference herein. 
   SUMMARY 
   An off gas extraction system provides superior results to other systems for cleaning polluted soil and recovery of chemicals from soil. Off gas is extracted, followed by a compression and condensation. Compression and condensation produce liquid condensates and an off gas that must be further treated to produce pollutant-free exhaust. A regenerative adsorber concentrates polluted off gasses, which are sent to the front of the system. Conventional scrubbers are used on the back end of the system to produce a final exhaust as prescribed by environmental regulation. Methods of accomplishing the same are similarly provided, including business methods for efficiently remediating polluted soil by optimizing target off gas selection and processing of the same to achieve compliance with changing environmental regulations. 
   According to a feature of the present disclosure, a system for extracting pollutants from off gas is disclosed comprising, in combination: at least one off gas extraction well, a compressor, a heat exchanger to condense fluid from off gas, a regenerative adsorbing unit having at least one regenerative adsorber, and a specific gravity separator. 
   According to another feature, a regenerative adsorber is disclosed comprising, in combination: at least one chamber containing activated alumina, where each chamber has at least one inlet and at least one outlet. The activated alumina is charged with a pollutant at high pressure and the pollutant is unloaded from the activated alumina at low pressure. 
   Moreover, further features of the present disclosure are disclosed including a method of extracting pollutant from soil comprising in combination: extracting an off gas, compressing the off gas, condensing the off gas to form at least one liquefied contaminant, adsorbing any residual pollutants from the compressed condensed off gas with at least one regenerative adsorber to produce a substantially pollutant-free off gas, scrubbing the substantially pollutant-free off gas with activated carbon, and determining compliance with applicable regulatory requirements. 
   Still more features of the present disclosure are disclosed including a method for optimizing extraction of pollutant from soil comprising, in combination: initiating testing to determine contaminants to be addressed at a remediation site, generating a preliminary plan to optimize recovery of contaminants, cross referencing the preliminary plan to a database of recovery parameters defined by a regulatory authority, executing the plan with an off gas extraction system to recover the contaminants, verifying the nature and quantities of the species of recovered contaminants to form a set of data, and confirming that the data satisfy regulations imposed by a regulatory body. 
   Finally according to a feature of the present disclosure, there is disclosed a method comprising: determining a remediation site, recovering at least one contaminant from the site, separating recovered contaminants into at least one subset of contaminants, and recycling the separated recovered contaminants for reuse. 

   
     DRAWINGS 
     The above-mentioned features and objects of the present disclosure will become more apparent with reference to the following description taken in conjunction with the accompanying drawings wherein like reference numerals denote like elements and in which: 
       FIG. 1  is a block diagram of an embodiment of an off gas extraction system for removing pollutant from soils; 
       FIG. 2  is a block diagram of an embodiment of a module for preparing an off gas to have pollutant-laden vapor removed; 
       FIG. 3  is a block diagram of an embodiment of a compression/condensation system for condensing pollutant-laden vapor from a gas; 
       FIG. 4  is a block diagram of an embodiment of a regenerative adsorption system; 
       FIG. 5  is a flow chart of an embodiment of a method for removing pollutant-laden vapor from gas extracted from soil; 
       FIG. 6  is a flow chart of an embodiment of a process for addressing contaminants at a contaminated site; 
       FIG. 7  is a graph of an embodiment of experimental data of the system of the present disclosure; and 
       FIG. 8  is a graph of an embodiment of experimental data of the system of the present disclosure. 
   

   DETAILED DESCRIPTION 
   As used in the present disclosure, the term “off gas” shall be defined as gasses extracted from contaminated sources and includes soil vapors and previously collected soil vapors. 
   The industrial revolution marked a radical change to many aspects of society. Industrialized nations became increasingly productive and urbanized. Chemical production became centralized. Other industries utilized chemicals in the production process of other goods. Increased pollution was the result. Soil, air, and water carried unprecedented levels of pollutants over the last 200 years. 
   Nevertheless, during the middle of the 20 th  century, social conscience and government sought to eliminate or reduce pollution where possible. The United States government passed strict environmental laws and set aside funds for cleaning polluted natural resources. Similarly, corporations and companies are taking steps to improve the nature and quality of pollutants and to address polluted natural resources. 
   Traditionally, pollutants trapped in the soil have been very difficult to address. Contaminated soil provides a uniquely difficult problem in that it cannot be filtered like air or water. Rather, pollutants must be drawn out of the soil. Generally, the process of drawing out the pollutant requires air or water and heat to be used to enable extraction of the pollutant as a vapor or liquid, which must then be quarantined or cleansed. Often, pollutants are removed from the soil by off gas extraction processes. 
   Soil vapor extraction (SVE), also known as “soil venting” or “vacuum extraction”, is an in situ remedial technology that reduces concentrations of volatile pollutants. In this technology, a vacuum is applied to wells neat the source of contamination in the soil. Volatile constituents of the contaminant mass “evaporate” and the vapors are drawn toward and extracted through the extraction wells. Extracted vapor is then cleansed. The increased airflow through the subsurface can also stimulate biodegradation of some contaminants, especially those that are less volatile. Wells may be either vertical or horizontal. 
   SVE has been successfully applied to many petroleum derived volatile organic compounds (VOCs) as well as semi-volatile organic compounds (SVOCs). However, other chemicals present in the soil have been difficult, if not impossible, to remove using technologies prior to the present disclosure. Indeed, prior technologies are unsuited for remediation of halogenated chemicals, chloromethane, and many other volatile chemicals. 
   Prior technologies often rely on compression and condensation for removal of VOCs. These systems may also be coupled with scrubbing units for residual removals of contaminated vapor prior to release to the atmosphere. Usually, scrubbing units comprise granular activated carbon (GAC) traps. Once each GAC trap becomes saturated with residual contaminant, they must be replaced and new activated carbon used. Certain regenerative systems treat GAC with steam, which removes contaminants from the carbon. For certain chemicals, such as halogenated compounds, the heat and water from steam results in strong hydrohalic acids. These acids are difficult to handle, involve health and safety risks, cause corrosion, and consequently carry with them increased costs of remediation. 
   Moreover, other VOCs, such as chloromethane and freon are difficult to remove in compression and condensation steps due to their low condensation points. Thus, to remove these types of chemicals from the gas stream, the condensation process must cool the vapor to extremely low temperatures, which increases costs and makes prior SVE methods for dealing with these types of chemicals less attractive. Moreover, remediation sites may often contain these types of chemicals in combination with other VOCs. When contaminated vapors are not removed in the compression/condensation step, the scrubbing units become the primary SVE component for removing these types of VOCs. The result is more frequent replacement of the scrubbing reagents, as well as undesirable side effects previously discussed and many others. 
   Moreover, regenerative processes that require heat are potentially dangerous with VOCs that have high vapor pressures. Introducing heat in the presence of oxygen in these situations may lead to fires and explosions. In addition to potential destruction of hardware that may occur due to fires and explosions, the VOCs or dangerous byproducts may also be released generally into the atmosphere. Thus, a system is needed to allow SVE remediation for VOCs that are not suited to traditional VOC methods and systems. The present disclosure addresses this need by providing a novel enhanced SVE system and methods capable of remediation of soil containing difficult to remove VOCs. 
   Turning now to  FIG. 1 , there is shown an embodiment of a remediation and chemical recovery system  100 . Remediation and chemical recovery system  100  generally comprises a plurality of extraction wells  110  and SVE system  200 . SVE system  200  comprises a number of subsystems, according to embodiments, including vacuum and compression module  300 , vapor elimination module  400 , and contaminant recovery module  500 . Vacuum and compression module  300  removes off gas from extraction wells  110 , removes liquid constituents recovered in the off gas removal process, and compresses the off gas. Vapor elimination module  400  removes contaminated vapor from the gas, producing a substantially dry gas as an intermediate result. Finally, contaminant elimination module  500  collects chemical vapors and scrubs the substantially dry gas for residual contaminant. 
   According to an embodiment of vacuum and compression module  300  in  FIG. 2 , contaminated vapor is removed from extraction wells  110  and transferred via inlet conduit  302  into vacuum and compression module  300 . According to embodiments, water and gas are separated using gas/water separator  310  to prevent liquid from entering compressor  330 . According to embodiments, gas/water separator  310  may be, for example, a 60 gallon Manchester vertical tank (Manchester Tank, Franklin, T). Gas/water separator  310  comprises an inlet connected to inlet conduit  302 , a gas outlet, and a liquid out. 
   The gas outlet is connected to inlet blower, for example a Roots type blower (e.g., frame size 36 powered by 116 cfm at 10″ Hg, 5-10 horsepower, 3 phase, totally enclosed, fan cooled (TEFC) 240/280 volt electric motor). Blower  320  is used to create a vacuum that pulls vapor from extraction wells  110 . Other similar vacuum creation devices may be used depending on the desired gas flow rate, etc. as known and understood by a person of ordinary skill in the art. 
   As shown in  FIG. 1 , the liquid inlet connects to transfer pump  360 , which pumps liquid from gas/water separator  310  into initial contaminant recovery tank  370 . Generally, depending on the well configuration, little water will be extracted from extraction well  110 . However, if the water table is high, slurping may occur necessitating gas/water separator  310  to separate the water from the gas. According to this configuration, holes are inserted into pipes at each extraction well site, some above that water table and some below. The vacuum pulls both vapor and water from the well, which is then separated by gas/water separator  310 . 
   Transfer pump  360  removes liquid from gas/water separator  310 . Transfer pump  360  may be, for example, a centrifugal, 120/230 volt, ½ horsepower motor pump capable of moving 20 gallons per minute, according to embodiments. Naturally, extraction wells  110  that produce large volumes of water may need transfer pump  360  that is capable of pumping liquid at a more rapid rate. Similarly, extraction wells  110  producing only nominal amounts of water may be fitted with transfer pump  360  that moves fewer gallons per minute. The exact choice of transfer pump  360  will be known and understood by artisans. 
   Initial contaminant recovery tank  370  may be any tank suitable for the purpose of collecting contaminated liquids. As described below, a specific gravity separator may be disposed between transfer pump  360  and initial contaminant recovery tank  370  to separate each specific contaminant from the other contaminants, according to embodiments. 
   Turning back to  FIG. 2 , inlet blower  320  moves gas containing contaminated vapor from gas/water separator  310  to compressor  330 . Compressor may be any number of conventional air compressor systems known to artisans, e.g., a Quincy Model Q 5120 reciprocating compressor, 94 scfm at 175 psi, powered by a 25-horsepower TEFC 240/280 volt electric motor. A person of ordinary skill in the art will know and understand the applicable compressors to use based on the relevant parameters in the system. According to embodiments, air compressor  330  will be able to compress gas to at least 175 psi. Compressed gas containing contaminated vapor concentrates the contaminated vapor for later removal in vapor elimination module  400 . 
   After gas is compressed with gas compressor  330 , gas is routed to aftercooler  350 , which commences a first round of cooling for the compressed gas containing the contaminated vapor. According to embodiments, aftercooler  350  may be comprised of a Arrow model AFC 120-1 air to air cooler system (at 150 psi and 180 scfm). As gas is compressed, temperature of gas increases substantially in compliance with that algorithm defined by or known as the ideal gas law. Aftercooler  350  provides the initial cooling of hot gas prior to full condensation in vapor elimination module  400 . As the hot gas cools, initial condensation may occur and an amount of contaminated vapor may condense. The condensate is transferred from aftercooler  350  via aftercooler conduit  355  to initial contaminant recovery tank  510 . 
   Exhaust from vacuum and compression module  300  is directed to vapor elimination module  400  via vapor elimination inlet conduit  352 . According to embodiments, vapor elimination module  400  comprises condensation module  410  and regenerative adsorber module  450 . Vapor is initially directed to condensation module  410 . In condensation module  410 , a great majority of contaminated vapor is condensed and caused to be collected by primary contaminant recovery tank  510 . In regenerative adsorber module  450 , residual contaminated vapor is captured and routed to the front on SVE system  200  and rerouted into vapor elimination module  400 ; clean air from regenerative adsorber module  450  is exhausted to activated carbon scrubbers  520   a ,  520   b ,  520   c.    
   According to an embodiment shown in  FIG. 3 , further differentiation of other systems is schematically illustrated, whereby, for example condensation module  410  comprises a heat exchange system for reducing the temperature of the gas containing contaminated vapor. This module responds to ongoing challenges others have had in dealing with certain volatiles which are not easily converted into the liquid phase. The process causes many chemicals to condense into a liquid, which is subsequently routed to contaminant recovery module  500 . 
   According to embodiments, condensation module  410  comprises a plurality of heat exchanging mechanisms  412 ,  416 . Air/air heat exchanger  412  accomplishes initial cooling of compressed contaminated vapor. Importantly, air/air heat exchanger removes virtually all of the water and water vapor in the compressed gas. After initial cooling has occurred, the compressed contaminated vapor is transferred to air/refrigerant heat exchanger  416  via warm vapor conduit  414 . Further cooling of the compressed contaminated vapor occurs in air/refrigerant heat exchanger  416 , causing condensation of the compressed contaminated vapor as the temperature of the gas containing the contaminated vapor drops below condensation point depending on the chemical being condensed. At this stage the compressed vapor is virtually dry and free of water and water vapor, according to embodiments. 
   Air/air heat exchanger  412  and air/refrigerant heat exchanger  416  work in tandem to heat and cool their respective input and output gasses. The cold output from air/refrigerant heat exchanger  416  is routed through air/air heat exchanger  412  via cold vapor conduit  418 . Warm gas incoming to air/air heat exchanger  412  from aftercooler  350  via vapor elimination inlet conduit  352  is therefore cooled by the cold gas routed into air/air heat exchanger  412  and the cold gas in cold vapor conduit  418  is likewise warmed by warm gas incoming from aftercooler  350  via vapor elimination inlet conduit  352 . 
   According to embodiments, air/air heat exchanger  412  and air/refrigerant heat exchanger  416  are disposed in condensation module  410  in pairs. Typically, the pairs of heat exchangers  412 ,  416  work in cycles. During the cooling phase in air/refrigerant heat exchanger  416 , condensate of the compression contaminated vapors forms. Condensate will continue to form as long as refrigerant remains in air/refrigerant heat exchanger  416 . To remove the condensate, the air/refrigerant heat exchanger  416  must undergo a thawing cycle to liquefy the condensate and remove it, which requires the refrigerant to be removed. Thus, by using pairs, first air/refrigerant heat exchanger  416  cools while the second air/refrigerant heat exchanger  416  thaws. Once thawing is complete, the respective functions are reversed and the first air/refrigerant heat exchanger  416  thaws while the second air/refrigerant heat exchanger  416  cools. Thawed liquefied contaminant is removed from heat exchangers  412 ,  416  as would be known to artisans. The heat exchange process described herein is accomplished, according to embodiments, in cycles to optimize heat exchange and prevents air/refrigerant heat exchanger  416  from freezing up. 
   According to embodiments, refrigerant and warm gas to be cooled by refrigerant are input at the same location and experiences parallel flow rather than cross flow, as known in the art. Embodiments employing parallel flow are more rapidly cooled, allowing for shorter cycle times and improving the overall efficiency of the system. According to embodiments, cross flow configurations and parallel flow configurations may be chosen on a case by case basis as would be known to a person of ordinary skill in the art. 
   Air/refrigerant heat exchanger  416  exchanges heat as would be known to a person of ordinary skill in the art. That is, the refrigerant provides the cooling for the gas. The final temperature range of the gas depends on the coolant used, airflow, and other factors. According to embodiments, if a majority of contaminant condenses in air/air heat exchanger  412 , then gas flow may be increased or cycle time may be decreased as a matter of efficiency. Similarly, where contaminated vapor fails to condense at an efficient rate, gas flow may be decreased or cycle time may be increased to expose gas to refrigerant for a longer period. 
   According to other embodiments where heat exchange occurs in cycles, gas flow rate remains constant, but the duration the gas is exposed to the heat exchangers is varied. Thus, if air/air heat exchanger  412  inefficiently condenses vapor, the duration in the air/refrigerant heat exchanger  416  may be increased in each cycle. Thus, variations in the optimization of gas temperatures may likewise be effected. 
   According to embodiments, aftercooler  350  monitors the temperature of the compressed contaminated gas to deliver it to condensation module  410  within an optimal temperature range for condensation cycling. Compressed contaminated gas that is too cold will not effectively warm cold exhaust from air/refrigerant heat exchanger  416  and compressed contaminate gas that is too warm will be inefficiently cooled in condensation module  410  requiring cycle times to be increased to remove a substantial portion of contaminated vapors. Thus, tuning aftercooler to provide an optimal compressed contaminated gas temperature prior to delivery to condensation module  410  increases efficiency of the system and serves as an optimization step. 
   For example, condensed vapor leaves compressor  330  at approximately 250° F. and approximately 180 PSI. Aftercooler  350  reduces the temperature from approximately 250° F. to approximately 85° F. As previously described, an initial condensate will be formed as the gas is initially cooled in aftercooler  350 . The initial condensate is transferred to an initial contaminant recovery tank or, according to embodiments, primary contaminant recovery tank  510  in contaminant recovery module  500 . 
   Gas is transferred from aftercooler  350  to air/air heat exchanger  412  via vapor elimination inlet conduit  352 . Gas entering air/air heat exchanger is cooled from approximately 85° F. to approximately 20° F., as the heat exchange occurs between the gas from aftercooler  350  and the cold gas from air/refrigerant heat exchanger  416 . Further condensate is formed as the gas further cools to approximately 20° F. It is transferred to primary contaminant recovery tank  510  in contaminant recovery module  500  via contaminant recovery module conduit  420 , according to embodiments. Specific gravity separator  508  may be included to separate contaminants by specific gravity and store separated chemical contaminants in multiple contaminant recovery tanks  510 . 
   The gas cooled to 20° F. then transfers to air/refrigerant heat exchanger  416  for further cooling to a cold gas from approximately 20° F. to approximately (−30)° F. due to the heat exchange between gas and refrigerant, as known to artisans. As depicted in  FIG. 3 , refrigeration unit  430  provides refrigerant via refrigerant inlet conduit  432  to air/refrigerant heat exchanger  416  for cooling of the cold gas. To prevent freezing up problems, gas/gas heat exchanger  412  may be cycled with gas/refrigerant heat exchanger  416 , as would be known to artisans. Thus, prior to freezing up, warmer gas from gas/gas heat exchanger  412  is used to warm the cold gas in gas/refrigerant heat exchanger  416 . After cooling, the refrigerant returns to refrigeration unit  430  via refrigerant outlet conduit  434 , according to embodiments. At this point in the process, virtually all water vapor has been removed from the gas, but chemical vapors may remain due to varying dew points and vapor pressures. 
   According to an embodiment, the final temperature of the cold gas depends on the length of time the gas is cooled and the refrigerant. In air/refrigerant heat exchanger  416  final condensation occurs and the condensate is collected after thawing and transferred to contaminant recovery module  500  via contaminant recovery module conduit  420 . The dry cold gas is then transferred to air/air heat exchanger to cool incoming warm gas from aftercooler  350  and warm the cold gas. According to embodiments, cold gas is then touted to regenerative adsorber  450  to remove residual chemical vapors via regenerative adsorber inlet conduit  452 . 
   According to embodiments, multiple condensation modules  410  may be used in parallel or in series to improve efficiency of the condensation process. A person of ordinary skill in the art will understand that each remediation site may require optimization dependant on the particular contaminants at the site, their relative abundance, their vapor pressures, their dew points, and their specific heat of phase conversion. 
   However, the prior art systems have been unable to be industrially effective for condensation of more challenging contaminants. The present invention&#39;s optimizing differentiates it from extant systems, with condensation modules  410  used in parallel to provide for greater gas flow through the system. Conversely, condensation modules  410  may be used in series to expose contaminated vapor to subsequent condensation steps in an attempt to remove greater percentages of total contaminants during the condensation step, according to embodiments. 
   After the condensation step, residual contaminated vapor typically remains in the gas due to incomplete condensation or chemicals that are not cooled enough or for long enough for condensation to occur. According to an embodiment in  FIG. 4 , high-pressure gas containing residual contaminated vapor is routed to regenerative adsorber module  450  via regenerative adsorber inlet conduit  452 . As shown, two adsorption chambers  460   a ,  460   b  work in tandem to adsorb residual contaminated vapor. During operation, one adsorption chamber  460   a ,  460   b  adsorbs residual contaminated vapor while the other adsorption chamber  460   b ,  460   a  deadsorbs contaminated vapor. The process of desorption regenerates adsorption material  462   a ,  462   b  for re-adsorption of contaminated vapor. 
   According to an embodiment, an adsorption material  462   a ,  462   b  is activated alumina. A person of ordinary skill in the art will readily know and appreciate that other, similar materials may be used in adsorption module depending on the nature of the remediation site, the chemicals involved, and goals of each remediation project. Adsorption by adsorption materials, such as activated alumina, carbon, or resins, occurs at high pressure; desorption occurs at low pressure. Other similar materials and materials specifically suited to adsorption of specific chemicals are expressly contemplated as would be known to a person of ordinary skill in the art. Both adsorption and desorption are temperature insensitive processes, which makes the present system superior for many types of remediation, such as with halogenated chemicals due to the lack of necessity to introduce heat and form strongly acidic byproducts as a result in the desorption process. 
   Contaminated vapor is introduced to regenerative adsorber module  450  via regenerative adsorber inlet conduit  452 . Disposed between regenerative adsorber inlet conduit and each adsorption chamber  460   a ,  460   b  are inlet valves  454 . Inlet valve  454  control which adsorption chamber  460   a ,  460   b  is adsorbing residual contaminated vapor and adsorption chamber  460   a ,  460   b  desorbing contaminated vapor. During the adsorption process, inlet valve  454  is in an open position allowing gas containing residual contaminated vapor to enter adsorption chamber  460   a ,  460   b  and contact adsorption material  462   a ,  462   b . During the desorption process, inlet valve  454  is in a closed position to prevent gas from entering adsorption chamber  460   a ,  460   b.    
   During the adsorption process, gas containing residual contaminated vapor is forced through adsorption material  462   a ,  462   b  in adsorption chamber  460   a ,  460   b . Adsorption material  462   a ,  462   b  removes vapor from the gas, including contaminated vapor. As vapor is removed from the gas, adsorption material  462   a ,  462   b  charges with contaminated vapor. Gas leaving adsorption chamber  460   a ,  460   b  is therefore substantially clean. Artisans will recognize that one of flow rate of the gas containing contaminated vapor or cycle time will vary from remediation site to remediation site. 
   Depending on the types of chemicals being removed, the concentration of the contaminants, the relative amount of contaminated vapor removed in previous remediation steps, for example compression/condensation, and the efficiency of adsorption material  462   a ,  462   b  in removing particular vapors from the gas, the parameters within which the system runs will differ. To that end, a person of ordinary skill in the art will know and understand that flow rate or cycle time, adsorption material  462   a ,  462   b , surface area of adsorption material  462   a ,  462   b , and other similar variables known to artisans will be evaluated and optimized on a per site basis. In some cases, multiple regenerative adsorption modules  450  will be used in series to accomplish a desired reduction in contaminated vapor passing through vapor elimination module  400 . 
   According to an embodiment where adsorption material  462   a ,  462   b  is activated alumina or other materials, adsorption of vapor in gas occurs at high pressure. For example and according to an embodiment, cold gas leaving condensation module  410  is at approximately 150 PSI (referring back to  FIG. 1 ) having been compressed prior to entering condensation module  410 . After leaving condensation module  410  and entering regenerative adsorber module  450 , gas pressure is still at approximately 150 PSI. 
   Referring again to  FIG. 4 , once gas has been exposed to and caused adsorption material  462   a ,  462   b  to be charged with contaminated vapor, the exhaust is substantially clean. It escapes through clean exhaust conduit  472 . Disposed on clean exhaust conduit  472  are clean exhaust valves  474 , according to the exemplary embodiment. Generally, at least one clean exhaust valve  474  is disposed along clean exhaust conduit  472  per adsorption chamber  460   a ,  460   b , although multiple clean exhaust valves  474  are contemplated as would be known to artisans. Clean exhaust conduit  472  releases substantially clean gas into the ambient air or routes the substantially clean gas to scrubbers  530 , according to embodiments. A back pressure regulator may be disposed prior along clean exhaust conduit  472  to maintain a baseline of pressure in remediation and chemical recovery system  100 . 
   According to embodiments, clean exhaust valves  474  shunts a portion of substantially clean gas for the purpose of desorption. When clean exhaust valve  474  is “closed,” it allows a small flow of clean exhaust gas to flow to charged adsorption chamber  460   a ,  460   b  and through charged adsorption material  462   a ,  462   b . This low pressure flow causes adsorption material  462   a ,  462   b  to release the contaminated vapors collected in the charging step. These vapors exit through exhaust conduit  470  as inlet valve  454  is closed for charged adsorption chamber  460   a ,  460   b  as the desorption step occurs. 
   To that end, clean exhaust valves  474  are configured to shunt a portion of the substantially clean gas into adsorption chamber  460   a ,  460   b  that is desorbing contaminated vapor. Because desorption occurs at lower pressure, a small percentage of the total clean exhaust gas is diverted as a low pressure gas to desorbing adsorption chamber  460   a ,  460   b , while the remaining substantially clean gas continues through clean exhaust conduit  472 . The process of shunting a small percentage of substantially clean gas may be accomplished by partially opening clean exhaust valve  474  or through the use of a multiple valve system, as would be known to artisans. For example, clean exhaust valve  474  may comprise one valve that allows low-pressure substantially clean gas to pass during adsorption chamber&#39;s  460   a ,  460   b  desorption cycle and a separate valve that may be fully opened to allow high-pressure substantially clean gas to escape during the adsorption cycle. The implementation of such a system will be known and understood by a person of ordinary skill in the art. 
   Consequently, as one adsorption chamber, e.g.,  460   a , of regenerative adsorber module  450  is being charged with contaminated vapors and exhausting substantially clean exhaust gas, adsorption chamber,  460   b  is being desorbed of contaminated vapors previously collected and contained in adsorption material  462   b . Desorption occurs as a percentage of the substantially clean gas forming a low pressure flow is shunted into adsorption chamber  460   b . After adsorption chamber  460   a  becomes fully charged, the system is reversed and adsorption chamber  460   b  is charged with contaminated vapors while adsorption chamber  460   a  is desorbed of the previously collected contaminated vapors. 
   During the desorption cycle of adsorption chamber  460   a ,  460   b , adsorption material  462   a ,  462   b  starts in a state wherein adsorption material  462   a ,  462   b  is fully charged with contaminated vapor. As low-pressure substantially clean air is shunted into adsorption chamber  460   a ,  460   b , vapor contained in adsorption material  462   a ,  462   b  is released from adsorption material  462   a ,  462   b  into the low-pressure substantially clean gas. The resultant gas comprises concentrated contaminated vapor. The gas containing the concentrated contaminated vapor is then routed through exhaust conduit  470  to vacuum and compression module  300  for recompression and rerouting through compression/condensation. 
   Multiple regenerative adsorber modules  450  may be placed in series or in parallel as a matter of efficiency to ensure adequate removal of particularly difficult contaminants. Moreover, efficiencies of the present system may provide for increased gas flow rates, and thus more rapid remediation of a polluted remediation site, due to increased efficiency of remediation and chemical recovery system  100  over conventional SVE systems. 
   Thus, artisans will appreciate that nearly all contaminated vapor from the ground is eliminated by compression/condensation. Vapor that escapes compression/condensation is captured by adsorption material  462   a ,  462   b  for reconcentration during the desorption process. The reconcentrated contaminated media will then be more readily condensed out during a second round of compression/condensation owing to the increased concentration of the contaminated vapor, where it would have originally escaped due to the fact that the concentration of contaminated vapor dropped below a critical point where no additional contaminated vapor of a given chemical could be condensed out of the gas. The compression/condensation-adsorption cycle is repeated until the measured volumetric concentration output of contaminant being removed shows the remediation site is substantially clean. 
   Referring now also to  FIG. 1 , scrubbers  520   a ,  520   b ,  520   c  may be introduced into SVE system  200  to remove contaminated vapor that escapes regenerative adsorption module  450 . Scrubbers  520   a ,  520   b ,  520   c  may be conventional GAC traps. As shown in  FIG. 1 , scrubbers  520   a ,  520   b ,  520   c  may occur in series to achieve a desired gas concentration of contaminant. Scrubbers  520   a ,  520   b ,  520   c  are connected to vapor elimination module  400  via clean exhaust conduit  472 . The specific acceptable final concentration of each contaminant will be known to a person of ordinary skill in the art and defined by applicable environmental statute. According to embodiments wherein GAC is used as the scrubbing media, scrubbers  520   a ,  520   b ,  520   c  will periodically need to have GAC replaced once it becomes fully charged with contaminant. After gas is scrubbed to the desired contaminant concentration, gas is discharged to the ambient air via discharge conduit  530 . 
   According to an embodiment of a method for vapor extraction shown in  FIG. 5 , vapor is extracted from the soil of a remediation site  1010 . These vapors, as previously discussed contain vapors contaminated with pollutant. After extraction, the off gas is compressed  1020  as previously described. Thereafter, the compressed gas is cooled in a condensation process  1030 , which causes much of the contaminated vapors to condense into a liquid form that may be captured. 
   Residual contaminated vapors not captured by the compression and condensation process are routed to a regenerative adsorber  1040 . Once gas is treated in regenerative adsorber step, it is substantially clean. It is exposed to scrubbing with activated carbon  1060  to ensure the final exhaust is virtually clean. Prior to scrubbing, a portion of the substantially clean gas is routed through the regenerative adsorber at low pressure. The regenerative adsorber collects and then releases contaminated vapor as a concentrated vapor  1050  which is routed to the compression step  1020 . 
   Likewise disclosed is a method for optimizing the use of the systems of the present disclosures. The optimization method ensures efficient flow. Initially, plans are generated to do this based on ostensive containments to be addressed. These plans may be directed towards general remediation of a site, to specific contaminants, or according to the directive of a regulatory authority, such as the United States Environmental Protection Agency. Generally, the plan will include use of a remediation system, such as the SVE system disclosed herein. Depending on the particular contaminants to be addressed, optimizations of the remediation will address the particular parameters of the remediation system. 
   For example, a remediation site may be contaminated with difficult to remove contaminants such as chloromethane or freon that will be removed by compression and condensation inefficiently. In these types of cases, for example, airflow, cycle time, or both may be reduced to optimize performance of the remediation system. In other embodiments, airflow may be increased when compression and condensation is efficient. Additionally, the freeze and thaw cycles of the compression and condensation modules may be varied and optimized based on the plan. Similarly, decisions may be made to use systems with multiple compression and condensation modules and regenerative adsorber modules in series or in parallel, depending on embodiments. Similarly, the adsorption and desorption may be cycled to adjust the system to site conditions, as necessary and according to embodiments. 
   According to an embodiment of a method for addressing soil remediation as shown in  FIG. 6 , the site is first tested and the contaminants for a particular site identified  1100 . After determination of the types, concentrations, and relevant data regarding the contaminants, a remediation plan is developed  1110 . The remediation plan details flow rates, locations for extraction of contaminated vapor, and other similar considerations that would be useful in formation of the remediation plan. Artisans will understand the relevant considerations in the formation of the remediation plan. 
   Prior to, during or after formation of the remediation plan, the plan may be optimized  1120 , according, to embodiments. The optimization process generally comprises the cross-referencing of the contaminants to be removed with a database of parameters for removal of known contaminants. The database may be computerized or be another collection of data regarding the parameters in which contaminants may be extracted using a particular remediation technology. As contaminants will have varying extraction and chemical properties, a specific set of operating parameters for a remediation system may efficiently address a subset of contaminants while inefficiently addressing others. Optimization of the remediation plan will address the varying properties of the contaminants to create an efficient removal process that addresses all of the contaminants present without the undue waste in energy expenditure and resources associated with brute force and less efficient techniques. 
   After formation of an optimized remediation plan, the plan is executed  1130 . After and during execution of the plan, the nature and quantities of the contaminants removed may be evaluated  1140 , resulting in a set of data. This set of data then may be used to satisfy regulatory requirements imposed by a regulatory body  1150 , according to embodiments. Moreover these data may be used to evaluate the remediation plan and the progress in overall remediation of the site. 
   Once the contaminants are known, the preliminary plan may be optimized using a database of recovery parameters as provided by an entity commissioning the site remediation or a regulatory authority. As these parameters tend to vary by the remediation site or over time (e.g., state and Federal environment regulations), optimization remains current, and the execution of the plan occurs such that the applicable parameters are met or exceeded. 
   Execution occurs as would be known and understood by a person of ordinary skill in the art. For example, if the SVE system of the present disclosure is used, the process occurs as described herein according to the plan and in accordance with the optimization rules. 
   After or during execution of the plan, the exact nature and quantities of the species recovered and remaining may be measured as a metric for determination of the successful execution of the plan. Moreover, the quality of the exhaust released from the remediation system into the environment may be monitored and measured. These data may then be examined for compliance with the regulations imposed by the regulatory authority. Examples of regulatory authority may be environmental groups, government entities such as legislatures and enforcement agencies (e.g., EPA), and other groups maintaining standards for environmental remediation. 
   According to embodiments, recovered contaminants may be separated and reused. Recycling of pure or substantially pure contaminants reduces the need to produce the contaminants for use in other useful applications, which further reduces environmental impact by reducing waste associated with the production of the contaminants. Contaminants may be separated and reused as part of a remediation process, such as by installing a specific gravity separator as previously described, or in an after remediation process as would be known and understood by artisans. 
   Example 1 
   A site was selected for remediation in southern California, wherein the system optimization was conducted to maximize the efficiency of the soil vapor extraction (SVE) system and expedite site cleanup. The SVE system primarily targeted volatile organic compound (VOC)-impacted soils beneath a former refrigerant plant and the immediate surrounding areas. The results that follow detail the monitoring of well cycling and a description of treatment system performance over a 6-month period. 
   Pilot testing of the remedial system was initiated 3 years earlier. Full-scale operation began a year prior to the monitoring reported in Example 1. Routine system monitoring was conducted to maximize contaminant removal while complying with South Coast Air Quality Management District (SCAQMD) regulations and permits. 
   The site was constructed in 1919 to produce sulfuric acid and process spent sulfuric acid generated at an oil refinery, located west of the site. Since that time, chemical manufacturing operations included the following activities: sulfuric acid production from 1920 to 1972, phthalic anhydride manufacturing from 1963 to 1982 (the phthalic anhydride plant was demolished in 1996); and production of refrigerants from 1964 to 2003. 
   Refrigerants were initially produced in 1964, including chlorofluorocarbons (CFCs) and hydrochlorofluorocarbons (HCFCs) such as trichlorofluoromethane (R-11), dichlorodifluoromethane (R-12), chlorodifluoromethane (R-22), and 1,1-dichloro-1-fluoroethane (R-141b). Raw materials for CFC/HCFC production included hydrofluoric acid, carbon tetrachloride, chloroform, 1,1,1-trichloroethane (1,1,1-TCA), and antimony pentachloride catalyst. 
   Several blends of the refrigerant 1,1,2-trichlorotrifluorethane (R-113) with organics (used primarily in the electronics industry) were packaged at the site from the early 1980s through January 2003. Additional organic compounds including methyl alcohol, ethyl alcohol, cyclopentane, hexane, methylene chloride, isopropanol, and acetone were used in the different blends. Refrigerant blending and production ceased on Jan. 31, 2003. The site user implemented corrective action in the vicinity of the refrigerant plant to remove VOCs in the zone of greatest impact and to minimize future impacts to groundwater. 
   Various interruptions to the SVE system operation during the monitoring period occurred for demolition activities over the 6-month monitoring period. The system was shut down at one point to meet the ongoing construction health and safety requirements. 
   Previous investigations documented the presence of VOCs in soil, soil gas, and groundwater beneath the site. The highest concentrations of VOCs, including CFCs and HCFCs, were located beneath the refrigerant plant. 
   SVE was selected as the preferred remedial measure after evaluating several different methods and technologies. SVE is a treatment process that is proven effective in remediating coarse-grained soils impacted with VOCs. Physical site constraints, such as the depth of impacted soils and site operations, were also considered in the selection of an appropriate technology. 
   The SVE system included a network of 12 vapor extraction wells (VEW) screened in multiple depth intervals. The system presented in the present disclosure was used to extract VOCs from the remediation site. 
   During initial pilot testing of the system, vapors were extracted from only one well and the condensed fluids were collected in half-ton pressure cylinders. A Department of Transportation (DOT) 2.2 classification, 50,000-pound capacity iso-tanker was delivered to the site and connected to the treatment system. This tank provided additional capacity to allow full-scale SVE operation. The SVE system was expanded to extract from multiple wells and from wells with higher contaminant concentrations. 
   The SVE system operated under a SCAQMD permit. This site-specific permit was issued with the following conditions addressing air emissions at the outlet of the scrubbers:
         VOC concentrations shall not exceed 3 parts per million by volume (ppmv).   Carbon tetrachloride shall not exceed 1.8 ppmv.   Chloroform shall not exceed 0.9 ppmv.   Whenever the VOC concentration reaches 3 ppmv (as hexane), the carbon in the scrubbers shall be replaced with fresh adsorbent.       

   To ensure compliance with the SCAQMD permit, the system effluent was monitored by organic vapor sensors that were connected to the main system controls. The sensors automatically shut the system down if the effluent concentration exceeded the SCAQMD permit limit. 
   The initial phase SVE system installation included the installation of the condensation process equipment and piping to an existing well. Based on the radius of influence (ROI) data, it was determined that 12 wells were sufficient to accomplish the remediation goals. 
   During the monitoring period, the inventor periodically visited the site to conduct system maintenance operations, including adding oil to compressors, emptying drums, changing cylinders, and replacing filters, tubing, gaskets, carbon, and valves. 
   The delivery of a 50,000-pound capacity iso-tanker to the site immediately prior to the monitoring period provided greater operational flexibility and expanded product storage capacity. The full-scale operation strategy involves the cycling of 12 extraction wells to maximize the system influent concentrations. 
   The objective was to reduce extraction well concentration to less than 2000 ppmv. The outer wells were cycled periodically since demolition activities prevented use of other wells.  FIG. 7  illustrates the system influent VOC concentrations for the remediation site. As indicated, the peaks are indicative of new wells being opened and added to the SEV system. As of the end of the reporting period, all system wells appeared to be near or below 2000 ppmv. 
   VOC mass removal during the monitoring period is shown in  FIG. 8 . Measurements of product removed since the system operations began are listed in Table 5. The mass total does not include dissolved VOCs removed in the condensed aqueous waste stream or vapor-phase VOCs adsorbed to carbon, which are considered negligible in comparison to the pure-phase product removed. The total mass recovered was calculated by weighing the iso-tank before and after each replacement. The combined mass of solvents recovered during the monitoring period was 7,960 pounds. Over the course of the whole experiment, 110,202 pounds of VOCs were removed, as shown in  FIG. 8 . 
   While the apparatus and method have been described in terms of what are presently considered to be the most practical and preferred embodiments, it is to be understood that the disclosure need not be limited to the disclosed embodiments. It is intended to cover various modifications and similar arrangements included within the spirit and scope of the claims, the scope of which should be accorded the broadest interpretation so as to encompass all such modifications and similar structures. The present disclosure includes any and all embodiments of the following claims.