Abstract:
An energy-efficient continuous process (and apparatus) that eliminates or reduces the emission of BTX into the environment during a process of dewatering natural gas using glycol. The apparatus includes an absorption tower to dewater the natural gas, and a glycol dewatering unit that includes a reboiler and a distillation column. Overhead vapor, including steam and BTX vapor, from the distillation column is condensed in an air-cooled heat exchanger. The liquefied BTX may be separated for fuel, sale or other disposal. A fan is positioned to force or induce air to flow through the air-cooled heat exchanger. The fan may be driven by a hydraulic motor by pressure of a glycol process stream. In another embodiment, the overhead vapors from the distillation column are cooled against a stream of water-containing glycol being charged to the glycol dewatering unit thereby preheating this stream and reducing energy input to the reboiler.

Description:
BACKGROUND 
       [0001]    1. Field of the Invention 
         [0002]    The inventions relate to the de-watering of natural gas, and more particularly, relate to enhancements that improve the energy efficiency of the de-watering apparatus and processes while also reducing or eliminating the release of benzenes, toluenes and xylenes (“BTX”) into the environment. 
         [0003]    2. Description of the Related Art 
         [0004]    It is conventional in natural gas production to remove water from the gas. This water naturally occurs and is produced with the gas, in the continuous gas production stream. Removal of the water prevents or minimizes corrosion in the gas transportation pipelines and associated equipment, and avoids issues that could arise if temperatures were to drop below freezing point causing the water to convert to ice. In addition, certain “aromatic” hydrocarbon chemicals, such as benzenes (including ethyl-benzene), toluene and xylene, may also be present in the natural gas. These aromatics, generally known as “BTX” or “BETX” in the industry, have been identified as potentially hazardous to human health and release of these into the environment must be avoided. 
         [0005]    Equipment is often located at the natural gas production site to de-water the gas. Briefly, in general, the continuous gas de-watering process has equipment that includes an absorption tower where the produced natural gas is contacted with a moisture-absorbing chemical liquid, like ethylene glycol (hereinafter referred to as “glycol”) to absorb moisture from the gas. The glycol is re-constituted by flashing off the absorbed water as steam in a flash separator that operates in combination with a reboiler, which uses on-site produced natural gas as heating fuel. The reconstituted glycol exiting the reboiler, having most of the absorbed water removed, can then be recycled to the absorption tower for re-use in moisture absorption. 
         [0006]    An exemplary and illustrative process flow diagram of the de-watering equipment is shown in  FIG. 1 . In the process illustrated, the raw natural gas in line  12  is treated and exits the process as de-watered natural gas in stream  19 . The water removed from the natural gas is sent to safe disposal, and any BTX removed may be recovered for use as fuel in the process. In more detail, the raw natural gas in line  12  enters near the base of an absorption tower  20 , while glycol in line  14 , having been preheated in glycol preheater  22 , enters at the top of the absorption tower  20 . In the absorption tower  20  there is counter-current contact between the incoming raw natural gas and the glycol. This contact allows the glycol to strip water (and some BTX) out of the raw natural gas to produce a dried natural gas that exits from the top of tower  20  in line  18 . The gas in line  18  is relatively cooler than incoming glycol, and heat is transferred to the gas from the glycol (in line  14 ) in glycol cooler  22 . Thus, cooled glycol exits the glycol cooler  22  in line  15  and is routed to the top of absorption tower  20 , while natural gas, having been dewatered and warmed, exits the glycol cooler  22  in line  19  for routing to storage, transportation, and/or sale. 
         [0007]    On the “glycol-handling” side of the process, the water-containing glycol exiting the absorption tower  20  is dewatered and put in condition for recycling to the absorption tower  20 . Upon exiting from near the base of absorption tower  20  in line  16 , the water-containing glycol which is under pressure, drives a hydraulic motor  32 , which in turn drives the glycol transfer pump  34  that pumps the glycol to the absorption tower  20 . The water-containing glycol exits the hydraulic motor  32  in line  17 , and enters the glycol preheat exchanger  40 . In the glycol preheat exchanger  40 , the water-containing glycol is heated by taking heat from hot glycol in line  58 , that has been heated in the reboiler  54 , as explained later. The heated water-containing glycol exits the glycol preheat exchanger  40  in line  18  and is charged to a flash separator  45 . Here, BTX entrained in the glycol flashes off as vapor in line  46 , and can be routed for use as fuel in the process, and any excess may be vented to atmosphere. The liquid fraction exiting the flash separator  45  is charged to a glycol de-watering combination apparatus  50  that includes a reboiler  54  and a distillation column  52 . The combination apparatus separates the glycol from the water it absorbed in absorption tower  20  from the raw natural gas. Thus, de-watered glycol exits in line  58  from the base of the reboiler  54 , which is heated by natural gas, and water in the form of steam exits in line  56  from the top of the distillation column  52 . The steam and any BTX vapor in line  56  enters an overheads condenser  60 , in the form of a water-cooled heat exchanger, and loses heat and latent heat to the water entering the condenser  60  via line  64 . The condenser has vent that allows the release of non-condensable gasses and BTX via line  62  into the atmosphere. The condensed water and liquefied BTX from the overheads condenser  60  in line  66  enters an overheads drum  70  that has a vent  72  for releasing non-condensable gasses and BTX vapor to the atmosphere, and an exit line  74  to divert the condensate water that includes liquefied BTX for disposal. 
         [0008]    The above-described process and apparatus is typical of existing natural gas de-watering systems, albeit that some may depart from the system in some features. The apparatus is not designed to, and does not, significantly contain the release of BTX into the environment. 
       SUMMARY 
       [0009]    In an exemplary embodiment there is presented a continuous process apparatus for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment. The process apparatus includes an absorption tower configured for continuous counter-current contacting therein of upward flowing natural gas containing water with downward flowing glycol to dewater the natural gas. The absorption tower has an exit stream of water-containing glycol that includes benzenes, toluenes, and xylenes. The apparatus also includes a glycol dewatering unit comprising a reboiler and a distillation column. The glycol dewatering unit is configured for continuously receiving from the absorption tower, via a conduit, a continuous stream of glycol containing water and benzenes, toluenes, and xylenes. The glycol dewatering is configured to remove water from glycol to produce a first stream, in a first conduit, exiting from the reboiler containing glycol that has a reduced water content, and a second stream, in a second conduit, exiting from a top of the distillation column, that comprises overhead vapor that includes steam, benzenes, toluenes, and xylenes. A condenser, in continuous fluid communication with the second conduit, receives the overhead vapor from the distillation column. The condenser includes an air-cooled heat exchanger sized and configured to condense the received overhead vapor including the steam, benzenes, toluenes, and xylenes to form a condensate. A fan is located relative to the air-cooled heat exchanger to force or induce air to flow through the air-cooled heat exchanger. The fan may be driven by a hydraulic motor that is driven by glycol exiting from the absorption tower. The apparatus includes a condensate-receiving overheads drum in continuous fluid communication with the air-cooled heat exchanger to receive and contain the condensate from that includes liquefied benzenes toluenes and xylenes. As a consequence in the apparatus, under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0010]    Optionally, the exemplary embodiment includes a hydraulic glycol transfer pump. The pump may be driven by a second hydraulic motor driven by glycol exiting from the absorption tower. The second hydraulic motor may be upstream or downstream of the hydraulic motor driving the fan. 
         [0011]    Optionally, the process apparatus includes a control valve that controls a portion of the glycol exiting from the base region of the absorption tower to communicate via a conduit to the hydraulic motor of the fan of the air-cooled heat exchanger. 
         [0012]    Optionally, the process apparatus includes a temperature-sensor controller that controls the portion of the glycol exiting from the base region of the absorption tower to communicate via a conduit to drive the hydraulic motor of the fan to achieve condensation of the benzenes, toluenes, and xylenes included in the overhead vapor. 
         [0013]    In another exemplary embodiment, there is provided a continuous process apparatus for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment. The process apparatus includes an absorption tower configured for continuous counter-current contacting therein of upward flowing natural gas containing water with downward flowing glycol to dewater the natural gas. The absorption tower has an exit stream comprising water-containing glycol and entrained benzenes, toluenes, and xylenes. The apparatus also includes a glycol dewatering unit comprising a reboiler and a distillation column. The unit is configured for continuously receiving water-containing glycol from the absorption tower and is configured to remove water from glycol to produce a first stream, in a first conduit, exiting from the reboiler containing glycol that has a reduced water content, and a second stream, in a second conduit, exiting from a top of the distillation column that comprises overhead vapor, where the overhead vapor includes steam, benzenes, toluenes, and xylenes. In addition, the apparatus includes a condenser in continuous fluid communication with the second conduit to receive the overhead vapor from the distillation column. The condenser includes a heat exchanger in fluid communication with a conduit carrying water-containing glycol that exited from the base of the absorption column. The heat exchanger is sized and configured to utilize the water-containing glycol that exited from the absorption column as a cooling and condensing medium to condense the overhead vapor from the distillation column to form a condensate that includes water, and liquefied benzenes, toluenes, and xylenes. The apparatus further includes an overheads drum in continuous fluid communication via a condensate conduit with the condenser to receive and contain the condensate. The condensate can be separated into water and benzenes, toluenes, and xylenes. The benzenes, toluenes, and xylenes can be used as fuel or can be sold. As a consequence in the apparatus, under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0014]    Optionally, the process apparatus of includes a hydraulic glycol transfer pump driven by a hydraulic motor. The hydraulic motor may be driven by glycol exiting from the absorption tower. The hydraulic motor may be upstream or downstream of a conduit carrying glycol exiting from the absorption tower to the condenser. 
         [0015]    An exemplary continuous process for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment, includes the following steps. The step of continuous counter-current contacting of upward flowing natural gas containing water with downward flowing glycol to: (a) dewater the natural gas by absorbing the water in the glycol, and (b) remove benzenes, toluenes, and xylenes from the natural gas, to produce a water-rich glycol stream containing benzenes, toluenes, and xylenes, and a substantially water-free natural gas stream. In addition, the step of continuously stripping water from the water-rich glycol stream containing benzenes, toluenes, and xylenes to produce a first stream comprising glycol stripped of water, and a second stream, in vapor form, comprising steam and vapors of benzenes, toluenes, and xylenes. Further, the step of continuously condensing the vapor of the second stream to produce a liquid condensate of water and liquefied benzenes, toluenes, and xylenes. Whereby, during the continuous process, release of vapors of benzenes, toluenes, and xylenes into the environment is reduced or eliminated, and whereby a reduced energy input is required for the continuous process. As a consequence in the process, under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0016]    Optionally, the continuous process includes a step of continuously flowing the vapor through an air cooled heat exchanger and inducing or forcing ambient air through the heat exchanger with a fan driven by a hydraulic motor. 
         [0017]    Optionally, the continuous process includes operatively driving the hydraulic motor with a portion of the water-rich glycol stream from the step of counter-current contacting. 
         [0018]    Optionally, the continuous process includes sensing a temperature of ambient air, and using the sensed temperature to control the portion of the water-rich glycol stream from the step of counter-current contacting. 
         [0019]    Optionally, the continuous process includes continuously flowing the vapor through a condenser comprising a heat exchanger, wherein the heat exchanger is in fluid communication with a conduit carrying water-rich glycol from the step of counter-current contacting, and using the water-rich glycol as a cooling and condensing medium in the heat exchanger to condense the vapor of the second stream to form the condensate. 
         [0020]    Optionally, the continuous process includes sensing a temperature of ambient air, and using the sensed temperature to control the portion of the water-rich glycol stream from the step of counter-current contacting. 
     
    
     
       BRIEF DESCRIPTION OF THE DRAWINGS 
         [0021]    The foregoing aspects and many of the attendant advantages, of the present technology will become more readily appreciated by reference to the following Detailed Description, when taken in conjunction with the accompanying simplified drawings of exemplary embodiments. The drawings, briefly described here below, are not to scale, are presented for ease of explanation and do not limit the scope of the inventions recited in the accompanying patent claims. 
           [0022]      FIG. 1  is a process flow diagram depicting the major process equipment in a prior art system. 
           [0023]      FIG. 2  is a process flow diagram illustrating an example of an embodiment of the continuous process for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment. 
           [0024]      FIG. 3  is a process flow diagram illustrating another example of an embodiment of the continuous process for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment 
       
    
    
     DETAILED DESCRIPTION OF EXEMPLARY EMBODIMENTS 
       [0025]    The following non-limiting detailed descriptions of examples of embodiments of the invention may refer to appended Figures and are not limited to the drawings, which are merely presented for enhancing explanations of features of the technology. In addition, the detailed descriptions may refer to particular terms of art, some of which are defined herein, as appropriate and necessary for clarity. 
         [0026]    The term “raw natural gas” refers to produced natural gas that includes water, whether as entrained minute droplets or as water vapor, that must be removed. The gas may also contain BTX. 
         [0027]    The term BTX or BETX refers to “benzenes, toluenes, and xylenes” that are produced along with natural gas from subterranean formations. 
         [0028]    The term “reduction or elimination of benzenes, toluenes, and xylenes” means that the process and apparatus are designed to contain or combust the benzenes, toluenes, and xylenes from natural gas such that the benzenes, toluenes, and xylenes emitted into the atmosphere, under normal operating conditions, is zero or that 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment. 
         [0029]    Exemplary embodiments of a continuous process apparatus for removing water from raw natural gas and reducing or eliminating the release of BTX into the environment include energy conservation features as well. Accordingly, as compared to the prior art of  FIG. 1 , the exemplary embodiments of the inventive technology have significant advantages in both the environmental protection and the energy conservation areas. Moreover, existing equipment may be retrofitted to include the inventive technologies. 
         [0030]    In an exemplary embodiment illustrated in  FIG. 2 , as explained in more detail here below, the energy of a high pressure process stream is used to drive a hydraulic motor that powers a fan. The fan is used as a forced air or induced air fan to push or drag ambient air through a condenser for a stream of vapor that includes steam and BTX, to both cool and completely condense the vapor. By “completely condense,” we understand that there will be some vapor in equilibrium with the condensate, when the condensate is charged to a condensate holding container, and the relative concentrations of each of the components of the equilibrium vapor will be in chemically-related proportion to the concentration of the component in the condensate. Condensation of the BTX vapor along with the water-condensate reduces or eliminates release of the BTX into the environment; the water and liquefied BTX being immiscible can be separated as aqueous and hydrocarbon phases, and the separated BTX can either be sent to storage for subsequent sale, or used as combustion fuel in the natural gas treatment process. Moreover, by using a hydraulic-powered fan and an air cooled heat exchanger, the exemplary embodiment reduces energy consumption by not requiring electricity, which must be generated on site in remote locations. In addition, by eliminating the water cooler condenser  60  of the prior art, there are savings in terms of chemicals for water treatment, and running costs of the water treatment system and pump(s). Accordingly, the system has reduced costs of energy, equipment and chemicals, and is more environmentally friendly in that it reduces or eliminates BTX emissions. 
         [0031]    In the process illustrated in  FIG. 2 , the raw natural gas in line  212  is treated and compressed to exit the process as de-watered, compressed natural gas in stream  226 . The water removed from the natural gas is sent to safe disposal. Any BTX removed from the raw natural gas is recovered and may be used as fuel in the process, or may be sold. In more detail, the raw natural gas in line  212  enters near the base of an absorption tower  200 , while glycol in line  214 , having been cooled in glycol cooler  222  against exiting (dried) natural gas in line  218 , enters at the top of the absorption tower  200 . In the absorption tower  200  there is counter-current contact between the incoming raw natural gas and the glycol. This contact allows the glycol to strip water out of the raw natural gas to produce a dry natural gas that exits from the top of tower  200  in line  218 . The glycol also picks up BTX from the natural gas. The dried gas in line  218  is relatively cooler, and heat is transferred to the gas from the incoming (warmer) glycol (in line  214 ) in glycol cooler  222 . Thus, cooled glycol exits the glycol cooler  222  in line  215  and is routed to the top of absorption tower  200 , while dried natural gas exits the glycol cooler  222  in line  219  for routing to storage, transportation, and/or sale. 
         [0032]    On the “glycol-handling and BTX-removal” side of the process apparatus, the glycol is dewatered and put in condition for recycling to the absorption tower  200 . Upon exiting from near the base of absorption tower  200  in line  216 , the glycol, which is under pressure, drives a hydraulic motor  232 , which in turn drives the glycol transfer pump  234  that pumps the glycol to the absorption tower  200 . The glycol exits the hydraulic motor  232  in line  217 , and is routed under control of a control valve  282  either to a glycol preheat exchanger  240 , or to the hydraulic drive motor  284  of a fan  286  of an air-cooled heat exchanger  288 . The air-cooled heat exchanger  288  is a condenser for distillate vapors from the top of distillation column  252 , in line  256 . In some circumstances, such as in winter, when ambient temperature conditions are cold, such that condensation can take place in the air cooled heat exchanger without need for the hydraulic fan to operate, the fan is not operated. Thus, a temperature sensor-controller  283  senses the temperature of the condensate and controls the control valve  282  to direct an appropriate amount of glycol to drive the fan motor  284  to ensure complete condensation. The condensate is routed via conduit  271  to the condensate collection drum  270 , which contains both the condensed steam (water) as well as condensed (liquid) BTX. The liquid BTX may be separated from the water and routed to sales or for use as fuel in the process. BTX being immiscible with water, the separation of the lighter BTX phase floating on the water phase is relatively straightforward. For safety, the condensate drum  270  is equipped with a vent system  272  that might vent any BTX vapor to a flare system (not shown). Thus, in normal continuous operations, no BTX escapes into the environment from the overheads system of the distillation column  252 . Liquid water may be drained from the drum  370  from conduit  374  for disposal. The glycol exiting the fan drive motor  284  in conduit  217  is routed to the glycol preheat exchanger  240 . In the glycol preheat exchanger  240 , the glycol is heated by taking heat from hot (de-watered for recycling) glycol in line  258 , that has been heated in the reboiler  254 , as explained later. The heated glycol exits the glycol preheat exchanger  240  in line  218  and is charged to a flash separator  245 . Here, BTX entrained in the heated glycol flashes off as vapor in line  246 , and can be routed for use as fuel in the process, for example as heating fuel for the reboiler, or to a flare system. The liquid fraction exiting the flash separator  245  is charged to a glycol de-watering combination apparatus  250  that includes a reboiler  254  and a distillation column  252 . The combination apparatus  250  separates the glycol from the water it absorbed in absorption tower  220  from the raw natural gas. Thus, de-watered glycol exits in line  258  from the base of the reboiler  254 , which is heated by natural gas. The water removed water from the glycol, now in the form of steam, exits in line  256  from the top of the distillation column  252  along with residual volatiles, such as BTX vapor. The steam and BTX vapor in line  256  enters an overheads condenser  288 , as described above. The condensate enters an overheads drum  270  that has a vent  272  for releasing non-condensable gasses and BTX to flare. The liquefied BTX can be separated from liquid water (condensate) in drum  270  and routed for sale or for use as fuel in the process. Thus, the system reduces or effectively eliminates emissions of BTX to the environment, and by using the pressure of the glycol as the energy to drive the fan motor, the system also conserves energy. 
         [0033]    In the exemplary embodiment illustrated in  FIG. 3 , as explained in more detail here below, the energy of a high pressure water-rich glycol process stream is used to cool and condense a vapor stream from a distillation column that includes steam and BTX to produce complete condensation of the vapor stream to water and liquefied BTX, that may be sold or used as fuel in the process. This system eliminates the need for a water-cooled condenser, along with its costs for water treatment chemicals and pumping. Further, by transferring heat and latent heat of condensation of the vapor stream into the water-rich glycol process stream, this stream is heated up. As a consequence less energy must be added to the reboiler to heat up this stream when it enters the reboiler. Therefore, less fuel must be used to heat the reboiler. Accordingly, the system has reduced costs of energy, equipment and chemicals, reduces or eliminates BTX emissions, and is more environmentally friendly. Indeed, under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0034]    Referring to  FIG. 3 , the raw natural gas in line  312  is treated in a counter-current de-watering absorption process with glycol and then compressed to exit the process as de-watered, compressed natural gas in stream  326 . The water removed from the natural gas, and any BTX removed, is directed to further processing for glycol recovery for recycle, and BTX removal. In more detail, the raw natural gas in line  312  enters near the base of an absorption tower  300 , while glycol in line  314 , having been cooled in glycol cooler  322 , enters at the top of the absorption tower  300 . In the absorption tower  300  there is counter-current contact between the incoming raw natural gas and the glycol. This contact allows the glycol to strip water out of the raw natural gas to produce a dry natural gas that exits from the top of tower  300  in line  318 . The gas in line  318  is relatively cool, and can take up heat from the incoming (warmer) glycol (in line  314 ) to cool the glycol, in the glycol cooler  322 . Thus, cooled glycol exits the glycol cooler  322  in line  315  and is routed to and enters the top of absorption tower  300 , while warmed, de-watered natural gas exits the glycol cooler  322  in line  319  for routing to storage, transportation, and/or sale. 
         [0035]    On the “glycol-handling and BTX-removal” side of the process apparatus, the glycol is dewatered and put in condition for recycling to the absorption tower  300 . Upon exiting from near the base of absorption tower  300  in line  316 , the glycol which is under pressure, drives a hydraulic motor  332  which in turn drives the glycol transfer pump  334  that pumps the glycol to the absorption tower  300 . The glycol exits the hydraulic motor  332  in line  317 , and is routed to a counter-current heat exchanger condenser  390  to condense vapor exiting the top of distillation column  352 . The condensate which includes condensed steam and volatile hydrocarbons, such as BTX, is routed via conduit  371  to the condensate collection drum  370 . Drum  370  contains both the condensed steam (water) as well as condensed (liquid) BTX. Liquid BTX can be separated from the water condensate because of the immiscibility of BTX in water. The separated BTX may be sold or used as fuel in the process. For safety, the condensate drum  370  is equipped with a vent system  372  that might vent any BTX vapors to a flare system (not shown). Thus, no BTX escapes into the environment from the overheads system of the distillation column  352 . Liquid water may be drained from the drum  370  from conduit  374  for disposal. The heated glycol exits the condenser  390  in conduit  317  and is routed to the glycol preheat exchanger  340 . The further heated glycol exits the glycol preheat exchanger  340  in line  318  and is charged to a flash separator  345 . Here, some BTX entrained in the heated glycol flashes off as vapor in line  346 , and can be routed for use as fuel in the process, for example as heating fuel for the reboiler, or to a flare system. The liquid fraction exiting the flash separator  245  in line  348  is charged to a glycol de-watering combination apparatus  350  that includes a reboiler  354  and a distillation column  352 . The combination apparatus separates the glycol from the water it absorbed in absorption tower  320  from the raw natural gas. It uses less energy than in the prior art because whereas in the prior art apparatus heat in the condensate is removed into water in a water-cooled condenser  60 , in the exemplary embodiment the heat of condensation on cooling is recovered in the condenser  390  into the glycol being charged to the reboiler-distillation column combination  350  in conduit  318 . Thus, the glycol in conduit  318  is hotter and less fuel needs to be added to reboiler  354  to effect de-watering. De-watered glycol exits the reboiler-distillation column combination  350  in line  358  from the base of the reboiler  354 , and the removed water, in the form of steam, exits in line  356  from the top of the distillation column  352  along with volatiles, such as BTX. The steam and BTX in line  356  enters an overheads condenser  390 , as described above. The condensate enters an overheads drum  370  that has a vent  372  for releasing non-condensable gasses and BTX to flare. Thus, the system reduces or effectively eliminates emissions of BTX to the environment, and by recovering the heat otherwise lost from condensate cooling and condensing, it requires less fuel to the reboiler, thereby conserving energy. Under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0036]    In an exemplary process for dewatering natural gas and reducing or eliminating release of benzenes, toluenes and xylenes into the environment, several steps may be included. These steps include: 
         [0037]    continuous counter-current contacting of upward flowing natural gas containing water with downward flowing glycol to: 
         [0038]    (a) dewater the natural gas by absorbing the water in the glycol, and 
         [0039]    (b) remove benzenes, toluenes, and xylenes from the natural gas, to produce a water-rich glycol stream containing benzenes, toluenes, and xylenes, and a substantially water-free natural gas stream; 
         [0040]    continuously stripping water from the water-rich glycol stream containing benzenes, toluenes, and xylenes to produce a first stream comprising glycol stripped of water, and a second stream, in vapor form, comprising steam and vapors of benzenes, toluenes, and xylenes; and 
         [0041]    continuously condensing the vapor of the second stream to produce a liquid condensate comprising water, and liquefied benzenes, toluenes, and xylenes 
         [0042]    whereby, during the process, under normal operating conditions, 95% to 99.9% of benzenes, toluenes, and xylenes separated from the natural gas are contained from the environment and are either used as fuel or processed for sale. 
         [0043]    While examples of embodiments of the technology have been presented and described in text and some examples also by way of illustration, it will be appreciated that various changes and modifications may be made in the described technology without departing from the scope of the inventions, which are set forth in and only limited by the scope of the appended patent claims, as properly interpreted and construed.