Patent Publication Number: US-6984257-B2

Title: Natural gas dehydrator and system

Description:
CROSS-REFERENCE TO RELATED APPLICATIONS 
     This application is a continuation-in-part application of U.S. patent application Ser. No. 10/071,721, entitled “Apparatus for Use with a Natural Gas Dehydrator”, to Heath, filed on Feb. 8, 2002 now U.S. Pat. No. 6,551,379, and the specification thereof is incorporated herein by reference. This application is also related to U.S. Pat. No. 5,766,313, entitled “Hydrocarbon Recovery System,” to Heath; U.S. Pat. No. 6,238,461, entitled “Natural Gas Dehydrator,” to Heath; and U.S. Pat. No. 6,364,933, entitled “Apparatus for Use with a Natural Gas Dehydrator,” to Heath; and the specifications thereof are incorporated herein by reference. 
     This application claims the benefit of the filing of U.S. Provisional Patent Application Ser. No. 60/377,259, entitled “Apparatus for Use With Natural Gas Dehydrator”, filed on Apr. 30, 2002, and the specification thereof is incorporated herein by reference. 
    
    
     BACKGROUND OF THE INVENTION 
     1. Field of the Invention (Technical Field) 
     The present invention relates generally to an apparatus and system for use with natural gas dehydrators of the type used to remove water and water vapor from a natural gas stream having a mixture of natural gas, liquid hydrocarbons, liquid hydrocarbon vapors, water and water vapors. The invention is particularly directed for use in the regulation of the glycol and the processing of all combustible gases with natural gas dehydrators. 
     2. Description of Related Art 
     Note that the following discussion refers to a number of publications by author(s) and year of publication, and that due to recent publication dates certain publications are not to be considered as prior art vis-a-vis the present invention. Discussion of such publications herein is given for more complete background and is not to be construed as an admission that such publications are prior art for patentability determination purposes. 
     An example of natural gas dehydrators is disclosed in U.S. Pat. No. 6,238,461 issued May 29, 2001 and U.S. Pat. No. 6,364,933 issued Apr. 2, 2002 to Heath and the disclosures therein are specifically incorporated herein by reference. In general, such systems comprise a separator for receiving oil and water liquids from “wet” (water vapor laden) gas; and a water absorber, which employs a liquid dehydrating agent such as glycol, for removing the water vapor from the wet gas and producing “dry” gas suitable for commercial usage. The glycol is continuously supplied by a pump to the absorber in a “dry” low-water vapor-pressure condition and is removed from the absorber in a “wet” high-water vapor-pressure condition. The wet glycol is continuously removed from the absorber and circulated through a reboiler, which includes a still column for removing the absorbed water from the glycol and heating the glycol to provide a new supply of hot dry glycol. Heating of the glycol in the reboiler is generally accomplished through use of a gas burner mounted in a fire tube. The hot dry glycol from the reboiler passes through a heat exchanger, where the hot dry glycol transfers some of its heat to incoming wet glycol going to the still column. The dry glycol subsequently passes to a dry glycol storage tank. A glycol passage is provided to enable passage of wet glycol from the absorber to the reboiler and to pump dry glycol from a storage tank to the absorber. Besides water, the wet glycol going to the still column of the reboiler of the natural gas dehydrator will contain natural gas and absorbed hydrocarbons, and other gaseous components. 
     On many dehydrators, a volume of natural gas is intentionally induced into the reboiler in order to dry the wet glycol to a higher concentration than can be accomplished by simply adding heat. The process of intentionally inducing a volume of natural gas into the reboiler is referred to as gas stripping. 
     In the still column of the reboiler of the natural gas dehydrator, the water, natural gas, and other hydrocarbons are separated from the glycol by the pressure reduction from the absorber pressure to approximately atmospheric pressure in the still column and by the application of heat to the reboiler. 
     The water, natural gas, other hydrocarbons and gases contained in the wet glycol stream which are separated in the still column from the wet glycol are exhausted as vapors into the atmosphere through the atmospheric vent on the still column unless facilities are installed to collect and dispose of the vented vapors. The hydrocarbon vapors released through the still column of a natural gas dehydrator are air pollutants. Specifically, certain hydrocarbons such as benzene, toluene, ethylbenzene, and xylene, commonly referred to as BTEX have been proven to be carcinogenic. Other gases such as hydrogen sulfide, when present, are toxic. 
     The gas dehydrator and systems for use with gas dehydrators disclosed in U.S. Pat. Nos. 6,238,461, 5,766,313, 6,364,933, and Ser. No. 10/071,721 offer solutions to at least some of the problems discussed above. The present invention provides improvements to such gas dehydrators and systems. 
     BRIEF SUMMARY OF THE INVENTION 
     The present invention relates to an apparatus for use with a natural gas dehydrator, and gas dehydrator systems. The preferred apparatus, method and system of the invention preferably comprises an absorber, wet glycol, dry glycol, a glycol-to-glycol heat exchanger, at least one separator apparatus, a reboiler, a condenser, and at least one circulating apparatus for wet glycol, dry glycol, gaseous hydrocarbons, and liquid hydrocarbons. Preferably, all gaseous hydrocarbons are circulated via the circulating apparatus to the reboiler and are not released to the atmosphere. Likewise, preferably all liquid hydrocarbons are collected. 
     A primary object of the present invention is to provide an improved and efficient system for use with a gas dehydrator. 
     A primary advantage of the present invention is that it is easy to operate and does not release combustible gases into the atmosphere. 
     Other objects, advantages and novel features, and further scope of applicability of the present invention will be set forth in part in the detailed description to follow, taken in conjunction with the accompanying drawings, and in part will become apparent to those skilled in the art upon examination of the following, or may be learned by practice of the invention. The objects and advantages of the invention may be realized and attained by means of the instrumentalities and combinations particularly pointed out in the appended claims. 
    
    
     
       BRIEF DESCRIPTION OF THE SEVERAL VIEWS OF THE DRAWINGS 
       The accompanying drawings, which are incorporated into and form a part of the specification, illustrate one or more embodiments of the present invention and, together with the description, serve to explain the principles of the invention. The drawings are only for the purpose of illustrating one or more preferred embodiments of the invention and are not to be construed as limiting the invention. In the drawings: 
         FIG. 1  is a flow diagram of one embodiment of the invention; 
         FIG. 2  is a flow diagram of another embodiment of this invention; 
         FIG. 3  is a flow diagram of another embodiment of this invention; 
         FIG. 4  is a sketch of a water exhauster of this invention; 
         FIG. 5  is a sketch of a blowcase of this invention; 
         FIG. 6  is a flow diagram of another embodiment of this invention; 
         FIG. 7  is a sketch of a hydrocarbon gas stripping system of this invention; 
         FIG. 8  is a flow diagram of another embodiment of this invention; 
         FIG. 9  is a sketch of a glycol storage and glycol reservoir of this invention; and 
         FIG. 10  is a flow diagram of another embodiment of this invention. 
     
    
    
     DETAILED DESCRIPTION OF THE INVENTION 
     The present invention is an apparatus and system for use with a natural gas dehydrator. The gas dehydrator and systems disclosed in U.S. Pat. Nos. 5,766,313, 6,238,461, 6,364,933, and Ser. No. 10/071,721 are useful in understanding the present invention and the disclosures are specifically incorporated herein by reference. 
     The volume and pressure of the natural gas flowing through the system of the present invention can vary in wide ranges. Each unit is designed by those skilled in the art to perform at wide ranges of volume and pressure of the natural gas being processed and various controls have been associated with the natural gas dehydrators so that these dehydrators can be operated in a conventional manner by those skilled in the art. The operation of the various components of this invention uses conventional apparatuses that are normally used in the operation of a natural gas dehydrator. Therefore, the specific parameters associated with the operation of the various components of this invention are parameters known by those skilled in the art. 
     As shown in the drawings, in accordance with the present invention, the natural gas is first passed through conventional two or three-phase inlet separator  3  to remove water and liquid hydrocarbons therefrom. The natural gas is then fed into absorber  2 , through inlet  4 , so that the natural gas can flow upwardly through absorber  2 . Dry glycol is introduced through inlet  6  and flows through spaced apart bubble trays or other contact medium (not shown) in absorber  2  and then downwardly through absorber  2 . The dry glycol functions primarily to remove water from the natural gas and becomes wet glycol. The treated natural gas exits through outlet  8  in the top portion of absorber  2  and is passed through tube side  9  of glycol-gas heat exchanger  10  and passes out as dry, saleable natural gas through pipe  12  at relatively high pressures, for example 50 PSIG to 1500 PSIG depending on the operating pressures of the pipeline system. It is understood that any type of conventional heat exchanger can be used in place of exchanger  10  illustrated in FIG.  1 . 
     In one configuration of the invention (see FIG.  1 ), the wet glycol is collected in wet glycol sump  14  in the bottom portion of absorber  2  and contains entrained and absorbed gases, liquid hydrocarbons, and water and exits absorber  2  at point  16 , is discharged by control valve  17  through filter  19  in pipe  18  to inlet  20  of reflux coil  22  located in still column  24  (explained below). The flow of the wet glycol is controlled by a throttling liquid level control (not shown) located in absorber  2  and operates motor valve  17  to maintain a constant level of wet glycol in the bottom of absorber  2 . The wet glycol flows through reflux coil  22 , cooling and condensing some of the hot vapors in the top of still column  24 . The wet glycol at inlet  20  is between approximately 90° and 120° F. and at exit  26  is approximately 150° F. The wet glycol exits reflux coil  22  at exit  26  and flows through pipe  28  where at point  30  it is combined with other wet glycol (explained below) flowing through pipe  32 . A by-pass can be provided to by-pass reflux coil  22  when desired. The combined wet glycol flows through pipe  34  and enters inlet  36  of wet glycol cooler  38 . Glycol cooler  38  may be one of many types of coolers. As shown in the drawings, the combined wet glycol flows through a radiator and is cooled by air pushed through the radiator by a fan. Preferably, the fan is driven at a constant speed and the amount of the cooling air passing through the radiator is controlled by a plurality of pivotally mounted shutters moved by suitable means, such as an air cylinder or other devices such as a servo motor which moves a rack to rotate each of the shutters between opened and closed positions such as that marketed by AIR-X-CHANGERS as MODEL 48H. In the system illustrated in  FIG. 1 , the combined wet glycol exits the wet glycol cooler at a temperature of between approximately 90° and 120° F. 
     The cooled combined wet glycol exits the glycol cooler  38  and flows through pipe  40  into inlet  42  of a three-phase emissions separator apparatus  50 . Free gaseous hydrocarbons contained in the wet glycol are released in the three-phase emissions separator apparatus  50  as a result of the reduction of pressure from the pressure of the absorber of between approximately 50 and 1500 PSIG to the pressure in the three-phase emissions separator which is between approximately 10 and 30 PSIG and preferably about 15 PSIG. Liquid hydrocarbons are separated from the combined wet glycol in the three-phase emissions separator apparatus  50  by a weir system or interface liquid level controller (not shown) and are withdrawn through outlet  52  and flow through control valve  54  and pipe  55  to storage (not shown) or other apparatus. The amount of the wet glycol from the combined wet glycol entering the emissions separator  50 , after the gases and liquid hydrocarbons have been removed, is then combined with a fixed volume of wet glycol contained in the emissions separator  50 . The fixed volume of wet glycol is continuously recirculated. Therefore, the total volume of wet glycol in the emissions separator may be described as at least two portions of wet glycol. One portion is that required to be continuously circulated through one type of apparatus as explained below and another portion to be passed through glycol-to-glycol heat exchanger  64  for heat exchange with the hot dry glycol exiting the reboiler as explained below. From the glycol-to-glycol heat exchanger the heated wet glycol flows to the still column and into the reboiler. The volume of wet glycol exiting emissions separator  50  to enter the glycol-to-glycol heat exchanger  64  is about the same volume as the volume of glycol being pumped into absorber  2  by glycol pump  76  (see FIG.  1 ). The volume of dry glycol pumped is usually in the range of 3 to 6 gallons of dry glycol for each pound of water removed from the gas stream. The amount of dry glycol pumped is determined in a conventional manner known to those skilled in the art. The volume of wet glycol flowing out of emissions separator  50  to the glycol-to-glycol heat exchanger  64  is controlled by control valve  53  which is controlled by a throttling liquid level control (not shown) located in emission separator  50 . 
     The freed gaseous hydrocarbons exit through outlet  56  in the top portion of the three-phase emissions separator apparatus  50  and flow through pipe  58  into a system, such as that described in the U.S. Pat. No. 5,766,313, to be used as fuel in a reboiler as described therein. 
     Another portion of wet glycol passes from three-phase emissions separator  50  through pipe  60  and enters tube side  62  of glycol-to-glycol heat exchanger  64 . It is understood that any type of heat exchanger may be used in place of the heat exchanger  64  shown in FIG.  1 . Another portion of wet glycol in glycol-to-glycol heat exchanger  64  is heated by the hot dry glycol therein and flows from glycol-to-glycol heat exchanger  64  through pipe  66  and enters still column  24  of conventional reboiler  68 , such as that illustrated in the &#39;313 Patent. Another portion of wet glycol is changed into hot dry glycol which is then fed through pipe  70  into glycol-to-glycol heat exchanger  64  and is cooled by the other portion of wet glycol. The partially cooled dry glycol then passes through pipe  72  into dry glycol storage tank  74  from which it is pumped by pump  76  through pipe  78  into the gas to glycol heat exchanger  10  to be further cooled by the natural gas flowing through heat exchanger  10  and into pipe  12 . 
     The one portion of the wet glycol in emissions separator  50  exits through pipe  86  and enters pump  88 . The one portion of wet glycol exiting from pump  88  separates at point  90  into the first stream of wet glycol flowing through pipe  92  and a second stream of wet glycol flowing through pipe  94 . The wet glycol in pipe  94  passes through filter  96  and then through pipe  98  into effluent condenser  84 . As described above, the second stream of wet glycol exits effluent condenser  84  through pipe  32  and is combined at point  30  with the wet glycol in pipe  28 . 
     In a second configuration of the invention, as shown in  FIG. 2 , the wet glycol is collected in wet glycol sump  14  in the bottom portion of absorber  2  and contains entrained and absorbed gases, liquid hydrocarbons and water and exits absorber  2  at point  16 . It is discharged by control valve  17  through filter  19  in pipe  18  to point  30  where the wet glycol from absorber  2  combines with cooled wet circulating glycol from glycol cooler  38  (explained below). The flow of the wet glycol from absorber  2  is controlled by a throttling liquid level control (not shown) located in absorber  2  and operates control valve  17  to maintain a constant level of wet glycol in the bottom of absorber  2 . The combined wet glycol flows through pipe  41  into inlet  42  of three-phased emissions separator apparatus  50 . Free gaseous hydrocarbons contained in the wet glycol from absorber  2  are released in three-phased emissions separator  50  as a result of the reduction of pressure from the pressure of the absorber of between 50 and 1500 PSIG to the pressure in three-phased emissions separator  50  which is between 10 and 30 PSIG and preferably about 15 PSIG. Liquid hydrocarbons are separated from the wet glycol in three-phased emissions separator  50  by gravity and by a weir system or an interfacing liquid level controller (not shown) and are withdrawn through outlet  52 , control valve  54 , and pipe  55  to storage (not shown) or other apparatus. The wet glycol entering emissions separator  50 , after the gases and liquid hydrocarbons have been removed, is then combined with a fixed volume of wet glycol contained in emissions separator  50 . The fixed volume of wet glycol is continuously recirculated. Therefore, the total volume of wet glycol in the emissions separator has at least two portions of wet glycol. One portion is that required to be continuously circulated (explained below) and another portion is to be passed through a glycol-to-glycol heat exchanger  64  for heat exchange with the hot dry glycol exiting reboiler  68  (explained below). From glycol-to-glycol heat exchanger  64  the heated wet glycol flows to still column  24  and into reboiler  68 . The volume of wet glycol exiting emissions separator  50  through control valve  53  to enter the glycol-to-glycol heat exchanger  64  is about the same volume as the volume of glycol being pumped into absorber  2  by the glycol pump  76  (see FIG.  2 ). The volume of dry glycol pumped is usually in the range of 3 to 6 gallons of dry glycol for each pound of water removed from the gas stream. The amount of dry glycol pumped is determined in a conventional manner known to those skilled in the art. The volume of wet glycol flowing out of emissions separator  50  to the glycol-to-glycol heat exchanger  64  is controlled by control valve  53  which is controlled by an interfacing liquid level control (not shown) located in emissions separator  50 . To overcome any potential pressure drop, in excess of the gas pressure in emissions separator  50 , which might occur below control valve  53  as a result of friction drop in the glycol piping, glycol-to-glycol heat exchanger, or other apparatus, valve  53  is located to receive glycol from the discharge of circulating pump  88  at approximately 100 PSIG above the pressure in emissions separator  50  (explained below). 
     The freed gaseous hydrocarbons exit through outlet  56  in the top portion of three-phased emissions separator apparatus  50  and flow through pipe  58  into a system such as that described in the U.S. Pat. No. 5,766,313, to be used as fuel in a reboiler as described therein. 
     The other portion of wet glycol passes from three-phased emissions separator  50  through pipe  86 , circulating pump  88 , and pipe  61  to point  65 . At point  65 , the other portion of wet glycol is split into two streams. As described below, one stream of wet glycol flows through pipe  92  to power eductor  112 . The second stream of wet glycol flows through pipe  94  to point  90  where the second steam of wet glycol splits into a third wet glycol stream and a fourth wet glycol stream. The third wet glycol stream flows through pipe  67 , control valve  53 , and pipe  57  and enters tube side  62  of glycol-to-glycol heat exchanger  64 . It is understood that any type of heat exchanger may be used in place of heat exchanger  64  (Shown in FIG.  2 ). The third wet glycol stream in glycol-to-glycol heat exchanger  64  is heated by the hot dry glycol therein and flows from glycol-to-glycol exchanger  64  through pipe  66  and enters still column  24  of conventional reboiler  68  such as that illustrated in the &#39;313 Patent wherein the other portion of wet glycol is changed into hot dry glycol which is then fed through pipe  70  into the shell side of glycol-to-glycol heat exchanger  64  and is cooled by the other portion of wet glycol. The partially cooled dry glycol then passes through pipe  72  into a dry glycol storage tank  74  from which it is pumped by pump  76  through pipe  78  into the gas to glycol heat exchanger  10  to be further cooled by the natural gas flowing through heat exchanger  10  and into pipe  12 . Dry glycol storage  74  has vent pipe  75  which vents dry glycol storage  74  to the atmosphere. Pipe  75  is connected to dry glycol storage  74  at point  77 . 
     The fourth wet glycol stream flows at approximately 100 PSIG pressure created by circulating pump  88 , through pipe  95 , filter  96 , pipe  97 , fixed choke  101  and pipe  98  to enter the shell side of overhead condenser  84 . Fixed or variable choke  101  or a control valve actuated by a pressure control device can control the volume of wet glycol flowing through pipe  98 . The temperature of the wet glycol entering the shell side of overhead condenser  84  is substantially the same as the temperature of the wet glycol contained in emissions separator  50 . The temperature of the wet glycol in emissions separator  50  is maintained by a thermostat, located in emissions separator  50 , which opens and closes shutters on glycol cooler  38  (explained below), and the temperature of the glycol in emissions separator  50  is normally maintained at approximately 90 to 120 degrees Fahrenheit. The fourth wet glycol stream flows through the shell side of overhead condenser  54  where the fourth wet glycol stream is in heat exchange relationship with the hot effluent from still column  24  (explained below). The fourth wet glycol stream passes from overhead condenser  84  through pipe  33  to the inlet  20  of a reflux coil located in still column  24  (explained below). The fourth wet glycol stream flows through reflux coil  22  cooling and condensing some of the hot vapors in the top of still column  24 . The fourth wet glycol stream exits reflux coil  22  at exit  26  and flows through pipe  29  to inlet  36  of wet glycol cooler  38 . If desired, a bypass line can be provided to bypass reflux coil  22 . Glycol cooler  35  may be one of many types of coolers useful in accordance with the present invention. The drawings show the wet glycol flowing through a radiator and cooled by air pushed through the radiator by a fan. Preferably, the fan is driven at a constant speed and the amount of the cooling air passing through the radiator is controlled by a plurality of pivotally mounted shutters moved by a suitable means, such as an air cylinder or other devices such as a servo motor which moves a rack to rotate each of the shutters between opened and closed positions such as that marketed by AIR-X-CHANGERS as model 48H. In the system illustrated in  FIG. 2 , cooled wet glycol stream  4  exits glycol cooler  38  at point  35  at a temperature of between approximately 90 and 120 degrees Fahrenheit. From point  35  the fourth, cooled wet glycol stream flows through pipe  37  to point  30  where it combines with the wet process glycol from absorber  2  and the combined wet glycol flows through pipe  40  to inlet  42  of emissions separator  50 . 
     During the standard glycol dehydration process, gases and liquid hydrocarbons generated by the process are routinely released to the atmosphere. The gases and liquid hydrocarbons released to the atmosphere are the result of gas being entrained or absorbed in the dry glycol while it is contacting the natural gas in the absorber. Additional gas is entrained in the wet glycol when a pressure actuated pump is used to pump the dry glycol into the absorber. The entrained and absorbed gases and hydrocarbons are released from the wet glycol at two points in the process. First, most of the entrained gases are released from the wet glycol in the emissions separator by a reduction of pressure. Second, the balance of gases, liquid hydrocarbons, and water are substantially released from the wet glycol by the application of heat in the reboiler as well as by stripping in the still column. 
     One of the goals of the process of this invention is to eliminate the atmospheric pollution and the wasting of hydrocarbon energy that now occurs in most glycol dehydration of natural gas. To accomplish this goal, the process collects all the combustible gaseous vapors and liquid hydrocarbons generated by the glycol dehydration process. The collected combustible vapors are sent to the burner fuel system to be used as fuel gas in heating the reboiler. The collected liquid hydrocarbons are routed to a liquid storage and handling system. 
     As stated above, the other portion of wet glycol entering reboiler  68  is subjected to the heat in the reboiler and an effluent is formed in still column  24 . This effluent may comprise liquid water, liquid hydrocarbons, vaporized water, gases and vaporized hydrocarbons. These effluents may be treated in systems similar to those described in the &#39;461 and &#39;933 Patents or by a system illustrated in  FIG. 1 , wherein the effluent In still column  24  exits Into pipe  82  and passes through the tube side of effluent condenser  84  where it is cooled as described below. Effluent condenser  84  may be of the type illustrated in the &#39;461 and &#39;933 Patents. If desired, an effluent condenser such as that illustrated in FIGS. 6 and 7 of the &#39;933 Patent may be modified so that the fans illustrated in the &#39;933 Patent and labeled “234” and 252″ therein may be continuously operated and not intermittently by a thermostat as described therein. Instead, the control of the temperature in the effluent condenser may be controlled by pivotally mounted shutters located in either the exit portion or the entrance portion of the effluent condenser. These pivotally mounted shutters may be operated between opened and closed positions by a servo motor, air cylinder, or other similar device controlled by a thermostat. As shown in  FIG. 2 , the effluent passes through tube side  109  of effluent condenser  84  where it is cooled to approximately 90 to 120 degrees Fahrenheit by wet glycol entering the shell side of effluent condenser  84  via pipe  98 . The cooled effluent includes both gaseous and liquid components which are routed to separator  102  via pipe  100 . The cooled effluent exiting effluent condenser  84  flows through pipe  100  and enters separator  102  which Is similar to the separator shown in  FIGS. 8 and 9  of the &#39;933 Patent except that it is mounted In a vertical position instead of the horizontal position. 
     In separator  102 , the gaseous hydrocarbons are withdrawn from the upper portion of separator  102  through pipe  104 ; the liquid hydrocarbons collected in separator  102  are withdrawn through pipe  108  and control valve  110  to the hydrocarbon storage facilities, the water is withdrawn through pipe  118  and control valve  121  to disposal. The first stream of wet glycol passing through eductor  112  creates a vacuum to draw the gaseous hydrocarbons through pipe  104  and entrains the gaseous hydrocarbons in the first stream of wet glycol. The first stream of wet glycol passing through eductor  112  compresses the gaseous hydrocarbons entrained therein to the pressure maintained in emissions separator  50  and then flows through pipe  114  into emissions separator  50  wherein the gaseous hydrocarbons separate from the first stream of wet glycol and flow with the freed gaseous hydrocarbons through pipe  58  to the fuel system. Although other types of devices may be used to create the vacuum and compress the gases, an eductor is the preferred device to be used in the present invention. 
       FIGS. 3  to  5  illustrate another embodiment of the present invention. These Figures incorporate a large part of  FIG. 2  wherein the same reference numerals have been applied to corresponding parts of FIG.  2 . In  FIGS. 3  to  5 , there is illustrated an embodiment of the invention wherein additional water is removed from the dry glycol in pipe  70  to make super dry glycol. 
     As illustrated in  FIG. 3 , the dry glycol in pipe  70  enters water exhauster  120  (explained below), wherein additional water is removed from the dry glycol to make super dry glycol which exits water exhauster  120  and flows through pipe  122  into the shell side of glycol-to-glycol heat exchanger  64  and then through pipe  72  into what is now super dry glycol storage  74 . From storage  74 , the super dry glycol is pumped to absorber  2  and then completes the above described closed loop system by returning to reboiler  68  via emissions separator  50 , pipe  86 , circulating pump  88 , pipe  61 , pipe  94 , pipe  67 , control valve  53 , pipe  57 , glycol-to-glycol heat exchanger  64 , and pipe  66  to still column  24 . 
     The cooled, wet glycol exits glycol cooler  38  at point  35  and flows through pipe  44  to inlet  164  of a condenser tube bundle  160  mounted in water exhauster  120 , as described below, to condense some of the vapors in the vapor section of water exhauster  120 . The condensate (mainly water and some hydrocarbons) is transmitted to blowcase  124  through pipe  126 . Blowcase  124  has a weir system that separates the condensate into its water and hydrocarbon components. Water from blowcase  124  is discharged by control valve  178  into pipe  128  to combine at point  59  with the wet glycol flowing in pipe  57 . Control valve  178  is controlled by a liquid level control (not shown) mounted in water chamber  172  of blowcase  124 . Hydrocarbons from blowcase  124  (see  FIG. 5 ) are preferably discharged by control valve  188  through pipe  113  into hydrocarbon chamber  111  of vacuum separator  102 . In some applications, the hydrocarbons are dumped directly to the hydrocarbon storage. Control valve  188  is controlled by a liquid level control (not shown) mounted in hydrocarbon chamber  184  of blowcase  124 . 
     Except during the dumping cycle of blowcase  124 , the pressure in blowcase  124 , water exhauster  120  and reboiler  68  is the same. The equal pressure in blowcase  124 , water exhauster  120  and reboiler  68  is established and maintained by connecting equalizing pipes  130  and  134  to inlet  136  of still column  24 . 
     Water exhauster  120 , blowcase  124  and the flow of fluids is preferably as illustrated in  FIGS. 4 and 5 ; however, other systems, such as those described in U.S. Pat. Nos. 3,589,984 and 4,332,643 and in the article Coldfinger by L. S. Reid may also be used in accordance with the present invention. As illustrated in  FIG. 4 , dry glycol at about 390° F. having a glycol concentration of approximately 98.6 percent weight concentration exits reboiler  68  through pipe  70  to water exhauster  120 . Dry glycol  143  in water exhauster  120  is retained for about thirty (30) minutes and is changed, as described below, into super dry glycol that flows over dam  145  into weir system  147  which separates any entrained oil and the super dry glycol. Super dry glycol  148 , having a glycol concentration of about 99.8 percent weight concentration, exits water exhauster  120  into pipe  122  and flows through the shell side of the glycol-to-glycol heat exchange  64  and thereafter flows as described above. Free oil  173  exits weir system  147  of water exhauster  120  through pipe  150  and pipe  149  and enters through inlet  151 , the weir section  190  of blowcase  124  (explained below). 
     Dry glycol  143  in water exhauster  120  is maintained at approximately 390° F. by thermo jet coil  153  which is connected to reboiler  68  at point  154 . Thermo jet coil  153  continuously circulates hot dry glycol out of reboiler  68 . The thermo jet utilizes a small volume of the recovered gas from emissions separator  50  flowing through a small orifice  155  to create a flow of hot dry glycol through coil  153 . The hot dry glycol flows through thermo-jet coil  153  and returns to reboiler  68  through pipe  157  and enters reboiler  68  at point  159 . 
     The cooled, wet glycol flows from outlet  35  of glycol cooler  38  through pipe  44  to inlet  164  of water exhauster  120 . The cooled, wet glycol, at a temperature of between approximately 90 to 120 degrees Fahrenheit, enters condenser tube bundle  160  at point  164  and exits at point  165 . From point  165 , the cooled wet glycol flows through pipe  163  to point  30  where it combines with the process glycol from absorber  2 , and, as previously described, from point  30 , the cooled wet glycol flows through pipe  41  to inlet  42  of emissions separator  50 . The relatively cool wet glycol flowing through condenser tube bundle  160  cools the vapors in vapor section  162 . Cooling of the vapors in vapor section  162  results in the condensation of some of the vapors in vapor section  162  changing the partial pressure equilibrium of the various vapor components in vapor section  162 . The vapors in vapor section  162  generally include four components comprising water, glycol and condensable and non-condensable hydrocarbons. Since water has a relatively low boiling temperature compared to glycol, it has a greater vapor pressure than glycol and is the largest component of the vapors in vapor section  162 . Liquids condensed from vapor section  162  are collected on collection tray  168  and removed from water exhauster  120  at point  169 . Condensation of the vapors and the removal of the condensed liquids from water exhauster  120  continually changes the partial pressure equilibrium of the vapors in vapor section  162  and causes the liquid components (glycol, water and hydrocarbons) in dry glycol  143  in water exhauster  120  to react to re-establish their percentage of the equilibrium vapor pressure in vapor section  162 . Being the largest component of the vapors in vapor section  162 , water is the largest component condensed and is the primary component evolved from hot dry glycol  143  while re-establishing the partial pressure equilibrium of the vapors in vapor section  162 . Therefore, the body of hot dry glycol  143  in water exhauster  120  becomes increasingly water dry so that super dry glycol flows from weir system  147  into pipe  122 . 
     The condensed liquids collected on collection tray  168  of water exhauster  120 , removed via point  169  and line  126 , are routed to three-phasing weir chamber  190  of blowcase  124 . Three-phasing chamber  190  separates the condensates from water exhauster  120  into water and hydrocarbon components and, through a weir system, routes the water through valve  182  into water chamber  172  and the hydrocarbons through valve  176  into hydrocarbon chamber  184  of blowcase  124 . Vent pipe  130 , vent pipe  134 , and vent pipe  250  equalize the pressure in water exhauster  120 , blowcase  124 , dry glycol storage  74 , and glycol reservoir vessel  244  with the pressure in reboiler  68  by connecting into still column  24  at point  136 . 
     Referring to  FIG. 5 , when the water level in chamber  172  of blowcase  124  reaches a level to actuate liquid level controller  174 , a pressure signal is sent to close normally opened valve  182  and to open normally closed valves  178  and  180 . Closing valve  182  temporarily stops the transfer of water from three-phasing chamber  190  into water chamber  172 . Opening valve  180  allows recovered gas from emissions separator  50  to enter water chamber  172  to provide the pressure energy to partially evacuate water chamber  172  through water dump valve  178  and line  128 . The evacuated water is mixed and entrained into the wet glycol in line  57  before the wet glycol enters tube side  62  of glycol-to-glycol heat exchanger  64 . When the water level lowers to a preset level, liquid level controller  174  vents pressure signal and valves  182 ,  178 , and  180  return to their normal positions. The gas in water chamber  172  flows through normally opened valve  182  into three-phasing chamber  190 . Once the pressure in water chamber  172  and three-phasing chamber  190  equalizes, water again begins to flow from three-phasing chamber  190  into water chamber  172 . The power gas, which was released into three-phasing chamber  190 , passes from outlet  175  through equalizing pipes  134 , and  130  into an inlet  136  of still column  24 . 
     The operation of hydrocarbon chamber  184  mirrors the operation of water chamber  172 . Liquid level controller  181  operates the same as liquid level controller  174 . Normally opened valve  176  operates the same as normally opened valve  182 . Normally closed valves  188  and  189  operate the same as normally closed valves  178  and  180 . The hydrocarbons dumped through valve  188  are preferably transferred through pipe  113  to hydrocarbon chamber  111  of vacuum separator  102 . In some applications, the hydrocarbons dumped from hydrocarbon chamber will be transferred directly to the oil storage facilities. 
       FIG. 6  discloses another embodiment of the invention.  FIG. 6  incorporates a large part of  FIG. 2  wherein the same reference numerals have been applied to corresponding parts of FIG.  2 . In  FIG. 6 , there is illustrated another embodiment of the invention wherein additional water is removed from the hot, dry glycol as the hot, dry glycol is exiting reboiler  68  through packed stripping column  237  mounted in reboiler  68 . As illustrated in  FIG. 6 , hot, dry glycol at approximately  98 . 6  percent weight concentration exits reboiler  68  and flows downwardly through packed stripping column  237 . While flowing downwardly through packed stripping column  237 , the hot, dry glycol comes into intimate contact with heated and vaporized, liquid hydrocarbon gases that are flowing up, counter flow to the hot dry glycol. While flowing in intimate contact with the hot dry glycol, the heated, liquid hydrocarbon gases “gas strip” additional water from the hot dry glycol, and the hot dry glycol exits, at approximately 99.8 weight concentration, from stripping column  237 . The super dry glycol enters pipe  70  and flows through glycol-to-glycol heat exchanger  64  and pipe  72  into super dry glycol storage  74 . Super dry glycol storage  74  may be vented to the atmosphere or operating under a vacuum as shown in FIG.  9 . From glycol storage  74 , the super dry glycol is pumped to absorber  2  and completes the above described closed loop system by returning to reboiler  68  via emissions separator  50 , circulating pump  88 , pipe  61 , pipe  94 , pipe  67 , control valve  53 , pipe  57 , glycol-to-glycol heat exchanger  64 , and pipe  66  to still column  24 . 
     The heated, liquid hydrocarbon gases, required to strip additional water from the hot dry glycol exiting reboiler  68  through packed stripping column  237 , flow through pipe  233  to the gas inlet of stripping column  237 . The heated, liquid hydrocarbon gases enter stripping column  237  and flow upwardly through the hot dry glycol and exit from the top of stripping column  237  into reboiler  68 . From reboiler  68  the heated, liquid hydrocarbon gases flow into still column  24  to mix with the other gases and water vapor contained in still column  24 . The total of gases contained in still column  24  are effluents. The effluents rise to the top and exit still column  24  at point  27 . As previously described, the effluents flow, under a vacuum, through pipe  82 , overhead condenser  84  and pipe  100  into vacuum separator  102 . 
     Overhead condenser  84  cools the effluent and most of the water. Hot, vaporized, liquid hydrocarbons, contained in the effluent, are changed from a vapor to a liquid phase. The effluent enters vacuum separator  102  and, through the weir system of vacuum separator  102 , are transferred to hydrocarbon chamber  111  of vacuum separator  102 . Most of the liquid hydrocarbons transferred to hydrocarbon chamber  111  are again used in a closed loop system (described below), to strip additional water out of the hot glycol flowing out of reboiler  68  through stripping column  237 . 
     The heated, liquid hydrocarbon gases used in stripping column  237  to remove additional water from hot glycol exiting reboiler  68 , are obtained by heating a portion of the hydrocarbon liquids which have been recovered as previously described, in hydrocarbon chamber  111  of vacuum separator  102 . Referring to  FIG. 7 , when the level of hydrocarbons in hydrocarbon chamber  111  reach the high level set point of snap acting liquid control  192 , liquid level control  192  sends a pressure signal to the common port of three-way pressure switch  194  such as supplied by Wellmark, Inc. Three-way pressure switch  194  is actuated by an adjustable spring working against a pressure-loaded diaphragm. The pressure to load the diaphragm of pressure switch  194  is supplied by throttling liquid level control  196  mounted in hydrocarbon reservoir vessel  198 . The throttling liquid level control  196  maintains a relatively fixed level of hydrocarbons in reservoir vessel  198  by increasing or decreasing the pressure signal being sent to three-way pressure switch  194 . As the liquid level control  196  senses the level in reservoir vessel  198  needs to be raised, it increases the pressure signal to three-way pressure switch  194  shifting the three-way switch to open port  202  and close port  200 . When the level in reservoir vessel  198  rises to the high level set point, the output of liquid level control  196  decreases to where three-way pressure switch  194  reverses and port  202  closes and port  200  opens. 
     When port  202  of three-way pressure switch  194  is opened and port  200  is closed, any hydrocarbons being dumped from hydrocarbon chamber  111  of vacuum vessel  102  by liquid level control  192  are routed to hydrocarbon reservoir vessel  198  through pipe  204 , pipe  206 , control valve  208 , and pipe  210 . When port  200  of three-way pressure switch  194  is opened and port  202  is closed, any hydrocarbons being dumped from the hydrocarbon chamber  111  of vacuum vessel  102  by liquid level control  192  are routed to storage (not shown) through pipe  204 , pipe  212 , control valve  214 , and pipe  216 . By only sending recovered liquid hydrocarbons to storage when reservoir vessel  198  is operationally full, the previously described system insures that there is always enough liquid hydrocarbons in reservoir vessel  198  to operate the hydrocarbon stripping system. 
     Reservoir vessel  198  is maintained at a pressure of between approximately 5 and 10 pounds lower than the pressure used to evacuate hydrocarbon chamber  111  of vacuum vessel  102 . Back-pressure regulator  238 , which is connected to reservoir vessel  198  by line  236 , is set to relieve, through pipe  240 , any pressure in reservoir vessel  198  that is in excess of the high pressure set point. The gases that are released from reservoir vessel  198  flow through pipe  236 , back-pressure regulator  238  and pipe  130  to inlet  136  on still column  24 . The vented gases flow into still column  24  where they mix with the effluents in still column  24 . As previously described, the vented gases along with the other effluents are recovered in vacuum separator  102 . Pressure regulator  230  is set approximately 5 pounds lower then the high pressure set point on back pressure regulator  238 . When the pressure in reservoir vessel  198  drops approximately 5 pounds below the high pressure set point, pressure regulator  230  begins to open and either recovered gas from emissions separator  50  or gas from the supply gas system flows through pipe  234 , pressure regulator  230 , and pipe  232  into reservoir vessel  198 . Preferably, the gas passing through pressure regulator  230  to maintain the low-pressure set point in reservoir  198  would, as shown, come from the recovered gas system. 
     The liquid hydrocarbons in reservoir vessel  198  are released into the hydrocarbon stripping system by control valve  218 . Control valve  218  is operated by pressure-stat  220  such as supplied by Kimray, Inc. Pressure-stat  220  has an adjustable spring that opposes a pressure-loaded diaphragm. The diaphragm of pressure-stat  220  is connected through line  226  to pipe  224 . As the pressure rises in pipe  224 , the increased pressure on the diaphragm of pressure-stat  220  causes pressure-stat  220  to react to decrease the pressure on the diaphragm of control valve  218 . Decreasing the pressure on the diaphragm of control valve  218  causes control valve  218  to partially or completely close, decreasing or stopping the flow of hydrocarbons through pipe  222  and control valve  218 . As the pressure in pipe  224  decreases, the decreased pressure on the diaphragm of pressure-stat  220  causes pressure-stat  220  to react to increase the pressure on the diaphragm of control valve  218 . Increasing the pressure on the diaphragm of control valve  218  causes control valve  218  to partially or completely open increasing the flow of hydrocarbons through pipe  222  and control valve  218 . 
     From outlet  219  of control valve  218 , the recovered, liquid hydrocarbons flow through pipe  223  to the inlet of either heat exchange coil  221  mounted in reboiler  68  or a heat exchange coil mounted in an indirect heater (not shown). To heat the recovered, liquid hydrocarbons on new dehydrators, it is preferable to use heat exchange coil  221  mounted in reboiler  88 . To heat the recovered, liquid hydrocarbons on retrofitted dehydrators, it is preferable to use a heat exchange coil mounted in an indirect heater (not shown). For this embodiment, the operation of a new dehydrator with a heat exchange coil mounted in the reboiler is described. The recovered, liquid hydrocarbons flow through heat exchanger coil  221  which is immersed in the hot glycol contained in reboiler  68 . While in heat exchange relationship with the hot glycol in reboiler  68 , the recovered, liquid hydrocarbons gain heat causing the recovered, liquid hydrocarbons to vaporize and increase in pressure. The hot, vaporized, liquid hydrocarbons exit heat exchanger coil  221  and flow through pipe  224  to fixed choke  228 . Fixed choke  228  is sized to pass the volume of vaporized, liquid hydrocarbons required to super dry hot glycol exiting stripping column  237  at point  235 . Pressure-stat  220  controls the pressure in pipe  224  as well as allowing (within limits) the pressure in pipe  224  to be raised or lowered to either increase or decrease the volume of vaporized, liquid hydrocarbons flowing through fixed choke  228 . Pressure-stat  220  must be set to maintain the maximum pressure in pipe  224  to at least 5 psig below the minimum set pressure in hydrocarbon reservoir  198 . 
     The hot, vaporized, liquid hydrocarbons exit fixed choke  228  and flow through pipe  233  to the gas inlet of stripping column  237 . As described above, the hot, vaporized, liquid hydrocarbons flow upwardly through the packing in stripping column  237  coming in intimate contact with the hot glycol which is flowing downwardly out of reboiler  68  through the packing in stripping column  237 . While in intimate contact with the hot glycol in stripping column  237 , the hot, vaporized, liquid hydrocarbons cause additional water to be removed from hot, dry glycol exiting reboiler  68  and super dry glycol exits stripping column  237  at point  235  and flow into pipe  70 . 
     To complete the closed loop stripping system, as previously described, the hot, vaporized, liquid hydrocarbons flow through stripping column  237 , reboiler  68 , still column  24 , pipe  82 , overhead condenser  84 , and pipe  100  into the weir section of vacuum separator  102  where the condensed liquid hydrocarbons are transferred into hydrocarbon chamber  111 . From hydrocarbon chamber  111 , liquid hydrocarbons, enough to keep reservoir vessel  198  operationally full of liquid hydrocarbons, are transferred through pipe  204 , pipe  206 , control valve  208 , and pipe  210  into reservoir  198 . From reservoir  198 , the liquid hydrocarbons flow through pipe  222 , valve  218 , heat exchange coil  221 , pipe  224 , fixed coke  228 , and pipe  233  into the hot, vaporized, liquid hydrocarbon inlet of stripping column  237 . 
     In some applications, where it is anticipated that high temperature gas (110 to 140 degrees Fahrenheit) will be encountered, it may be desirable to eliminate the hot glycol flow exiting the absorber from the glycol flow to the glycol cooler. Eliminating hot glycol from the absorber flowing through the glycol cooler significantly decreases the cooling load on the glycol cooler. 
       FIG. 8  discloses another embodiment of the invention which eliminates the hot glycol flow from the absorber combining with the glycol flow to the glycol cooler.  FIG. 8  incorporates a large part of FIG.  3  and  FIG. 6  wherein the same reference numerals have been applied to corresponding parts of FIG.  3  and FIG.  6 . Either of the processes to obtain super dry glycol as shown by  FIG. 3  or  FIG. 6  are applicable for use with the embodiment shown in FIG.  8 . To simplify the description of the embodiment shown by  FIG. 8 , the process to obtain super dry glycol, as shown in  FIG. 3 , has been selected for the description of the embodiment shown by FIG.  8 . 
     As illustrated in  FIG. 8 , wet glycol is collected in wet glycol sump  14  in the bottom portion of absorber  2  and contains entrained and absorbed gases, liquid hydrocarbons, and water and exits absorber  2  at point  16 . The flow of the wet glycol is controlled by a throttling liquid level control (not shown) located in absorber  2  which operates control valve  17  to maintain a constant level of wet glycol in the bottom of absorber  2 . The wet glycol is discharged by control valve  17  and flows through pipe  13  to inlet  11  of three-phased flash separator  49 . 
     Free gaseous hydrocarbons contained in the wet glycol are released in three-phased flash separator  49  as a result of the reduction of pressure from the pressure of the absorber of between approximately 50 and 1500 PSIG to the pressure in the three-phased flash separator which is generally between approximately 75 and 125 PSIG. Liquid hydrocarbons are separated from the wet glycol in three-phased flash separator  49  by a weir system or interface liquid level control (not shown) and are withdrawn through pipe  51 , control valve  59  and pipe  79  to storage (not shown) or other apparatus. Control valve  59  is operated by a liquid level control (not shown) mounted in three-phase flash separator  49 . 
     The freed gaseous hydrocarbons exit three-phased flash separator  49  and flow through pipe  81 , back-pressure regulator  85 , pipe  87 , pressure regulator  89 , and pipe  91  to point  47  where the freed gaseous hydrocarbons combine with gaseous hydrocarbons from emissions separator  50  which are flowing to point  47  through pipe  45 . The operation of emissions separator  50  is explained below. From point  47 , the combined gaseous hydrocarbons flow through pipe  58  into a system such as that described in U.S. Pat. No. 5,766,313, to be used as a fuel in a reboiler as described therein. 
     Backpressure regulator  85  maintains the minimum set pressure on three-phased flash separator  49 . Pressure regulator  89  controls the maximum set pressure on emissions separator  50 . Backpressure regulator  93  controls the maximum set pressure on three-phased flash separator  49 . In the event the pressure in three-phased flash separator  49  builds to a point high enough to actuate back pressure-regulator  93 , the excess pressure is relieved through pipe  91 , back-pressure regulator  93  and pipe  101 . 
     Wet glycol exits three-phased flash separator  49  and flows through pipe  15 , particulate filter  19 , pipe  31 , control valve  23  and pipe  39  to inlet  20  of reflux coil  22 . Control valve  23  is preferably operated by an interfacing liquid level control (not shown) mounted in three-phased flash separator  49 . Wet glycol flows through reflux coil  22  cooling and condensing some of the hot vapors in the top of still column  24 . The wet glycol at inlet  20  is between approximately 110 to 130 degrees Fahrenheit and at the exits approximately 160 degrees Fahrenheit. The wet glycol exits reflux coil  22  at exit  26  and flows through pipe  103  to inlet  63  of tube side  62  of glycol heat exchanger  64 . It is understood that any type of heat exchanger may be used in place of glycol-to-glycol heat exchanger  64 . The wet glycol flowing through tube side  62  of glycol-to-glycol heat exchanger  64  is heated by the hot glycol therein and flows from glycol-to-glycol heat exchanger  64  through pipe  66  and enters still column  24  of conventional reboiler  68 , such as that illustrated in the &#39;313 Patent wherein wet glycol is changed into hot, dry glycol which is then fed through pipe  70  into water exhauster  120 . Water exhauster  120  and blowcase  124  operate as previously described so that hot, super dry glycol exits from water exhauster  120  through pipe  122 , enters the shell side of heat exchanger  64  and is cooled by the cool glycol flowing through tube side  62  of glycol-to-glycol heat exchanger  64 . The partially cooled super dry glycol then passes through pipe  72  into a super dry glycol storage  74  from which it is pumped by pump  76  through pipe  78  into the gas to glycol exchanger  10  to be further cooled by natural gas flowing through heat exchanger  10  and into pipe  12 . The cooled super dry glycol exits gas to glycol heat exchanger  10  through pipe  6  and enters absorber  2  where it comes into contact with wet natural gas flowing through absorber  2 . After the super dry glycol has been contacted by wet natural gas, it collects as wet glycol in sump  14  of absorber  2  and the closed glycol loop has been completed. 
     A second loop system is shown by FIG.  8 . The second loop system incorporates all the components required to recover the effluents which exit the still column of a dehydrator. The major components in the second loop system are emissions separator  50 , vacuum separator  102 , glycol cooler  38 , and overhead condenser  84 . 
     At start up of the second loop system, all major components and associated equipment and piping composing the second closed loop system, which require a glycol flow, are charged with glycol, and, at the same time, a level of glycol is established in emissions separator  50 . The glycol level in emissions separator  50  remains relatively constant. Pipe  119  facilitates making the original charge of glycol in the second closed loop glycol system. Pipe  119  is connected at point  121  to discharge pipe  78  from glycol pump  76  and at paint  123  to emissions separator  50 . If introducing glycol into the second loop glycol system is desired, glycol may be introduced by opening a manual valve (not shown) so that glycol can be pumped by pump  78  through pipe  78  and pipe  119  into emissions separator  50 . 
     The glycol charge in the second loop is continuously circulated from emissions separator  50  by circulating pump  88 . The glycol, at a pressure of approximately 100 PSIG higher than the pressure in emissions separator  50 , flows through line  61  to point  65 . At point  65  the glycol stream splits. The first glycol stream flows through pipe  92  and provides energy to power eductor  112  (described below). The second glycol stream flows from point  65  through pipe  69 , particulate filter  96 , pipe  97 , fixed choke or other control  101 , and pipe  98  to inlet  107  of the shell side of overhead condenser  84 . Fixed choke or other control  101  controls the volume of glycol that is flowing through pipe  98  into overhead condenser  84 . The second stream of glycol flows through the shell side of overhead condenser  84  and cools hot effluent from still column  24 . The second stream of glycol exits overhead condenser  84  at exit  117  and flows through pipe  43  to inlet  36  of glycol cooler  38 . The design and function of glycol cooler  38  has been previously described. The cooled second stream of glycol exits glycol cooler  38  at point  35  and flows through pipe  44  to inlet  164  of condenser tube bundle  160  mounted in water exhauster  120 . Condenser tube bundle  160  functions as previously described to cool hot vapors in the vapor section of water exhauster  120 . The second stream of glycol exits condenser tube bundle  160  and flows through pipe  177  where it enters emissions separator  50  at point  42 . 
     As previously described, heat applied to the wet glycol in reboiler  68  releases effluents that exit from still column  24  at point  27 . From point  27 , the effluents flow through pipe  82 , overhead condenser  84 , and pipe  100  into vacuum separator  102 . The function of vacuum separator  102  and eductor  112  has been previously described. Emissions separator  50  has the same function as previously described, but since no processed glycol is being received or discharged by emissions separator  50 , no automatic control of the glycol level in emissions separator  50  is required nor is there any need for emissions separator  50  to be three-phased. 
     The glycol storage on most glycol dehydrators operates at atmospheric pressure. A pipe  75 , as shown in  FIG. 2 , is generally used to vent to the atmosphere the glycol storage of a dehydrator. Pipe  75  is opened to the atmosphere and is connected to glycol storage  74  at point  77 . 
     Two problems are created when the glycol storage of a dehydrator is vented to the atmosphere. The first problem is that any excess glycol (more than the capacity of the storage to handle) that flows into the storage as a result of overfilling of the dehydrator, upset of the process, or malfunction of the equipment will flow out of the glycol storage through a vent line such as pipe  75 . Depending upon how the installation of the dehydrator is designed to handle glycol storage overfill conditions, any glycol which overfills the storage and flows out a vent pipe such as pipe  75  could contaminate the environment. As a minimum, unless special accommodations have been made, any glycol, which flows out pipe  75 , will be wasted. The second problem that occurs when the glycol storage of a dehydrator is vented to the atmosphere is that the hot glycol in the storage is allowed to contact oxygen in the air. Oxygen in contact with hot glycol will cause degradation of the glycol. 
       FIG. 9  shows another embodiment of the invention.  FIG. 9  incorporates a large portion of  FIG. 3  wherein the same reference numerals have been applied to corresponding parts of FIG.  3 . In  FIG. 3  there is illustrated an embodiment of the invention wherein the glycol storage operates under a vacuum to eliminate the problems of the glycol storage being vented to the atmosphere. 
     As illustrated in  FIG. 3 , glycol storage  74  is connected to point  136  of still column  24  by vent pipe  246 , vent pipe  250 , vent pipe  134 , and vent pipe  130 . Still column  24  operates under a vacuum. Glycol storage  74  is also connected to glycol reservoir  244  by vent pipe  248 . Glycol storage  74  is also connected to glycol reservoir  244  by glycol fill pipe  258 , control valve  254  and pipe  260 . Glycol reservoir  244  is connected to high-pressure discharge pipe  78  by pipe  272 , fixed choke  268 , pipe  266 , control valve  262 , and pipe  264 . Operating glycol storage  74  in a closed loop glycol system under a vacuum eliminates the problems of hot glycol coming into contact with air and of glycol being wasted or contaminating the environment. 
     As shown in  FIG. 9 , glycol storage  74  provides the glycol to the suction of glycol pump  76  (glycol pump  76  may be a stand alone pump or it may be a pump that is internally mounted in the glycol storage). It is necessary at all times to maintain, in glycol storage  74 , a glycol level adequate to provide the suction head to pump  76 . To maintain the glycol level in glycol storage  74 , a reverse acting, interface liquid level control  255  is utilized. Liquid level control  255  puts out a pressure signal that increases as the glycol level in glycol storage  74  lowers and decreases as the glycol level in glycol storage  74  rises. The pressure signal from liquid level control  255  is connected to a control valve  254  and to a reverse acting pressure switch  256  such as a Kimray 3 PGRA Throttle-Reverse Pilot. Pipe  258  connects control valve  254  to reservoir vessel  244 . Pipe  260  connects control valve  254  to glycol storage vessel  74 . The lower opening diaphragm pressure (15 PSIG) of control valve  255  is adjusted by turning jackscrew  257  to compress the diaphragm spring. As the glycol level in glycol storage vessel  74  lowers, the output pressure of liquid level control  255  increases. When the output pressure of liquid level control  255  reaches 15 PSIG, control valve  254  begins to open and control valve  254  will remain open until the output pressure of liquid level control  254  drops below 15 PSIG. While control valve  254  is open, glycol in reservoir vessel  244  flows through pipe  258 , control valve  254 , and pipe  260  into glycol storage  74  maintaining the lower level of glycol in storage vessel  74 . 
     As previously described, the output from liquid interface level control  255  is connected to pressure switch  256  as well as control valve  254 . The lower operating pressure of pressure switch  256  is set at 5 PSIG by adjustment of jackscrew  259 . When a condition exists where more glycol from glycol-to-glycol heat exchanger  64  enters through pipe  72  into glycol storage  74  than pump  76  is pumping to absorber  2 , the glycol level in glycol storage  74  will rise. As the glycol level in glycol storage  74  rises, the output pressure of liquid level control  255  decreases. When the output pressure of liquid level control  255  drops to 5 PSIG, pressure switch  256  outputs a throttling pressure signal to control valve  262  beginning the opening of control valve  262 . 
     The downstream side of control valve  262  is connected by pipe  264  to reservoir vessel  244  at point  270 . The upstream side of valve  262  is connected by pipe  266 , fixed choke  268 , and pipe  272  to pump  76  high pressure (50 to 1500 PSIG) discharge pipe  78  which supplies the lean glycol to absorber  2 . When control valve  262  is open, fixed choke  268  controls the volume of glycol flowing to reservoir vessel  244 . Fixed choke  268  is preferably sized to allow no more the 25% of the output volume of pump  76  to flow from pipe  78  through valve  262  into reservoir vessel  244 . As a result of allowing some of the glycol being pumped by pump  76  to be transferred to reservoir vessel  244  instead of entering absorber  2 , the glycol overfill level in glycol storage  74  lowers. Lowering the glycol level in glycol storage  74  causes the output pressure from liquid level control  255  to increase. When the output pressure from liquid level control  255  again reaches 5 PSIG, pressure switch  256  bleeds off the pressure signal to control valve  262  and control valve  262  closes, stopping the flow of glycol from pipe  78  into reservoir vessel  244 . 
     Normal operation of glycol storage  74  is when the output of liquid level control  255  is between 5 and 15 PSIG. Opening and closing control valves  254  and  262  maintains the level in glycol storage  74  at the normal condition where adequate glycol is supplied to pump  76  and no hot glycol contacts air, contaminates the environment, or is wasted. By using interfacing liquid level control  255 , liquid hydrocarbons that might enter glycol storage vessel  74 , through contamination of the process glycol, will not materially change the glycol level in glycol storage  74 . Liquid hydrocarbons, which might enter glycol storage  74 , would separate and float on top of the glycol. Over time, the liquid hydrocarbons can build to a high level on top of the glycol in glycol storage  74 , and any additional liquid hydrocarbons will need to be removed. As shown in  FIG. 3 , the outlet of pipe  261  is located close to the top of glycol storage  74  and exits glycol storage  74  at point  263 . The purpose of pipe  261  is to set the upper level of any liquid hydrocarbons that might collect on top of the glycol in glycol storage  74 . Liquid hydrocarbons that exit glycol storage  74  through outlet  263  flow through pipe  265  to point  267  where the liquid hydrocarbons combine with the liquid hydrocarbons from water exhauster  120 . The combined stream of liquid hydrocarbons flows through pipe  149  to enter at point  151  into blowcase  124 . As previously described, the weir system of blowcase  124  transfers the liquid hydrocarbons into oil chamber  184 . From oil chamber  184  the liquid hydrocarbons are transferred to either the hydrocarbon chamber  111  of vacuum separator  102  or to storage (not shown). 
     There are applications where the amount of gas, recovered by the previously described invention, can be more than the amount of gas required to fire the reboiler. One example, of an application where the amount of gas recovered by the invention might be more than is required by the reboiler to heat the dehydration process, is at compressor stations where widely varying flow rates and temperatures of the gas being processed by the absorber can create conditions where excess gas can be recovered. A second example, of an application where the amount of gas recovered by the invention might be more than is required by the reboiler to heat the dehydration process, is where the composition of the gas being processed by absorber  2  creates unusually high BTU values for the recovered gas. 
     In applications where the amount of gas recovered by the invention is more than is required by the reboiler to heat the dehydration process, the excess recovered gas can be used for other purposes. Some of the other possible uses of the excess recovered gas are in a plants fuel system or the firing of other production equipment on the gas well or plant location. 
     In applications where there is no other use for excess gas recovered by the invention, the excess gas can be consumed by increasing the heat load on the reboiler.  FIG. 10  discloses another embodiment of the invention.  FIG. 10  incorporates a large portion of  FIG. 3  wherein the same reference numerals have been applied to corresponding parts of FIG.  3 . In  FIG. 10 , there is illustrated an embodiment of the invention whereby additional heat load, more then the heat load required by the dehydration process, can be applied to the reboiler. 
     To illustrate the present invention, the dehydration process utilizing the invention&#39;s gas recovery system and water exhauster system for obtaining super dry glycol has been chosen. Any of the other dehydration gas recovery processes previously described can be used to illustrate the present invention. 
     Referring to  FIG. 10 , the components necessary to inject water into still column  24  are added to the flow diagram illustrated by FIG.  3 . Pipe  278  is connected to outlet  276  located close to the bottom of the recovered water section created by the weir system in chamber  123  of vacuum separator  102 . Water flows from outlet  276  through pipe  278  to the suction inlet of metering pump  282 . Metering pump  282  may be electrically or pneumatically powered and is designed to allow the output volume to be varied over a wide range. From the discharge of metering pump  282 , recovered water is pumped through pipe  284  to point  286 . At point  286  the water pumped by metering pump  282  mixes with hot wet glycol flowing in pipe  66  from glycol-to-glycol heat exchanger  64 . The mixture of water and hot wet glycol enters still column  24  at point  288 . Considering the firing efficiency of the fire tube in reboiler  68 , each pound of water injected into still column  24  causes approximately 2000 BTU of excess gas to be consumed by reboiler  68 . In applications where injecting the water into still column  24  is not practical, the water can be injected directly into reboiler  68 . 
     The injected water at point  288  converts to steam and mixes with other effluents in still column  24 . As previously described, the effluents exit still column  24  at point  27  and flow through pipe  82 , overhead condenser  84 , and pipe  100  into the weir section of vacuum separator  102 . 
     The injected water flows in a closed loop system from vacuum separator  102  to still column  24  and overhead condenser  84 , then back to vacuum separator  102 . While flowing through the closed loop system, the injected water changes phase twice. The water exits vacuum separator  102  as a liquid, reboiler  68  adds heat which converts the liquid to steam, and overhead condenser  84  condenses the steam back to a liquid before the water returns to vacuum separator  102 . 
     The approximately 1200 BTU per pound of water that is removed from reboiler  68  by converting the injected water to steam increases the heat load on overhead condenser  84  by an equal amount. By heat exchange with the glycol flowing in the shell side of overhead condenser  84 , heat from the steam is transferred to the flowing glycol. The flowing glycol exits overhead condenser  84  and flows through pipe  33 , reflux coil  22 , and pipe  29  to glycol cooler  38  where heat is removed from the flowing glycol by exhausting the heat into the atmosphere. 
     The preceding examples can be repeated with similar success by substituting the generically or specifically described components and/or operating conditions of this invention for those used in the preceding examples. 
     Although the invention has been described in detail with particular reference to these preferred embodiments, other embodiments can achieve the same results. Variations and modifications of the present invention will be obvious to those skilled in the art and it is intended to cover in the appended claims all such modifications and equivalents. The entire disclosures of all references, applications, patents, and publications cited above are hereby incorporated by reference.