Abstract:
A column of solvent containing foaming contaminants is provided. Gas is educted into the solvent in the column so as to generate foam in the column. The gas is educted into the column independently of the input flow of solvent into the solvent using a pumparound arrangement with the solvent. Foam generation continues so as to push the foam up in the column, wherein much of the solvent that is in the foam is allowed to drain back down into the column. The foam passes through concentrators which increase the residency time of the foam in the column to further dry the foam and to create larger bubbles. The drier foam is pushed out of the column and into a container. The foam is broken up into gas and the liquid foaming contaminants. The gas is recirculated for injection into the column even after foaming has stopped. The foaming contaminants are concentrated at the surface level of the solvent in the column. These contaminants are removed from the column. A liquid separator separates immiscible liquids, such as oil, from the solvent.

Description:
This is a divisional application of application Ser. No. 09/794,286, filed Feb. 27, 2001 Now U.S. Pat. No. 6,602,423. 

   FIELD OF THE INVENTION 
   The present invention relates to apparatuses and methods for removing contaminants that can cause foaming in solvents that are used to process hydrocarbons such as natural gas. 
   BACKGROUND OF THE INVENTION 
   Hydrocarbon gas is frequently processed before storage, transportation through a pipeline or use. Processing removes undesirable components from the gas, such as moisture or sour contaminants. 
   Processing gas to remove moisture is referred to as dehydration. Hydrocarbon gas containing moisture is typically dehydrated by exposing it to the solvent triethylene glycol. The moisture is removed from the hydrocarbon gas in order to increase the heating value of the gas and to reduce the condensation of free liquid water during transportation or storage. The removal of the moisture also reduces the formation of gas hydrates that foul pipeline equipment. 
   In a typical glycol dehydration unit, the gas is dehydrated in a gas-liquid contactor, which is typically a tower. The wet gas enters the contactor at the bottom, while the dry gas exits from the top. Inside of the contactor, the gas passes through a shower of glycol solvent. The lean liquid solvent enters the contactor at the top and the rich liquid solvent (solvent containing moisture) exits the contactor from the bottom. The liquid solvent drains down inside of the contactor through a series of internal trays or packing. The gas is forced up through the solvent shower. When the gas physically contacts the liquid solvent, the mass of the water vapor in the gas is transferred to the solvent. 
   The rich solvent is processed for reuse. Reusing the solvent is desirable for environmental reasons (disposal of the solvent is both difficult and expensive) and also because replacing the solvent is expensive. Processing the solvent removes the moisture wherein the solvent is said to be lean. 
   Processing gas to remove sour contaminants is referred to as sweetening. Sour gas smells like rotten eggs. The sour contaminants are sulfur compounds (for example, hydrogen sulfide). These sulfur-containing compounds are removed because, when the compounds are combined with water, sulfuric acid is formed. Another contaminant in the gas is carbon dioxide. When the carbon dioxide is combined with water, carbonic acid is formed. Removing these acid forming contaminants is desirable in order to minimize corrosion in the vessels and pipelines used to store and transport the gas. 
   The gas sweetening process is similar to the dehydration process. The gas is forced upward through a shower of sweetening solvent in a gas-liquid contactor. The sweetening solvent is an amine solvent. The contaminants are removed by the sweetening solvent. 
   The sweetening solvent is processed for reuse, for the same reasons that the dehydration solvent is processed for reuse. Processing the solvent removes the sour contaminants. 
   In both the dehydration process and the sweetening process, the gas-liquid contactor requires careful balancing of the physical parameters of the gas and the liquid. When the contactor is in equilibrium, the gas exits out of the top and the rich solvent (the solvent being rich with either moisture or sour contaminants) exits out of the bottom, as described above. Also, when the system is in equilibrium, the amount of gas that is processed is maximized. 
   One sign that equilibrium is lost is when some of the liquid solvent is carried out of the contactor with the gas. This occurs if the gas rate through the contactor is too high or if the solvent contains relatively high concentrations of foaming contaminants. Such foaming contaminants include well treatment chemicals, liquid hydrocarbons (such as crude oil), corrosion inhibitors, suspended solids and excessive amounts of antifoam chemicals. Foaming is evident when the foam exits the top of the contactor. This is known as “carrying over” or “puking”. 
   Foaming of the solvent is undesirable because foaming leads to a loss of efficiency of the contactor, causes contamination of the gas with the solvent, and results in the loss of the expensive solvent. 
   In the prior art, attempts have been made to solve the foaming problem. The prior art treats the solvent by passing it through activated carbon to adsorb the foam causing surfactants. In addition, the solvent is passed through filters to remove small suspended particles. Such particles stabilize the foam once it is formed. 
   The prior art systems suffered from several problems. The filters require replacement and disposal. Disposal of the used filters can be expensive due to environmental concerns. In addition, the filters themselves are expensive. Filters are also very specialized, being suited only to a narrow range of contaminant types or sizes. It is difficult to select a proper type of filter for the particular foaming contaminant present in the solvent. That is to say that the effectiveness of the filter is dependent on the filter matching the particular type of the foaming contaminant. Typically, the particular type of foaming contaminant is unknown, resulting in guess work as to the particular filter which is to be used. 
   My U.S. Pat. No. 6,080,320 teaches a method and apparatus for removing foaming contaminants from solvents. I have made improvements to both the method and the apparatus. 
   One of these improvements provides a much cleaner solvent than ever before obtained, thereby increasing the overall efficiency of the hydrocarbon processing. Foaming contaminants comprise surfactants. In the gas-liquid contactor, a frothing is desired in order to remove the impurities (water, sour contaminants, etc.) from the hydrocarbon gas. This process is known as mass transfer, wherein the impurities are transferred from the hydrocarbon gas to the liquid solvent. 
   The presence of foaming contaminants reduces the efficiency of the gas-liquid contactor. This is because the foaming contaminants resist the transfer of mass from the gas to the liquid, thereby reducing the quantity of mass that is transferred. The quantity of mass transferred is adversely affected even if the contactor does not exhibit signs of foaming (such as foam production at the top of the contactor or variations in the pressure at the gas outlet). In the prior art, the operator of the contactor detects a foaming problem by detecting foam at the top of the contactor or by a pressure change in the gas outlet. If foam is detected, then the operator adds anti-foaming agents to the solvent. 
   However, the contactor efficiency is reduced even by a quantity of foaming contaminants that is too small to cause detectable foaming. Thus, even if foaming is undetected by the operator, the efficiency is likely to be relatively low. Furthermore, the addition of anti-foaming agents does not reduce the amount of foaming contaminants. Instead the anti-foaming agents work to reduce the stability of the foam; the foaming contaminants are not tied up. Consequently, the foaming contaminants continue to adversely affect the contactor efficiency. 
   Another improvement eliminates the need for a compressor to introduce the gas into the apparatus as well as making the introduction of gas independent on the solvent inlet flow. The gas is used to create foam for the removal of the foaming contaminants. Compressors are expensive and can be bulky. An eductor can be used in the solvent input line, but this makes the flow of gas into the apparatus dependent upon the flow of solvent into the apparatus. 
   Still another improvement modifies the structure of the foam that is generated. Modifying the foam structure results in a drier foam (one that contains less solvent) and bubbles that are more easily broken for ultimate recovery of the liquid component of the foam. 
   Still another improvement isolates unwanted liquids from the solvent, such as oil. This results in cleaner solvent. 
   SUMMARY OF THE INVENTION 
   It is an object of the present invention to provide a method and apparatus for improving the mass transfer capabilities in hydrocarbon processing. 
   It is another object of the present invention to provide an improved method and apparatus for removing foam contaminants from hydrocarbon fluid processing solvents. 
   It is another object of the present invention to provide a method and apparatus for removing foam contaminants from hydrocarbon fluid processing solvents which provides gas to the solvent independently of the solvent flow. 
   It is another object of the present invention to provide a method and apparatus for removing foam contaminants from hydrocarbon fluid processing solvents, wherein the foam structure is modified to reduce solvent content and to make the foam more manageable. 
   It is another object of the present invention to provide a method and apparatus for removing liquid contaminants from hydrocarbon fluid processing solvents. 
   The present invention provides a method of removing contaminants from a solvent which is used to process hydrocarbon fluids. A column is provided, which column has a top end. The contaminated solvent is introduced into the column at a first location. The contaminated solvent is in a liquid form and has a top level within the column. Gas is introduced into the contaminated solvent in the column at a second location that is below the first location so as to generate bubbles in the liquid and drive the contaminants to the top level of the liquid. The contaminants are removed from the top level of the liquid. 
   In accordance with one aspect of the present invention, the solvent is removed from the column at a third location that is below the second location. 
   The present invention also provides a method for removing foaming contaminants from solvent which is used to process hydrocarbon fluids. A column having a top end and a carryover coupled to the top end of the column is provided. The contaminated solvent is introduced into the column at a first location. Gas is introduced into the column at a second location that is located below the first location, whereby foam is generated in the column. The foam comprises the gas, the solvent and the foaming contaminants. Foam generation is continued so as to push the foam into the carryover and out of the column, whereby a portion of the foaming contaminants are removed from the column. Gas introduction at the second location is continued even after foaming stops so as to drive the foaming contaminants to a top level of the liquid solvent and the column. The solvent is removed from the column at a third location that is below the second location. 
   In accordance with another aspect of the present invention, the foaming contaminants are removed from the top level of the liquid. 
   In accordance with still another aspect of the present invention, the step of introducing gas into the column at a second location further comprises the step of removing gas from the column at a location above a surface level of the liquid and educting the gas with a flow of solvent taken from the column. 
   In accordance with still another aspect of the present invention, the flow of solvent into the column for educting gas is greater than the flow of solvent into the column at the first location. 
   In accordance with another aspect of the present invention, the foam is coarsened as it is pushed, whereby the foam becomes drier and easier to shear. 
   In accordance with another aspect of the present invention, the contaminated solvent comprises immiscible liquid, wherein the method further comprises the step of separating the immiscible liquid, from the solvent as the solvent is introduced into the column. 
   In accordance with still another aspect of the present invention, the immiscible liquid is separated from the solvent at either the first location or the second location or both. 
   In accordance with another aspect of the present invention, the step of introducing gas into the column at a second location further comprises the step of removing gas from the column at a location above a surface level of the liquid and educting the gas with the flow of solvent taken from the column. The foam is coarsened as it is pushed, whereby the foam becomes drier and easier to shear. The contaminated solvent comprises immiscible liquid, which immiscible liquid is separated from the solvent as the solvent is introduced into the column. 
   The present invention also provides a facility for processing hydrocarbons utilizing solvent to remove contaminants from the hydrocarbons. The solvent contains foaming agents. There is provided a fluid-liquid contactor having a hydrocarbon input, a hydrocarbon output, a lean solvent input and a rich solvent output. A solvent recycler is connected between the lean solvent input and the rich solvent output, the solvent recycler processing rich solvent exiting through the rich solvent output into lean solvent for introduction into the contactor by way of the lean solvent input. A column has a top end, it has a solvent inlet in a first location. The solvent has a gas inlet in a second location that is below the first position, wherein gas bubbles up through the solvent in the column. The column having a solvent output in a third location located below the second location. The solvent inlet and solvent outlet are connected to the solvent recycler. An outlet in the column is located in a liquid surface level of the column, wherein contaminants can be removed through the outlet from the column. 
   A method is provided for removing foaming contaminants from solvent which is used to process hydrocarbon fluids. A column is provided having a top end, the top end having an outlet that provides communication between the column and a container. The contaminated solvent is introduced into the column at a first location. At a second location, gas that is obtained from either the column or the container using the solvent from the column is educted into the contaminated solvent so as to drive the foaming contaminants to the top level of the solvent. The contaminants are removed from the top level of the solvent. 
   In accordance with still another aspect of the present invention, the step of removing the contaminants from the top level of the solvent further comprises the step of generating foam so as to push the foam up the column, and allowing a portion of the solvent in the foam to drain back down the column, wherein the foam at the top end of the column has less solvent than the foam that is lower in the column, and pushing the foam out through the outlet and into the container and removing the solvent from the column by way of a location that is below where the gas is injected. 
   In accordance with still another aspect, the present invention further comprises the step of coarsening the foam as it is pushed, whereby the foam becomes drier and easier to shear. 
   In accordance with still another aspect of the present invention, the flow of solvent into the column for educting gas is greater than the flow of solvent into the column at the first location. 
   In accordance with still another aspect of the present invention, there is provided the step of separating immiscible liquid from the solvent as the solvent is introduced into the column. 
   The present invention provides a method of removing foaming contaminants from solvent which is used to process hydrocarbon fluids. A column having a top end, the top end having an outlet that provides communication between the column and a container. The contaminated solvent is introduced into the column. Gas is introduced into the contaminated solvent so as to generate foam in the column, the foam comprising the gas, the solvent and the foaming contaminants. Foam is continued to be generated so as to push the foam up the column. Passing the foam through at least one concentrator so as to dry the foam and form larger bubbles and pushing the foam out through the outlet and into the container. The solvent is removed from the column by way of a location that is below where the gas is injected. 

   
     BRIEF DESCRIPTION OF THE DRAWINGS 
       FIG. 1  is a side view of the apparatus of the present invention, in accordance with a preferred embodiment. 
       FIG. 2  is a cross-sectional view of the liquid-liquid separator. 
       FIG. 3  is a view showing the manufacture of the liquid-liquid separator. 
       FIGS. 4A and 4B  are plan and side views respectively of a concentrator, in accordance with a preferred embodiment. 
       FIGS. 5A and 5B  are plan and side views respectively of a concentrator, in accordance with another embodiment. 
       FIGS. 6A and 6B  are plan and side views respectively of a concentrator, in accordance with another embodiment. 
       FIGS. 7A and 7B  are plan and side views respectively of a concentrator, in accordance with another embodiment. 
       FIGS. 8A and 8B  are plan and side views respectively of a concentrator, in accordance with another embodiment. 
       FIGS. 9A and 9B  are plan and side views respectively of a concentrator, in accordance with another embodiment. 
       FIG. 10  is a side view of the apparatus of the present invention, without a liquid-liquid separator at the solvent input and without a sparger, shown during foaming. 
       FIG. 11  is a side view of the apparatus, with a liquid-liquid separator and a sparger, showing during liquid coalescing. 
   

   DESCRIPTION OF THE PREFERRED EMBODIMENT 
   The present invention is used to remove contaminants, such as surfactants, from solvent that is in turn used to process hydrocarbon gas (such as natural gas). A predecessor system and method was disclosed in my earlier U.S. Pat. No. 6,080,320. The complete disclosure of U.S. Pat. No. 6,080,320 is incorporated by reference herein. 
   Examples of hydrocarbon gas processing units include dehydration units and sweetening units. The present invention can also be used on solvents that are used to process hydrocarbon liquids. 
   Dehydration units and sweetening units have solvent recycling equipment. The solvent recycling equipment takes the rich solvent and removes the moisture or sour contaminants to produce lean solvents. 
   The foam remover apparatus  211  of the present invention can be installed and operated in conjunction with the solvent recycling equipment. As the solvent circulates through the gas-liquid contactor, it takes up contaminants (for example, moisture or sour contaminants) from the gas. The solvent may also take foaming contaminants from the gas. The solvent exits the gas-liquid contactor and enters the solvent recycling equipment. The solvent recycling equipment will remove moisture and sour contaminants from the gas, but not the foaming contaminants. Consequently, some of the solvent is processed by the foam remover apparatus  211  to remove the foaming contaminants. 
   The foam remover apparatus  211  has a first column  213 , a second column  215  and a conduit  217  or carryover connecting the upper ends of the first and second columns  213 ,  215 . 
   The first column  213  has a solvent inlet  219  that is connected to a tap in the solvent recycling system, a gas inlet  221  and a solvent outlet  223 . 
   The solvent inlet  219  is connected to a solvent inlet pump  224 . The pump  224  pumps solvent from the solvent recycling system into the first column. A liquid-liquid separator  225  is located inside of the first column  213  below the liquid level  227 . Referring to  FIG. 2 , the separator  225  has a perforated pipe  229  or tube, one end of which has a fitting  231 . The fitting  231  has a threaded coupling  233  to couple to a wall of the first column  213  and another threaded coupling  235  to couple to the solvent input line  237  (see  FIG. 1 ). The other end of the pipe  229  is closed. The pipe  229  is wrapped with a screen material  239 ,  241 . In the preferred embodiment, the screen  239 ,  241  is a shaved metal or steel wool. Two wraps  239 ,  341  are provided. The wraps of steel wool can have different porosities. For example, the inner wrap  239  can be less porous or finer than the outer wrap  41 . As shown in  FIG. 3 , the screen can be applied by rolling the pipe  229  inside of the sheet of steel wool. Preferably, the steel wool allows solids to flow through in order to prevent the accumulation and eventual blockage of the screen. 
   Referring back to  FIG. 1 , the gas inlet  221  is connected to a sparger  243  located inside of the first column  213  and below the separator  225 . The sparger  243  can be substantially identical to the separator  225 . In the preferred embodiment, gas is educted into the sparger from the second column  215 . The eduction fluid is the solvent, as pumped from the first column  213  in a pump around arrangement. A pump  245  withdraws solvent from a location in the first column  213  that is below the sparger  243 . The pump  245  injects the solvent through an eductor  247  and into the sparger  243 . The gas from the second column  215  is drawn into the eductor via line  249  from the second column  215  and thus into the sparger  243 . 
   The solvent outlet  223  is located below the sparger  243  and may be located at the bottom of the first column  213 . A pump  251  withdraws the clean solvent from the first column  213  and reintroduces it into the solvent recycling system. 
   The first column  213  and the conduit  217  are fitted with one or more concentrators  253 A,  253 B,  253 C, such as coarsening screens. The screens extend across the path of the foam as the foam moves from the first column  213  into the second column  215 . The concentrators are used to modify the foam by drying the foam and by manipulating the bubble size to a more shearable condition. In the preferred embodiment, as shown in  FIG. 1 , three screens are used. The first screen  253 A, closest to the liquid level  227  of the first column  213 , has relatively large perforations. The second screen  253 B, next closest to the liquid level of the first column, has relatively small perforations. The third screen  253 C, closest to the second column, has the largest perforations. 
     FIGS. 4A–9B  schematically illustrate various types of concentrators. In  FIGS. 4A and 4B , the concentrator is an expanded metal grating  255 . ( FIG. 4A  shows a plan view,  FIG. 4B  shows a side or edge view.) The grating  255  is circular in circumference, so as to fit into the conduit  217 . The grating  255  is typically transverse to the path of the foam traversing the conduit  217 , although it need not be so. 
   In  FIGS. 5A and 5B , the concentrator includes an imperforate plate  257  that partially closes the conduit to the passage of foam. The plate does not completely close off the conduit  217 ; the remaining opening is filled with an expanded metal grating  255  or other type of screen (such as is shown in  FIGS. 6A ,  7 A and  9 A). 
   In  FIGS. 6A and 6B , the concentrator is a screen  259  or mesh. The screen  259  may require stiffening elements or supports to span across the conduit  217 . 
   In  FIGS. 7A and 7B , the concentrator is a pack of steel wool  261 . As shown in  FIG. 7B , the pack is thicker than a grating  255  or screen  259 . Supports  263  are provided to contain and support the steel wool inside of the conduit  217 . The steel wool pack drains liquid quite well from the foam passing therethrough. In addition, the bubbles exiting the steel wool pack tend to be small or fine. 
   In  FIGS. 8A and 8B , the concentrator includes helical vanes or baffles  265  that direct the foam along a helical path inside the conduit, thus effectively lengthening the distance the foam must traverse to reach the second column. The longer distance allows the foam to dry more. 
   In  FIGS. 9A and 9B , the concentrator is a metal plate  267  with perforations  269  formed therein (such as by punching or by drilling). 
   Thus, as can be seen by  FIGS. 4A–9B , there are a wide variety of concentrators for drying the foam and changing the bubble size. Other types of concentrators can be used as well. 
   The conduit  217  forms, in the preferred embodiment, an upside down “U”, although other shapes can be utilized. The concentrators drain solvent from the foam. Therefore, the concentrators are located so that the solvent draining therefrom flows into the first column, instead of the second column. 
   A drain line  270  is at the bottom of the second column  215 . A pump  273  recirculates fluid from the drain line  270  to a spray head  271 . Another pump  275  discharges fluid from the drain line  270 . The first column  213  has an opening in the wall at or slightly below the surface level  227 . This opening  278  is connected to a line  277 , which in turn leads to the contaminant discharge. 
   The operation of the apparatus  211  will now be described with respect to  FIG. 10 . The apparatus of  FIG. 10  is not equipped with a liquid-liquid separator  225  or a sparger  243 . 
   The contaminated solvent is pumped into the first column  213  by the pump  224  via the solvent input  219 . The level  227  of liquid solvent  228  in the first column  213  is maintained relatively constant. Above the solvent in the conduit  217  and the second column  215  is gas. A portion of this gas is removed by the line  249  and is educted into the solvent  228  in the first column  213 , wherein gas bubbles  270  are formed in the solvent. The gas is educted using a pumparound arrangement, wherein solvent is removed from the first column  213  and reintroduced by way of the eductor  247 . The pumparound arrangement allows the amount of gas that is introduced into the first column to be independent of the amount of solvent that is introduced into the first column. In the preferred embodiment, the pump around pump  245  pumps more volume than does the solvent inlet pump  224 . For example, the pumparound pump  245  can pump 150 gpm (gallons per minute), while the solvent inlet pump  224  pumps only 5–7 gpm. (These volumes can of course vary depending on the physical size of the apparatus  211 .) This allows for much more gas to be introduced into the solvent to concentrate the foaming contaminants, wherein the efficiency of the apparatus is increased. The eductor  247  functions as a sparger, wherein the gas is injected into the first column  213  in a distributed manner. 
   If the concentration of foaming contaminants in the solvent is high enough, foam will be produced above the solvent surface level  227 . The constant production of foam in the first column  213  forces the foam through the concentrators  253 A,  253 B,  253 C in the conduit  217  and into the second column  215 . As the foam rises and passes through the concentrators  253 A,  253 B,  253 C, the foam is coarsened, wherein it is dried due to the increased residency time in the first column and due to the foam contacting draining structure on the concentrators. As the foam passes through a concentrator, such as a screen  259  (see  FIG. 6A ), some of the liquid in the foam contacts the screen mesh and is drawn by gravity down along the mesh to the wall of the conduit  217  and from there drains into the reservoir of solvent in the first column. Thus, the concentrators should be angled with respect to the horizontal in order to allow this draining function to occur. The first concentrator  253 A has relatively large perforations so that the foam emerging from the first concentrator has coarser, or larger bubbles, than the foam that is just below the first concentrator. Foam with relatively large bubbles drains or dries quicker than does foam with relatively small bubbles. This coarsened foam then proceeds to the second concentrator  253 B, which concentrator has smaller perforations than does the first concentrator. As the foam passes through the second concentrator, the foam again is dried because some of the liquid in the foam will contact the solid elements of the concentrator and be drained to the wall of the conduit. The foam that emerges from the second concentrator  253 B is somewhat finer due to the finer perforations of the second screen. Providing a concentrator with fine perforations produces a drier foam. The foam then proceeds through the conduit and enters the third concentrator  253 C, which has relatively large perforations. Again the foam is dried. The foam that emerges from the third concentrator has relatively large bubbles. The combination of large bubbles in the foam and a relatively dry foam (because much of the liquid has been drained away by the concentrators) produces a foam that can be easily sheared. The foam continues on through the conduit where it enters the second column  215 . A spray head  271  sprays solvent obtained from the bottom of the second column  215  onto the foam. The liquid spray shears the foam and causes any remaining solvent and foaming contaminants in the foam to fall to the bottom of the second column. This liquid in the bottom of the second column is recirculated by the pump  273  back up to the spray head. In addition, some of the liquid is periodically removed from the second column  215  and discharged by the discharge pump  275 . 
   The concentrators  253  are located so as to drain solvent into the first column. The number, spacing and type of concentrators can vary from the example described herein. 
   The apparatus  211  thus effectively removes the foaming contaminants from the solvent and does so with a minimal waste of solvent. The foaming contaminants will eventually be removed from the solvent to the point of such a low concentration wherein the foaming can no longer be sustained in the conduit  217 . Even though foaming can no longer be sustained, the solvent still is likely to have foaming contaminants. These foaming contaminants, even at low concentrations, can adversely affect the mass transfer in the hydrocarbon fluid processing. 
   The invention can further reduce the concentration of foaming contaminants in the solvent, wherein the mass transfer efficiency of the solvent is increased. The solvent continues to be introduced into the apparatus  211  for further removal of foaming contaminants. The introduction of gas into the solvent by the eductor  247  concentrates the foaming contaminants at or near the surface level  227  of the solvent. The drain line  277  has an opening  278  located at the surface level of the solvent in the first column. From time to time, a valve in the drain line  277  is opened and some of the liquid (containing the foaming contaminants and some solvent) is discharged through the drain line  277 . In this manner, the concentration of foaming contaminants in the solvent can be further reduced, thereby increasing the efficiency of mass transfer of the solvent in a gas-liquid contactor during hydrocarbon processing. 
     FIG. 11  shows the apparatus  211  in accordance with another embodiment, wherein the liquid-liquid separator  225  and sparger  243  are provided. If the solvent contains any immiscible liquids, such as oil, then preferably these liquids should be cleaned from the solvent. The solvent is injected into the first column  213  via the liquid-liquid separator  225 , which separator coalesces the contaminant liquids such as oil. In addition, the pumparound sparger  243  acts as a liquid-liquid separator. In fact, because the flow rate through the sparger  243  is higher than through the separator  225 , much of the contaminant liquids are likely to be separated by the sparger. 
   The solvent and immiscible liquid enters the pipe  229  of the separator  225 ,  243  and passes through the steel wool. The oil droplets are slowed from impacting the wire structure of the steel wool. The slowed oil droplets are impacted by other oil droplets, wherein the droplets coalesce. Some of the droplets do not impact the wire structure and pass through to a turbulent zone, where the oil droplets coalesce by impact. Once coalesced, the droplets settle or migrate to the surface level  227 . The gas bubbles assist in the surface migration. The drain line  277  can be opened to remove the liquid contaminants from the surface level  227 . 
   The foregoing disclosure and showings made in the drawings are merely illustrative of the principles of this invention and are not to be interpreted in a limiting sense.