Patent Abstract:
Petroleum solvent vapors which discharge from a dry cleaning dryer in a heated gaseous mixture of vapors and air are condensed and recovered, and heat energy is recovered for productive use elsewhere. The gaseous mixture of vapors and air is sprayed with relatively cool water to condense the solvent vapors. The resulting liquid mixture of water and solvent is withdrawn from the spray chamber and is subjected to gravitational separation. Water reclaimed in the separation process is reused in the spray chamber. Recovered solvent is reused in a dry cleaning washer. The gravitational separation process is preferably carried out in a series of gravitational separators, and heat is withdrawn from at least one of the separation units for productive use in a heat consuming device.

Full Description:
BACKGROUND OF THE INVENTION 
     1. Field of the Invention 
     The present invention relates generally to dry cleaning systems, and more particularly to a dry cleaning system wherein petroleum solvent vapors discharging from a dry cleaning dryer are condensed and the condensed solvent vapors are separated from a condensing liquid so the liquid solvent may be reused. 
     2. Prior Art 
     There are two distinct types of solvents used in the dry cleaning industry, namely &#34;synthetic solvents&#34; and &#34;petroleum solvents.&#34; The so-called &#34;synthetic solvents&#34; are halogenated hydrocarbons such as perchloroethylene, 1,1,2-trichloro-1,2,2-trifluoroethane (Freon 113), trichlorethylene, carbon tetrachloride, and the like. The so-called &#34;petroleum solvents&#34; are petroleum distillate fractions and have been categorized by the International Fabricare Institute as being of various types including Stoddard solvents, solvents meeting &#34;140-F&#34; specifications, odorless solvents, low end point solvents and the like. Due to its acceptance in the industry, the term &#34;petroleum solvent&#34; is here intended to include petroleum distillate fractions used as dry cleaning solvents while the term &#34;synthetic solvent&#34; is intended to include halogenated or similarly treated hydrocarbons used as dry cleaning solvents. 
     The synthetic solvents are characteristically expensive and have, in the prior art, been reclaimed by condensing solvent vapors for reuse as disclosed in U.S. Pat. Nos. RE 19,986 and 3,110,544. Condensation units designed to reclaim synthetic solvents are expensive systems normally incorporating substantial lengths of cold water condensing coils. Petroleum solvents, on the other hand, are substantially less expensive and their vapors have been discarded, although the condensation and recovery thereof is suggested in U.S. Pat. No. 1,795,006. The accepted practice of discarding petroleum solvent vapors is a substantial waste of a valuable chemical resource. 
     In addition to the problem that venting solvent vapors to the atmosphere is wasteful, it also creates an air pollution problem. Yet, at present, the only commercially available solutions to the recovery of petroleum solvent vapors require the use of either carbon absorption units or the use of the same condensation type reclamation units that are used to recover synthetic solvent vapors. Both of these solutions are regarded by the industry as far too expensive to warrant adoption for the recovery of petroleum solvent vapors. While the air pollution problem could conceivably be resolved by burning the vapors, this solution is unproven and could create additional unforeseeable air pollution problems. Moreover, burning the vapors provides no recovery of the solvent for reuse. 
     Still another drawback of present day systems which discharge heated mixtures of petroleum solvent vapors and air to the atmosphere is that no recovery is made of the substantial amount of heat energy in these mixtures. Much heat energy is wasted by these systems. 
     SUMMARY OF THE INVENTION 
     The present invention overcomes the foregoing and other drawbacks of prior proposals, and provides a relatively inexpensive technique for recovering valuable petroleum solvent and heat energy from gaseous mixtures discharged from dry cleaning dryers, and for concomitantly reducing the amount of vented petroleum solvent vapors thereby minimizing airborne contaminates. 
     In the preferred practice of the present invention, the mixture of hot air and petroleum solvent vapors which discharges from a dry cleaning dryer is passed through a lint remover and into a spray chamber where relatively cool water is sprayed into the heated gaseous mixture. The solvent vapors condense and form, with the water, a liquid mixture. As the vapors condense, they sacrifice heat to the liquid mixture. Vented from the spray chamber is a cooled gaseous mixture of air, water vapor and a very small quantity of solvent vapor. Withdrawn from the spray chamber is a heated liquid mixture of water and solvent. 
     The water-solvent mixture gravitates into a primary gravitational separator which is of significant volume and provides a long residence time in an environment with a low vertical liquid velocity. Due to the specific gravity difference between water and the solvent, the liquid components separate quite readily into an upper solvent layer and a lower water layer. Due to the long residence time in the primary separator, such particulates as may remain in the water-solvent mixture following lint filtration drop out in the primary separator and can be periodically removed. The solvent eventually accumulates in the primary separator so that its level rises to a solvent outlet and passes into a secondary separator where additional water and/or particulates are allowed to drop out of suspension. Solvent from the secondary separator is delivered into a storage tank and is ultimately returned to a dry cleaning washer for reuse. 
     Spray water is recycled after being collected in the primary separator. Due to a loss of water vapor from the spray chamber, additional make-up water is added to the spray system as needed. The need for additional water is sensed by determining the water level in the primary separator. 
     Heat energy is withdrawn from the liquid water-solvent mixture via a heat exchange coil located in the primary separator. Ambient temperature water is circulated through the heat exchange oil and is heated by the mixture for productive use in a suitable heat consuming device. The recovered heat energy can be used to pre-heat wash water or for any other suitable heat consuming use. 
     As will be apparent from the foregoing summary, it is a general object of the present invention to provide a novel and improved dry cleaning system featuring recovery of petroleum solvent vapors discharged from one or more petroleum solvent dryers. 
     Other objects and a fuller understanding of the invention may be had by referring to the following description and claims taken in conjunction with the accompanying drawings. 
    
    
     BRIEF DESCRIPTION OF THE DRAWINGS 
     FIG. 1 is a schematic illustration, partly in cross-section and partly in elevation, of a dry cleaning system embodying certain features of the preferred practice of the present invention; and, 
     FIG. 2 is an enlarged sectional view of a portion of a spray chamber illustrated in FIG. 1, as seen substantially from a plane indicated by a line 2--2 in FIG. 1. 
    
    
     DESCRIPTION OF THE PREFERRED EMBODIMENT 
     Referring to FIG. 1, a dry cleaning system 4 includes a dry cleaning washer 6, a dry cleaning dryer 8, a lint collector 10, and a petroleum solvent recovery system indicated generally by the numeral 12. 
     The washer, dryer, and lint collector units 6, 8, 10 are conventional, commercially available apparatus. A suitable washer is sold by Washex Machinery Corporation of Wichita Falls, Tex. 76306, under the model designation 500FPA. A suitable dryer is sold by Challenge-Cook Brothers, Inc. of Industry, Calif. 91745, under the model designation DFSD-4.  A suitable line removal unit is sold by ECI Air-Flyte Corporation of Fairfield, N.J. 07006. 
     The washer 6 includes an enclosure 14 which houses a perforated drum 15 into which fabrics may be loaded for washing in the presence of a petroleum solvent. A suitable door 16 provides access to the drum 15. At the inception of a dry cleaning washing cycle, a liquid petroleum dry cleaning solvent is admitted into the enclosure 14 through a suitable fitting 18. At the end of the washing cycle, liquid is drawn off through a valved conduit 19 and the load extracted to a damp condition with liquid returning to a liquid solvent treating unit 20. 
     The dryer 8 includes an enclosure 21 which houses a perforate drum 22 into which washed and solvent-extracted fabrics are loaded for vaporizing the remaining solvent. A suitable door 23 provides access to the drum 22. An air inlet 24 communicates the interior of the enclosure 21 with the atmosphere. 
     During a drying cycle, a fan 30 draws air into the enclosure 21 through the inlet 24. Air passing through the inlet 24 is heated, by any suitable means, such as a steam coil 32, to evaporate liquid solvent remaining or sorbed on fabric in the drum 22. A mixture of hot air and hot solvent vapor exits from the dryer 8 through a conduit 34 and through the lint removal unit 10. 
     The temperature of the heated air passing through the dryer 8 during the drying cycle depends on the boiling point of the solvent employed. Typical temperatures are in the range of 120°-170° F which is sufficient to rapidly evaporate liquid solvent. 
     A typical 400 pound load petroleum solvent dryer exhausts a mixture of hot air-solvent vapor at a range of 9,000-12,000 cubic feet per minute and exhausts about 12 gallons of solvent vapor to the atmosphere during each complete cycle of operation. Because a typical dryer operates at about two cycles per hour, it will be evident that there is delivered to the atmosphere a considerable quantity of hydrocarbon vapor which constitutes an air pollution problem and which can be valuable if recovered. Moreover, the exhausted solvent vapor and air mixture carries with it a substantial amount of heat energy which could be used productively if reclaimed. 
     The conduit 34 delivers the hot air-solvent vapor mixture from the dryer 8 through the lint collection unit 10 to the solvent vapor recovery system 12. The system 12 has a spray chamber 40 including a large receptacle 41 having an upwardly directed atmospheric vent 42 immediately above a baffle plate 44, a downwardly directed liquid outlet 46, and a plurality of spray heads 48 for spraying a condensing liquid such as water into the chamber 40. The spray heads 48 may be of any suitable type and are illustrated in FIG. 2 as comprising an upright conduit 50 connected to a cross conduit 52. A plurality of spray openings 54 are provided in the cross conduit 52. The upright conduits 50 are sealed against the bottom of the receptacle 41 by suitable connectors 56. 
     A major factor affecting operational efficiency of the spray chamber 40 is its operating temperature. Naturally, the inlet temperature will approach the drying temperature of the dryer 8. In a typical design, the temperature of the exhaust gases exiting through the vent 42 will be in the range of 70° to 170° F. The inlet temperature of the condensing liquid also substantially affects efficiency of the spray chamber 40. Desirably, inlet water temperature is in the range of 80° to 85°. 
     Another major factor affecting operational efficiency in the chamber 40 is the tendency for condensed solvent to separate from air and water vapor flowing therethrough. Accordingly, the spray chamber 40 should be of sufficient size so that the upward gas velocity toward the gas outlet 42 is sufficiently low to allow any liquid droplets formed by the condensing solvent vapor to drop out of suspension by gravity. In general, gas velocities on the order of 5 to 10 feet per second are necessary to move liquid droplets vertically. Consequently, the horizontal cross-sectional area of the chamber 50 should be sufficient to lower the upward gas velocity substantially below 5 feet per second. In an installation designed to handle 9,000 cubic feet per minute of air-solvent vapor mixture, a spray chamber 8 feet × 8 feet × 8 feet will reduce the gas velocity substantially below 2.5 feet per second. Accordingly, any liquid solvent droplets will fall out of suspension and, because of the inclined floor of the chamber 40, these droplets will gravitate to the liquid outlet 46. 
     A liquid drainpipe 58 extends from the liquid outlet 46 into the interior of a primary separator 60. The primary separator 60 may be of the centrifugal variety but is preferably of the gravitational type. The drainpipe 58 preferably extends below the normal water level 62 in the gravitational separator 60 and desirably has a downwardly inclined discharge end 64 to spread the effluent mixture across the cross-sectional area of the separator 60 to prevent particulate buildup immediately below the discharge end 64. The primary separator 60 comprises a vessel 66 of significant height and sufficient cross-sectional area to allow gravitational separation of water and solvent into distinct layers 68, 70 respectively. The vessel 66 provides an upwardly opening atmospheric vent or outlet 72, a water outlet 74 toward the bottom thereof, and a solvent outlet 76 in an upper sidewall portion thereof. A valved conduit 78 opens into the interior of the vessel 66 below the water outlet 74 for removing accumulated particulates as by dumping to a suitable sewer connection. 
     The size of the solvent recovery system 12, including such components as the spray chamber 40 and the vessel 66, depends on the total output of the number of dryers 8 which feed air and solvent vapor mixtures into the chamber 40 for separation. As will be apparent, the vessel 66 will be required to handle a large quantity of liquid if several large capacity dryers feed into the chamber 40, and will be required to handle a much smaller quantity of liquid if only a single, small capacity dryer feeds into the chamber 40. As will be explained more fully hereinafter in conjunction with a water circulation system 80, a typical installation for a 400 pound petroleum solvent unit as previously discussed will require the delivery of 50 to 75 gallons per minute of water through the circulation system 80, depending on the temperature of the delivered water. Accordingly, the vessel 66 may be on the order of 1500 to 2000 gallons working capacity. 
     The water circulation system 80 includes a pump 82 of sufficient size to handle the requisite quantity of condensing liquid. The pump 82 has an inlet in communication with the water outlet 74, and has an outlet in communication with a conduit 84. The cnduit 84 communicates with a liquid manifold 86 having a leg 88 extending in communication with the vertical conduits 50 of the spray heads 48. 
     Because a significant quantity of water is lost in the form of vented vapor, it is necessary to periodically add water to the system. To this end, a water make-up line 89 is connected from a suitable source to the conduit 84 and is provided with a liquid level conduit valve 90. The valve 90 is operated in any suitable fashion, as by the provision of a float 92 having a density less than water but greater than that of the petroleum solvent being recovered. The float 92 operates through any suitable control linkage 94 sealed against the vessel 66 by a suitable connector 96. As the water level 62 is lowered, as naturally occurs due to the loss of vented water vapor in the spray chamber 40, the float 92 is caused to move downwardly thereby opening the valve 90 and delivering make-up water into the conduit 84. As soon as the water level 62 rises to an appropriate level, the float 92 acts through the linkage 94 to close the valve 90. 
     Make-up water is preferably delivered into the conduit 84 rather than into the separator 60 for several reasons. First, the condensing efficiency in the spray chamber 40 depends, to a substantial extent, on the temperature of water delivered through the spray heads 48. By adding make-up water to the conduit 84, it is evident that the temperatures of delivered water is as low as possible. Second, as will be discussed hereinafter in conjunction with a heat recovery system 98, it is desired to remove significant quantities of heat from liquid in the vessel 66. Consequently, it would be selfdefeating to admit relatively cool water into the separator 60. 
     The solvent outlet 76 of the primary separator 60 is connected by a drainpipe 100 to the lower end of a secondary separator 102. The secondary separator 102 may be of the centrifugal type but is preferably gravitational, permitting additional separation between a solvent layer 104 and a water layer 106 to occur. The secondary separator 102 comprises a much smaller vessel 108 than is used in the primary separator 60. The vessel 108 is provided with an atmospheric vent 110, a valved water-sediment outlet 112 for connection to a sewer line, a solvent outlet 114, and a suitable sight glass 116 for visually locating the water level 118. The sight glass 116 allows an operator to drain water from the vessel 108 when the water level 118 becomes too high. 
     If only one dryer 8 is incorporated in the dry cleaning system 4, the quantity of liquid handled by the secondary separator 102 is rather small. Assuming a loss of 12 gallons of petroleum solvent in vapor form per operation cycle, two cycles per hour, 70% recovery efficiency in the spray chamber 40 and 90% separation efficiency in the primary separator 60, a total quantity of liquid handled by the separator 102 will be less than about 20 gallons per hour. Accordingly, a 30 gallon working capacity separator will provide a residence time of greater than 1.5 hours in the vessel 108. 
     The solvent outlet 114 is connected through a suitable conduit 120 to a solvent storage tank 122 which may be above or below ground and which is in turn connected by a suitable conduit 124 to a solvent pump 126. An atmospheric vent 127 is provided in the top of the tank 122. The solvent pump 126 is adapted to receive liquid solvent from a solvent tank 128 which forms part of the liquid solvent treating system 20. The solvent tank 128 has a valved outlet 130 for periodically removing sediment from the tank&#39;s bottom. The solvent pump 126 is arranged to deliver liquid solvent through a conduit 132 to the solvent inlet fitting 18 of the washer 6. A valve 134 is interposed in the conduit 132. 
     It should be evident that the liquid solvent treating system 20 may be more sophisticated than a simple settling tank. Specifically, a conventional still (not shown) may be provided to distill a portion or all of the liquid solvent accumulating in either of the storage tanks 122, 128. 
     The heat recovery system 98 comprises an inlet line 144, a heat exchange coil 160, and an outlet line 168. The components 144, 160, 168 can form part of a closed circulation heat exchange system, but are shown in FIG. 1 as comprising a system for pre-heating inlet water for a water heater 146. In the embodiment of FIG. 1, the inlet line 144 is connected to a source of pressurized water, and the outlet line 168 feeds water to the hot water heater 146. Water which has been heated in the hot water heater 146 exits through a supply line 170. While the hot water heater 146 has been shown in FIG. 1, it will be understood that the heat using device 146 may be of any desired type. 
     The inlet conduit 144 extends through the wall of the vessel 66 and connects to an inlet leg 158 of the heat exchange coil 160 of any suitable type preferably having a plurality of heat exchange fins 162 thereon. The coil 160 has an outlet leg 164 extending through the wall of the vessel 66. The inlet and outlet legs 158, 164 are sealed to the wall of the vessel 66 by suitable connectors 166. A suitable conduit 168 delivers partially heated water from the coil 160 to the hot water heater 146. 
     Because the water layer 68 in the separator 60 is at an elevated temperature, it will be apparent that preheating of the water supply to the hot water heater 146 occurs. It will also be apparent that preheating of water delivered to the water heater 146 acts to lower the temperature of liquid in the vessel 66, thereby lowering the temperature of water delivered to the spray heads 48. Because recovery efficiency in the chamber 40 is partially dependent on inlet water temperature, it will be seen that withdrawing heat from the separator 60 acts to increase efficiency of the solvent vapor recovery system 12. 
     While it is ordinarily desirable to conduct the lint separation and solvent-vapor recovery steps in separate and distinct operations, these steps can be combined and carried out utilizing the spray chamber 40 for both functions. If lint remains in the mixture of solvent and air vapor which enters the chamber 40, the spray water impinging on it will cause it to settle to the bottom of the chamber 40. A screening chamber 198 can be provided in the conduit 58 and an accessibly removable screen 200 can be inserted within the chamber 198 to collect the lint. 
     Although the invention has been described in its preferred forms with a certain degree of particularity, it is understood that the present disclosure of the preferred forms has been made only by way of example and numerous changes in the details of construction and the combination and arrangement of parts may be resorted to without departing from the spirit and the scope of the invention as hereinafter claimed. It is intended that the patent shall cover, by suitable expression in the appended claims, whatever features of patentable novelty exist in the invention disclosed.

Technology Classification (CPC): 3