Method for delivery of a vapor phase product to a point of use

Abstract: Provided are a novel system and method for delivery of a vapor phase product to a point of use, as well as a novel on-site chemical distribution system and method. The system for delivery of a vapor phase product includes a storage vessel containing a liquid chemical under its own vapor pressure, a column connected to receive the chemical in liquified state from the storage vessel, wherein the chemical is fractionated into a contaminated liquid heavy fraction and a purified light vapor fraction and a conduit connected to the column for removing the purified light vapor fraction therefrom. The system is connected to the point of use for introducing the purified vapor fraction thereto. Particular applicability is found in semiconductor manufacturing in the delivery of electronics specialty gases to one or more semiconductor processing tools.

Description: BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a system and a method for delivery of a vapor phase product to a point of use. The present invention also relates to an on-site chemical distribution system and to a method for on-site distribution of a chemical. The invention has particular applicability in the delivery of electronics specialty gases used in the manufacture of semiconductor devices to one or more semiconductor processing tools. 2. Description of the Related Art In the semiconductor manufacturing industry, different chemicals are supplied to processing tools in gaseous form for carrying out a variety of semiconductor fabrication processes. Examples of such processes include diffusion, chemical vapor deposition (CVD), etching, sputtering and ion implantation. These chemicals are conventionally referred to as electronics specialty gases (ESG's). Many of the chemicals employed in the above processes, while introduced to the processing tools in the gaseous state, are stored as liquids under their own respective vapor pressures. Typically, the liquid chemicals have room temperature vapor pressures greater than atmospheric pressure. These chemicals are conventionally stored in gas cylinders which are housed within gas cabinets. A typical volume of such a gas cylinder is less than about 50 liters. A partial list of chemicals stored in this manner, the pressures under which they are stored and their critical pressures are provided below in Table 1: Chemical Formula Vapor Pressure of Gas at 20 C (psia) Critical Pressure (psia) Ammonia NH 3 129 1636 Boron Trichloride BCl 3 19 1071 Carbon Dioxide CO 2 845 1118 Chlorine Cl 2 100 634.7 Chlorotrifluoride ClF 3 26.1 837.4 Dichlorosilane SiH 2 Cl 2 24 746.6 Disilane Si 2 H 6 48 956.9 Hydrogen Bromide HBr 335 1240 Hydrogen Chloride HCl 628 1198 Hydrogen Fluoride HF 16 940.2 Nitrous Oxide N 2 O 760 1050 Perfluoropropane C 3 F 8 115 388.5 Sulfur Hexafluoride SF 6 335 545.0 Tungsten Hexafluoride WF 6 16 619.1 A single gas cabinet typically supplies the chemical vapor to a single or at most several semiconductor processing tools. Operation of the gas cabinets and the cylinders housed therein can be a hazardous, labor intensive and costly activity. As the chemical is depleted, it is imperative that the gas cylinder be replaced with careful and proper handling procedures. In order to reduce the total number of gas cabinets required in the semiconductor manufacturing facility, it has recently been proposed that a single gas cabinet service multiple processing tools. Since the volumes of the cylinders housed in the gas cabinets do not increase with the number of processing tools being serviced, replacement frequency of the cylinders in the cabinets necessarily increases. It is, however, desirable to minimize the frequency of cylinder replacement, not only for safety concerns but also to reduce the risk of introducing impurities that may cause significant product loss. In addition to increasing the frequency of gas cylinder replacement, the instantaneous flowrate of the gas being withdrawn from each cylinder increases with the additional processing tools serviced by a given gas cabinet. Such an increase in flowrate can lead to the presence of entrained liquid droplets in the gas stream, which can result in flowrate fluctuations, accelerated corrosion and premature failure of flow control components in the gas distribution system. Furthermore, the corrosion products can lead to contamination of the highly pure process gases. This contamination can have deleterious effects on the processes being run, and ultimately on the manufactured semiconductor devices. It is known from EP-A-452 493 a method to avoid moisture contamination of high purity gases by using pipes and valves systems without organic material to flow these gases. To meet the requirements of the semiconductor processing industry and to overcome the disadvantages of the related art, it is an object of the present invention to provide novel systems for delivery of a chemical stored as a liquid under its own vapor pressure. The systems make possible the simultaneous servicing of multiple processing tools and additionally can perform a purification function, whereby highly pure gases useful in semiconductor manufacture can be produced. Because of such purification function, the systems make possible the use of a relatively low purity starting material, which material would otherwise not be useful, for example, in semiconductor manufacturing. According to one aspect of the invention, entrained liquid droplets in the gas obtained from the liquid chemical can be minimized or eliminated. As a result, single phase process gas flow can be obtained, in contrast to known systems and methods. It is a further object of the present invention to provide novel methods for delivery of a chemical stored as a liquid under its own vapor pressure, which methods can be practiced on the inventive systems. It is a further object of the present invention to provide a novel on-site chemical distribution system, and a method for on-site chemical distribution which method can be practiced on the system. SUMMARY OF THE INVENTION The foregoing objectives are met by the method in accordance with claim 1. According to the present invention, a storage vessel contains a liquid chemical under its own vapor pressure. A column is connected to receive the chemical in liquified state from the storage vessel, wherein the chemical is fractionated into a contaminated liquid heavy fraction and a purified light vapor fraction. A conduit is connected to the column for removing the purified light vapor fraction therefrom, wherein the system is connected to the point of use for introducing the purified vapor fraction thereto. The method of the invention has particular applicability in the delivery of an electronics specialty gas to one or more points of use in a semiconductor manufacturing facility, for example to one or more semiconductor processing tools. BRIEF DESCRIPTION OF THE DRAWINGS The objects and advantages of the invention will become apparent from the following detailed description of the preferred embodiments thereof in connection with the accompanying drawings, in which: FIG. 1 is a schematic diagram of a system for delivery of a vapor phase product in accordance with one aspect of the invention; FIG. 2 is a schematic diagram of a system for delivery of a vapor phase product in accordance with a further aspect of the invention; FIG. 3 is a schematic diagram of a system for delivery of a vapor phase product in accordance a further aspect of the invention; FIG. 4 is a schematic diagram of a system for delivery of a vapor phase product in accordance a further aspect of the invention; and FIG. 5 is a schematic diagram of on-site chemical distribution system in accordance with a further aspect of the invention. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS OF THE INVENTION The present invention provides an effective way to provide a high purity chemical which is stored as a liquid under its own vapor pressure to one or more points of use, for example, processing tools used in the fabrication of semiconductor devices. As used herein, the term "a liquid chemical under its own vapor pressure" means a chemical, which at ambient conditions would be in the gas phase, has had its temperature and/or pressure modified such that it is in its liquid state at or near (i.e., within about +5 C of) its boiling point. With reference to FIG. 1, a preferred embodiment of the inventive system and method will be described. The system includes a storage vessel 1 which contains a chemical stored as a liquid under its own vapor pressure. The liquid chemical can be generated on-site and stored in a bulk storage vessel or, more typically, the liquid chemical is delivered to the use site via bulk transport vessel, for example, a tube trailer. Storage vessel 1 preferably has an internal volume of greater than about 100 liters, preferably from about 200 to 60,000 liters. Sizing of the components and the flowrates involved are not to be limited, but depend on the specific application involved. The specific liquid chemical contained in storage vessel 1 is dependent on, for example, the processing tools being serviced and the processes being run therein. In semiconductor manufacturing processes, typical liquid chemicals include those electronics specialty gases (ESG's) specified in Table 1 above, i.e., ammonia (NH 3 ), boron trichloride (BCl 3 ), carbon dioxide (CO 2 ), chlorine (Cl 2 ), chlorotrifluoride (ClF 3 ) dichlorosilane (SiH 2 Cl 2 ), disilane (Si 2 H 6 ), hydrogen bromide (HBr), hydrogen chloride (HCl), hydrogen fluoride (HF), nitrous oxide (N 2 O),perfluoropropane (C 3 F 8 ), sulfur hexafluoride (SF 6 ), trichlorosilane (SiHCl 3 ), and tungsten hexafluoride (WF 6 ). Additional ESG's include, for example, the class of materials known as perfluorocarbons (PFC's). For electronics manufacturing applications, it is desirable that storage vessel 1 be compatible with the liquid chemical contained therein and with the high purities required in the manufacturing process. The storage vessel is preferably constructed of stainless steel and can be surface treated, for example, by mechanical polishing or electropolishing and passivation. The liquid chemical contained in the storage vessel is preferably of high purity. However, because of the purification function of the system and method, the liquid chemical purity can be relatively low compared with conventional practice. Storage vessel 1 is connected to a conduit 2 for transferring the chemical in liquified form from the storage vessel to other components of the system. Suitable materials of construction for liquid transferring conduit 2 and other conduits which contact the chemical in liquified form generally include but are not limited to, 316 stainless steel. The specific material selected, however, will depend upon the specific liquid chemical being used. Flowrates throughout the system will depend on the specific applications involved, and the system is preferably designed around the flowrate requirements. A high purity block, bleed and purge system 3 can be disposed downstream of the point of connection of storage vessel 1 to conduit 2. The purpose of the block, bleed and purge system 3 is to ensure that contaminants are not introduced into the system during replacement of storage vessel 1. In the exemplified embodiment, block, bleed and purge system 3 includes a high purity inert purge gas source 4, such as nitrogen, argon or helium, for the removal of ambient contaminants and for the removal of residual chemicals in the system during replacement of storage vessel 1. Preferably, a nitrogen-driven venturi purge system is employed for this purpose. A purge gas line 5 is connected to conduit 2 downstream of the point of connection of storage vessel 1. The purge gas is typically bled off through a bleed line 6, which can be connected to a waste treatment unit 7 for further processing. Depending upon the specific chemical employed, waste treatment unit 7 can comprise, for example, a unit for adsorption, scrubbing, thermal decomposition, storage or a combination thereof. To reduce the quantity of liquid chemical and/or contaminated purge gas that is sent to waste treatment unit 7, it is desirable to minimize the volume of block, bleed and purge system 3. Control of the gas flow in block, bleed and purge system 3 can be accomplished by manipulation of valves V1 and V2 in conduit 2, valve V3 in purge gas line 5 and valve V4 in bleed line 6. The system can be further integrated with a cycling valve, so that removal of ambient contaminants or residual chemical can be accomplished through a series of pressure-vacuum cycles. Flow control throughout the system, including operation of block, bleed and purge system 3, can be automated with a controller 8. Suitable control means are known in the art, and include, for example, one or more programmable logic controllers (PLCs) or microprocessors. After connection of storage vessel 1 to the system and purging, the liquid chemical can be transported through the system from the storage vessel, in liquified form, into a column 9, which is in fluid communication with the storage vessel. The liquid chemical is introduced into the column at an intermediate point thereof. Flow of the chemical into the column can be aided by use of a pump 10, such as a positive displacement pump. A redundant pump is preferably provided in case pump 10 should fail. The inlet of pump 10 is preferably connected as closely as possible to the purge block to minimize pressure losses on the suction side. The outlet of pump 10 is connected to a conduit 11 through which the liquid chemical is transported to column 9. Depending on the nature of the impurities to be removed and the degree of purification desired, it may be desirable to employ a plurality of columns. Where multiple columns are used, they may be disposed in series or in parallel. Multiple column systems are further described below in reference to FIG. 2. Various types of columns are envisioned for use with the invention. The column should allow intimate contact between liquid and vapor phases, whereby a purified vapor can be obtained therefrom. Suitable columns include, for example, distillation, absorption and adsorption columns, and chemical conversion/reaction units of the trace impurity or impurities. Where multiple columns are employed, the columns can be of the same or a different type. The column typically contains one or more liquid-vapor phase contact promoting devices, such as structured, ordered and random packing materials, or sieve, bubble-cap, valve, Kittel plate, flexitray, shower trays and other special tray designs, to provide for a high degree of contact between the liquid and vapor phases in the column. Of these liquid-vapor phase contact promoting devices, randomly packed column and bubble-cap are preferred. Suitable packing materials are known in the art, and include, for example, Rachig rings, Lessing Rings, Berl saddles, spiral partition rings and grid packing. Suitable materials of construction for the packing materials include, for example, glass, quartz, ceramics and stainless steel. Choice of the packing type and material of construction is dependent on factors, such as the chemical being purified and its mass flow rate. Where an adsorbent is to be employed in the column, the particular adsorbent and amount thereof will depend on the particular chemical being treated, as well as the impurity or impurities to be removed. Typical adsorbents include, for example, ascerite for CO 2 removal from N 2 O, metal impregnated carbons for sulfur compound removal from CO 2 , activated carbons for removal of volatile hydrocarbons, and molecular sieves, alumina and silica based products. Where trays are employed in the purification column, the trays are typically constructed of stainless steel. The total number of trays will depend on the specific chemical being treated and the nature and concentration of impurities therein, as well as the degree of purification desired. Liquid feed to column 9 can be controlled by use of a controller 8. The controller description set forth above applies also to the liquid feed controller, and to each of the controllers to be described below. Thus, while FIG. 1 illustrates a single controller for controlling various aspects of the system, the use of multiple controllers is also envisioned. The controller can operate, for example, based on input from a level sensor/transmitter 24 which monitors the liquid chemical level at the bottom of column 9. The controller can turn on and off pump 10 as required to maintain the liquid chemical level at the bottom of the column at a desired, predetermined level. The level sensor/transmitter can be, for example, a differential pressure gauge, a flat or other known means to measure the liquid level in the column. The liquid level sensor/transmitter is preferably in communication with pump 10 via controller 8 to control the liquid level in the column. While the pressure and temperature maintained in the column will vary depending on the specific liquid chemical being treated and the nature of the impurities therein, column 9 preferably operates at a pressure of from about 1 to 100 bar, more preferably from about 5 to 20 bar, and at a temperature of from about -200 to 300 C, more preferably from about -40 to 150 C. The liquid chemical introduced into the column is fractionated into a contaminated liquid heavy fraction, and a light vapor fraction. As used herein, the term "heavy fraction" refers to a stream removed from a portion of a column below the liquid feed stage. The heavy product is in a liquid state, and is preferably removed from the bottom of the column. Also as used herein, the term "light vapor fraction" refers to a stream removed from a portion of a column above a feed stage. The light vapor product is preferably removed from the top of the column. At least a portion of the contaminated liquid heavy fraction is converted into a saturated vapor in reboiler/vaporizer 12. The saturated vapor is returned to column 9 through a conduit 13, connected to the column at a point below conduit 11. In this way, the saturated vapor and the liquid chemical introduced into column 9 can contact each other intimately in a countercurrent manner. A high purity vapor thereby can be produced. Conduit 18 is connected to the column at a point above conduit 11, preferably at the top of the column, for removing the high purity vapor therefrom. The high purity vapor stream has a purity compatible with semiconductor manufacturing processing, preferably in the ppm or sub-ppm range. The heat duty Q in for vaporizer 12 can be provided by a heat source, such as an electric heater for direct heat input or a heating medium stream, for example, water, glycol solution, halocarbon fluids, or other heat transfer fluids which are known to those skilled in the art. Residual contaminated liquid in the vaporizer can be periodically drained therefrom through vaporizer purge line 14. Such purging can help to minimize the concentration of the heavier, i.e., high boiling, components in the saturated vapor. The removed contaminated liquid can be introduced into a holding vessel 15, which can be periodically drained using pump 16. This waste material can be sent to a waste treatment unit and/or can be pumped into a container for shipment back to the chemical supplier for purification and reuse. Various aspects of the operation of vaporizer 12, such as the heat duty Q in required to vaporize a major portion of the liquid feed can be controlled by a controller 8 based on the total system pressure. The total system pressure can be measured by any known means, such as pressure sensor 17 in conduit 18. The controller can additionally be used to control purging of the contaminated liquid from the vaporizer on a predetermined schedule. In order to remove or minimize any entrained liquid droplets present in the high purity vapor withdrawn from the column through conduit 18 and to prevent the formation of such droplets due to condensation, the high purity vapor can be superheated. Such superheating can ensure single phase gas flow. This superheating can be achieved by use of one or more superheaters 19, with the pressure of the high purity vapor upstream of the superheater being controlled by a pressure regulator 20. The superheater can be any unit which effectively removes the entrained liquid droplets from the gas stream. For example, a heat exchanger (e.g., a shell-and-tube type heat exchanger) using a suitable heat transfer fluid, for example, halocarbons such as freons (e.g., freon 22), can be used for this purpose. Other examples of suitable structures for superheating the gas include a resistance-type heater, heater grid-type packing material, heated sintered or porous structures, and any other direct or indirect methods of heating. The temperature of the vapor passing through the superheater is monitored at its outlet by temperature monitor 21. To prevent the formation of condensate caused by expansion and cooling of the gas as it passes through pressure regulator 22 and the subsequent gas distribution piping, the heat duty Q in supplied to the high purity vapor can be regulated by controller 8. An additional feature of the invention is a surge tank 23. Surge tank 23 acts as a reservoir for the high purity vapor, and minimizes pressure fluctuations in the gas delivered to the point(s) of use. As shown in the exemplified embodiment, the superheater and surge tank are preferably provided in combination as a single unit. The superheater can alternatively be disposed in series with the surge tank. The pressure in the surge tank, or combination surge tank/superheater, is preferably maintained at only several psi, for example, from 0,069 to 2,01 Bars (1 to 30 psi), above the normal distribution piping system pressure, but significantly lower, for example, from 1,38 to 3,45 Bars (20 to 50 psi) than the purification column pressure. In addition to the above, a reflux condenser 68 can be provided for providing reflux to column 9. To allow servicing of the one or more points of use, gas distribution piping is connected thereto. Thus, in the case of semiconductor manufacturing, one or more semiconductor processing tools can be connected to receive the high purity vapor. FIG. 2 illustrates a further aspect of the present invention, wherein a plurality of columns are employed. By employing a plurality of columns, higher levels of purity for the gas phase product may be obtained than for the single column system and method, especially if both light and heavy impurities exist in the feed chemical. The description set forth above with respect to FIG. 1 is applicable to the plural column system, with various differences being outlined below. First column 25 is disposed between pump 10 and second column 9, which corresponds to the column described in reference to FIG. 1. The chemical contained in storage vessel 1 is introduced into first column 25 in liquified form at a feed stage at an intermediate point in the column. The types of columns described above with reference to FIG. 1 are applicable to column 25. The liquid feed into first column 25 is fractionated into a liquid heavy fraction and a light vapor fraction. The light vapor fraction is removed from first column 25 through conduit 26 disposed above the feed stage, preferably at the top of the column. The light vapor fraction is introduced into condenser 27, and is at least partially condensed therein. A portion of the condensate is reintroduced into column 25 through conduit 28 as reflux, which is connected to the column at a point above the feed stage. The remainder of the light vapor fraction is removed from the system through conduit 29. The waste vapor can optionally be further processed, for example, by a waste treatment facility. The cooling duty Q out for condenser 27 of first column 25 is provided by a refrigeration cycle which includes refrigeration unit 30 and a cooling medium transported to and from the condenser through lines 31 and 32, respectively. The operational pressure and temperature of first column 25 are such that conventional refrigerants can be used as the cooling medium. Suitable refrigerants are known to those skilled in the art, and include, for example, freons such as from 11, 12, 21, 22, 113, 114, 115, 134b, 142b, 152a and 216. The cooling duty for the condenser can be provided by an open refrigeration cycle, which may use a different cooling medium, such as liquified or gaseous N 2 , O 2 or Ar, liquid CO 2 or water. The liquid heavy fraction is removed from first column 25 through conduit 33. At least a portion of the removed liquid heavy fraction is introduced into a reboiler 34. At least a portion thereof is vaporized and reintroduced in vapor form into first column 25 at a point below the feed stage through conduit 35. The heat duty Q in for reboiler 34 can be provided by a heat source, such as an electric heater for direct heat input or a heating medium stream, for example, water, a glycol solution or a halocarbon fluid. Other suitable heat transfer fluids are known to those skilled in the art. That portion of the liquid heavy fraction which is not introduced into the reboiler is introduced into second column 9 in liquified form using pump 10 (described above). As another option, if the operational pressure difference between first column 25 and second column 9 is sufficient to allow flow, pump 10 may be replaced by a control valve for flow control. The remaining components of the system and method steps are as described above with reference to FIG. 1. Operation of the condenser and/or the reboiler can be controlled by use of a single or multiple controllers, such as described above. As shown in the exemplified embodiment, controller 8 controls the heat duty to reboiler 34. For the exemplary two-column system, first column 25 preferably operates at a pressure in the range of from about 1 to 100 bar, more preferably from about 5 to 20 bar, and at a temperature in the range of from about -200 to 300 C, more preferably from about -40 to 150 C. The second column 9 preferably operates at a pressure in the range of from about 1 to 100 bar, more preferably from about 5 to 20 bar, and at a temperature in the range of from about -200 to 300 C, and more preferably from about -40 to 150 C. These conditions are, of course, dependent on the specific gas being treated and the nature of the impurities contained therein. The use of multiple columns is not limited in any way by the illustrated preferred embodiment. In this regard, more than two columns can be employed in the present invention, and the columns can be linked in a variety of ways depending, for example, on the chemical being treated and the nature of impurities. Furthermore, the multiple columns can be disposed in series and/or in parallel. FIG. 3 illustrates a further exemplary embodiment of the system for delivery of a vapor phase product in accordance with the invention. The components and methods discussed with respect to this aspect of the invention can also be used in conjunction with the systems and methods discussed above with reference to FIGS. 1 and 2 and vice versa. The liquid chemical in storage vessel 1 is introduced into the system through conduit 2, with the flowrate into the system being controlled by valve V1, which can be, for example, a solenoid or air actuated valve. Single phase flow of the liquid chemical to pump 10 is desirable to prevent a vapor lock that could result in stoppage of the liquid chemical flow. The conventionally used liquid ESG's, however, are sensitive to ambient temperature fluctuations. For example, nitrous oxide (N 2 O) exists only in the gas phase at a temperature greater than its boiling point of 37 C. Since a single phase liquid is desired to be introduced into the purification column, the nitrous oxide should be cooled if the ambient temperature exceeds about 36 C. The other liquid ESG chemicals would similarly benefit from a cooling step to maintain the liquid phase of the product. To help ensure single phase liquid flow, the liquid chemical removed from storage vessel 1 can be introduced into a liquid subcooler 50 which can prevent vaporization of the liquid chemical. This is particularly desirable when the bulk delivery system is installed outdoors, wherein the ambient temperature can have significant fluctuations. Liquid subcooler 50 can take the form of, for example, a vessel wrapped with copper tubing or a cooling jacket through which a cooling fluid passes, a shell and tube heat exchanger, or other known heat exchange means. Fresh coolant passes from conduit 51 through the subcooler and exits the subcooler through conduit 53. Flowrate of the coolant, which controls the amount of energy removed from the liquid chemical in the subcooler, is controlled based on the temperature of the liquid chemical leaving the subcooler through conduit 55 as measured by temperature sensor 57. This flow control, as well as control of the other variables in the system, can be automated with one or more controllers (not shown). Suitable controllers are known in the art and include, for example, one or more programmable logic controllers (PLCs) or microprocessors. The subcooled liquid chemical can next be introduced into a degasser-liquid reservoir unit 52. A constant supply of liquid chemical can be stored in unit 52 through appropriate control, resulting in uninterrupted flow of liquid chemical to column 54. The liquid level in the degasser-liquid reservoir unit 52 is monitored by a level sensor 56, which can be, for example, a differential pressure gauge, a float or other means to measure liquid level in the column. Valve V1, which controls flow of the liquid chemical into the system, is controlled based on the signal from level sensor 56. When the liquid chemical reaches a low setpoint value in unit 52, valve V1 is opened allowing the liquid chemical to enter the unit until the liquid chemical level reaches a maximum setpoint level. Alternatively, the liquid chemical can be continuously introduced into unit 52 to maintain a constant liquid level. Unit 52 additionally acts in a degassing capacity, removing any gas phase product generated from the liquid chemical downstream of the liquid subcooler and in the reservoir itself. Any gas in the headspace of reservoir unit 52 is removed via conduit 58, connected to a top portion of the unit. This gas can be sent to a detoxification unit 60, with flow from unit 52 being controlled by valve V2. From degasser-liquid reservoir unit 52, the liquid chemical can be introduced by pump 10 into column 54. Alternatively, the method for delivery of the liquid phase product can be accomplished with a pressure feed system which can use an inert gas such as helium (He), argon (Ar) or nitrogen (N 2 ). The gas can be introduced directly into unit 52 for direct pressurization or, alternatively, a bladder inside unit 52 can be employed. Column 54 includes a vaporizers 12 which is fed by the liquid chemical passing down the column. A level sensor 62 is provided for vaporizer 12 to monitor the liquid level therein. The liquid level in vaporizer 12 determines whether pump 10 (or the pressure feed system, if applicable) should send fluid to column 54 or not. To accomplish this, level sensor 62 sends a signal to a controller (not shown) which, in turn, sends a control signal to pump 10 (or the pressure feed system). As described above with reference to FIG. 1, the heat duty Q in required to vaporize a major portion of the liquid feed can be controlled by a controller (not shown) based on the total system pressure. The total system pressure can be measured by any known means, such as pressure sensor 17. The controller can additionally be used to control purging of the contaminated liquid from the vaporizer on a predetermined schedule. Suitable types of vaporizers are known to persons skilled in the art, and include, for example, a shell and tube heat exchanger or a small heated vessel. Automatic control of the heat duty provided to the vaporizer can be performed with a controller, for example, a programmable logic controller (PLC) or other control devices known in the art. Advantageously, multiple vaporizers 12 can be used for redundancy and to allow for a range of operating flow rates. While column 54 can take various forms as described above with reference to FIGS. 1 and 2, the exemplary column includes lower and upper fractionation zones 64, 66. A portion of the vapor from upper fractionation zone 66 is removed through conduit 18 as a high purity vapor stream. As in the previously discussed embodiments, the high purity vapor stream has a purity compatible with semiconductor manufacturing processing, preferably in the ppm or sub-ppm range. Light contaminants, such as nitrogen (N 2 ) and oxygen (O 2 ) can be removed from the top of column 54 after passing through upper fractionation zone 66 by use of a reflux condenser 68 followed by a liquid-gas separator 70. Reflux condenser 68 removes energy from the gas, thereby condensing a portion of the vapor stream and leaving the light contaminants in gas form. The gas containing the contaminants is removed from liquid-gas separator 70 through conduit 72 and back pressure regulator 74, and can be sent to a detoxification unit 76 for further treatment. The condensed stream can be returned as reflux to column 54 via conduit 72 after passing through liquid-gas separator 70. Use of reflux in this manner aids in achieving good separation in the column. In addition, the reflux allows for continuous operation of vaporizer 12, preventing shutdown thereof. This is particularly beneficial since a significant amount of time may be required to restart the vaporizer once shutdown has occurred. Thus, the system can respond quickly to fluctuations in flow rate requirements which may vary anywhere from 0 to 100% of capacity. A purified gas stream is withdrawn from a middle section of column 54 through conduit 18, which is passed through a back pressure regulator 78 and into a superheater 19. Back pressure regulator 78 is employed to control the pressure inside column 54, and superheater 19 ensures single phase vapor flow in the event liquid droplets or a mist are present in the purified vapor stream exiting column 54. Suitable superheaters 19 have been described above with reference to FIGS. 1 and 2. The amount of energy supplied to superheater 19 can be controlled based on the temperature of the vapor in the outlet conduit 82 of the superheater, as measured by temperature sensor 84. In the illustrated example, this can be achieved by automatically controlling valve V3 which adjusts the flowrate of a heating fluid introduced into the superheater via conduit 86 and removed therefrom via conduit 88. After the purified vapor stream passes through superheater 19, its pressure is adjusted by regulator 90 and is next introduced into a vapor surge tank 92. Vapor surge tank 92 is a gas phase tank serving as a reservoir which can dampen pressure swings due to changes in flow usage, and can assure continuous supply of the vapor phase product to the point(s) of use at the desired pressure even when there are fluctuations in flow demand. The pressure of the vapor product from vapor surge tank 92 is further reduced by a pressure regulator 94, and the gas can next be introduced into one or more valve manifolds (not shown), each of which can serve one or more process tools. FIG. 4 illustrates an optional embodiment of the invention which can be implemented with the methods and systems described above with reference to FIGS. 1-3. In this embodiment, a portion of the liquid heavy fraction can be removed from a portion of column 9 below the liquid feed stage, preferably from the bottom of column 9, via conduit 43 for reintroduction into column 9 as reflux. Use of a reflux liquid in this manner can advantageously eliminate entrained droplets which may contain impurities, such as metals, in the vapor stream in column 9. The elimination of droplets occurs as a result of the more efficient liquid-vapor contact brought about by the liquid reflux. This can result in a vapor product of greater purity. As illustrated, conduit 43 carries a portion of the liquid heavy fraction from column 9 to a point upstream of pump 10. The liquid heavy fraction can then be mixed with the fresh liquid chemical for introduction into the column. By use of a reflux flow in the above manner, the reflux ratio (liquid/vapor) can be set to a value greater than 1.0 to achieve intimate contact between the vapor and reflux liquid. This allows the column to be operated at the optimum reflux ratio even given significant fluctuations in the flow of vapor from column 9. A variation of the above-described systems and methods as applied to a system and a method for on-site chemical distribution will now be described with reference to FIG. 5. As in the above-described systems and methods, the on-site distribution system and method begin with a storage vessel 1 which contains the chemical stored as a liquid under its own vapor pressure. The storage vessel is connected to a conduit 2 for transferring the chemical in liquified form from the storage vessel to the other components of the system. A high purity block, bleed and purge system 3 can be disposed downstream of the point of connection of storage vessel 1 to conduit 2 to prevent contamination of the system. The pressure of the liquid chemical in conduit 2 can be measured and regulated by pressure sensor P and regulator 36, respectively, the control of which can be automated by use of a controller. In the exemplary embodiment, the liquid chemical is introduced into a liquid reservoir 37, from which it is drawn and delivered to the remainder of the system. The internal volume of the liquid reservoir will depend on factors such as the liquid chemical flow requirements of the system. Suitable materials of construction for the liquid reservoir are the same as those set forth with respect to storage vessel 1. It is desirable to eliminate or at least to minimize the formation of gas in the liquid reservoir. Such gas typically forms as a result of the pressure drop which occurs whenever the chemical is drawn off from the liquid reservoir. The elimination of this gas is particularly desirable prior to introduction of the liquid into a pumping system to prevent cavitation. To minimize gas formation, it is desirable to control the level of the liquid chemical in the reservoir to a value greater than some predetermined minimum value. This control can be accomplished, for example, by detecting the liquid level in the reservoir with a level sensor connected to a controller 38. Based on the measured level, additional liquid chemical can be introduced into the reservoir from storage vessel 1 as needed. In addition, an exhaust conduit 38 can be provided for removing the gas from the liquid reservoir by operation of control valve V5. The gas removed through exhaust conduit 38 can be further treated, for example, by a waste treatment facility. The above described operations can be automated by use of, for example, controller 38 alone, or with one or more additional controllers. From liquid reservoir 37, the liquid chemical is distributed throughout the remainder of the system by use of one or more pumps 10", such as a positive displacement pump. For example, a single pump 10" downstream from the storage vessel can be used to transport the liquid chemical to each of the vapor supply systems 38, as illustrated. As another possibility, each vapor supply system can have one or more dedicated pumps for transport of the liquid chemical thereto. The liquid chemical is introduced from pump 10" into main conduit 42, and then via conduits 39 to a plurality of vapor supply systems 38, disposed in parallel with one another. To control flow to each of the vapor supply systems, a respective shut-off valve S and a controller therefor can be provided. The vapor supply systems each produce a purified vapor stream which is directed to one or more points of use 40. In the exemplified embodiment, the vapor supply systems supply an electronics specialty gas to one or more semiconductor processing tools. The details of the vapor supply systems are provided above with reference to FIGS. 1-4. In this regard, the vapor supply systems include those components disposed downstream of the pump 10 in FIGS. 1, 3 and 4 and 10' in FIG. 2, leading up to the point of use. According to a preferred aspect of the invention, an excess of the liquid chemical is introduced into conduit 41, such that the liquid feed to the vapor supply systems does not run out. Main conduit 42 preferably includes a recycle leg to return back to liquid reservoir 39 that portion of the liquid chemical which is not introduced into the vapor supply systems. To control back-pressure in conduit, a pressure monitor P and control valve V6 are preferably provided in the recycle leg of the conduit. The control valve can be operated with a controller based on the pressure value measured by the pressure monitor. By controlling back-pressure, supply of the requisite amount of liquid chemical to the vapor supply systems can be ensured. Because of the difference in density between the liquid and gas phase chemical, it is possible to use piping for transporting the liquid chemical which is of significantly smaller diameter than that used for transportation of the chemical in its gaseous state. Thus, less space is required for the liquid chemical distribution piping than if the chemical were transported entirely in the gas phase. Such liquid phase transport also helps to reduce pressure fluctuations when compared with gas phase distribution. As a result of each of the systems and methods described above, characteristics of the gas being delivered can be maintained through wide fluctuations in flow rate. Such variations can result from the system's feeding numerous points of use which have flow rate requirements independent of each other. Fluctuations in the instantaneous flow rate requirement of greater than about one thousand times the average flow rate may be present without adversely affecting the performance of the systems and methods. Furthermore, the performance characteristics of the systems and methods described above can be maintained throughout the campaign of the chemical storage vessel irrespective of the amount of liquid present therein. It is preferred, however, that the storage vessel be replaced when the chemical volume amounting to about 1 to 20% of the total volume of the vessel (depending on the specific chemical) remains. Additionally, a wide array of use patterns is possible with the present invention. For example, the invention is compatible with continuous and intermittent operations. This allows flexibility in process design and can maximize the overall effectiveness of the equipment.

Claims: A method for delivery of a vapor phase product to a point of use, the method comprising: providing a storage vessel containing a relatively low purity liquid chemical under its own vapor pressure selected from the group consisting of ammonia (NH 3 ), boron trichloride (BCl 3 ), carbon dioxide (CO 2 ), chlorine (Cl 2 ), chlorine trifluoride (ClF 3 ), dichlorosilane (SiH 2 Cl 2 ), trichlorosilane (SiHCl 3 ), disilane (Si 2 H 6 ), hydrogen bromide (HBr), hydrogen chloride (HCl), hydrogen fluoride (HF), nitrous oxide (N 2 O),perfluoropropane (C 3 F 8 ), sulfur hexafluoride (SF 6 ), tungsten hexafluoride (WF 6 ) and a perfluorocarbon, under its own vapor pressure; introducing a stream of the chemical in liquified state into at least a column, whereby the chemical is fractionated into a contaminated liquid heavy fraction and a purified light vapor fraction; and introducing the purified light vapor fraction to the point of use. The method according to claim 1, further removing a portion of the contaminated liquid heavy fraction from the column and reintroducing it as reflux to the column. The method according to claims 1or 2, further comprising cooling the liquid chemical in a liquid subcooler between the storage vessel and the column. The method according to claims 1 to 3, further comprising removing vapor formed from the liquid chemical in a degasser disposed between the storage vessel and the column. The method according to claims 1 to 4, further comprising a step of superheating the purified light vapor fraction prior to the introducing to the point of use. The method according to claims 1 to 5, further comprising removing a light impurity-containing stream from the column at a point above the point of removal of the purified light vapor fraction, condensing a portion of the light impurity-containing stream in a reflux condenser, and returning the condensed portion to the column as reflux. The method according to claims 1 to 6, further comprising condensing a portion of the light vapor fraction and returning the condensed portion to the column as reflux. The method according to claims 1 to 7, further comprising containing the purified light vapor fraction in a surge tank prior to the introducing to the point of use. The method according to claims 1 to 8, wherein the point of use is one or more semiconductor processing tools. The method according to claims 1 to 9, wherein the column is operated at a pressure of from about 1 to 100 bar, and at a temperature of from about -200 to 300 C. The method according to claims 1 to 10, providing a plurality of columns, each column fractionating a liquid introduced therein into a respective heavy liquid fraction and a respective light vapor fraction, a first column of the plurality of columns being connected to receive, as the liquid introduced therein, the chemical in liquified state from the storage vessel; and removing from a second column of the plurality of columns the respective light vapor fraction; introducing the second column light vapor fraction to the point of use. The method according to claim 11, further comprising removing a portion of the contaminated liquid heavy fraction from the second column and reintroducing it as reflux to the second column. The method according to claims 11 or 12, further comprising cooling the liquid chemical in a liquid subcooler between the storage vessel and the first column. The method according to claims 11 to 13, further comprising removing vapor formed from the liquid chemical in a degasser disposed between the storage vessel and the first column. The system according to claims 11 to 14, further comprising condensing a portion of the light vapor fraction and returning the condensed portion to the second column as reflux. The method according to claims 11 to 15, further comprising containing the light vapor fraction from the final column in a surge tank prior to the introducing to the point of use. The method according to claims 1 to 16 wherein the light vapor fraction is superheated to minimize any entrained liquid droplets.

Inventors: JURCIK BENJAMIN J, PAGANESSI JOSEPH E, TOMITA SHINJI, UDISCHAS RICHARD, WANG HWA-CHI, YOKOGI KAZUO, JURCIK, BENJAMIN J., PAGANESSI, JOSEPH E., TOMITA, SHINJI, UDISCHAS, RICHARD, WANG, HWA-CHI, YOKOGI, KAZUO, Tomita, Shinji, Harima Technical Center, Yokogi, Kazuo, Harima Technical Center
Applicants: AIR LIQUIDE, L'AIR LIQUIDE, S.A. A DIRECTOIRE ET CONSEIL DE SURVEILLANCE POUR L'ETUDE ET L'EXPLOITATION DES PROCEDES GEORGES CLAUDE
Application year: 1999
Main classification: F25J3
IPC codes: F17C7, B01J4, F25J3