Producing pure carbon dioxide

Abstract: A feed gas stream containing from about 35 to about 98% by volume of carbon dioxide is united with a recycle stream and then compressed in compressor 102. The compressed gas stream is dried in a drier 110, cooled in a cooler 114, and separated in a distillation column 116 to produce a substantially pure liquid carbon dioxide product and a waste gaseous stream comprising carbon dioxide, oxygen and nitrogen. The waste stream is separated in a pressure swing adsorption apparatus 124 to provide a carbon dioxide-enriched stream which is the one united with the feed gas stream.

Description: This invention relates to a process for producing substantially pure carbon dioxide from a feed stream containing carbon dioxide and at least two other components. The invention also relates to apparatus for freezing food with liquid carbon dioxide. Carbon dioxide is conventionally obtained as a gaseous by-product from the production of ammonia or hydrogen a well as from fermentation plants. The by-product generally contains at least 98% carbon dioxide. It is known to convert the gaseous by-product into pure liquid carbon dioxide by distillation at recoveries exceeding 94% by weight. Conventional distillation columns used for producing liquid carbon dioxide typically operate at a pressure of about 1790 kPa (about 260 psia) and a column condenser temperature of about -32°C (-25°F). The waste gas removed from the top of the column as an overhead stream contains under these conditions about 75% by volume of carbon dioxide. Accordingly, the amount of carbon dioxide lost as waste is about three times the amount of impurities in the feed. It therefore follows that carbon dioxide recovery decreases significantly as the concentration of carbon dioxide in the feed decreased. Efforts at treating low concentration carbon dioxide feeds have focused on decreasing the carbon dioxide concentration in the column overhead. This has been done either by increasing the column operating pressure or by decreasing the column condenser temperature. However, both of these methods suffer from significant disadvantages. When the column pressure is increased the solubility of inert impurities such as oxygen and nitrogen in the liquid carbon dioxide product increases. In addition, the power needed for the refrigeration cycle increases and adds to the cost of the process. Further, at significantly higher pressures and in the presence of impurities such as oxygen, phase behaviour limitations make it impossible to produce pure carbon dioxide by vapour-liquid separation. Similarly, there are significant disadvantages in reducing the column condenser temperature. In conventional systems, much of the equipment including the distillation column is made of carbon steel. The lowest temperature which carbon steel can withstand is -37°C (-35°F). Stainless steel such as type 304 can be used at temperatures as low as -46°C (-50°F), but at a significant increase in material cost. By decreasing the temperature of the column from -37°C to -46°C (-35°F to -50°F), it is possible to increase the recovery of carbon dioxide from a given feed concentration. Similarly, it is possible to increase the carbon dioxide recovery at a given temperature if the pressure is increased. Nonetheless, the carbon dioxide recovery from these conventional systems is below 94% by weight if the concentration of the carbon dioxide feed is less than about 89% by volume. Pressure swing adsorption has been used as an alternative to solvent absorption for separating carbon dioxide. For example, US -A- 4,077,779 discloses a process for separating methane from carbon dioxide. US -A- 4,639,257 (corresponding to GB-A-2 174 379) discloses a process for producing liquid carbon dioxide in which a membrane separator is used to separate gaseous carbon dioxide from components of a waste stream. The system is said to be useful to treat low concentration feed sources by compressing the feed gas to high pressures of at least 1380 kPa (200 psia). The membrane separation disclosed in US -A- 4,639,257 is limited to removing only those impurities which are significantly less permeable through the membrane than carbon dioxide, and are not suitable for the separation of impurities such as oxygen, which although slightly less permeable than carbon dioxide, are not readily separated by membrane separation systems. Further, dual compression is required when the membranes are first installed to separate the feed. Thus, the feed gas must be compressed before membrane separating and then the carbon dioxide-rich permeate must be recompressed prior to recycling to the distillation column. These requirements add significantly to the cost of the process and significantly limit its application. US-A-4 072 276 relates to a method of chilling articles with a liquified gas, in which an exhaust gas including vapour vapour evolved from the liquified gas, is compressed refrigerated and returned into heat exchange relationship with the articles. The present invention utilises a combination of distillation and pressure swing adsorption to separate a liquid carbon dioxide product from an exhaust gas evolved from a food freezing system that employs liquid carbon dioxide as a freezing medium. According to the present invention there is provided a process for producing substantially pure carbon dioxide from a feed stream containing carbon dioxide and one or more other components comprising the steps of: a. distilling the carbon dioxide feed thereby to form a substantially pure liquid carbon dioxide product and a first waste stream containing carbon dioxide; b. separating the first waste stream by pressure swing adsorption into a carbon dioxide-enriched stream and a carbon dioxide-depleted second waste stream; and c. recycling the carbon dioxide-enriched stream to the distillation step; characterised in that the two other components are oxygen and nitrogen, the feed stream is a gaseous by-product obtained from a refrigeration system employing liquid carbon dioxide to freeze food, and the first waste stream is separated by pressure swing adsorption. The invention also provides an apparatus for freezing food using liquid carbon dioxide comprising: a. a freezer adapted to freeze food using liquid carbon dioxide; b. means for respectively conveying non-frozen food to the freezer means and withdrawing frozen food from the freezer; c. an outlet from the freezer of the discharge of a gaseous mixture comprising carbon dioxide, nitrogen and oxygen from the freezer; characterised in that the apparatus additional includes: d. a distillation column for separating the gaseous mixture having an inlet for the gaseous mixture, and one outlet for substantially pure liquid carbon dioxide product and another outlet for a first waste stream containing carbon dioxide; e. a pressure swing adsorption separator adapted to separate the first waste stream into a carbon dioxide-enriched stream and a carbon dioxide-depleted second waste stream; and f. means for recycling the carbon dioxide-enriched stream to the distillation column. The process and apparatus according to the invention will now be further described by way of example with reference to the accompanying drawings, in which: Figure 1 is a schematic circuit diagram of a conventional distillation system for converting gaseous carbon dioxide into substantially pure liquid carbon dioxide; Figure 2 is a graph the recovery of carbon dioxide is shown plotted against the concentration of carbon dioxide into substantially pure liquid carbon dioxide; Figure 3 is a schematic diagram illustrating a first apparatus according to the present invention wherein at least a portion of the waste gas from a pressure swing adsorber is used to regenerate the drier; Figure 4 is a schematic diagram illustrating a second apparatus according to the present invention wherein at least a portion of the carbon dioxide-rich stream is used to regenerate the drier; and Figure 5 is a schematic diagram illustrating a system wherein an apparatus as shown in Figure 3 treats a vent gas from a food freezer, which uses liquid carbon dioxide to freeze food, to produce liquid carbon dioxide at high recoveries for return to the food freezer. Referring to Figure 1, there is shown a conventional distillation system for the production of liquid carbon dioxide from a gaseous stream containing carbon dioxide. Specifically, a feed gas stream is sent via line 2 to a multistage compressor 4 and then via line 5 to a cooler 6 in which condensate water is removed and then discharged via line 8. The cooled feed gas stream is sent via line 10 to a drier 12 where it is dried by an adsorbent (such as alumina) which adsorbs water vapour but not carbon dioxide. The dried feed gas stream proceeds via line 14 to a second cooler 16 and then to a distillation column 18 via line 20. In the distillation column 18, a liquid reflux stream is produced by a refrigeration system including a condenser 22. Substantially pure liquid carbon dioxide is removed from the bottom of the column 18 via line 24. A gaseous waste product containing a predominant amount of carbon dioxide and impurities such as nitrogen gas is separated and removed as an overhead stream via line 26 to a heat exchanger 28 wherein it is heated. The gas stream is sent via line 30 to a heater 32. It is common practice to integrate the heat-exchanger 28 and the feed cooler 16, so that all or part of the cooling energy required for cooling the feed is provided by the waste stream from the distillation column 18. Thus, line 14 may be made to run in countercurrent relationship to line 26 within the heat exchanger 28 thereby eliminating the separate cooler 16. The gas stream is heated in the heater 32 to a temperature sufficient to regenerate the drier 12 (which it enters via line 34) so as to dry the cooled feed stream coming from the cooler 6 via line 10. Thereafter, the waste stream including all of the carbon dioxide contained therein is vented to the atmosphere via line 36. Because the waste stream contains a major portion of carbon dioxide, the conventional system of Figure 1 is suited only for feeds containing a high carbon dioxide concentration. Referring to Figure 2 there is shown a plot of carbon dioxide recovery versus carbon dioxide feed concentration under varying pressure and temperature conditions in the distillation column. It should be noted that all concentrations of the carbon dioxide in gas streams including the feed are expressed as a percentage by volume and all carbon dioxide recoveries are expressed as a percentage by weight. Plots 1 to 4 of Figure 2 represent the recoveries obtained using the above-described conventional system. For example, by operating the column at 1792 kPa (260 psia) and a temperature of -32°C (-25°F) (plot 1), it is possible to obtain a 94% weight recovery of carbon dioxide only when the feed concentration is about 98% by volume. Under the most rigorous conventional column conditions (e.g. a pressure of 2344 kPa (340 psia); a temperature of -46°C (-50°F), a 94% weight recovery of carbon dioxide can be obtained only when the feed concentration is at least 89% by volume. Thus, the conventional distillation system is useful only for high carbon dioxide concentration feed systems. However, there is a need for carbon dioxide recovery systems where the carbon dioxide concentration is significantly less than 89% by volume and may be as low as about 35% by volume. In particular, commercial refrigeration units employing liquid carbon dioxide for freezing foods contaminate the liquid carbon dioxide with nitrogen and oxygen (from air) to the extent that the spent carbon dioxide may contain as much as 50% or more of the contaminants. Typically this contaminated stream is vented to the atmosphere because recovery of the carbon dioxide is not economically feasible. This is because conventional systems, as previously described in connection with Figure 2, sacrifice carbon dioxide recovery as the level of carbon dioxide in the feed decreases. Further, even when the carbon dioxide concentration in the feed lies between 89% and 98% by volume, there is a definite need to obtain recoveries significantly exceeding 94% by weight when the availability of feed gas is limited compared to product liquid carbon dioxide requirements. By using the process and apparatus according the to present invention, it is now possible to obtain high recoveries of carbon dioxide exceeding 94% by weight from a feed having a low concentration of carbon dioxide, such as that obtained as a vent gas from conventional carbon dioxide food freezing refrigeration systems. More specifically, a distillation system is shown in Figure 3 employing a pressure swing adsorber which can achieve at least 94% by weight carbon dioxide recovery from a feed having a low concentration of carbon dioxide and particularly a concentration of carbon dioxide in the range of about 35 to about 98% by volume. Further, for feed streams wherein the carbon dioxide concentration is between 89% and 98% by volume, it is possible to obtain liquid carbon dioxide recoveries exceeding 98% by weight using the system shown in Figure 3. As shown in Figure 3, a feed gas stream is sent via a line 100 to a compressor 102 and then the compressed gas stream is passed via a line 104 to a cooler 106 where the stream is cooled to condense water therefrom. The condensate is removed via a line 107. The gas stream is then sent via line 108 to a drier 110. Heat to regenerate the drier 110 is at least partially supplied by all or part of a waste stream from a pressure swing adsorber apparatus as described hereinafter so as to dry the gas stream. The dried feed stream flows via line 112 to a cooler 114 and the cooled stream flows into a distillation column 116 via the line 115, which column 116 houses the condenser 119 of a refrigeration unit to obtain a liquid reflux, for separating the feed into a pure liquid carbon dioxide product and a waste stream containing a significant amount of carbon dioxide. The liquid carbon dioxide product is removed from the bottom of the distillation column 116 via a line 117. The waste stream leaves the distillation column 116 via a line 118 and is warmed from a column temperature of, for example, about -37°C(-35°F) to about 32°C (90°F) in a heat exchanger 120. In an analogous manner to that described previously in connection with the conventional system of Figure 1, the heat exchanger 120 and the cooler 114 can be integrated so that all or part of the cooling energy required for cooling the feed can be provided by the cold stream leaving the distillation column 116 which requires warming. The heated waste stream obtained from the heat exchanger 120 is sent via a line 122 to a pressure swing adsorber 124. The pressure swing adsorber (PSA) 124 contains a molecular sieve or activated carbon adsorbent for separating carbon dioxide from the other gases in the waste stream. A typical example of the molecular sieve is zeolite 13X manufactured by Laporte Industries, Inc. PSA is a well-known apparatus for separating the components of a mixture of gases as a result of the difference in the degree of adsorption among them on a particulate adsorbent retained in a stationary bed. Typically, two or more such beds are operated in a cyclic process comprising adsorption under pressure and desorption under comparatively lower pressure or vacuum. The desired component or components of the gas mixture can be obtained during either of these stages. The cycle may contain other steps in addition to the fundamental steps of adsorption and regeneration, and it is commonplace where such a unit contains more than two adsorbent beds to have N beds cycled (360/N)° out of phase, thereby providing a pseudo-continuous flow of desired product. As shown in the embodiment of Figure 3, the waste stream is separated in the PSA 124 into a carbon dioxide-enriched recycle stream (obtained during desorption) which is sent via a line 126 to a vacuum pump 127, and a waste stream 130 (comprising the non-adsorbed gas and produced during adsorption) containing a relatively small amount of carbon dioxide. The carbon dioxide-rich stream is sent from the pump 127 via a line 128 to join the feed gas in line 100. The waste stream is released from the PSA 124 under pressure via a line 130 to a pressure reducing valve 132 where the pressure is reduced before the waste stream enters the drier 110. All or a portion of the reduced pressure stream then passes through line 134 and enters a heater 136 where the stream is heated to provide regeneration for the drier 110 via a line 138. As shown specifically in Figure 3, the amount of reduced pressure waste stream used to regenerate the drier 110 may be controlled by providing a pathway for the flow of at least a portion of the waste stream outside of the drier 110. Thus all or part of the waste stream can by-pass the drier 110 via a line 140 before being reunited with the waste stream leaving the drier 110 via a line 141. In another embodiment of the apparatus according to the invention as shown in Figure 4, all or a portion of the carbon dioxide-enriched stream from the line 138 is used to regenerate the drier 110 instead of the waste stream from the PSA apparatus 124. More specifically, the carbon dioxide stream from the line 128 is sent to the heater 136 and via the line 138 to the drier 110. Any by-pass carbon dioxide is sent through the line 140. The carbon dioxide stream leaves the drier 110 and is cooled in a cooler 142 before returning to the feed line 100 via the line 144. In the embodiment described in Figure 4, the waste stream which leaves the PSA 124 via the line 130 passes through the pressure reducing valve 132 before being discharged from the system. It will be readily understood from the embodiments shown in Figures 3 and 4, that the recycling of all or part of either the waste stream or the carbon dioxide-enriched stream for regenerating the drier is a preferred feature of the invention. As shown in Figure 2, by plots 5 and 6, the process of the present invention can consistently exceed recoveries of 94% by weight of carbon dioxide for low concentration feeds containing as low as 35% carbon dioxide. As a result waste streams from highly contaminated carbon dioxide containing sources such as commercial food freezing systems using liquid carbon dioxide for freezing food can be treated to recover highly pure liquid carbon dioxide which can be recycled to the food freezer and thereby reduce the cost of commercial refrigeration. The preferred embodiment of the process according to the present invention is to operate at high recoveries exceeding 94% by weight for any feed stream having a concentration of about 35% to about 98% by volume carbon dioxide, though, if desired, the process can operate at lower than 94% by weight carbon dioxide recoveries. Referring to Figure 5, there is shown an overall system wherein the apparatus shown in Figure 3 is applied to recover liquid carbon dioxide from the vent gas of food freezers employing liquid carbon dioxide for food freezing. Food such as meat, e.g. chicken, enters a food freezer 200 via a line 201 such as a conveyer belt. The food passes through the freezer 200 and is sprayed with liquid carbon dioxide entering the food freezer 200 via a line 204. The frozen food leaves the freezer via an outlet 202 for packaging. The carbon dioxide gas is exhausted from the freezer via a line 205 at regular time intervals when necessary in order to maintain the freezer at the desired temperature. In commercial food freezer systems, air leaks into the food freezer 200 through the food inlet 201 and the food outlet 202 during normal operation, and whenever the freezer doors are open. The air is vented with the waste carbon dioxide via a line 205. To assist the evacuation of the air/carbon dioxide mixture from the freezer, pressurised air is sent into the line 205 via a line 206. The pressurised air may be generated by a fan or similar device. The pressurised air also serves to warm the air/carbon dioxide mixture in the line 205. The resulting vent gas is sent via the line 205 to a control valve 207 which is provided to maintain the flow of the vent gas to the carbon dioxide recovery system. The vent gas is sent to a gas holder 208 which serves to collect the vent gas and to provide a uniform recycle feed stream via a line 209. This feed stream enters the carbon dioxide recovery system 210 previously described in connection with Figure 3. The liquid carbon dioxide obtained from the system via a line 212 is combined with make-up liquid carbon dioxide from a line 213 and sent to the freezer 200 via the line 204. The make-up liquid carbon dioxide is needed to compensate for the carbon dioxide losses resulting from leakage through the food inlet 201 and the food outlet 202 of the freezer system and the carbon dioxide which may be lost in the recovery system. COMPARATIVE EXAMPLE In a conventional carbon dioxide generating system of the type described in Figure 1, 223.0 lb mol/hr of a feed containing 85% carbon dioxide, 11.85% of nitrogen and 3.15% oxygen was employed as the carbon dioxide feed. (1 lb mol = 453.592 mol). The feed was transmitted at a temperature of 35°C (95°F) and a pressure of 105 kPa (15 psia) to the compressor 4 where the pressure was increased to 1861 kPa (270 psia) and the temperature to 150°C (300°F). The compressed feed was cooled to 35°C (95°F) and then forwarded to a drier where the water content was reduced from saturation to an amount given a dew point of -62°C (-80°F). The dried feed was then cooled to -18°C (0°F) and sent to the distillation column. Pure liquid carbon dioxide was obtained from the bottom of the column at a flow rate of 126.1 lb mol/hr. A waste stream (96.9 lb mol/hr) containing 65.4% carbon dioxide, 27.28% nitrogen and 7.25% oxygen was discharged as an overhead stream from the column at a temperature of -37°C (-35°F) and a pressure of 1764.9 kPa (256.0 psia) and sent to a heat exchanger for warming to 32°C (90°F). A portion of the waste stream (17.9 lb mol/hr) was then sent to a heater to raise the temperature to 150°C (300°F) to provide for the regeneration of the drier. The remainder of waste stream (79.0 lb mol/hr) by-passed the heater and joined the other portion of the waste stream. The combined waste stream was vented to the atmosphere at the rate of 96.9 lb mol/hr. Almost two thirds of the discharged waste gas was carbon dioxide. EXAMPLE 1 The same feed (85% carbon dioxide) at the same flow rate (223.0 lb mol/hr) and under the same conditions used in the comparative example was processed through the system of the present invention described in connection with Figure 3. Because of the recycle of the carbon dioxide-enriched stream from the PSA to the original feed, the flow rate to the compressor was 284.8 lb mol/hr. The feed entered the distillation column at the same temperature and pressure conditions as in the comparative example and produced pure liquid carbon dioxide at a flow rate of 186.0 lb mol/hr. The waste stream (98.9 lb mol/hr) containing the same composition as the comparative example was fed to the PSA to separate the carbon dioxide from the contaminants. The carbon dioxide-enriched stream leaving the PSA contained 98.9% carbon dioxide at a flow rate of 61.8 lb mol/hr which was recycled to the feed. The waste stream leaving the PSA at the rate of 37.0 lb mol/hr contained only 8.82% carbon dioxide with the balance being nitrogen and oxygen. One portion of the stream (22.8 lb mol/hr) was used to regenerate the drier while the balance (14.2 lb mol/hr) by-passed the drier and combined with the other portion of the waste stream for venting. EXAMPLE 2 A feed containing 93.0% carbon dioxide, 5.53% nitrogen and 1.47% oxygen at the same flow rate and under the same pressure and temperature conditions as in Example 1 wad processed through the system of the present invention described in Figure 4. Because of the recycle of the carbon dioxide-enriched stream from the PSA, the flow rate of the feed to the compressor was 252.0 lb mol/hr. The flow rate of the liquid carbon dioxide leaving the distillation column was 205.9 lb mol/hr while a waste stream containing the same composition as described in Example 1 was fed to the PSA. The resulting carbon dioxide-enriched stream contained 98.9% carbon dioxide and was recycled at the rate of 29.0 lb mol/hr. A portion of this stream (20.2 lb mol/hr) was used to regenerate the drier. A waste stream discharged from the PSA at the rate of 17.1 lb mol/hr was reduced to a pressure of 140 psia. The waste stream contained 8.82% carbon dioxide. It will be understood that the use of the carbon dioxide-enriched stream is desirable when the initial feed concentration of carbon dioxide is high (eg 93% by volume). This is because the waste stream discharged from the PSA is inadequate to regenerate the drier. EXAMPLE 3 In a carbon dioxide generating system of the type described in Figure 3, 223.0 lb mol/hr of a feed containing 35% carbon dioxide, 51.35% of nitrogen and 13.65% oxygen was employed as the carbon dioxide feed. The feed was transmitted at a temperature of 35°C (95°F) and a pressure of 103 kPa (15 psia) to the compressor 102 where the pressure was increased to 350 psia and the temperature to 150°C (300°F). Because of the recycle of the carbon dioxide-enriched stream from the PSA to the original feed, the flow rate to the compressor was 320.2 lb mol/hr. The compressed feed was cooled to 35°C (95°F) and then forwarded to a drier where the water content was reduced from saturation to an amount giving a dew point of 62°C (-80°F). The dried feed was then cooled to -18°C (0°F) and sent to the distillation column. Pure liquid carbon dioxide was obtained from the bottom of the column at a flow rate of 73.3 lb mol/hr. A waste stream (247.0 lb mol/hr) containing 40.1% carbon dioxide, 47.3% nitrogen and 12.6% oxygen was discharged as an overhead from the column at a temperature of -50°F and a pressure of 340.0 psia and sent to a heat exchanger for warming to 32°C (90°F). The waste stream was then fed to the PSA wherein the carbon dioxide was separated from the contaminants. The carbon dioxide-enriched stream leaving the PSA contained 97% carbon dioxide at a flow rate of 97.1 lb mol/hr which was recycled to the feed. The waste stream leaving the PSA at the rate of 149.9 lb mol/hr contained only 3.3% carbon dioxide with the balance being nitrogen and oxygen. One portion of the stream (25.7 lb mol/hr) was used to regenerate the drier while the balance (124.2 lb mol/hr) by-passed the drier and combined with the other portion of the waste stream for venting.

Claims: A process for producing substantially pure carbon dioxide from a carbon dioxide feed stream containing carbon dioxide and at least two other components comprising the steps of: a. distilling the carbon dioxide feed thereby to form a substantially pure liquid carbon dioxide product and a first waste stream containing carbon dioxide; b. separating the first waste stream into a carbon dioxide-enriched stream and a carbon dioxide-depleted second waste stream; and c. recycling the carbon dioxide-enriched stream to the distillation step; characterised in that the two other components are oxygen and nitrogen, the feed stream is a gaseous by-product obtained from a refrigeration system employing liquid carbon dioxide to freeze food, and the first waste stream is separated by pressure swing adsorption. A process according to Claim 1 further including the steps of compressing the carbon dioxide feed stream; drying said compressed feed stream; and cooling said dried feed stream upstream of distilling it. A process according to Claim 2, further including the step of passing at least a portion of the second waste stream to a drier to provide heat to the drier and thereafter venting the second waste stream from the drier means. A process according to Claim 2, further including the step of passing at least a portion of the carbon dioxide-enriched stream to a drier to provide heat to the drier means and thereafter passing said carbon dioxide-enriched stream to the distillation step. A process according to any one of Claims 1 to 4, wherein the concentration of carbon dioxide in the feed is from 35 to 98% by volume. A process according to any one of the preceding claims, wherein the separation by pressure swing adsorption employs at least two beds, said beds containing a molecular sieve or activated carbon as an adsorbent. A process according to any one of the preceding claims, wherein the step of distilling the carbon dioxide feed is conducted at a temperature of from -32°C to -46°C (-25°F to -50°F) and a pressure of from 1790 kPa to 2340 kPa (260 psia to 340 psia). Apparatus for freezing food with liquid carbon dioxide comprising: a. a freezer (200) adapted to freeze food using liquid carbon dioxide; b. means (201 and 202 respectively) for respectively conveying non-frozen food to the freezer (200) and withdrawing frozen food from the freezer (200); c. an outlet (205) from the freezer of the discharge of a gaseous mixture comprising carbon dioxide, nitrogen and oxygen from the freezer (200); characterised in that the apparatus additionally includes: d. a distillation column (116) for separating the gaseous mixture having an inlet (115) for the gaseous mixture and one outlet (117) for a substantially pure liquid carbon dioxide product and an other outlet (118) for a first waste stream containing carbon dioxide; e. a pressure swing adsorption separator (124) adapted to separate the first waste stream into a carbon dioxide-enriched stream and a carbon dioxide-depleted second waste stream; and f. means (127, 128) for recycling the carbon dioxide-enriched stream to the distillation column (116). Apparatus according to Claim 8, further including a compressor (102) for compressing the gaseous mixture, a drier (110) for drying the compressed gaseous mixture and means (114) for cooling the dried gaseous mixture. Apparatus according to Claim 9, further including means (130, 132, 134, 136, 138) for passing at least a portion of the second waste stream to the drier (110) to provide heat to the drier (110). Apparatus according to Claim 9, further including means (126, 128, 136, 138) for passing at least a portion of the carbon dioxide-enriched stream to the drier (110) to provide heat to the drier and means (142, 144) for passing the carbon dioxide-enriched stream from the drying means to the distillation column (116).

Inventors: KRISHNAMURTHY RAMACHANDRAN, MACLEAN DONALD L, KRISHNAMURTHY, RAMACHANDRAN, MACLEAN, DONALD L.
Applicants: BOC GROUP INC, THE BOC GROUP, INC.
Application year: 1990
Main classification: F25J3
IPC codes: F25J3, B01D53, C01B31