MX2010011017A - Carbon dioxide recovery. - Google Patents

Abstract

Disclosed herein is a method and system for separating carbon dioxide (CO2) from a C02 containing gas stream containing water vapor and additional impurities, for example, nitrogen, oxygen, sulfur oxides, nitrogen oxides, and mercury. The C02 is captured by subjecting the CO2 gas feed stream to a temperature swing adsorption step. The temperature swing adsorption step comprises an adsorption step for producing a substantially dry carbon dioxide-depleted stream, and an adsorbent regeneration step comprising heating the adsorbent bed to produce a substantially water vapor-free carbon dioxide stream. Moisture from the gas stream containing CO2 is optionally removed by pressure swing adsorption, temperature swing adsorption, membrane separation, or absorption prior to CO2 capture.

Description

RECOVERY OF CARBON DIOXIDE Field of the Invention The method and system described herein captures carbon dioxide (C02) from fterion such as flue gases of a year and makes C02 available for similar uses.

Background of the Invention If you stop checking the emissions of adero such as C02 / these can affect climatic conditions. The conversion of fuel such as coal and natural gas to energy is one of greenhouse gases. Greenhouse emissions can be reduced by several means to the efficiency of the solvent combustion process, typically an amine, which is a part of the current generated during ombustión. The pre-combustion captures the chemical reaction of the fuel co and then with steam to produce an amount of carbon and hydrogen. The carbon dioxide of this current through a process of O2 and hydrogen can be used as combustion of energy. If oxygen is used to combust a combustion gas containing carbon, which can be easily separated.

The post-combustion capture of C02 results in absolute efficiency for the generation and in approximately 28-30% of relative reduction for a power plant for existing power plants taking capital and operating costs to separate C02. Net energy production also decreases by 30% or more. s to significantly reduce sanitation and capital associated with the C02 capture. For post-combustion capture, Dep ergía (DOE, for its acronym in English) has a 35% increase in energy cost after C02.

Most studies that deal with post-combustion c use amine or ammonia processes to remove carbon dioxide from combustion. Processes based on absorptions such as the requirements of ficatives. The best absorbents based on am is C02 adsorption on base adsorbents ranging from 140-240 kcal / kg or 252-432 Btu / lb (Va. And AL Myers, "Adsorption Equilibrium Data H ice Hall, Englewood Cliffs, NJ , 1989.) for a fifth of the heat of absorbing amine-based systems, there is a need for practical adsorption systems that provide a high yield of carbon dioxide for a long period of time in adsorption heats.

The oscillation adsorption systems are extensively tempered for such applications as natural gas drying, and water removal and cryogenic distillation of air. These amines eliminate less than 2% impurities and the regeneration rate that contains the impurities to 1000 C / day of C02 in the feed is 8,000 m3 (5.3 million kilograms, a size that makes the systems icos to capture dioxide). carbon fiber.

The method and system described in this pr solution for the efficient capture of C02 u or based on oscillation and pressure adsorption cycles.

Brief Description of the Invention This brief description is provided for the introduction of concepts in a simplified form, additionally in the detailed description. This brief description does not intend to identify any key or inventive aspects of the subject matter claimed to determine the scope of the claimed subject by approximately 10 percent by volume of im- cide by subjecting a C02 gas stream to temperature swing dsor- sion. The temperature oscillation reaction comprises a step to produce a substantially dry exhausted stream, and a regeneration step comprising heating the adsorbent bed with a substantially free C02 stream. The temperature in the adsorption stage of the emperature during the step of regenerating the ta up to about 80 ° C to 300 ° C. The temperature oscillation adsorption duration is from approximately 2 minutes to 60 minutes.

The adsorption is generally carried out in sa at temperatures between 10 ° C and 80 ° C and under pressure from 1.07 to 40.0 absolute bars. The concent In one modality, the impurities that buy moisture, hydrocarbons, oxides of nitrogen, and mercury are removed before the ads.

Moisture removal is carried out using, by oscillation by pressure, adsorption by or emperature, membrane separation, and adsorption of the adsorption process by oscillation d in a range of approximately 4 m immately 60 minutes and the duration of adsoation of temperature is in an interimely 1 hour to 12.0 hours. The content of the moisture removal stage is reduced to -40 ° C or lower. The adsorbents, by activated n, carbon molecular sieves, zeoli 4A, 5A, 13X, NaY and CaY, organic compounds, natural zeolites, nat zeolites In both modalities, the material contained by direct heat transfer or indir C02 current of 'high purity. The onal of C02 is carried out by the evacuation of the heating. The C0 produced is pnally by means of a membrane process, or styling, an adsorption process, or a sifter to remove impurities that include nitrogen, oxygen, argon, sulfur oxides, and moisture. Part of the purified C02 as a rinse in the separation system or system described is effective for the 80% or greater amounts in voices of the C02 current.

Brief Description of the Figures The brief description above, as well as FIGS. 2A-2D, illustrate exemplary embodiments of the C02 separation system at optionally humidity in a first step followed by capture of C02 by reaction in a second separation unit.

Figure 3 illustrates by way of example the moisture adsorption system wherein the additional impurities, for example sulfur hydrocarbon or nitrogen oxides, and mercury are removed from a combination of ossaturation and pressure adsorption.

Figure 4 illustrates by way of example the separation scheme of C02 where the C02 is fed by adsorption or reacted by direct or indirect heating of steam, hot water or a dry stream or combustion to improve the efficiency of C02. combing the concentration of C02 resulting from the heat generated in process 6 can be like current 15. A part of the current is like current 20 and used in the C02 80 situation described below. The current part 15 is taken out as the current 25 and can be used for other purposes, for example, for generation of synthesis gas in the unit 35, low pressure current or water quality 30, can be used in the system Separation can be sent to unit 5 for steam generated from the electric power generated in the unit rse to the separation system of C02 80 via the remaining electric power can supply the final such as the industial customers can be raised, if required, By a blower or a blower 65 after the unit 6 containing C02 is from a chemical plant or from a pre-combustion process, the C02 stream may contain additional impurities, hydrogen, hydrocarbons, and carbon monoxide. of coal or gas-fired combustion gas flue gas typically rise between 1.07 bar to 1.34 bar, which is a C02-containing stream generated in industrial or industrial, the pressure of the current that 1.07-1.34 bar and may not have to elevate or gasification where the fuel is air or oxygen, * the pressure of the current that can be several atmospheres and would not have to 1 process of combustion with oxygen the gas of c tive (SCR) for 0 geno, electrostatic precipitators for the wet purifiers for sulfur oxides. The molecules, oxides of nitrogen, and oxides of sulfur necessary if the current comes from a partial oxidation or reformation.

The stream containing C02 exits from the current unit 70 and enters the separation system of separation from C02 80 contains at least one material that removes C02 from the run by adsorption or chemical reaction. The ratio of approximately 1.07 bars abs immately 40 absolute bars. Depending on the hoist for the capture of C02, the system of sepa 0 may contain additional units for the re s components in the feed stream of C02 by adsorption, the humidity of the imenta tion 70 would have to be removed before the 2 and the current exhausted in C02 85 would be rela in this case, a part or all of the current 95, can be used to regenerate the moisture content 79.

The C02 captured in the separation system of erado by desorption of C02. The energy for the 02 can be supplied by means of the current 35 or the electricity represented by the Other external sources of ricity can also be used to regenerate the material in the C02 80 a.tion. The adsorbent or reagent cited directly by the current or condensate is capable of handling it. The material in the CO2 sediment can also be regenerated by C02 from the C02 80 separation system. The regeneration is illustrated as in Figure 1. More than 80% of the impurities are amined in the separation section. of C02.

The desorbed C02 leaves the separation system to line 105 and is sent to a system of .purifi 25. A vacuum pump 110 can be used to choose the recovery of C02 from the system known as 0. Part of the C02 product enters the pump. the current 100 and is connected to the current 105 d of the vacuum pump 110. The current coming out of the vacuum pump 110 is combusted by the stream of C02 product entering the C02 125 signal as the current 120. The purity of C02 product 120 produced dur eration depends on the concentration of the separation of C02 80 is wet, ta humidity. The purified C02 comes out as the purification system of C02 125. The run is a small part of the current 120, the current 130 can be used for p is in the separation system of C02 80. This is in the system of separation of C02 80 as the purified C02 product leaves C02 125 as the 140 nible current for industrial food or industrial applications, improved recovery and sequestration. The current of C02 product to be compressed, liquefied or both before S applications.

Figures 2A-2D illustrate by way of example of the separation system of C02 80. As described below in relation to 4, additional beds for other such as cooling, pressurization, scrubbing can be used. The rinsing step can be carried out by relatively pure C02 145. As illustrated in Figure 1, the stream of C02 product leaves the C02 80 as the stream 105 and additional optional element 100.

In Figure 2B, the wet C02 stream 7 s of a membrane dryer 71 where the feed stream is emitted. The dry run 72 is sent to the adsorption bed on which the C02 of the feed is stirred at dry C02 leaving the CO2 station 80. While the C02 is adsorbed by another bed 81 it is being regenerated. humidity comes out of the vacuum pump 74 between 75.

In FIG. 2C, the wet C02 stream is 7 s of an absorption system 76 where the feed stream is mediated by a medium such as ethylene glycol. The moisture-using beds would normally contain a structured or structured water transfer and the adsorbent phases would flow in the counter-rotating direction of dry feed 72 leaving the station 76 to be sent to C02 adsorption beds. 81 limits the C02 of the feed and a current 02 dry 85 leaves the ras separation system the C02 is being adsorbed at least to 81 is being subjected to regeneration or regenerated solvent entity 78 is sent to the 76th room for moisture removal. The current is taken by means of heat exchange with power, or the current 95 can be heated dir or electric power. The current loaded with absorption system 76 as current 75.

In Figure 2D the wet C02 stream 70 passes moisture adsorption system 79 where the feed stream is removed by an activated alumina, silica gel or a dry feed medium sieve 72 that leaves the humidity system. 79 is sent to the beds of 2 81 where the C02 of the feed is removed exhausted in C02 leaves the separation system While the C02 is removed in one or more of C02 81, at least some other bed is removed by means of the hot heat exchanger. The stream 95 can also easily use electrical power. The current flows out of the wetting adsorption system 73. A vacuum pump can be used to provide additional driving force for the medium, and the moisture-laden current flows out in vacuum mba 74 as the current 75.

The moisture adsorption system 79 may contain multiple humidity adsorption beds as well as other impurities and heavy carbides that may prevent the adsorption of C02 adsorption beds 81. The moisture beds in the moisture adsorption system 7 n designed to remove some of the impurities d ufre, oxides of nitrogen and mercury in the food for the desorption of other impurities t heavy hydrocarbons, sulfur oxides, or geno and mercury. This can be done in three or more beds and is described immediately.

Figure 3 illustrates by way of example the moisture adsorption system 79 wherein the additional ezas, for example, hydrocarbons, nitrogen oxides, and mercury are roasted from a combination of adsorption per oscil on and temperature, adsorption system by oscillation and temperature of three beds for removal of impurities is illustrated in Figure 3; However, moisture and impurities are removed in a three-bed system. If there is no need for impurities such as carbide oxides, two beds can be used operating in a wet feed into the adsorption system 79 as the stream 70 through the valves and 220, respectively. These valves 200, 2 wave the flow of the feed gas in directions 230, 235 and 240, respectively. Each sensor 230, 235 and 240 have first layers of a 235a and 240a, respectively, which components such as activated alumina, molecular silica gel such as zeolites 3A, 4A, 5A and moisture ion. Within the containers 230, layers 230a, 235a and 240a are located 230b, 235b and 240b, respectively, the selective adsorbents for hydrogen and sulfur, and mercury. Activated adsorbents, zeolites such as 13X, and gnadas can be used to adsorb these i connected to discharge lines with valves 2 respectively. Depending on the bed being emitted, the stream containing dry C02 leaves moisture sorption 79 through one of these as stream 72 and is sent to the s 2 80 system. 80 is used to regenerate ads ad beds. For PSA or VSA regeneration mode, e 95 enters through valve 290 and then u 250, 265 and 280 and exits ad system 79 via the corresponding valves 205, 2 current 73. If a vacuum pump or the purge gas 95 leaves the ad system 79 as the current 75. For the reg mode the purge gas 95 is heated in the heat exchanger cal 96 and enters the containers The various layers are preferably contained in simple elements, as shown in the figures, layer may be contained in containers, either. The duration of each complete cycle of the s, at most, of several minutes (mins) typical minutes, while the duration of the reg is generally approximately 1-1, during any simple phase of the recipients in the PSA mode If the VSA will experience PSA or VSA while the third will carry out a single stage of regeneration, it will be assumed that process A is carried out with pressurization at pressure during the adsorption stage and reduced to atmospheric pressure. or lower during egeneration. The pressure in the ex ca container; and a third phase, in which the recipients undergo an alternate cycle of PSA or VSA while in the container 235 experience reg.

At the beginning of stage 1 of the first so, one of the containers 230 or 235, for example 230 is in the adsorption mode and is in the regeneration mode. With the r initially in the adsorption mode, alit a 70 enters the bed through the open valve of the bed through the open valve 24 for adsorption, the. vessel 230 is pressurized on adsorption through valve 200. Mitation 70 passes through the vessel 230 substantially all the vapor of carbides, sulfur oxides and mercury and humidity 79 is heated in the tank. heat exchanger 96 and then flows through 240a and 240b into vessel 240. While heated it passes through layers 240a and 2b 240, the purge gas desorbs the moisture hydrocarbons, the nitrogen oxides and sulfur from different layers that have been gradually deposited in the PSA or VSA 1 stages in this vessel. The regeneration gas, desorbed joints exits from vessel 240 to open 225. After a certain time with moisture entrainment in stream 72 and the heat retentate in the bed, typically from 4 to 60 mi. to experience regeneration the container 235 begins to remove moisture ezas. The containers 230 and 235 continue ezas As the PSA or VSA process progresses in the recipi, several impurities such as sulfur oxides and uals are desorbed more strongly than the vapors accumulate in these vessels because they are not the purging step of the ossification or oscillation of the adsorption. empty. When the accumulation of components in one or more layers reaches the point of adversely affecting the efficiency of gasification, the first phase of the process involves the second phase.

During the second phase of the process recipients 235 and 240 are in alternate service of PS sorbents in vessel 230 under reg. At the beginning of stage 1 of this phase of the container 235 or 240, for example the r of adsorbent 240 and exits through the valve of the purge gas entering the ADS 79 system is heated in a heater or intercam 96 and then flows through the layers 230a to container 230 and desorbe the moisture residues carbides, the oxides of nitrogen and sulfur, and the ace different layers that have gradually been aquarium 230 in the stages of PSA or VSA given out in this vessel 230. The aeration, together with the impurities desorbed from the valve 230 through the open valve 205. D or time based on the concentration of humectant 72 and the retention of the heat front in vessel 235 begins to experience regas that the vessel 240 begins to remove impurities. The containers 235 and 240 continue to run and the third phase is started.

During the third phase of the process, recipients are in the PSA or VSA service and the adsorbent 235 undergoes thermal regeneration. The third phase is similar to the operation of the second phase. After they complete the three or so, they start again with phase one and re-phases in a cyclical way.

Like the PSA or VSA beds, the reaction or reaction of C02 (beds A to E in the experiment undergo a cyclic process for continuous proportion and also to maximize recovery).

These beds contain one or more materials that are significant for C02 with respect to major elements of the flue gas, no, nitrogen and argon. Some of the materials in Figure 4 would typically experience eqionation, equalization, rinsing with CO2, heating with evacuation, cooling with esurization. Depending on the material and the process, different combinations can be used to maximize the recovery of C02. Some of the cycles can be eliminated such as the cooling of beds. During the C02 81 adsorption operation, any impurities in the feed to the captive section will be removed because most bents have a greater affinity for oxides of Since most adsorbents have C02 by nitrogen oxides, the nitrogen oxides in the feed would pass through the exhausted current. separation system of C02 80. In the diagram schematically a process of capture of beds. The stage of feeding C02 and the roduction of C02 are continuous in this cycle. C02 is illustrated using a process s the capture process of C02 is not limited to OS. The process can use less than five lech inco beds although a minimum of d is required to carry out the capture at the same time and p 02. As illustrated in Figure 4 above, a bed is removing C02 entaking using adsorption or reaction, Another feeding stage of equalization and pressurizing the bed is producing C02 while the bed is producing C02 during the treatment and evacuation and the fifth stage. Each individual stage of the capture process is of the order of 2-60 minutes for productivity. of process. A typical five-bed configuration cycle from the figure to Table I.

The feed to the adsorbers should be at a temperature between approximately ° C and at pressures between approximately 1. bar, and at a temperature in the impedance of 20 ° C and 60 ° C. For the capture of combustion of a power plant, the pressures will be imediately 1.07 and 1.34 bars. The temperatures are in the range of 80 ° C and typically in the range of about -150 ° C. The concentration of C02 in the accumulated recesses during the normal operation The operation of several valves is illustrated in steps 1 and 2 of Table I. In both stage the A bed, the supply gas 72 enters before the open valve 302, the C02 is c? The bed and the current exhausted at C02 exits the current 85 through the valve open stage 1, the beds B and E expel pressure through the valves and 430. During stage 2, bed B is p The bed A through the open valves During both stages 1 and 2, the bed C is reheated under vacuum and the valves 366 s 02 product of high purity exits as the pump S enters the vacuum pump 110. As 1 and 2, bed D is regenerated by heating As shown in Table I, several stages of aeration are significantly faster than typical adsorption by temperature oscillation. These stages are of the order of hours. For adsorbs that are tolerant to moisture, it can be heated by direct heating with steam although this will have to be followed to remove the steam, and then the bed will cool. For adsorbents or reagents that before to moisture such as direct zeolite with steam is not an option with dry gas will be very slow. For these beds they can be heated indirectly. One configuration is the configuration of shell and tube adsorbents or reagents are contained in small tro and the heating medium flows straight is a plate configuration and the adsorbents are contained in alternate atoms and heated fluid alternating parallel atoms. It can be used heated as the heating medium of shell and tube and the confi lac and frame, cold fluid C02 removal cap can be used to remove the reaction or chemical reaction. Cold flow was also carried out for the cooling stages 0. For modernization applications, it is easy to use the heating or pressure water as the regeneration medium per cycle. The interruption of the steam power cycle would be modernized with more vertical beds. Use is discussed above. If a C02 purification is used, an ion of the C02 current is allowed to permeate the C02 stream of higher purity as the rinsing current in the C02 portion. The rest of the stream is used more and used for the recovery of oil, industrial applications of C02 · If a projection is used for the purification of C02, the is as oxygen and sulfur dioxide are reaction with a degassing and The purified corr can be further compressed and used. If a process of purification of C02 is used, the C02 produces a pipeline and the non-condensable ones are r Example 1 Zeolite 5A commercially available from t to 8 x 12 (approximately 1.5 mm) was obtained from Corporation and charged in two 18 mm diameter. The total weight was approximately 500 grams of feed with an immaterially 12.5% C02 with the oxygen residue, to simulate the combustion gas of coal burning energy, through a flow rate of 11 ndar./ min and at a pressure of 1.34 standard bars refer to 21.1 ° C and 1 O adsorbent was cooled with a jacket with water / glycol mixture at 30 ° C. The report was heated with a shirt containing the II. Capture Process Cycle of C02 from two to Bed A Bed B Tie Stage Adsorption Heating with 8 evacuation Equalization Inactive Rinse Inactive heating Heating Pressurization Heating with Adsorption evacuation Equalization Inactive Rinse Inactive Warming Pressurization Heating ° C an average purity of CO 2 of 99 was obtained. Average CO 2 concentration of 88%. For a temperature of 40 ° C, an average purity of 2% and an average recovery of C02 of 84% were obtained.

Example 3 The process of Example 1 was run with a zeolically available 8 x 12 ida mesh size from Aldrich Corporation. The nutrient pressure, and the concentration of C02 of feeds as in Example 1 and the cycle of p abla II was used. Again, the daytime concentrations of C02 and the C02 product were analyzed as useful for infrared C02. For a temperature of 20 ° C, an average purity and an average CO 2 recovery of 87% were obtained. Feed rate of 30 ° C was obtained standard / min. The adsorbent bed was cooled to containing a water / glycol mixture at 20 ° C. of process of Table II. The bed was regenerated with a shirt containing a mixture of water. The concentrations in the exhausted product stream were analyzed using a analyzed sample. For these process conditions, an average of C02 of 91% and a recovery pr of 86%. The results of this example indicates that the present invention can provide ables and recoveries for currents that are very low in carbon dioxide such as the energy that burns natural gas.

Comparative Example 1; The zeolite of Example 1 was used for a 0.5 minute oscillation adsorption process, a rinsing time, an evacuation time of 4.0 minutes, and a 0.5 minute resurfacing, a C02 dioxide of 81.5 was obtained. % and an average recovery. The reduction of the feed flow to 2. give per minute decreased the average purity at average rate to 26%. For a standard flow of food per minute and a 2-minute reduction cycle, equalization of 0.25 minutes, .5 minutes, evacuation of 2 minutes, and presuri minutes) an average purity of 59 average generation of 43.9% was obtained.

The comparison of the results of this example 1 indicates that the performance both in terms of C02 and purity of CO2 is without thermal regeneration of the beds. of 4.5 minutes, and a presurization time of 0.25 minutes house one, and most of the heat of adsorption of water is given. The dry product from the bed of ads to purge after reducing the pr imadamente. the atmospheric The product dew point that emerged from the beds was null and concentration of the humidity of the lower part to 1 part per million (ppm) for a few days.

This example illustrates that under certain conditions of feed of the separation of rse at very low humidity levels for measurement of C02 in the separation section of C urga in a process in which the hume to C02 adsorption is removed would be The exhausted current in ra of C02 offers several advantages. The process can for modernization applications as well as plants. The modifications required for nergy for the applications of modernize ficativamente small that the necessary ones for l 2 with base of amines. The process is applicable to energy sources that burn coal as those that are natural. The process is also applicable to entities such as the process streams of chemical reagents that contain cation dioxide from the adsorption processes where the geno and sulfur (N0X and S0X) in the feed with the solvent irreversibly and ion to levels below about 10 pp in the feed does not adversely affect the ad xigen in the feed has no effect as a power plant that burns natural gas for coal gasification.

The above examples have been provided for purposes of explanation and will not be considered as limiting the present method here. Although the invention has been described in several embodiments, it is understood that the same have been used herein, they are palpitation and illustration, rather than words of li, although the invention has been described herein with particular materials and modalities. , it is intended to be limited to the particular features; Rather, the invention extends to all methods and functional uses, such that they are included within the appended claims. That

Claims (1)

1. CLAIMS The invention having been described as before as property contained in the ndications: 1. A method for separating carbon dioxide from gas containing water vapor and onales, characterized in that it comprises the following steps one or more times: subjecting the gas stream to a first moisture ion, wherein substantially all of the gas in the gas stream is removed using a group comprising pressure adsorption, slip adsorption, membrane separation, and absorption; subjecting the gas substantially free of steam to water vapor, and wherein the substantially dry stream of carbon from the second portion by temperature swing is used for regeneration bents in the first stage of re d using one of a Oscillation adsorption mode, a combination oscillation adsorption mode thereof, to provide a sora for a membrane drying step, stir the absorbent in the absorption stage. 2. The method according to claim 1, because the pressure of the gauge current of about 1.07 to about, the concentration of carbon dioxide is valued from about 3% to 60% in volume of gas is in an approximate range. 80 ° C. This is because the temperature in the second period due to temperature oscillation during the adsorbent process increases to approximately 300 ° C. 5. The method according to the claimed one because the duration of the second reaction by oscillation of temperature is in approximately 2 minutes to 60 minutes. 6. The method of compliance with the claimed claim is that the gas is a combustion gas lanta of energy that burns coal, a plant dusts natural gas, and a refinery. 7. The method according to claim 1 wherein the adsorbent used in the removal of moisture is selected from an activated alumina, silica gel, and A, 13X, NaY and CaX, natural metal framework compounds, natural and selected zeolites. , modified activated carbon and pi clays 10. The method according to claim 1, because the purity of the stream of d not substantially free of water vapor produces the adsorption step by higher temperature oscillation. 11. The method according to claim 1 wherein the regeneration steps of heating the bed of direct adsorbent or gas or indirectly using steam or nte in a heat exchange configuration. 12. The method of compliance with the claim because additionally comprises the bed after heating the bed to by temperature oscillation carbides, oxygen, nitrogen, argon, and or. 15. The method according to claim 1, wherein the additional impurities of the group comprising hydrocarbons, sulfur oxides, and mercury are removed from the first stage of moisture removal. 16. The method according to claim 1 wherein the adsorbents used for the hydrocarbons, nitrogen oxides, river oxides are selected from activated carbon, impregnated zeolites, modified activated carbons. 17. The method according to claim 1, the moisture removal process performs the following steps one or more times: subjecting the gas to a cyclic process of pressure adsorption comprising alternating the tion and the stages of regeneration of the adsorbent. adsorption and the second section, thus substantially removing all of the gas, while desorbing the water vapor re impurities of the adsorbents in the first zone of the third adsorption section of the adsorbents; subjecting the gas to a cyclic pressure-adsorption process comprising alternation of the adsorption section and the regeneration stages of the adsorption section and the third section, thus substantially removing all of the gas, while desorbing the water vapor. impurities of the adsorbents in the first zone of the first adsorption section of the adsorbents. 18. The method according to claim 1 wherein the step of heating is carried out at a temperature in an immately 80 ° C-300 ° C. 19. The method according to claim 1 wherein the stream of gas containing and additional impurities is sent directly to the adsorption stage by first oscillating the moisture and impurities added to the second stage of adsorption by oscilture comprises an adsorption step. for product depleted in carbon dioxide, and an adsorbent aeration which comprises heating the ica additionally by means of a distillation process, a degassing adsorption process to remove impurities in nitrogen, oxygen, argon, ns oxides. of sulfur, and humidity. 22. The method according to claim 1 wherein part of the carbon dioxide is used to provide a high purity rinse of the adsorption stage by temperature oscillation of a stream of dioxide substantially free of water vapor. 23. The method of compliance with the claim because the second stage of temperature adsorption comprises multiple beds undergoing the steps of adsorption ation, rinsing of CO2 heating