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    • 专利摘要:
    Installation and procedure to recover gaseous substances from gaseous streams. It allows to recover CO2 from combustion gases with great cost savings compared to using other technologies currently under development, without producing environmentally harmful substances. The installation comprises: a) a first Gas Treatment Module (Module 1), to receive a first gaseous inlet stream (1) comprising nitrogen oxides, sulfur oxides and CO2, said first gas treatment module (Module 1) is where the temperature and pressure are accommodated to proceed with its drying, eliminating water, nitrogen and sulfur oxides, unburned and rest of suspended solids, preparing the first outlet stream (13) for injection in the second Module where the gas separation process will take place, with a composition that allows operation under design conditions according to the adsorbent material specifications. The second outlet stream (12) incorporates the separated water, the sulfur oxides, the unburned ones, partially the nitrogen oxides and remains of suspended solids removed from the inlet gas stream (1); b) a second CO2 Separation Module (Module 2), where the first outlet stream (13) of Module 1 is treated by a PSA adsorption / desorption process to separate the selected gases enriching the third outlet stream (27) of Module 2. The separation of gases occurs taking into account the selectivity of the adsorption process that presents a certain adsorbent porous solid, generating two output streams, a third output stream (27) with a higher concentration of the gaseous substances to be extracted than those of the first inlet stream, and a fourth outlet stream (16) with a concentration of the gaseous substances to be extracted lower than those of the first inlet stream (13); and c) a third Module where the CO2 purification process will take place (Module 3), optional, where the third outlet stream (27) of Module 2 is treated through a PSA adsorption / desorption process to separate the selected gases enriching the fifth outlet stream (44) of Module 3. The separation of gases occurs according to the selectivity of the adsorption process that presents a determined porous adsorbent solid, generating two outlet streams, a fifth outlet stream (44) with a concentration of the gaseous substances to be extracted greater than those of the first inlet stream, and a sixth outlet stream (16) with a concentration of the gaseous substances to be extracted lower than those of the third inlet stream (27).
    公开号:ES2751176A1
    申请号:ES201830944
    申请日:2018-09-29
    公开日:2020-03-30
    发明作者:Moreno Carlos Manuel Padilla
    申请人:Bluegeneration S L；
    IPC主号:
    专利说明:

    [0001]
    [0002] INSTALLATION AND PROCEDURE FOR RECOVERING GASEOUS SUBSTANCES A
    [0003]
    [0004] OBJECT OF THE INVENTION
    [0005]
    [0006] The present invention can be included in the technical field of the treatment of any gaseous stream composed of atmospheric gases, in particular, the treatment of combustion exhaust gases, among other mixtures.
    [0007]
    [0008] Said installation and procedure can be applied for the recovery of any gaseous substance that is part of the gaseous stream to be separated.
    [0009]
    [0010] The object of the invention refers to an installation, its control system and a method for recovering substances, particularly greenhouse gases, mainly carbon dioxide (CO2), from gaseous streams, impoverishing said gaseous streams in the substances recovered.
    [0011]
    [0012] BACKGROUND OF THE INVENTION
    [0013]
    [0014] In the coming years, based on compliance with EU regulations and the COP21 (Paris) and Kyoto agreements, it will be necessary to reduce the emission of greenhouse gases beyond what can be reduced through energy efficiency techniques and by substitution with renewable energy sources. The most important of these greenhouse gases is CO2, although not the only one.
    [0015]
    [0016] One of the ways to carry out reductions in the emissions of these gases is to use means of separation of the gaseous substances contained in gaseous streams with the aim of capturing greenhouse gases.
    [0017]
    [0018] Until now, the methods used for the separation of gaseous substances focused mainly on physical-chemical processes that seek to use polarity / apolarity, molecular size, oxidative / reducing characteristics and the change of state of the substances that make up the gaseous stream. . Such procedures are highly Energy demanding and / or include the elaboration of intermediate chemical products that are harmful to the environment, which implies high safety costs to avoid the release into the atmosphere of said harmful products.
    [0019]
    [0020] Comparing with different previous patents, it is observed that the system proposed as a device of the present invention is substantially different for the preferred embodiment of the present invention.
    [0021]
    [0022] US8052777 patent "Vessel, system, and process for minimizing unequal flow distribution".
    [0023]
    [0024] Description : PSA (Pressure Swing Adsorption) process chambers with internal partitions for homogeneous flow distribution. These systems can contain one or more walls that make up different beds of adsorbent material, leaving two different bell-shaped sides to spread the flow in the chamber.
    [0025]
    [0026] Analysis : System with two cameras working in false continuous, one adsorbing and the other desorbing, in the PSA process. Initially created to purify H2 streams with a high percentage of this gas, and with Zeolite A or X type adsorbent material, aluminas, etc. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0027]
    [0028] US8268043B2 patent “Modular compact adsorption bed”
    [0029]
    [0030] Description : Modular and compact structure of adsorbent beds. Before conventional bed chambers, this structure has a plurality of connected beds to form the integrated structure. It offers great product separation capacity per unit volume compared to conventional ones. The modular design that is presented returns low manufacturing costs and ease in transporting the assembly and repairs, as well as high simplicity when loading the adsorbent material.
    [0031]
    [0032] Analysis : Suitable for accommodating adsorbents to capture CO2, N2 or H2O. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the proposed system as a device for the present invention.
    [0033]
    [0034] US6994111 patent “Toroidal vessel for uniform, plug-flow fluid distribution applications”
    [0035]
    [0036] Description : The present design is an improvement of the conventional adsorption chambers, whose work is of type "plug-flow fluids applications", processes with an inlet and an outlet in which a uniform distribution of the flow in the interior is desired (applications chromatography or processes with adsorption beds.) The proposed chamber is of a toroidal type that allows an efficient laminar distribution.
    [0037]
    [0038] Analysis : Chamber design that pursues concise objectives, these being to treat a flow with uniform, homogeneous distributions and with large areas of exchange. Toroidal chamber, with inputs at the bottom and outputs at the top. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0039]
    [0040] Patent US1683567A2 "Reactor with an annular adsorptively active bed and an annular inert bed"
    [0041]
    [0042] Description : The system is made up of multi-cameras. One of the internal rings or subchambers of the system houses the adsorbent material, while the other chamber contains an inert material to the adsorption process that is created in the first, both separated by a gas or permeable liquid. The gas inlet to be processed is introduced by the supply and is processed as it flows to the outermost ring, being extracted by the connection to the outside.
    [0043]
    [0044] Analysis : Device similar to that analyzed in the previous patent US 6994111, the main difference between the two being the guiding of the effluent inside the chamber, from concentric ring inside to outside. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention. Furthermore, this system requires other intermediates for its operation in addition to the initial adsorbent porous material.
    [0045]
    [0046] Patent EP1500424A1 "Pressure Swing Adsorption system multi-chamber canister" Description : Multi-chamber system for PSA processes. An initial chamber receives the compressed fluid for the process and distributes it evenly to the sieves with Zeolite-type adsorbent material. The chambers have multiple internal compartments to, among other objectives, maintain a uniform temperature in chambers, this also serves to promote adsorption and not have large thermal gradients that would disturb the uniformity of the gas concentration in the chamber.
    [0047]
    [0048] Analysis : Chamber aimed at improving the PSA adsorption process initially designed to treat atmospheric air that will be fed through the compressor shown in the figure at the top of the chamber. Compartmentalized chamber not concentric but with parallel axis arrangement. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0049]
    [0050] Patent US5931022 "A ir purification process with thermal regeneration"
    [0051]
    [0052] Description : Use of alumina-type adsorbent, such as Zeolite 13X (negatively charged aluminosilicates), in PSA processes for purification of gas streams by CO2 removal. A process of regeneration of the adsorbent is proposed, according to which the adsorbent bed will be heated to a certain temperature, removing the stored remains of CO2 and H2O from the material. This process is necessary since, despite the initial conditioning, a small percentage of water always enters in the form of steam, which after certain adsorption / desorption cycles succumbs to the adsorptive capacity of the Zeolite. The proposed process consists of periodic heating after certain adsorption / desorption cycles, heating.
    [0053]
    [0054] Analysis : System that uses Zeolite X type adsorbent material. PSA processes for CO2 capture. Regeneration of the bed after successive adsorption / desorption cycles to remove residual CO2 and H2O not desorbed in the desorption phase by applying heat (thermal regeneration). The temperature of thermal regeneration, when it comes to processes such as those covered in the patent, is in the optimal range of (100-250 ° C). The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention. Likewise, it introduces heating of the fluidized bed to improve its cyclical regeneration capacity. It is a PTSA process, completely different from the PSA process proposed as a device of the present invention.
    [0055] US6362122 patent “Heating the composite o f zeolite and binder with aqueous caustic solution; washing, drying and roasting; decarboxylation ”
    [0056]
    [0057] Description: Process for the regeneration of Zeolite-type composite materials after use in adsorption, for example in adsorption of carbonaceous compounds. The process consists of contacting the material with a caustic solution, such as sodium hydroxide, isolation of the compound, washing with water, drying and, finally, calcined. The result is a regenerated material. Contact with the aqueous caustic solution is carried out between 20 and 110 ° C for a time of 1 to 48 hours, then it is washed with water and dried. The calcination phase is carried out between 500 and 700 ° C for a time of 1 to 24 hours.
    [0058]
    [0059] Analysis : Regeneration of adsorbent materials, among the suitable Zeolites. Proposal for regeneration with caustic solution, succession of the process: Contact with solution in isolation conditions (20/110 ° C; 1/48 hours). Contact with H2O and subsequent drying. Calcination (500/700 ° C; 1/24 hours). It is a PTSA (Pressure and Thermal Swing Adsorption) process, completely different from the PSA process proposed as a device of the present invention which does not require cyclical regeneration.
    [0060]
    [0061] Patent US6402814 "Adsorption, regeneration, depressurization cycle"
    [0062]
    [0063] Description : The described regeneration process, which involves depressurization of the chambers after adsorption, includes a heating phase, during which the porous bed is purged with a gas, and a cooling phase, during which the porous bed is purged with a cooling gas. The process refers to treatment of beds in TSA (Thermal Swing Adsorption) processes with alumina or zeolite adsorbents (X, L, XLA, etc.) to purify air currents (removing CO2 and [H2O] v) destined for plants located downstream distillation or cryogenics.
    [0064]
    [0065] Analysis : Process designed for the regeneration of Zeolites type X, L and XLA, initially designed to work in TSA processes. Succession of the process proposed in the patent: Chamber depressurization after adsorption. Heating. Gas purged. Gas cooling. It is a TSA process, completely different from the PSA process proposed as a device of the present invention.
    [0066] Patent EP1574246A1 "Periodic high temperature regeneration or f thermal swing adsorption systems"
    [0067]
    [0068] Description : Improved TSA type system to avoid water damage in the CO2 adsorption system of gas streams by adsorbing with Zeolite X. This is solved by periodically heating the adsorbent bed to a temperature higher than the phase design temperature. desorption. It is presented as an alternative, or complement, to the typical dehumidification processes in which the gas stream is made to flow through a bed, before the chamber, of silica gel or alumina.
    [0069]
    [0070] Analysis : Regeneration in TSA process. Proposed Process: Initially adsorbed by contacting the gas stream with a selective adsorbent to remove the desired components from the stream. After the adsorption of regenerates, heating to a temperature in the range of (40-400) ° C. Chamber and porous bed cooling down to the initial process temperature. Periodically, and not between cycle and cycle, a second regeneration is carried out preferably between 200 and 400 ° C, and in a second phase of experimentation, the temperature is strictly 50 ° C or more above that of the first regeneration (first regeneration). : between 40 and 400 ° C). It is a TSA process, completely different from the PSA process proposed as a device of the present invention which does not require cyclical regeneration.
    [0071]
    [0072] US5968234A patent "Adsorption of water and carbon dioxide onto solid adsorbent to separate from feed air to be purified, periodically regenerating adsorbent with portion of nitrogen-containing compressed gas from the air separation unit ( ASU)"
    [0073]
    [0074] Description : System of regeneration of adsorbent materials type Zeolite X, Y, A, silica gel, chabazite, mordenite and mixtures of them when they begin to present low yields in the adsorption of CO2. To carry out the proposed thermal regeneration, a stream enriched in N2 is used, specifically using the stream formed by the molecules that the material does not capture during the adsorption phase. This regenerating stream undergoes a multistage compression process before regenerating, giving it a considerable pressure increase.
    [0075]
    [0076] Analysis : Regeneration for adsorbent materials type Zeolite X, Y, A, ..., which have been used in CO2 and / or [H2O] capture processes v. Through a compression process Multistage the part of the stream not adsorbed at high pressure is introduced into the chamber. The high pressure stream will be highly enriched in N2 and will avoid having traces of CO2 and H2O as well as hydrocarbons. It is a process of regeneration of porous materials, not of separation or purification, completely different from the PSA process proposed as a device of the present invention.
    [0077]
    [0078] US5938819A patent "Preferential adsorption or f carbon dioxide at low operating pressure followedby regeneration or f adsorbent by purging with dry air; simplification ”
    [0079]
    [0080] Description : Separation in PSA process in large quantities of CO2 from an effluent mainly composed of CH4, the adsorbent is of a typology rich in natural Na. The removal in the regeneration of the residual CO2 that collapses and reduces the adsorbent material is carried out at moderate pressures, close to atmospheric, and with a high volume of air. In this way, CO2 carries out a leaching process (in metallurgy: extraction from a mineral of a species of interest by means of reagents) and leaves the adsorbent bed, returning the adsorbent capacity. Evaluating results with different operating modes, it is determined that the large amount of air is more influential than the high pressure.
    [0081]
    [0082] Analysis : PSA process to adsorb CO2 and generate effluent rich in CH4 through the use of material rich in natural Na. In the regeneration phase instead of high pressures to attack the material, it submits it to moderate pressures but high volumes of air. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0083]
    [0084] Patent US0061747 "Dynamic and continuous control for pressure swing adsorption"
    [0085]
    [0086] Description : Parameter control process to regulate PSA gas flow treatment system. In the "example" case shown in the patent, an air flow is treated to separate O 2 from N2 by Zeolites. The objective of this system is to monitor in real time at least one parameter of the flow (P, T, flow, % of some component, dew, humidity, etc.) The monitored parameters are compared with threshold values (critical values that upon detection will activate actions on the system components.) The system of this patent consists of a PSA block, where adsorption, and a "sentinel" block, which continuously monitors the desired parameters. This control system is valid for CO2 capture systems (exhaust from plants, factories, etc.), NH3 or H2S (refineries).
    [0087]
    [0088] Analysis : Control of PSA systems. The example treated in patent refers to separation of N2 from O2 in air currents. Control system equally valid for capturing CO2, NH3 or H2S. Integration of components, which are, adjustment system, control system and alarm system. The control system describes one of the possible control systems applicable to PSA processes. Completely different from the one proposed in the device of the present invention, in which the sentry block is not necessary to control all the control and alarm parameters in real time and simultaneously.
    [0089]
    [0090] US4472177A patent "Controlsystem and method forair fractionation by vacuum swing adsorption"
    [0091]
    [0092] Description : System and control method for VSA (Vacuum Swing Adsorption) processes. Through predetermined values of concentrations and pressures introduced into the control system, alternation between chambers and phases is carried out in each chamber. In the case of adsorption, the system is ready for when certain product concentration values are detected at the outlet. a process shutdown is imposed. In the same way, when desorption is performed, this process will be interrupted when values below a certain threshold are detected.
    [0093]
    [0094] Analysis : VSA process control. Structures are presented for the control of valves and switches that interconnect a programmable controller with the separation system. A variable time system is presented that controls each of the stages of the process carried out by the control system of the separation process. The specific case treated is a VSA process, with two parallel adsorption columns, two pretreatment chambers downstream of the columns and two chambers for upstream desorption. Although the PSA process proposed for the present invention uses vacuum systems to produce pressure desorption, it also uses entrainment by means of explosive injections inside the desorption chambers to achieve the extraction of the adsorbed gases in the shortest possible time. in the porous material, as well as the extraction by excess pressure from the adsorption pressure to the atmospheric pressure, therefore the systems are completely different.
    [0095]
    [0096] Patent US4696680 "Method and apparatus for the selective separation or f gaseous coal gasification producís by pressure swing adsorption ”
    [0097]
    [0098] Description : Gas separation system by PSA process of a mixture composed of these from a coal gasifier. The objective is to sequentially separate the gases in a discrete way (H2, CH4, CO, CO2, ...) thanks to their different adsorption / desorption pressures. These pressures range from atmospheric pressures to pressures of 5 to 35 bar (g). In a first phase, CO2 and H2S are adsorbed, in a second phase, CO, H2 and CH4. The H2 outlets serve to pressurize the following adsorption chambers, reaching these values from 5 to 35 bar (g). The main objective is the obtaining with high purity of H2, 99.7%, and with less than 0.01% of sulfurous compounds. Process sequence: The mixture is introduced into the first adsorption column and this is pressurized so that the gases are adsorbed sequentially. After reaching the desired pressurization level, the chamber begins to be depressurized. With the decrease in pressure, the set of gases (H2, CO, CH4) is evacuated first. Continuing the descent to Patm and reaching negative relative pressures, the acid assembly (CO2, H2S) is evacuated. The two sequential outputs are derived to different process lines. By repeating the process for each set of gases, pressurizing and depressurizing appropriately, H2, CO and CH4 on the one hand and CO2 and H2S on the other are completely separated and with high purity levels.
    [0099]
    [0100] Analysis : Sequential separation process of gas mixture by PSA process. Mainly oriented to gases from coal gasification (H2, CO, CH4, CO2 and H2S). The treated pressures range from 0 bar to 35 bar in order to obtain high purity all gases separately. The system describes the PSA process sequentially, non-continuously and without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as the device of the present invention. Process developed for gasification prior to combustion of a gaseous fuel and therefore to work at high pressure, compared to that of the present invention developed to treat gases from combustion and therefore at low pressure.
    [0101]
    [0102] WO Patent 2009/073928 "A plant and process for recovering carbon dioxide"
    [0103]
    [0104] Description : PSA system with Zeolite X or Y type adsorption material. Originally for treatment with gaseous effluents with a high percentage of CO2 (> 50%), such as vents from soft drink carbonation plants. The conditions of entry to the system are between (10-90 ° C) and (1-2) bar. Desorption is performed in a vacuum range between (2-50) kPa or (0.02-0.5) Pub. As an extra energy recovery process, it sends the CO2-poor stream leaving the chamber during adsorption, which will be between (10-40 ° C), to cool the coolant that works by cooling the rings of the vacuum pumps. The system aims to simulate a pseudo-continuum in which the two chambers of the system work alternately one in adsorption and the other in desorption. The transition of the chamber that ends the desorption, to P approx. 0.02 bar, up to atmospheric pressure, is done through the interconnection of both chambers, since pressures are balanced because one is depressurized and the other at 2 bar. This avoids the use of common chamber emptying methods or purges that are carried out in the interval between the end of adsorption and the beginning of desorption (this type of purge is usually carried out in the "Heavy purge" type). with currents product of high concentration in CO2 or "Light purge" when they are residual currents with lower concentration of CO 2).
    [0105]
    [0106] Analysis : PSA system, Zeolite X or Y adsorbent material, treatment of CO2 concentration in gaseous effluents with high concentrations of this gas (> 50%). Adsorption processes: Between 10 and 40 ° C and between 1 and 2 bar. Desorption process: Vacuum between 0.02 and 0.5 bar. Apparently meets the conditions of false continuum by alternating chambers in adsorption / desorption. New Features: Depressurization is done by interconnection between chambers. In the WO 2009/073928 system, both chambers are connected, making it a parallel derivative and the equalization process ends when the pressures in both chambers are equalized. In our device of invention, recirculation occurs, through vacuum pumps, to the desired CO2 concentration. The system describes the PSA process allowing equalization between chambers but without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0107]
    [0108] Patent US3885927 "Removal o f carbon dioxide from gas stream s"
    [0109]
    [0110] Description : Capture of carbon dioxide from less polar gaseous currents than carbon dioxide, passing the flow through a Zeolite type X matrix, silicon / aluminum ratio <1.15. Particularly effective process when the adsorption phase is applied with temperatures above 20 ° C and low percentages of carbon dioxide in the streams.
    [0111]
    [0112] Analysis : Adsorption system with Zeolites X. It recommends applying low temperatures in the process, starting it at around 20 ° C, since it assumes that during the process there will be an increase due to compressions and other pretreatment phases. Define the range as admissible if it is between 30 and 80 ° C. It makes special reference to the fact that the CO2 in the initial gas stream has a partial pressure greater than 25 mbar. It is a more scientific-technical patent for research than for engineering development, and therefore the exposition of a specific operating procedure is not appreciated. The system describes the PSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0113]
    [0114] US5689974A patent "Method and apparatus for pre-purification for air cryogenic separation plant"
    [0115]
    [0116] Description : Pre-purification method for separation of water vapor and CO2 from an air stream for its subsequent derivation to the cryogenic phase. It states that the flow can be operated by adsorption at high temperatures without precooling.
    [0117]
    [0118] Analysis : The method includes the steps of: Adsorption: At defined pressure and temperatures between 10 and 45 ° C. Depressurization from P of adsorption. Followed by phases of heating, cooling and repressurization. It is recommended to carry out the adsorption with the introduction of the flow into the chamber at speeds between 0.05 and 0.4 m / s. The chamber will have an initial tray with suitable adsorbent to remove the humidity from the flow and another tray to capture the CO2. The system describes the PTSA process directly without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as the device of the present invention.
    [0119]
    [0120] Patent US5906675 "A ir purification process"
    [0121]
    [0122] Description : Three-chamber adsorption system with zeolites and alumina activated in parallel. The process has three steps: The first, a PSA, is carried out in the first two chambers (acting alternately in adsorption / desorption) while the third chamber is in thermal regeneration.
    [0123]
    [0124] Analysis : PSA adsorption process. Alternation of three chambers in parallel, working respectively on adsorption, desorption and regeneration. The cameras have five levels to capture the compounds. The system describes the PTSA process directly without the ability to allow control over the concentration of the third or fifth output currents of the proposed system as a device of the present invention.
    [0125] US6106593A Patent "Purification o f air"
    [0126]
    [0127] Description : Prior to cryogenic separation of components of the air stream, it is passed through an alumina matrix to remove moisture, a 13X Zeolite matrix to adsorb carbon dioxide, and finally a Zeolite type X matrix. without binder calcium to adsorb nitrous oxides and, depending on the gas, ethylene.
    [0128]
    [0129] Analysis : Conditioned by adsorption for subsequent cryogenization process. TSA process. Chamber division into three divisions (Activated Alumina, Zeolite 13X and Zeolite X). The system describes the PSA process allowing equalization between chambers but without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0130]
    [0131] Patent EP1226860B1 "Method or f operating a thermal swing adsorption system and corresponding apparatus"
    [0132]
    [0133] Description : Gas treatment process to remove the percentages of CO2 and H2O steam from the effluent, or at least significantly reduce it. This method is especially useful when the treated gas is going to be used in cryogenic separation or air purification processes. The reason for the favorable removal of carbon dioxide for cryogenic processes is because this compound tends to liquefy and, where appropriate, freeze when the effluent as a whole is brought to the cryogenic state.
    [0134]
    [0135] Analysis : TSA adsorption process. Chambers divided into different sections with different adsorbents. The humidity will be captured with silica gel, alumina or activated alumina. CO2 will be adsorbed by 13 X zeolite. Adsorption is recommended to be carried out at temperatures between 10 and 50 ° C. The system describes the PSA process allowing equalization between chambers but without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0136]
    [0137] Patent US6273939 "Process for purifying a gas stream of its N2O impurities"
    [0138] Description : TSA process to purify gaseous currents, such as air, mainly from N2O and traces of CO2 or C2H4. The adsorbent material used for the removal is Zeolite (preferably with a Si / Al ratio of 1 to 1.5), carried out at temperatures between -40 and 80 ° C.
    [0139] Analysis : TSA process to increase reliability of industrial plants. Main objective: Withdrawal of N2O from outgoing currents. Use Zeolites as adsorbing material. The system describes the TSA process without the ability to allow control over the concentration of the output currents (27) or (44) of the proposed system as a device of the present invention.
    [0140]
    [0141] Patent EP0449576A1 "Purifying fluids by adsorption"
    [0142]
    [0143] Description : Prior to cryogenic separation of components of the air stream, it is passed through an alumina matrix to remove moisture, a 13X Zeolite matrix to adsorb carbon dioxide, and finally a Zeolite type X matrix. without binder calcium to adsorb nitrous oxides and, depending on the gas, ethylene.
    [0144]
    [0145] Analysis : Conditioned by adsorption for subsequent cryogenization process. TSA process. Chamber division into three divisions (Activated Alumina, Zeolite 13X and Zeolite X). The system describes the PSA process allowing equalization between chambers but without the ability to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0146]
    [0147] Patent US4770676 "Recovery o f Methane from Land Fill Gas"
    [0148]
    [0149] Description : Integrated PTA-PSA system capable of separating currents formed by the mixture of CH4 (30-70%) and CO2 (70-30%) and other traces of hydrocarbons in series. The first stage by TSA adsorption removes impurities and the second stage by PSA adsorption separates CH4 from CO2. Designed to separate CH4 and CO2 from streams where both gases are the majority compared to the rest that only constitute traces.
    [0150]
    [0151] Analysis : The system describes a first TSA adsorption process that separates impurities followed by a second PSA process that separates CH4 from CO2. Designed for different gas currents, it does not allow equalization between chambers nor does it have the capacity to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention.
    [0152]
    [0153] US20030047037A1 Patent “Process for Removal or f Carbon Dioxide for Use in Producing Direct Reduced Iron ”
    [0154]
    [0155] Description : PSA adsorption system made up of several columns in parallel with several adsorption layers made up of different solid adsorbent materials. Desorption is carried out by vacuum in countercurrent.
    [0156]
    [0157] Analysis : The system describes a PSA adsorption process that separates the CO2 from the gas stream but does not have the capacity to allow control over the concentration of the output streams (27) or (44) of the proposed system as a device for the present invention.
    [0158]
    [0159] Patent application ES 2407584A2 "Process for Removal or f Carbon Dioxide for Use in Producing Direct Reduced Iron"
    [0160]
    [0161] Description : PTSA adsorption system formed by several columns in parallel using Zeolites 13X and / or Active Carbon as adsorbent material. Desorption is carried out under vacuum, favoring extraction by heating cycles.
    [0162]
    [0163] Analysis : The system describes a PTSA adsorption process that separates CO2 from the gas stream. It does not have the capacity to allow control over the concentration of the output currents (27) or (44) of the system proposed as a device of the present invention and is based on the use of a different PSA process.
    [0164]
    [0165] DESCRIPTION OF THE INVENTION
    [0166]
    [0167] The present invention describes a device and a method of recovering gaseous substances from gaseous streams. Said procedure is based on carrying out the PSA adsorption / desorption process of the gas stream, although using an inert adsorbent porous material selective for the gaseous substance to be separated, carried out under operating conditions and using a procedure that allows efficiencies similar to rest of the existing systems at very competitive costs in comparison.
    [0168]
    [0169] The invention is applicable to a multitude of gaseous substances, although the substances that fall within the group of greenhouse gases, mainly carbon dioxide, are preferred, although the invention is also viable for recovering other greenhouse substances, such as water vapor, suspended particles, nitrogen oxides, and sulfur oxides.
    [0170]
    [0171] The process of the invention is based on a cycle of two or three sequential phases that first comprises a treatment of the gases to be separated (Module 1), second a separation of gases (Module 2) and third a purification of the separated gas (Module 3 ), the latter being optional depending on the characteristics of the gas stream enriched with the substance to be separated (as can be seen in Figure 1).
    [0172]
    [0173] Applying the same gas treatment, gas separation and gas purification system (optional) with different previously selected porous adsorbent materials, it is and can be used to separate any inlet gas stream into the system to enrich the stream of final output in the previously selected gases, being applicable to any composition since both the proposed PSA adsorption / desorption process, the equipment used and the proposed porous materials are inert and do not produce intermediate substances that are potentially dangerous or harmful to the environment. Likewise, operating pressures and temperatures are relatively low and moderate (respectively) to represent a risk to the operation.
    [0174]
    [0175] Module 1 accommodates in pressure, temperature and composition the gases entering this phase, so that from a first inlet stream (1) results in two outlet streams, a first dry stream of gases prepared for entry to the second phase of gas separation (13) and a second output stream made up of the first gases removed, mainly suspended particles, water vapor and sulfur oxides (12).
    [0176]
    [0177] Module 2 through a process of separation and concentration by physical-chemical adsorption PSA obtains from the first output stream (13) from Module 1, two output streams: a third output stream (27) with a concentration of the gaseous substances to be extracted greater than those of the first inlet stream, and a fourth outlet stream (16) with a concentration of the gaseous substances to be removed less than those of the first inlet stream (13).
    [0178]
    [0179] And finally, Module 3, through a process of separation and concentration by PSA physical-chemical adsorption similar to that of the second phase, although adapted to the composition of the gas stream to be treated, which it obtains from the third stream of output from the previous phase (27), two output streams: a fifth output stream (44) with a concentration of the gaseous substances to be extracted greater than that of the third outlet stream from the previous phase, and a sixth outlet stream (34) with a concentration of the gaseous substances to be removed less than that of the third outlet stream from of the previous phase.
    [0180]
    [0181] Depending on the specific parameters of the procedure and the regulatory requirements that must be met at all times, the procedure may have the three previous Modules, only the first two, be iterative, repeating any of the three previous Modules in several stages, so that the first output current (13) of Module 1 constitutes the input current of each Module 2; and the third output current (27) of each Module 2 is the input current to each Module 3.
    [0182]
    [0183] The second output stream (12) of Module 1 will be managed either as liquid waste or it can be neutralized with NaOH or KOH type bases, for its chemical stabilization prior to its evacuation. The fourth (16) and sixth (34) output streams, as they are gaseous, will be managed according to their content as added value atmospheric gases or they will be released directly to the outside, they become biologically inert.
    [0184]
    [0185] In the event that the substance is selected from the greenhouse exhaust gases, the inlet stream (1) to Module 1 can come from any stream comprising greenhouse gases, preferably from at least one exhaust gas stream Combustion, hereinafter referred to as exhaust stream, for example, from fossil fuel thermal power plants, biomass combustion plants, boilers that use fossil fuels or biomass to produce Primary Energy, etc.
    [0186]
    [0187] Initially, said inlet stream (1) is directed, as the first inlet stream to Module 1, to carry out the first phase of gas treatment where the temperature and pressure are adjusted to proceed with its drying, eliminating water, nitrogen oxides and sulfur, the unburned and other suspended solids, preparing the first output stream (13) for injection in Module 2, where the gas separation process will take place, with a composition that allows operation under design conditions thereof in accordance with the specifications of the adsorbent material. The second outlet stream (12) incorporates the separated water, the sulfur oxides, the unburned ones, partially the nitrogen oxides and the remains of suspended solids removed from the gas stream. input (1).
    [0188]
    [0189] Module 2 treats the first output stream (13) of Module 1 through a PSA adsorption / desorption process to separate the selected gases, enriching the third output stream (27) of Module 2. Gas separation occurs according to the selectivity of the adsorption process that presents a certain porous adsorbent solid. In the preferred case, the porous material used is active and selective against CO2 and CO.
    [0190]
    [0191] The adsorption and desorption processes are carried out in one or more adsorption / desorption reactors (14), in series, with the adsorption process acting first, followed by the PSA desorption process, repeating these processes indefinitely alternately. To achieve continuous operation of Module 2, it is necessary to double the number of adsorption / desorption reactors (14), so that while half performs the adsorption process, the other half performs the PSA desorption process working in parallel.
    [0192]
    [0193] During the adsorption process (Figure 2), the first outlet stream (13) circulates through the inner and outer surface of the porous adsorbent material disposed inside the adsorption / desorption reactors. The fourth output stream (16) is depleted in the selected gases and can be released to the outside with a composition very similar to that of the outside atmosphere, or it can try to obtain its recovery as industrial gases. The selected gases remain inside the adsorption / desorption reactors (14) adhered by means of Van der Waals forces, weak bonds and hydrogen bonds, among other forces of physical / chemical origin present. The adsorption process ends when the porous adsorbent material inside the adsorption / desorption reactors (14) becomes saturated and stops adsorbing the selected gases.
    [0194]
    [0195] During the adsorption process, the adsorption / desorption reactors (14) that carry out the adsorption process are connected to the first output current (13) of Module 1 and are isolated from the PSA desorption system. During the PSA desorption process, the adsorption / desorption reactors (14) are isolated from the first output stream (13) of Module 1 and are connected to the vacuum system that will allow the extraction of the gases adhered to the contained adsorbent porous material inside to enrich the third exhaust gas stream (27) of Module 2, enriched in the selected gases.
    [0196]
    [0197] The fourth output stream (16) of Module 2 consists of the depleted gas stream in the selected gases from the adsorption / desorption reactors (14) that are carrying out the adsorption process, which can be managed as atmospheric gases with added value, or will be emitted directly into the outside atmosphere if it is biologically inert.
    [0198]
    [0199] In Module 2, the desorbed gas stream follows three different stages. First, see Figure 3. During the first stage of the PSA desorption process, the stream (21) is re-injected into the inlet gas stream to Module 1, as long as the control system (45) of the system as a whole provides it. . Secondly, during the second stage of the PSA desorption process, the gases are accumulated in various storage lung tanks before leaving this phase, constituting the third outlet gas stream (27) of Module 2, ending when it is achieved. desorb approximately the same mass of selected gases that was initially adsorbed during the adsorption process (Figure 4 describes the evolution of the key parameters during the PSA desorption process proposed in the present invention).
    [0200]
    [0201] The third stage is repeated several times, as many as necessary to finish the second stage, interrupting it, consisting of the re-injection of the desorbed and accumulated gases in the aforementioned tanks, for injection, as current (24) in the adsorption reactors / desorption (14) that are carrying out the PSA desorption process in an explosive way, when their pressure reaches a threshold value below a predetermined vacuum (approximately 80%), in order to carry the largest number of molecules of the selected gases and improve the performance of the vacuum pumps used to carry out the PSA desorption process. At the end of each of the third stages, the second stage of the desorption process continues.
    [0202]
    [0203] In the event that the concentration of the selected gases present in the third output stream (27) of Module 2 is less than that required by system specifications, a Module 3, based on the previous PSA adsorption / desorption process will be included.
    [0204]
    [0205] The operation of Module 3 will be similar and in series to the operation of Module 2 above, using as the inlet gas stream the third outlet stream (27) enriched in the selected gases from Module 2, using the same (or different) material porous adsorbent than that used in Module 2, provided it is selective towards the gases selected for their separation and purification.
    [0206] The sixth exhaust gas stream (34) from the third phase of gas purification may be reinjected into the adsorption / desorption reactors (31) that are carrying out the adsorption process in both Module 2 and Module 3; or be emitted directly into the outside atmosphere, depending on its composition and whether or not it is biologically inert, as determined through the control system (45) of the invention.
    [0207]
    [0208] To achieve continuous operation of the system as a whole, Modules 2 and 3 will each have half of the adsorption / desorption reactors (14), (31) performing the adsorption process, while the other half will be performing the PSA desorption process. When both processes are finished, the control system (4) will alternate its operation, ensuring that half of the adsorption / desorption reactors (14), (31) of each Module are always carrying out the adsorption process, continuously and without affecting to the flow of the first inlet stream (1) to Module 1.
    [0209]
    [0210] Meanwhile, the other half of the adsorption / desorption reactors in each phase will be performing the described PSA desorption process. At all times, the control system (45) will try to adjust the adsorption (tadsorption) and desorption (torption) times as much as possible, so that it will always be observed that torsorption <tadsorption in each of Modules 2 and 3.
    [0211]
    [0212] The points or threshold values of the concentration of the selected gases in the desorbed streams (27) and (44), the concentration of the selected gases in the system inlet stream (1), the amount of water and the rest of the gases greenhouse effect present in the first stream entering the system (1), its pressure and temperature conditions, its mass and / or volumetric concentrations; and the adsorption and desorption times of the adsorption / desorption reactors (14), (31) of Modules 2 and 3 are, apart from multiple signals internal to the system as a whole, the main inputs that govern the control system (45) of the invention.
    [0213]
    [0214] It is important to note that the proposed device and procedure can be used in principle at any pressure and temperature, although, depending on the characteristics, known in the state of the art, of PSA adsorption / desorption systems using porous materials as material adsorbent, operating pressure range, pressures below 10 bar (g), and operating temperatures not exceeding 50 ° C have been selected, in order to protect the porous material used, to obtain an acceptable performance of the system in its set and reduce operation and maintenance costs.
    [0215]
    [0216] In the case of the adsorption steps to be carried out by the adsorption / desorption reactors (14), (31), of Modules 2 and 3, the system will try to optimize the adsorption process by maximizing the amount of gases selected in such a way that the adsorbed amount is maximized, exceeding 95% of the amount present in the first input current to the system and approach 100% as much as possible.
    [0217]
    [0218] The basic parameters of the procedure are as follows:
    [0219]
    [0220] - the nature and concentration of the substance or substances to be separated present in the first input stream (1) to Module 1.
    [0221] - the minimum percentage by weight that is required to be removed from each substance, with respect to the percentage of said substance contained in the first input stream (1) to Module 1. - the minimum concentration of each separate substance required for the third stream of output (27) of Module 2 or the fifth output current (44) of Module 3 (optional), as required.
    [0222] - The system as a whole will allow its installation and operation regardless of the source of greenhouse gases, pressure, temperature and concentration of the selected gaseous substance, adapting its operation automatically.
    [0223] - The system as a whole is modular, interchangeable, compact and scalable.
    [0224]
    [0225] Based on these basic parameters, the operating pressure and temperature parameters of each of the three modules are selected, while with the mass concentration of the gases selected to be separated during the entire process, the different stages of the PSA desorption process in Modules 2 and 3 (optional), in order to achieve the mass concentration of the gases to be separated selected for their desired concentration and / or separation, by means of reinjection processes at different points of the systems that make up the three Modules, to achieve maximum adsorption of the selected gases to be separated from the main stream of inlet gases (1) to Module 1, increasing the adsorption and desorption performance of the system as a whole, by means of a complex control system (45) .
    [0226]
    [0227] By means of the procedure described in the present invention, a recovery of gaseous substances from gaseous streams is carried out with significant energy savings ( around 45%), savings in equipment costs (around 75%) and savings in operation and maintenance costs (around 75%) compared to the procedures for separating gases and capturing greenhouse gases currently in operation, as well as avoiding the generation of products that are harmful to the environment, with the savings in carbon footprint and environmental impact that this implies.
    [0228]
    [0229] Additionally, the procedure of the invention favors the synergy between companies, since the by-products of the process can be acquired as raw material by other companies.
    [0230]
    [0231] DESCRIPTION OF THE DRAWINGS
    [0232]
    [0233] To complement the description that is being made and in order to help a better understanding of the characteristics of the invention, according to a preferred example of practical embodiment thereof, a set of drawings is included as an integral part of said description. where, by way of illustration and not limitation, the following has been represented:
    [0234]
    [0235] Figure 1.- General view of the device of the invention and its operation.
    [0236] Figure 2.- Evolution of the key parameters of the adsorption process in the device of the invention.
    [0237] Figure 3.- Stages of the PSA desorption process of the invention and its operation.
    [0238] Figure 4. Evolution of the key parameters of the desorption process in the device of the invention.
    [0239] Figure 5.- View of the installation of the invention and its operation.
    [0240]
    [0241] PREFERRED EMBODIMENT OF THE INVENTION
    [0242]
    [0243] Next, with reference to the attached Figure 5, a preferred embodiment of the device of the invention is presented, applied to the recovery of a gaseous substance component of the inlet gas stream to the invention.
    [0244]
    [0245] A stream of inlet gases (1), mainly from fossil fuel combustion systems to obtain Primary Energy, enters Module 1 for its analysis, adaptation in pressure, temperature and content in other effect gases greenhouse, impurities and water vapor. This stream (1) is mobilized from the installation where it is generated by an impulsion system (2) and is conducted through a pipe system for its entry and treatment in Module 1, constituting the stream of gases (3) whose characteristics are similar to those of current (1), but with a constant flow according to the characteristics of the control system (45) of the invention.
    [0246]
    [0247] The stream (3) has concentrations of CO2 (1% - 25%), water vapor (0% - 25%), O2 (0% - 35%) and the rest, N2, Ar, other greenhouse gases, unburned, ashes, etc., according to the characteristics of the previous combustion installation. The temperature range is between 60 ° C and 800 ° C and at pressure slightly above atmospheric. The control system (45), depending on the characteristics of the current (1), will manage the equipment of Module 1 and its operation to optimize the operation of the system as a whole.
    [0248]
    [0249] The gas stream (3) is treated in a first group of gas exchangers (4) to reach a temperature of around 40 ° C or lower. The first group of exchangers uses water, air or any fluid (i) to cool the stream (3), obtaining an outlet coolant stream (iii) according to the legal limits for its treatment or evacuation abroad.
    [0250]
    [0251] Due to the characteristics of the cooling process of the stream (3), the excess water present condenses, along with part of the greenhouse gases, unburned, ash and other unwanted components, constituting the stream (6) of water to be treated later. The output current of this group of exchangers (5), at a temperature of around 40 ° C or less, is semi-dry with saturated water content according to its temperature.
    [0252]
    [0253] To this gas stream is joined the gas stream (21) from Module 2, which will be explained later, constituting the stream (7), which is compressed to pressures below 10 bar (g) in the compression (8), at the outlet of which the gas stream (9) prepared for its entry into the drying system (10) is obtained.
    [0254]
    [0255] The drying system (10) removes the water present in the stream (around 99.9%) obtaining the first outlet stream (13) from Module 1 for delivery to Module 2. Stream (13) is suitable for temperature (20 ° C - 45 ° C), pressure (1 - 9 bar (m)) and humidity (Approx. 0%) to optimize the adsorption process to the maximum. The drying system is cooled by a refrigerant fluid similar to that used in the heat exchange group (4), using inlet (ii) and outlet (iv) currents in accordance with the legal limits for its treatment or evacuation to the Exterior.
    [0256]
    [0257] The drying system (10) produces a second outlet stream (11) where the condensed water from stream (9), remaining sulfur oxides, unburned, ash and other greenhouse gases are removed. The streams (6) and (11) come together and constitute the liquid stream (12) which is the second output stream of Module 1, which is treated prior to its evacuation abroad or for its subsequent recovery.
    [0258]
    [0259] The operation of Module 1 is adjusted by means of the control system (45), adapting its operation at all times to the needs of the adsorbent material of Modules 2 and 3; and to the characteristics of the current (1).
    [0260]
    [0261] The output current (13) from Module 1 is injected into Module 2 in the adsorption / desorption reactors (14) that are carrying out the adsorption process, according to the instructions of the control system (45). After passing through these adsorption / desorption reactors (14) the output current of each one (15) is directed to a single output conduit of Module 2 for its forwarding to Module 1 where, as current (16) it is released to the outside (if it is biologically not active) or to the evacuation installation that has the combustion system from which the current is initially taken (1).
    [0262]
    [0263] In the rest of the adsorption / desorption reactors that are carrying out the PSA desorption process, the exhaust current of the gases located inside the adsorption / desorption reactors (14) constitutes the current (17), which has an enrichment in the gases selected for their variable separation over time depending on the vacuum extraction process, going from a CO2 concentration of 0.4% to approximately 65% - 85% depending on the characteristics of the current ( 1).
    [0264]
    [0265] By means of the vacuum pumps (18), the current (17) is extracted and driven by the compressor (20) to favor its injection as current (21) to Module 1 for mixing with the current (5) during the first phase of desorption process described above, ending its function when the control system (45) so determines. At that time, stream (17) becomes stream (22) that is stored in the first tank Lung (23) of Module 2. Once the maximum filling pressure is reached, the rest passes as current (25) to the second tank Lung (26) of Module 2 from which the current (27) is obtained for its extraction abroad or for injection as input current to Module 3.
    [0266]
    [0267] The stream (24) starts from the first lung tank (23) of Module 2 and is used as a drag stream in the third phase of the PSA desorption process described above and is injected directly into the adsorption / desorption reactors (14) that are find themselves doing the desorption process.
    [0268]
    [0269] The operation of Module 2 is adjusted by means of the control system (45) adapting at all times the operation of the active systems located in Module 1 to the needs of the average and maximum concentration of CO2 in the output current of Module 2 and for the purposes for the desorption process optimization of the adsorption / desorption reactors (14) that carry out the desorption process in Module 2.
    [0270]
    [0271] The output current (27, 28) from Module 2 before being injected into Module 3 in the adsorption / desorption reactors (31) that are carrying out the adsorption process, according to the instructions of the control system (45) , is mixed with the current (36), constituting the current (29), to which the current (33) is mixed, to constitute the current (30), which is the one that is finally injected as input current to the adsorption / desorption reactors (31) that are carrying out the adsorption process in Module 3. The currents (33) and (36) are explained below.
    [0272]
    [0273] After passing through these adsorption / desorption reactors (31) the output stream from each adsorption / desorption reactor (32) is directed for injection to the rest of the adsorption / desorption reactors as current (33) for mixing with the current (29) or is carried through an outlet conduit of Module 3 to be forwarded to Module 1 where, as current (34) it is released to the outside (if it is biologically not active) or to the evacuation installation that has the combustion system from which the current (1) is initially taken, according to what the control system (45) of the invention indicates.
    [0274]
    [0275] In the rest of the adsorption / desorption reactors (31) that are carrying out the PSA desorption process, the exhaust current of the gases located inside the adsorption / desorption reactors constitutes the current (39), which has a enrichment in the selected gases for their variable separation over time depending on the vacuum extraction process, going from a CO2 concentration of 65% - 85% to approximately 95% - 100% depending on the characteristics of the current ( 1).
    [0276]
    [0277] By means of the vacuum pumps (38), the current (39) is extracted and driven by the compressor (37) to favor its injection as current (36) to the current (28) to constitute the current (29) during the first phase of the desorption process described above, ending its function when the control system (45) so determines. At that moment, the stream (35) becomes the stream (39) that is stored in the first lung tank (40) of Module 3. Once it reaches the maximum filling pressure, the rest stops as stream (42) at second lung tank (43) of Module 3 from which the current (44) is obtained for its extraction abroad.
    [0278]
    [0279] The stream (41) starts from the first lung tank (40) of Module 3 and is used as a drag stream in the third phase of the PSA desorption process described above and is injected directly into the adsorption / desorption reactors (31) that are find themselves doing the desorption process.
    [0280]
    [0281] The operation of Module 3 is adjusted by means of the control system (45) adapting at all times the operation of the active systems located in Module 1 to the needs of the average and maximum concentration of CO2 in the output current of Module 3 and for the purposes for the desorption process optimization of the adsorption / desorption reactors that carry out the desorption process in Module 3.
    权利要求:
    Claims (25)
    [1]
    1. - Installation to recover gaseous substances from gaseous streams, figure 1, characterized in that it comprises:
    - a first module for treating atmospheric gases, equipped with a first inlet duct to transport the first compression stream (8) and the drying system (10) to the first set of heat exchangers (4), a first flow of gaseous inlet gases (1) comprising at least one substance to be recovered. Said first Atmospheric Gas Treatment Module is equipped with the rest of active systems that Modules 2 and 3 require for its correct operation (vacuum pumps (18), (38), impulsion systems and compressors (20), (37 ), appropriate pipes and valves, lung tanks (23), (26), (40), (43), electrical system and control system), according to what is required for the correct operation of the control system (45). Likewise, it is equipped with a first outlet duct to mobilize the first outlet stream (13) towards Module 2 after its adaptation in composition, pressure and temperature; a second outlet duct to mobilize the liquid stream (12), a second inlet duct to manage the gases adsorbed in the adsorption / desorption reactors (14) of Module 2, a third outlet duct to send the enriched gas stream in at least one substance to be separated (27) to Module 3, a third inlet duct to manage the gases adsorbed in the adsorption / desorption reactors (31) of Module 3 and a fourth outlet duct to send the enriched gas stream in at least one substance to be separated (44) to the outside.
    [2]
    2. - Installation to recover gaseous substances from gaseous streams according to claim 1, characterized in that it additionally comprises: - a set of sensors that allow the monitoring of the pressure, temperature and concentration conditions of the substance to be concentrated in the output stream (13).
    - a control system (45) that allows controlling the optimal concentration characteristics of the selected gaseous substance, of the water content of the current (13), its pressure and temperature to optimize the operation of Modules 2 and 3.
    - a control system (45) that allows the system to operate at its optimum point of pressure, concentration, humidity and temperature throughout Modules 2 and 3, acting on the different atmospheric gas separation equipment that make up the Module 1.
    [3]
    3. - Installation to recover gaseous substances from gaseous streams according to claim 1, characterized in that it comprises:
    - a second module for the separation of atmospheric gases, equipped with a first inlet conduit to transport sufficient piping and valves to the adsorption / desorption reactors (14), for the correct operation of the described PSA adsorption / desorption process, a first gaseous inlet gas stream (9) comprising at least one substance to be recovered and which comes from the first outlet stream of Module 1. Likewise, it is provided with a first outlet duct to mobilize the desorbed gas stream after the desorption process PSA (15) for shipment to Module 1 where the desorption process described will be controlled, according to what is required for the correct operation of the control system (45).
    [4]
    4. - Installation to recover gaseous substances from gaseous streams according to claim 1, characterized in that it additionally comprises: - a set of sensors that allow the monitoring of the pressure, temperature and concentration conditions of the substance to be concentrated in the output stream (27).
    - a control system (45) that allows controlling the average and maximum concentration in the substance to be separated obtained in the output current of Module 2 (27) depending on what is required by technical specifications, whose operation is automatic and adaptable without modification , to the characteristics of the input current to the system (1) and the output current (27).
    - a control system (45) that allows the system to operate at its optimum point of pressure, concentration, humidity and temperature throughout Module 2, acting on the different atmospheric gas separation equipment that make up Module 1.
    [5]
    5.- Installation to recover gaseous substances from gas streams according to claims 1 and 3, characterized in that it comprises:
    - a third purification module for atmospheric gases, equipped with a first inlet duct to transport enough pipes and valves to the adsorption / desorption reactors (31) for the correct operation of the described PSA adsorption / desorption process, a first gaseous inlet gas stream (44) comprising at least one substance to be recovered and which comes from the fifth outlet stream of Module 1. Likewise, it is provided with a first outlet duct to mobilize the desorbed gas stream after the desorption process PSA (32) for shipment to Module 1 where the desorption process described will be controlled, according to what is required for the correct operation of the control system (45).
    [6]
    6. Installation for recovering gaseous substances from gas streams according to claims 1 and 3, characterized in that it additionally comprises:
    - a set of sensors that allow the monitoring of the conditions of pressure, temperature and concentration of the substance to be concentrated in the outlet stream (44).
    - a control system (45) that allows controlling the average and maximum concentration in the substance to be separated obtained in the output current of Module 3 (44) according to what is required by technical specifications, whose operation is automatic and adaptable without modification , to the characteristics of the input current to the system (1) and the output current (44).
    - a control system (45) that allows the system to operate at its optimum point of pressure, concentration, humidity and temperature throughout Module 3, acting on the different atmospheric gas treatment equipment that make up Module 1.
    [7]
    7.- Installation to recover gaseous substances from gas streams according to claims 1 and 3, characterized in that it comprises:
    - the interconnection of one or more Modules 1 with one or more Modules 2, characterized in that the output current (13) of each Module type 1 is the current input of each Module type 2.
    [8]
    8. - Installation to recover gaseous substances from gaseous streams according to claims 1 and 3, characterized in that it additionally comprises:
    - a set of sensors that allow the monitoring of the pressure, temperature and concentration conditions of the substance to be concentrated in the outlet streams (13) and (27).
    - a control system (45) that allows controlling the average and maximum concentration in the substance to be separated obtained in the output currents of Module 1 (13) and Module 2 (27) depending on what is required by technical specifications, whose Operation is automatic and adaptable without modification, to the characteristics of the input current to the system (1) and to the output current (13) and (27).
    - a control system (45) that allows the system to operate at its optimum point of pressure, concentration, humidity and temperature throughout Modules 1 and 2 and 3, acting on the different atmospheric gas treatment equipment that make up Module 1.
    [9]
    9. - Installation to recover gaseous substances from gaseous streams according to claims 1,3, 5 and 7, characterized in that it comprises:
    - the interconnection of one or more Modules 1 with one or more Modules 2 and with one or more Modules 3, characterized in that the output current (13) of each Module 1 is the input current of each Module 2 and the output current (27) of each Module 2 is the input current of each Module 3.
    [10]
    10. - Installation to recover gaseous substances from gaseous streams according to claims 1, 3, 5 and 7, characterized in that it further comprises:
    - a set of sensors that allow the monitoring of the conditions of pressure, temperature and concentration of the substance to be concentrated in the outlet streams (13), (27) and (44).
    - a control system (45) that allows controlling the average and maximum concentration in the substance to be separated obtained in the output streams of Module 1 (13), Module 2 (27) and Module 3 (44) depending on what is required by technical specifications, whose operation is automatic and adaptable without modification, to the characteristics of the input current to the system (1) and to the output current (13), (27) and (44).
    - a control system (45) that allows the system to operate at its optimum point of pressure, concentration, humidity and temperature throughout Modules 1, 2 and 3, acting on the different atmospheric gas treatment equipment that make up Module 1.
    [11]
    11.- Procedure for recovering gaseous substances from gaseous streams, using the installation described in any one of claims 1 to 10, separating a substance of interest characterized in that it comprises the following steps:
    - introduction of the first inlet stream (1) in Module 1 for treating atmospheric gases, resulting in a first outlet stream (13) with a concentration of the substance to be recovered greater than that of the first inlet stream (1 );
    - measurement of the characteristics of flow, concentration, pressure and temperature of the substances in the stream (1) to be recovered in the first outlet stream of Module 2 (27).
    - comparison of the previous measurements with some pre-established criteria through the control system (45).
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (1) to Module 1 and of the output of the first output stream (13).
    - control and adjustment of the adsorption and desorption times to try to meet the pre-established criteria for the operation of the system as a whole, alternating adsorption / desorption reactors (14) of Module 2 to achieve continuous operation that does not affect the installation gas generator to be separated. - action on the teams that make up Module 1 to carry out the PSA adsorption and desorption processes in the adsorption / desorption reactors (14) of Module 2 described at their optimum point of operation and performance.
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (13) to Module 2 and the output of the first output stream (27).
    [12]
    12. Procedure for recovering gaseous substances from gaseous streams, according to claim 11, characterized in that it further comprises purifying a substance of interest characterized in that it comprises the following steps:
    - introduction of the first inlet stream (1) in Module 1 for treating atmospheric gases, resulting in a first outlet stream (13) with a concentration of the substance to be recovered greater than that of the first inlet stream (1 );
    - measurement of the flow, concentration, pressure and temperature characteristics of the substances in the stream (1) to be recovered in the first outlet stream of Module 3 (44).
    - comparison of the previous measurements with some pre-established criteria through the control system (45).
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (1) to Module 1 and of the output of the first output stream (13).
    - control and adjustment of the adsorption and desorption times to try to meet the pre-established criteria for the operation of the system as a whole, alternating adsorption / desorption reactors (14) of Module 2 to achieve continuous operation that does not affect the installation gas generator to be separated. - action on the teams that make up Module 1 to carry out the PSA adsorption and desorption processes in the adsorption / desorption reactors (14) of Module 2 described at their optimum point of operation and performance.
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (13) to Module 2 and the output of the first output stream (27).
    - control and adjustment of the adsorption and desorption times to try to comply with the pre-established criteria of operation of the system as a whole, alternating adsorption / desorption reactors (31) of Module 3 to achieve continuous operation that does not affect the installation gas generator to be separated. - action on the equipment that make up Module 1 to carry out the PSA adsorption and desorption processes in the adsorption / desorption reactors (31) of Module 3 described at their optimum point of operation and performance.
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (27) to Module 3 and of the output of the first output stream (44).
    [13]
    13.- Installation to recover gaseous substances from gaseous streams according to claim 11, characterized in that the substance to be recovered is a greenhouse gas.
    [14]
    14. - Installation to recover gaseous substances from gaseous streams according to claim 13, characterized in that the greenhouse gas is selected from carbon dioxide, nitrogen, nitrogenous gases and phosphorous and / or sulfur gases.
    [15]
    15. - Installation to recover gaseous substances from gas streams according to claim 14, characterized in that the substance to be recovered is nitrogen oxides.
    [16]
    16. - Installation for recovering gaseous substances from gaseous streams according to any one of claims 13 to 15, characterized in that the first inlet stream (1) comes from a combustion exhaust stream.
    [17]
    17. - Installation to recover gaseous substances from gaseous streams according to claim 16, characterized in that the substance to be recovered is a greenhouse gas.
    [18]
    18. - Installation to recover gaseous substances from gaseous streams according to claim 17, characterized in that the greenhouse gas is selected from carbon dioxide, nitrogen, nitrogenous gases and phosphorous and / or sulfur gases.
    [19]
    19. - Installation to recover gaseous substances from gas streams according to claim 18, characterized in that the substance to be recovered is sulfur oxides, water vapor and / or oxygen.
    [20]
    20. - Installation for recovering gaseous substances from gaseous streams according to any one of claims 17 to 19, characterized in that the first inlet stream (1) comes from a combustion exhaust stream.
    [21]
    21. - Procedure for recovering gaseous substances from gaseous streams, using the installation described in any one of claims 1 to 10, performing an extraction of a substance of interest characterized in that it comprises the following steps:
    - introduction of the first inlet stream (1) in Module 1 for treating atmospheric gases, resulting in a first outlet stream (13) with a concentration of the substance to be recovered greater than that of the first inlet stream (1 );
    - measurement of the characteristics of flow, concentration, pressure and temperature of the substances in the stream (1) to be recovered in the first outlet stream of Module 2 (27).
    - comparison of the previous measurements with some pre-established criteria through the control system (45).
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (1) to Module 1 and of the output of the first output stream (13).
    - control and adjustment of the adsorption and desorption times to try to meet the pre-established criteria for the operation of the system as a whole, alternating adsorption / desorption reactors (14) of Module 2 to achieve continuous operation that does not affect the installation gas generator to be separated. - action on the teams that make up Module 1 to carry out the PSA adsorption and desorption processes in the adsorption / desorption reactors (14) of Module 2 described at their optimum point of operation and performance.
    - adaptation of the operating conditions of concentration, pressure and temperature of the first input stream (13) to Module 2 and the output of the first output stream (27).
    [22]
    22.- Installation to recover gaseous substances from gaseous streams according to claim 20, characterized in that the substance to be recovered is a greenhouse gas.
    [23]
    23.- Installation to recover gaseous substances from gaseous streams according to claim 22, characterized in that the greenhouse gas is selected from carbon dioxide, nitrogen, nitrogenous gases and phosphorous and / or sulfur gases.
    [24]
    24.- Installation to recover gaseous substances from gaseous streams according to claim 23, characterized in that the substance to be recovered is carbon dioxide.
    [25]
    25. Installation for recovering gaseous substances from gaseous streams according to any one of claims 22 to 24, characterized in that the first input stream (1) to Module 1 comes from a combustion exhaust stream.
    the third input stream (27).
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    同族专利:
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    US20220001324A1|2022-01-06|
    ES2751176B2|2021-07-21|
    WO2020065107A1|2020-04-02|
    EP3858463A1|2021-08-04|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US5906675A|1997-09-30|1999-05-25|The Boc Group, Inc.|Air purification process|
    US20020110504A1|2001-02-09|2002-08-15|Gittleman Craig S.|Carbon monoxide adsorption for carbon monoxide clean-up in a fuel cell system|
    US20040179998A1|2003-03-14|2004-09-16|Gittleman Craig S.|Fuel processor module for hydrogen production for a fuel cell engine using pressure swing adsorption|
    US8012446B1|2010-07-08|2011-09-06|Air Products And Chemicals, Inc.|Recycle TSA regen gas to boiler for oxyfuel operations|
    ES2407584A2|2011-11-21|2013-06-13|Iberdrola Ingeniería Y Construcción, S.A.U.|Installation and procedure to recover gaseous substances from gaseous currents |
    US61747A|1867-02-05|manning |
    US1683567A|1924-06-25|1928-09-04|Moody Lewis Ferry|Hydraulic turbine|
    US3885927A|1974-02-05|1975-05-27|Union Carbide Corp|Process for removing carbon dioxide from gas streams|
    US4472177A|1982-09-09|1984-09-18|Air Products And Chemicals, Inc.|Control system and method for air fractionation by vacuum swing adsorption|
    US4696680A|1985-10-03|1987-09-29|The United States Of America As Represented By The United States Department Of Energy|Method and apparatus for the selective separation of gaseous coal gasification products by pressure swing adsorption|
    US4770676A|1986-05-16|1988-09-13|Air Products And Chemicals, Inc.|Recovery of methane from land fill gas|
    ZA911499B|1990-03-30|1991-12-24|Boc Group Inc|Purifying fluids by adsorption|
    JP3416391B2|1995-05-25|2003-06-16|日本酸素株式会社|Pretreatment method and apparatus for air liquefaction separation apparatus|
    EP1500424B1|1997-01-31|2007-12-05|RIC Investments, Inc.|Pressure swing absorption system with multi-chamber canister|
    US5938819A|1997-06-25|1999-08-17|Gas Separation Technology Llc|Bulk separation of carbon dioxide from methane using natural clinoptilolite|
    US5931022A|1997-09-30|1999-08-03|The Boc Group, Inc.|Air purification process with thermal regeneration|
    US5968234A|1998-04-14|1999-10-19|Air Products And Chemicals, Inc.|Temperature swing adsorption with regeneration by elevated pressure ASU nitrogen-enriched gas|
    US6106593A|1998-10-08|2000-08-22|Air Products And Chemicals, Inc.|Purification of air|
    FR2784599B1|1998-10-20|2000-12-08|Air Liquide|PROCESS FOR PURIFYING A GAS STREAM IN ITS N2O IMPURITIES|
    FR2799390B1|1999-10-08|2002-06-07|Air Liquide|METHOD FOR TREATING A GAS BY MODULATED TEMPERATURE ADSORPTION|
    US6362122B1|1999-11-08|2002-03-26|Uop Llc|Regeneration of spent zeolite compositions|
    AT340629T|2001-01-25|2006-10-15|Air Prod & Chem|METHOD FOR OPERATING A TEMPERATURE CHANGE ADSORPTION SYSTEM AND CORRESPONDING DEVICE|
    US6562103B2|2001-07-27|2003-05-13|Uop Llc|Process for removal of carbon dioxide for use in producing direct reduced iron|
    EP1463587B1|2001-12-21|2011-05-11|Amalgamated Research, Inc.|Toroidal vessel for uniform, plug-flow fluid distribution applications|
    US7128776B2|2004-03-10|2006-10-31|Air Products And Chemicals, Inc.|Periodic high temperature regeneration of thermal swing adsorption systems|
    AU2008336265B2|2007-12-12|2013-06-27|Process Group Technologies Pty Ltd|A plant and process for recovering carbon dioxide|
    US8052777B2|2009-06-29|2011-11-08|Uop Llc|Vessel, system, and process for minimizing unequal flow distribution|
    US8268043B2|2009-12-23|2012-09-18|Praxair Technology, Inc.|Modular compact adsorption bed|
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