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    • 专利摘要:
    In the present invention called "compression plant for air separation installations with conversion of residual energy into electrical power and cooling by absorption cycle" the arrangement of an APC cycle integrated in an ASU process is presented. The residual heat of several thermodynamic processes of the main ASU process in the absorption cycle is used in order to obtain electrical energy and cooling capacity. Within the APC cycle, a branch for generating power through a turbine/generator and another for generating cold or cooling energy is established. It is possible to vary the amount of working fluid that is sent to each branch so that the operation of the APC cycle prioritizes power generation or cooling. The electric power and the generated industrial cold are used in order to reduce the specific consumption of the ASU plant. (Machine-translation by Google Translate, not legally binding)
    公开号:ES2736963A1
    申请号:ES201800160
    申请日:2018-07-03
    公开日:2020-01-09
    发明作者:Mantinan Daniel Blanco；Gomez Javier Romero；Gomez Manuel Romero；Insua Alvaro Baalina
    申请人:Universidade da Coruna；
    IPC主号:
    专利说明:

    [0001]
    [0002] COMPRESSION PLANT FOR AIR SEPARATION FACILITIES
    [0003]
    [0004] TECHNICAL FIELD OF THE INVENTION
    [0005]
    [0006] The present invention belongs to the technical field of air separation processes of the ASU (Air Separation Unit) type. A type ASU involves, among others, compression and cooling processes resulting in unused waste energy.
    [0007]
    [0008] This invention is based on the use of residual energy (Waste heat or Low Grade Thermal Energy) through its conversion into electrical energy and cooling generation capacity by means of a thermodynamic absorption cycle, APC (Absorption Power Cycle), in which they are used Multi-component working fluids such as Li-Br, Li-CI or Ca-Ci solutions, among others, characterized by their relatively low, multiple and variable boiling temperature.
    [0009]
    [0010] OBJECTIVE OF THE INVENTION
    [0011]
    [0012] The objective of the present invention called "COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION BY ABSORPTION CYCLE" is the reduction of specific consumption in cryogenic air separation units. The specific consumption of an ASU is defined as the energy consumed to generate each unit of final product (high purity industrial gases).
    [0013]
    [0014] The reduction in specific consumption is due to the use of residual thermal energy in ASU-type air separation processes and the integration of a power cycle by absorption operating with a relatively low boiling temperature fluid such as a lithium-bromide solution. (LiBr). The APC allows the conversion of residual thermal energy to electrical energy via mechanical energy through its branch of power and the simultaneous conversion of residual thermal energy into refrigeration production through its cooling branch, so it is here described as dual. In this way, the power branch takes advantage of the steam quality to generate electrical power through a turbine-alternator assembly while the cooling branch decreases the temperature of the cooling water (hereinafter Chilled Cooling Water or CCW), which is used at various points in the ASU to thermodynamically improve various processes and reduce, in this way, specific consumption.
    [0015]
    [0016] BACKGROUND OF THE INVENTION
    [0017]
    [0018] The ASUs (plural of ASU), are understood here as those whose processes are developed at cryogenic temperatures and that obtain as a final product various constituent gases of the atmosphere in a segregated manner. The processes that develop at temperatures below the range of -100 to -150 ° C are considered cryogenic.
    [0019]
    [0020] Cryogenic air distillation plants have many common and typical elements even within different models or types. Examples of historical references of these processes and which may be clarifying in this invention are, among others, US2048076A (Process for separating low boiling gas mixtures), US3127260A (separation of air into nitrogen, oxygen and argon), US3216206A (Low temperature distillation of normally gaseous substances), US3261168A (Separation of oxygen from the air), US3327488 (Refrigeration system for gas liquefaction), US4817393A (Companded total condensed lox-boil air distillation) where the term “companded” is used as a reference to the process performed by a “Compander”, EP0321163A2 (Separating argon / oxygen mixtures) where the “Waste Gas”, EP0341854A1 (Air separation process using packed columns for oxygen and argon recovery), US3358460A (Nitrogen liquefaction with plural work expansion of feed as refrigerant) is cited where a nitrogen liquefaction system is described and in which the term "make-up" is used for the gas coming from the homon compressor imo, so that it precedes the main compressor of the liquefaction or recycle system, EP0717249A2 (Air Separation), US4746343A (Method and apparatus for gas separation), US4883518A (Process for air fractionation by low-temperature rectification), US6116027A (Supplemental air supply for an air separation system) where the importance of initial compression in ASUs is discussed and a supplementary method of air supply is contributed.
    [0021] In ASU plants, air and electrical energy are used as main, but not necessarily exclusive, raw materials. In addition, in all of them there are thermodynamic processes of high specific energy consumption such as the initial compression of the air to the appropriate pressure for the distillation process.
    [0022]
    [0023] The main energy sink of a typical ASU is the main air compressor, Main Air Compressor or MAC, located in the initial section called "front-end" according to the art that characterizes these plants. Air distillation ASUs currently installed, in general, do not recover waste heat resulting from thermodynamic processes of high energy consumption, such as the main and initial air compression in the MAC or auxiliary line compressors (gas compressors high purity industrial products as a final product, typically - but not limiting oxygen and nitrogen gas). GOX is called gaseous oxygen and GAN is gaseous nitrogen.
    [0024]
    [0025] In addition, some cryogenic air separation plants are equipped with mechanical-electrical refrigeration machinery in order to cool cooling water by a compression-lamination cycle of classical steam. The difference between the usual cooling water (Cooling Water or CW) and the cooled cooling water (CCW) is established here. CW, usually fresh or salt water, is the fluid used in industrial environments that is used to refrigerate industrial processes and, in general, is cooled to temperatures close to atmospheric by means of natural or forced draft cooling towers. The cooled cooling water (CCW) obtained in the APC is sent to the cooler by direct contact after the last stage of MAC compression known in the technical art that characterizes these installations as Direct Contact After-Cooler (DCAC) and which serves as of MAC last stage cooler. In the direct contact cooler, the CW and CCW currents come into direct contact with the air, countercurrent, in order to cool it and perform some washing of unwanted particles and components.
    [0026]
    [0027] In other ASUs, a stream of gas composed mostly of nitrogen is used, from the distillation section, but does not meet the specifications to be sent online as a high purity final product (known in the art referred to as “Waste Gas ”) to obtain CCW in a tower adequate cooling (known in the art in which this type of facility is treated as “Waste Chilling Tower.” The CCW obtained in this way is also sent to DCAC. Cooling that occurs in the “Waste Chilling Tower” can also be replaced , totally or partially, by the cooling capacity of this invention.
    [0028]
    [0029] In the current state of technology, there is still no industrial plant design planned for the joint operation of the compression processes of an ASU with the industrial power and cold generation system using APC. Many of these cryogenic processes are characterized by having as an energy sink the cooling water or other energy evacuation fluid whose characteristic is to have a low relative temperature. Low quality residual energy is considered characterized by being at temperatures between 60 and 140 ° C as an indicative range, but not limiting. In addition, in this invention, various thermodynamically beneficial uses, in terms of energy consumption, of the CCW generated within the ASU process are specified.
    [0030]
    [0031] As a result of all the above, there are no known plants such as the one detailed in the present invention, where processes of compression and cooling of air and its components are involved, with conversion of residual thermal energy into electrical energy and cooling by means of a dual system of power-absorption cooling in combination in an environment of cryogenic air distillation.
    [0032]
    [0033] BRIEF DESCRIPTION OF THE INVENTION
    [0034]
    [0035] In this invention, the arrangement of a thermal silver that integrates an APC absorption cycle into an ASU main process for the use of residual energy and industrial cold generation is presented.
    [0036]
    [0037] As the largest energy sink in an ASU is the MAC, an important source of residual energy is its inter-stage cooling exchangers. In this invention, said energy is recovered by an intermediate cooling loop that, after heating, serves as a hot fluid in the APC evaporator. There are several sources of residual energy of relative importance, in addition to MAC and in ASU-type processes, which are also taken into account. The possible uses of the CCW generated in the APC are also contemplated. The invention is characterized by understand,
    [0038]
    [0039] a) An absorption power cycle or Absorption Power Cycle (APC), formed, not limited to, by.
    [0040]
    [0041] - A section of electric power generation by means of a turbine / alternator assembly.
    [0042] - An industrial cold generation section formed by a condenser exchanger and an evaporator exchanger.
    [0043] - A common section with an exchanger-absorber, pump, exchanger-recuperator, exchanger-evaporator, phase separation tank.
    [0044]
    [0045] b) An air compressor that, as part of this invention together with the APC system, performs the MAC function integrated in an ASU installation. It is characterized by understanding, among others and depending on the needs of the ASU plant, by the following components:
    [0046]
    [0047] - A driving system of the electric motor type or an alternative internal combustion engine or a steam turbine or a gas turbine. In the case of the steam turbine, the corresponding steam condenser is also included.
    [0048] - A number "n" of compression stages, "n" being the necessary and non-limiting stages to maintain adequate flow, temperatures and compression ratio in the art that characterizes thermodynamic compression processes in the current state of the art.
    [0049] - An “n-1” number of inter-stage heat exchangers-refrigerators.
    [0050] - A direct air-water contact tower that performs the chiller function after the last compression stage with CW or CCW injection or both.
    [0051]
    [0052] c) A loop of cooling fluid that acquires thermal energy in all the residual energy sources specified in this invention and delivers it in the exchanger-evaporator of the common section of the APC cycle.
    [0053]
    [0054] It is possible to vary the amount of working fluid that is sent to each branch so that the operation of the APC cycle prioritize electricity generation, industrial cold generation or a combination of both with the desired percentage of each. The possibility of generating industrial cold in the APC cycle matches the needs of specific refrigeration in the DCAC used in many ASU plants. This capacity is not limited to the use in this element and can be used in the thermodynamic improvement of processes in other areas of a typical ASU.
    [0055]
    [0056] This invention is proposed using a LiBr solution as a working fluid for the APC (but not limited to). It is possible to vary the concentration of the fluid to adapt it to the most appropriate operating conditions. The most suitable operating conditions with respect to the concentration of LiBr are those that allow recovering as much residual energy as possible. In addition, the use of multi-component working fluids allows, for a given composition and pressure, the boiling-condensation point of the fluid is not fixed, but varies within a range. The consequence of this is that, in heat exchangers, especially in evaporators and condensers, the pinch point approach temperatures are closer and longer lasting in the heat transfer process.
    [0057]
    [0058] DESCRIPTION OF THE FIGURES
    [0059]
    [0060] This section includes, by way of illustration and not limitation, the components of Figures 1,2, 3, 4 and 5 to show and facilitate the understanding of the invention.
    [0061]
    [0062] Figure 1. ASU MAC system with DCAC postcooler that uses CW and CCW by conventional compression-lamination cooler. Previous art figure.
    [0063]
    [0064] Figure 2. ASU MAC system with DCAC postcooler that uses CW and CCW cooled by “Waste Chilling Tower”. Previous art figure.
    [0065]
    [0066] Figure 3. “COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE”.
    [0067] Figure 4. “COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE” added various sources of residual energy and industrial cold sinks.
    [0068]
    [0069] Figure 5. Partial representation of a generic ASU, of interest for compression of the present invention. Previous art figure.
    [0070]
    [0071] The numbers referenced in Figure 1 (Fig. 1) are identified as follows:
    [0072]
    [0073] (1) Atmospheric air at the expiration of the MAC (Main Air Compressor).
    [0074] (2) Compressed and cooled air after the DCAC postcooler.
    [0075] (3) Water vapor inlet to the MAC turbine.
    [0076] (4) Condensed water after passing through the MAC turbine condenser.
    [0077] (5) Cooling water (CW) that is directed at cooling waste heat sources. (6) Return of cooling water from waste heat sources.
    [0078] (7) Cooling tower and cooling water pump set.
    [0079] (8) Cooling water after passing through the DCAC.
    [0080] (9) CCW chilled cooling water from the mechanical mechanical chiller.
    [0081] (10) Cooling water (CW) of the cooling tower.
    [0082] (11) MAC turbine.
    [0083] (12) MAC drive turbine condenser.
    [0084] (13) First stage of the MAC.
    [0085] (14) MAC first stage cooler exchanger.
    [0086] (15) Second stage of the MAC.
    [0087] (16) MAC second stage cooler exchanger.
    [0088] (17) Third stage of the MAC.
    [0089] (18) MAC third stage cooler exchanger.
    [0090] (19) Fourth stage of the MAC.
    [0091] (20) DCAC (Direct Contact Aftercooler), air-contact direct-contact postcooler.
    [0092] (21) CW return pump to the cooling tower from the DCAC.
    [0093]
    [0094] Numbers referenced in Figure 2 (Fig. 2), not matching those in Figure 1, They are identified as follows:
    [0095]
    [0096] (9) CCW chilled cooling water from the “Waste Chilling Tower”. (22) Cooling tower by “Waste gas” or “Waste Chilling Tower”.
    [0097] (23) Hot waste gas at the exit of the Waste Chilling Tower.
    [0098] (24) CW towards the “Waste Chilling Tower”.
    [0099] (25) “Waste Gas” from the cryogenic distillation column to the “Waste Chilling Tower”.
    [0100]
    [0101] The numbering referenced in Figure 3 is identified as follows:
    [0102]
    [0103] (1) Atmospheric air in the aspiration of the MAC (Main Air Compressor).
    [0104] (2) Compressed and cooled air after DCAC.
    [0105] (3) Water vapor inlet to the MAC turbine.
    [0106] (4) Condensed water after passing through the MAC turbine condenser.
    [0107] (5) Cooling water (CW) that is directed at cooling waste heat sources. (6) Return of the cooling water to the APC evaporator.
    [0108] (7) CW from the DCAC to the APC evaporator and / or cooling tower. (8) Hot water cooling to cooling tower (not shown). (9) Chilled cooling water (CCW) from the APC evaporator. (10) Cooling water (CW) from the cooling tower to the DCAC.
    [0109] (11) MAC turbine.
    [0110] (12) MAC drive turbine condenser.
    [0111] (13) First stage of the MAC.
    [0112] (14) MAC first stage cooler exchanger.
    [0113] (15) Second stage of the MAC.
    [0114] (16) MAC second stage cooler exchanger.
    [0115] (17) Third stage of the MAC.
    [0116] (18) MAC third stage cooler exchanger.
    [0117] (19) Fourth stage of the MAC.
    [0118] (20) DCAC (Direct Contact Aftercooler), air-contact direct-contact postcooler.
    [0119] (21) CW auxiliary pump at DCAC output
    [0120] (22) CW pump at the evaporator outlet of the APC to heat sources. (23) LiBr dissolution towards APC heat recovery
    [0121] (24) LiBr solution towards the APC evaporator.
    [0122] (25) LiBr solution towards the phase separator of the APC cycle.
    [0123] (26) LiBr dissolution steam towards APC power and cold branches.
    [0124] (27) LiBr dissolution steam in exhaustion of turbine towards APC absorber.
    [0125] (28) LiBr dissolution after the APC absorber to the APC circulation pump.
    [0126] (29) LiBr dissolution from the phase separator to the APC heat recuperator. (30) LiBr solution towards rolling valve.
    [0127] (30a) Constant enthalpy rolling valve.
    [0128] (31) LiBr dissolution from the rolling valve to the exhaustion of the APC turbine.
    [0129] (32) LiBr dissolution steam to APC lamination valve.
    [0130] (32a) Constant enthalpy rolling valve.
    [0131] (33) LiBr solution from laminating valve to APC Evaporator.
    [0132] (34) LiBr steam towards exhaustion of the APC turbine.
    [0133] (35) CW to the APC absorber.
    [0134] (36) CW from the APC absorber to the cooling tower (not shown).
    [0135] (37) CW to the APC capacitor.
    [0136] (38) CW of the APC condenser towards the cooling tower (not shown). (39) APC Evaporator.
    [0137] (40) APC phase separator.
    [0138] (41) APC heat recovery.
    [0139] (42) APC turbine.
    [0140] (43) APC absorber.
    [0141] (44) APC Evaporator.
    [0142] (45) APC condenser.
    [0143] (46) APC circulation pump.
    [0144] (47) APC cycle electric generator.
    [0145] (48) APC team section.
    [0146]
    [0147] Explanation of the numbering in Figure 4 not matching those in Figure 3:
    [0148]
    [0149] (5a) CW that is directed to receive residual heat (cooler exchangers
    [0150]
    [0151]
    [0152] inter-stages of GAN and GOX line compressors).
    [0153] (5b) CW that is directed to receive residual heat (Alternative or electric motor of the MAC).
    [0154] (5c) CW that is aimed at receiving residual heat (GAN liquefaction system, “make-up” and “recycle” or “recycle” compressors).
    [0155] (5d) CW that is directed to receive residual heat (Compressor Brayton reverse system).
    [0156] (6a) CW from residual heat source (GAN and GOX compressors).
    [0157] (6b) CW from residual heat source (Alternative or electric motor of MAC). (6c) CW from waste heat source (GAN liquefaction system).
    [0158] (6d) CW from residual heat source (Reverse Brayton System Compressor). (9a) CCW towards MAC aspiration.
    [0159] (9b) CCW towards cooling the MAC condenser.
    [0160] (9c) CCW towards the water cooling tower (CW).
    [0161] (49) Set of possible CW currents that are directed to take advantage of residual heat sources.
    [0162] (50) Set of possible CCW currents that are aimed at cooling processes in the ASU plant.
    [0163]
    [0164] Explanation of the numbering in Figure 5:
    [0165]
    [0166] (51) Compressor-turbine assembly known as “compander”.
    [0167] (52) GOX final line compressor.
    [0168] (53) GAN final line compressor.
    [0169] (54) Distillation set.
    [0170] (55) MAC of the section of the generic ASU represented.
    [0171]
    [0172] DETAILED DESCRIPTION OF THE INVENTION
    [0173]
    [0174] In the example case of Figure 1 (Fig. 1), the main and initial compression zone of an ASU installation is represented, without applying the improvement that this invention entails. The figure is not limiting. Each ASU plant has its own configuration with slight changes compared to Figure 1, which represents the initial main air compression zone. One of the most common MAC propulsion systems in ASUs is through an electric motor, although it is not exclusive. The number of Compression stages also varies. However, the use of a DCAC type contact cooler after the last stage of the MAC is widespread in almost all such cryogenic facilities.
    [0175]
    [0176] In this figural (non-limiting case-scenario), atmospheric air is sucked at point (1) by the first stage of the compressor (13). As a result of compression, the air is elevated in temperature and pressure. To reduce this temperature, an inter-stage cooler exchanger (14) is provided. At the exit of that exchanger, the second (15) and third (17) compression stages and their corresponding inter-stage cooler exchangers (16) and (18) are arranged. The fourth compression stage (19) has a DCAC (20). The air leaves the DCAC and goes to the rest of the ASU process (2).
    [0177]
    [0178] A stream of cooling water (CW) (5) from the cooling tower (7) is directed to the compression zone. The CW acts on the inter-stage cooling exchangers, as well as on the condenser (12) of the MAC turbine (11) and returns to the cooling tower (6). The mentioned turbine moves by means of water vapor. The exhaust steam of the turbine (3) is condensed in the condenser (12) leaving in a liquid state (4). There is also an incoming CW current (10) in the DCAC that returns to the cooling tower of the ASU pumped by the pump (21). In addition, there is a stream (9) of cooled cooling water (CCW), with a temperature lower than that of the CW, entering the DCAC. The CCW uses water, usually from the cooling tower (CW) of the ASU, which is cooled either with traditional electric compression-expansion refrigerators or with an auxiliary gas stream from the ASU process as explained in the figure two.
    [0179]
    [0180] Figure 2 represents another case-scenario, not limiting, similar to that of Figure 1 but with the addition of the “Waste Chilling Tower”. In many ASU installations, a gas stream of majority nitrogen composition is used, from the distillation section and through the MHE or "Main Heat Exchanger" as it is known in the art that characterizes these facilities, but does not meet the specifications to be sent online as the final product (known in the art in which these facilities are treated as "Waste Gas" to obtain CCW in the "Waste Chilling Tower"). The cooling that occurs in this tower is the result of direct contact between the “Waste Gas” and the CW. Therefore, the “Waste Chilllng Tower” replaces the electric chillers to obtain CCW in many ASU installations. The cooling produced by this tower can be replaced, totally or partially, by the cooling capacity of this invention, totally or partially unleashing the cooling potential of the "Waste gas" current. The element (9) of this figure is CCW that has been cooled in the “Waste Chilllng Tower” (22) by “Waste Gas” (25) by direct contact. The current (24) is CW incoming to (22) and ( 23) the hot “Waste Gas” after cooling the CW and protruding from the “Waste Chilling Tower”.
    [0181]
    [0182] Figure 3 is the COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE. The sources of residual heat of Figures 1 and 2 are the inter-stage exchangers of the MAC and the condenser of its drive turbine. The atmospheric air is sucked in point (1) by the first stage of the compressor (13). As a result of compression, the air is elevated in temperature and pressure. To reduce this temperature, an inter-stage refrigerator exchanger (14) is provided. At the exit of that exchanger, the second (15) and third (17) compression stages and their corresponding inter-stage cooling exchangers (16) and (18) are arranged. The fourth compression stage (19) has a DCAC (20). The air leaves the DCAC and goes to the rest of the ASU process (2).
    [0183]
    [0184] The CW pump (22) sends the cooling water to the waste heat sources (5) in a loop-type energy transfer circuit, in order to gain heat in the MAC turbine condenser (12) and in the exchangers inter stages (14), (16) and (18). Subsequently, the CW returns (6) to the APC evaporator (39) to give up this heat. The APC cycle (48) is a system for using residual energy through absorption that generates electrical energy and cooling capacity. In this invention, he designs a joint system plant that uses a lithium bromide (LiBr) solution as a working fluid in the APC cycle. Within this APC cycle (48) shown in Figure 3 and for non-limiting explanatory purposes, a distinction is made between:
    [0185]
    [0186] a) Common section formed by elements (39), (40), (41), (43), (46) and (30a).
    [0187]
    [0188]
    [0189] b) Power generation section formed by elements (42) and (47). c) Industrial cold generation section formed by the elements (44), (45) V (32a).
    [0190]
    [0191] The hot CW that has acquired heat in the waste heat sources of the ASU, transfers this energy in the evaporator (39) of the APC. From the evaporator, the heated LiBr (25) by residual energy is directed to a separating vessel (40) where a liquid-vapor phase separation occurs (lower and upper part respectively). Part of the steam (mainly more volatile components) of the LiBr (26) is directed to the power branch of the APC cycle and the other part to the cooling branch. The amount of LiBr circulated through the APC power or cooling branch can be varied according to operational needs, so that one, the other or a combination of them is prioritized.
    [0192]
    [0193] The power branch takes advantage of the quality of the steam to generate electric power through a turbine assembly (42) - alternator (47). In the turbine there is a process of transformation of the LiBr state characterized by a specific enthalpy relatively high in mechanical power and this in electrical energy in the generator moved by the turbine. In the exhaustion of the turbine (27), the LiBr has a relatively low specific enthalpy, but is still characterized as a biphasic liquid-vapor mixture. Condensation of this current occurs in the APC cycle absorber (43), the opposite process of the evaporator taking place, both in terms of phase change and in terms of concentration of volatile components. The cooling takes place by means of an incoming CW current in the absorber (35). Once condensed, the LiBr (28) is pumped by the pump (46) of the APC cycle. The high pressure LiBr (23) is directed to the heat recovery exchanger (41). In this equipment, the LiBr current undergoes a preheating to the evaporator (39).
    [0194]
    [0195] From the lower part of the phase separator (40) the hot LiBr current (29) is directed to the heat recovery exchanger to transfer energy. At the exit of the recovery exchanger, the LiBr current (30) undergoes constant enthalpy lamination by means of the valve (30a), lowering its temperature, to direct the exhaustion of the turbine (27).
    [0196] The cooling branch decreases the cooling water temperature so that it can be subsequently used (9) in the MAC last stage cooler or post-cooler (20), nominally in a direct contact air contact direct cooler (DCAC) ), in this non-limiting case, so that it integrates the APC cycle with the ASU or in any of the other systems referred to in Figure 4. The cooling of CW to obtain CCW is carried out in several steps. The first step is the condenser (45) where the LiBr solution is cooled with incoming CW (37) until the phase change to liquid (32) is achieved. This liquid stream undergoes constant enthalpy lamination by means of a valve adapted thereto (32a), thus obtaining a stream of cooled CW or CCW (33). This cold LiBr current absorbs heat from the outgoing CW current of the DCAC (20) which is driven (7) by the corresponding pump (21) in the evaporator (44), depending on the operational needs, part or all of this Cooling water can be returned to the cooling tower (8), instead of the evaporator and return to the DCAC via the route (10). The current of LiBr that has absorbed heat in the evaporator (44), is directed (34) to the exhaustion of the turbine of the power branch (27). In the exhaustion of the turbine, three currents are joined, (27), (31) and (34) which, as the same current, is directed in the liquefied state (28) to the system pump (46) after passing through the absorber (43).
    [0197]
    [0198] In addition to being able to control the passage of LiBr through the branch of power and / or cooling of the APC system, it is possible to vary the concentration of the LiBr solution depending on the operational needs that, in general but not limitation, seeks to obtain the conditions more favorable in thermodynamic criteria to maximize energy recovery, as long as fluid crystallization is avoided. The nature of the bi-component composition of LiBr causes condensation or evaporation to occur as a function of the concentration of each of them in the mixture.
    [0199]
    [0200] In figure 4, the CW currents that are directed to take advantage of residual heat sources alternative to those represented in figure 3 and typical in ASU installations are represented by the assembly (49).
    [0201]
    [0202] The element (5a) refers to the possibility of recovering residual heat from the MAC's motor-cooled electric motor, when it carries this type of motor
    [0203]
    [0204]
    [0205] refrigerated as a driving element. Another option is to send CW to the alternative internal combustion engine that moves the MAC, if this type of driving element is available. The option of the electric motor and that of the internal combustion engine, as well as the one shown in figure 3 or 4 of the steam turbine, are exclusive, so that, in general, there is only one operating as a driving element of the MAC, in a same ASU plant and at the same time. The element (5b) refers to the possibility of residual heat of the refrigeration system of the GOX final product line compressor (gaseous oxygen) -number (52) in Figure 5- and of the GAN final product line compressor ( gaseous nitrogen) -number (53) in figure 5- that usually equip ASU plants. In general terms, the use is similar to that of MAC inter-stage coolers. Element (5c) refers to the possibility of recovering residual heat from the “make-up” compressor and the “recycle” compressor (as they are known in the art that characterizes these cryogenic plants) of the GAN liquefaction system that It equips many of the ASU plants with this UN (liquid nitrogen) system. In general terms, the use is similar to that of the non-stage MAC coolers.
    [0206]
    [0207] The element (5d) indicates the possibility of recovering the residual heat of the CW that is sent to the air cooling after the compressor of the open and reverse Brayton cycle in the compressor-turbine assembly (commonly known as "compander" in the art that characterizes these facilities) and that it is used regularly in ASU plants prior to air entering the low pressure cryogenic distillation column (LPC) .The “compander” is represented in figure 5 with the number (51). a heat exchange after the compressor with the MHE, a cooler with CW is put in place to cool as much as possible the air after the compressor and before the MHE.The MHE is the main heat exchanger in an ASU plant and is represented in Figure 5. Unnumbered The high pressure (HPC) and low pressure (LPC) distillation columns are represented in a simplified manner in Figure 5 within the assembly (54).
    [0208]
    [0209] The use of waste heat sources follows a selective logic, that is, all, one, none or a combination of them can be used at will for the operation of this invention, provided they are not exclusive. Note that as they are represented, the use of a driving turbine
    [0210]
    [0211]
    [0212] in the MAC it would make the connection (5a), designed for alternative drive systems unnecessary. The elements (6a), (6b), (6c) and (6d) correspond to the hot returns to the APC evaporator of the CCW previously sent from the assembly (49). Group (50) refers to the set of uses that the CCW may have from the evaporator (44) of the APC. It consists of the elements (9a), (9b) and (9c).
    [0213]
    [0214] The element (9a) refers to the option of sending CCW to the MAC aspiration, in order to cool the air sucked by it. For obvious thermodynamic reasons, performing pre-compression cooling reduces the amount of energy needed for it. This is especially true in hot climates, where it is interesting to cool the air sucked into the MAC to reduce the energy required for compression. The above is a clear way to reduce the specific consumption of the ASU plant. The element (9b) refers to the option of sending CCW to the MAC turbine condenser, in the case that this is the propulsion method of this. Send CCW instead of CW to cool the condenser, the condensation temperature decreases after exhaustion of the turbine. This results in an increase in the enthalpy jump (Ah) in it. The increase in available Ah implies that for the same compression needs in the MAC, the steam flow required for said compression decreases. This, therefore, also leads to the reduction of the specific consumption of the ASU. Element (9c) refers to sending CCW to the return system to the cooling tower.
    [0215]
    [0216] The elements (7a), (7b) and (7c) correspond to the hot returns, towards the evaporator of the cold branch of the APC, of the CCW previously sent from the assembly (50), the (7c) being the contribution from the cooling tower
    [0217]
    [0218] Figure 5 proposes an example, non-limiting and simplified arrangement of the “frontend” of a generic ASU, which also includes the final line compressors of GOX (52) and GAN (53) and part of the distillation zone (54 ). Note that the configuration may change from one ASU to another. For example, GAN and GOX compressors may vary in their number of stages. Therefore, this figure should serve as an element to improve the description of the invention in its context of air distillation, but not limit it. The "compander" (51) is the compressor / turbine assembly that configures a reverse Brayton cooling system and open, usually used in ASUs, and whose main purpose is to pre-cool the air before entering the low pressure distillation column in the example in this figure.
    [0219]
    [0220] DESCRIPTION OF PREFERRED EMBODIMENTS OF THE INVENTION
    [0221]
    [0222] In accordance with the description of the invention with Figures 3 and 4, a preferred embodiment of the invention is highlighted "COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND COOLING BY ABSORPTION CYCLE" corresponding to the figure 3.
    [0223]
    [0224]
    one
    权利要求:
    Claims (6)
    [1]
    1st COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE characterized by comprising:
    a) An absorption power cycle or Absorption Power Cycle (APC), formed, not limited to, by:
    - An electrical power generation section by means of a turbine / alternator assembly.
    - An industrial cold generation section formed by a condenser exchanger and an evaporator exchanger.
    - A common section with an exchanger-absorber, pump, exchanger-recuperator, exchanger-evaporator, phase separation tank.
    b) An air compressor that, being part of this invention together with the APC system, performs the function of MAC integrated in an ASU installation, It is characterized by understanding, among others and depending on the needs of the ASU plant, by the following components:
    - A driving system of the electric motor type or an alternative internal combustion engine or a steam turbine or a gas turbine. In the case of the steam turbine, the corresponding steam condenser is also included.
    - A number "n" of compression stages, "n" being the necessary and non-limiting stages to maintain adequate flow, temperatures and compression ratio in the art that characterizes thermodynamic compression processes in the current state of the art.
    - An “n-1” number of inter-stage heat exchangers-refrigerators.
    - A direct air-water contact tower that performs the chiller function after the last compression stage with CW or CCW injection or both.
    c) A loop of cooling fluid that acquires thermal energy in all the residual energy sources specified in this invention and delivers it in the exchanger-evaporator of the common section of the APC cycle.
    d) A water cooling tower.
    [2]
    2a The operation procedure of the PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE
    according to claim 1, characterized in that the APC cycle cooling branch is operated to generate the minimum CCW necessary to maintain the air outlet temperature of the ASU DCAC at the desired level, with the aid of the CW. The remaining residual energy of the ASU process is used to generate electrical energy in the APC power branch.
    [3]
    3rd COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE according to any combination (inclusive or exclusive) of the preceding claims, characterized by using, in addition, at its discretion and depending on its Availability of the following sources of residual energy:
    to. Cooling exchangers of the final compressors of GAN (nitrogen gas) and GOX (oxygen gas).
    b. Cooling exchangers of the “make-up” and “recycle” or “recycle” compressors of the GAN liquefaction systems typical of ASU plants, similar to what is done with the GAN and GOX line compressors in section a .
    c. Refrigerator exchanger after the compressor of the reverse and open Brayton system prior to the distillation column and belonging to the “compander” or typical compressor-turbine assembly in ASU plants.
    [4]
    4th COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND COOLING BY ABSORPTION CYCLE according to any combination (inclusive or exclusive) of the preceding claims characterized by using e! Chilled water (CCW) at discretion and according to the needs in the following objectives:
    to. To an air cooling system in the MAC aspiration.
    b. To the MAC turbine capacitor, if any.
    c. To the cooling tower or source of the corresponding CW.
    [5]
    5th COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE according to any combination (inclusive or exclusive) of the preceding claims characterized by using one of the following as a working fluid of the APC cycle , instead of the LiBr:
    to. Aqueous solution of Lithium Chloride (LiCI).
    b. Aqueous solution of Calcium Chloride (CaCh).
    c. Water-ammonia solution.
    d. Ionic liquids
    and. Organic fluids such as amyl acetate, propane decane or isobutanedecane in combination with other refrigerants such as carbon dioxide.
    [6]
    6th COMPRESSION PLANT FOR AIR SEPARATION FACILITIES WITH RESIDUAL ENERGY CONVERSION IN ELECTRICAL POWER AND REFRIGERATION THROUGH ABSORPTION CYCLE according to any combination (inclusive or exclusive) of the preceding claims characterized by sending the APC cycle working fluid directly to the sources of residual heat of the ASU as an energy absorption fluid and in which, therefore, the waste heat exchangers act as an evaporator in the APC system.
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    同族专利:
    公开号 | 公开日
    ES2736963B2|2021-06-30|
    引用文献:
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    CN106091574A|2016-06-02|2016-11-09|成都深冷液化设备股份有限公司|The gas liquefaction equipment of a kind of band compression recuperation of heat and liquifying method thereof|
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    ES201800160A|ES2736963B2|2018-07-03|2018-07-03|Compression plant with conversion of residual energy into electrical power and refrigeration.|ES201800160A| ES2736963B2|2018-07-03|2018-07-03|Compression plant with conversion of residual energy into electrical power and refrigeration.|
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