Patent Application
20120174623
The invention relates to the field of separating gases and is targeted at optimizing a method of extracting one or more substances included in a gaseous mixture by anti-sublimation then melting.
The anti-sublimation process corresponds to the direct passage of one or more gases from the gas phase into the solid phase (the reverse-of the sublimation process).
More particularly, the invention relates to optimizing the management of the processes of frosting (or anti-sublimation) and defrosting comprising sublimation then melting on a plurality of heat-exchangers; implementing said processes requires managing the timing of distinct elementary operations.
In order to obtain anti-sublimation of a substance on a heat-exchanger, it is necessary for the substance to be at a partial pressure that is lower than that defined by its triple point, and also for the temperature of the surface of the heat-exchanger to be lower than that of the triple point of the substance.
Various gases are capable of undergoing an anti-sublimation process; CO2 is one example.
Document WO 02/060561 in particular describes a freezing method for extracting CO2 present in fumes from energy production units, the CO2 being frozen then defrosted in succession on two heat-exchangers.
However, that device exhibits undesirable effects, such as significant variations in the flow rate of the refrigerant fluids (or coolant and heat-transfer fluids) flowing in the freezing system, as well as undesirable energy losses.
Those undesirable effects are magnified when, as is usual, the extraction systems are large in size,
As an example, systems for extracting CO2 from the fumes from electricity production units using coal are very bulky. It should be recalled that a unit producing 800 MW [megawatts] of electricity with a thermal to electrical conversion efficiency of 44% emits approximately 620 t/h [(metric) tonnes/hour] of CO2 for a fume flow rate of 2 million Nm3/h [normal cubic meters per hour]. The flow cross section of the fumes over the CO2 frosting heat-exchangers can thus be about 1200 m2.
Extraction systems with dimensions of the same order are found in many industrial processes where gas separation is necessary and where the flow rates lie in the range 100000 m3/h [cubic meters per hour] to several million m3/h.
Thus, it is essential to reduce variations in the flow rates of refrigerant fluids or coolant and heat-transfer fluids as far as possible, and also to reduce variations in the flow rates of the gaseous mixtures passing through that type of facility.
A main aim of the invention is thus to overcome the problems identified above.
More particularly, the present invention proposes a method of extracting a substance included in a gaseous mixture, in an extraction system comprising:
each chamber comprising
the treatment of the gaseous mixture in each of the chambers comprising, in a cyclic manner, the following steps in succession:
the method further comprising a general sequencing step aimed at sequencing the passage from one step to another in each of the chambers such that the number of chambers undergoing the frosting step and also the total number of chambers undergoing the defrosting, recovery, and temperature-reduction steps are both equal to N, wherein, after a first cycle, the following two conditions are satisfied throughout the method
The present invention can be used to extract a substance that is capable of undergoing an anti-sublimation process.
More generally, the invention is applicable to any substance included in a gaseous mixture and characterized in that its partial pressure and its temperature are respectively lower than the pressure and the temperature of its triple point.
As an example, the invention is applicable to
On analyzing in detail a frosting and defrosting method such as that described in WO 02/060561, the inventors have succeeded in identifying a cycle comprising four distinct functional steps
The inventors have established that subdividing an extraction method temporally into four successive functional steps means that the heat-exchange areas employed and the flow rates of the refrigerant fluids associated either with frosting or else with defrosting can be managed more effectively.
Furthermore, it has been shown that appropriately selecting the numbers of chambers respectively undertaking each of the four functional steps throughout the method, produces significant advantages.
In particular, the invention makes it possible for the three distinct flows to be managed in coordinated and optimized manner, namely: the internal flow of the coolant fluids or refrigerant fluids for frosting; the internal flow of the heat-transfer fluids or the refrigerant fluids for defrosting, these flows passing in alternation through the heat-exchangers in the chambers carrying out the extraction method; and also the external flow of the gases to be separated moving over the external face of the freezing heat-exchangers.
More particularly, by means of the invention, the above three flows can be kept constant over time. This time constancy means that the heat-exchangers can be optimized in terms of energy. In addition, the continuity of the f lows obtained means that the compositions, in particular the compositions of the mixtures of refrigerant fluids (when they are used), can be optimized. These advantages are explained in particular by the fact that when the flow rates described above vary with time, the temperature differences between the circulating fluids also vary, which generates losses of efficiency in the system.
The continuity and constancy of the flow rates employed can also be used to optimize the operation of the compressors: their compression ratios may remain constant because of the constancy of the thermodynamic properties at the inlet to each compressor.
A refrigerant fluid (or a mixture of refrigerant fluids) is a fluid that evaporates when it absorbs heat and condenses when it releases heat.
In contrast, a coolant fluid only exchanges sensible heat: it heats up when it absorbs heat and it cools down when it releases its heat, solely by means of sensible heat.
It should be understood that in the remainder of the description, that for frosting and for defrosting the invention may make use equally well of refrigerant fluids or of coolant and heat-transfer fluids.
The inventors have determined the optimized sequencing for the four functional steps of the invention in each of the chambers of an extraction system.
More particularly, the inventors have determined the optimized distribution of the number of chambers of an extraction system that need respectively to undertake the steps of frosting, defrosting, recovery, and temperature-reduction.
As explained above, said optimized sequencing (or optimized distribution) can in particular mean that continuous or near-constant flow rates can be obtained for the refrigerant fluids or for the coolant and heat transfer fluids that flow successively through the heat-exchangers and through the first and second supply circuits up to the compressor intakes.
Thus, the invention can be used to significantly reduce the variations in the three distinct types of flow while extracting a substance. In other words, the invention can be used to significantly improve the distribution of the flows employed throughout the method of extracting the desired substance.
It should be noted that optimized energy efficiency of the extraction method is only achieved in reality once the flows employed reach a steady state in the system, i.e. after a first cycle has been carried out.
It should be noted that the term “gas to be separated” or “gaseous mixture” as used herein means a mixture of gas from which one or more substances are to be extracted by anti-sublimation.
It should also be noted that the description pertains to circumstances in which only a single substance is extracted from the gaseous mixture passing through the chambers. However, the skilled person will understand that the present invention is also applicable circumstances in which two or more substances are extracted from the gaseous mixture.
The anti-sublimation or frosting process involves the inverse operation to defrosting. However, the function of a heat-exchanger that freezes then defrosts is by its very nature discontinuous. Thus, one aim of the invention is to render the circulation of the three types of refrigerant fluid flows continuous in order to optimize the energy consumption of the functioning of the freezing systems producing said flows. More precisely, the three types of refrigerant fluid flow are employed as follows:
In order to ensure that these three types of refrigerant flow circulate continuously within the system, it is initially necessary for the steps of the cycle to be carried out on at least three distinct heat-exchanger surfaces operating in parallel, each heat-exchanger passing or not passing one of the types of refrigerant fluid flow as dictated by the step being carried out as described above).
In addition, it has been shown that the duration of the frosting step is equal to the duration of the other three steps of the method (i.e. the defrosting, recovery, and temperature-reduction steps). Since the steps of recovery and temperature reduction may be shortened and carried out on a single heat-exchanger surface during the defrosting period and since the defrosting step may be equal to half the duration of the frosting step, it has been found that for continuous operation on the surfaces of the heat-exchangers, it is necessary for the number N of heat-exchangers to be not less than 3 (N being an integer).
Furthermore, it has been found that when only three heat-exchangers are in use, the second flow of refrigerant fluid for frosting (i.e. that used for reducing the temperature of the heat-exchangers) is discontinuous in the extraction system since it is used only part of the time. When one of the three heat-exchangers carries out the recovery and then temperature-reduction steps over a given time sequence, the second refrigerant fluid flows only during the temperature-reduction step. That is why it is in fact necessary for the system to comprise 2N heat-exchangers so that all three types of refrigerant fluid flow are effectively continuous.
Consider, for example, the situation in which the extraction system comprises 6 chambers (i.e. N=3). In this situation, after a first cycle has been carried out, the following conditions are satisfied throughout the method:
Thus, at any time, there are three flows of the first type of refrigerant fluid for frosting, one flow of the second type of refrigerant fluid for frosting (for temperature reduction), and one defrosting flow.
Thus, as explained above, the heat-exchangers ref the extraction system of the invention carry out the steps of the method in accordance with the cycle described above. In each predetermined time sequence (10 or 15 minutes, for example), the valves of the system of the invention may change configuration so that the chambers move to a new step in the cycle. Despite the cyclic nature of the method, the flows described above remain continuous when the extraction system is viewed as a whole.
In a particular implementation, the frosting step also includes a sub-step of evacuating the chamber after closing the first and third pairs of valves.
Carrying out this evacuating sub-step advantageously means that undesirable residual gases present in the chamber can be evacuated at the end of the frosting step. Thus, at the end of the defrosting step, a chamber may contain a very pure gas, i.e. a gas with a very high concentration of the substance to be extracted. In this manner, during the recovery step it is possible to recover an extracted substance of very high purity, both in the liquid form and in the form of residual gases.
Recovering a very high purity residual gas is advantageous since the as may be of significant commercial value. As an example, carrying out this evacuation sub-step in the extraction method of the invention may be used to extract CO2 in a gaseous form of very high purity; this is highly attractive commercially.
Further, it has been recognized that after a first cycle has been carried out, the number of chambers carrying out the defrosting step is equal to N′, N′ being an integer that depends on the value of N,
More particularly, N′ is such that the ratio N′/N is equal to a value in the range one-third to one-half, said value being a function of the value of N.
As an example, it can be shown that the ratio N′/N is equal to the minimum value ⅓ when N=3. Similarly, it has been shown, for example, that the ratio N′/N is equal to the maximum value ½ when N=4.
In a particular implementation, the method of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to N/2 if N is equal to a power of two.
In another implementation, the method of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to (N/2)−1 if N is even and is not equal to a power of two.
In another implementation, the method of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to (N−1)/2 if N is odd.
It should be noted that whatever the selected number of chambers carrying out the defrosting step, the number of chambers carrying out the recovery step and the number of chambers carrying out the temperature-reduction step are, by definition, always selected so as to complement the number of chambers carrying out the defrosting step, i.e. so as to ensure the number of chambers carrying out the frosting step remains equal to the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps.
It should also be noted that when the integer N is equal to a power of 2 (N thus being 4 or more), the ratio N′/N is then equal to ½ and it is possible to obtain a constructal distribution of the three types of flow employed, i.e. dividing them by two. To this end, it should be recalled that the term “constructal” has its origin in the theory by Adrian Bejan. This theory states that the optimized architecture for access to flows in a plurality of branches is obtained when access to the flows of each branch is maximized. Such maximization is possible when each branch is divided by two, since this guarantees the same path length irrespective of the itinerary adopted by each of the flows under consideration,
The constructal distribution is all the more advantageous when, as recalled above, the general dimensions of the extraction systems are very large.
It should also be noted that when N is equal to a power of 2, it is not essential for the number of heat-exchangers carrying out the recovery step and the number of heat-exchangers carrying out the temperature-reduction step to be equal to a power of 2. When certain constraints are imposed, it is possible to select a different distribution for the recovery and temperature-reduction steps among the chambers of the extraction system, provided that the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps nevertheless remains equal to N.
In a particular implementation of the invention, the duration of the frosting step is substantially equal to the cumulative duration of said defrosting, recovery, and temperature-reduction steps.
It is also possible to carry out a preliminary step of determining the duration of the frosting step, this being determined from a measurement of a maximum pressure drop between the inlet and outlet of the chamber during a frosting step.
More particularly, the duration of a frosting step of a given extraction system may be determined by experiment by measuring the difference in the pressure of the gaseous mixture between the inlet, and the outlet from one chamber, during a frosting step of the extraction method.
This pressure drop is explained by the gradual growth of frost on the external surfaces of the heat-exchangers during frosting and by the gradual obstruction of the gas lines.
A typical value for the pressure drop is in the range +50 Pa [Pascal] to +500 Pa, this threshold constituting the signal for closing, via two valves (or two flaps), the inlet and the outlet of the chamber that has completed its frosting step.
In a particular implementation, the various steps of the extraction method are determined by instructions from computer programs.
As a consequence, the invention also provides a computer program on an information medium, said program being capable of being used in an extraction system or, more generally, in a computer, said program including instructions adapted to carrying out the steps of an extraction method as described above.
Said program may use any programming language and be in the form of source code, object code, or a code intermediate between source code and object code, for example in a partially compiled form, or in any other desirable form.
The invention also provides an information medium that can be read by a computer, and including instructions for a computer program as mentioned above.
The information medium may be any entity or device that is capable of storing the program. As an example, the medium may comprise storage means, such as a read-only memory (ROM), for example a compact disk (CD) ROM, or a microelectronic circuit ROM, or magnetic recording means, for example a floppy disk or a hard disk.
Furthermore, the information medium may be a transmissible medium such as an electrical or optical signal that may be routed via an electrical or optical cable, by radio or by other means. The program of the invention may in particular be downloaded from an Internet type network.
Alternatively, the information medium may be an integrated circuit into which the program has been incorporated, the circuit being adapted to execute or to be used in the execution of the method in question.
The present invention also provides a system for extracting a substance included in a gaseous mixture, the extraction system comprising:
each chamber comprising:
the control means being configured such that each heat-exchanger is connected alternately to the first and second supply circuits;
the control means also being configured to sequence passage from one step to another in each of the chambers such that the number of chambers carrying out the frosting step and also the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps are both equal to N; and
wherein the control means are also configured such that, after a first cycle, the following two conditions are satisfied throughout the method:
The extraction system of the invention and the particular embodiments below have the same advantages as those demonstrated relative to the extraction method and its particular implementations.
In a particular embodiment, the control means are also configured such that the frosting step includes a sub-step of placing the chamber under vacuum after said closure of the first and third pairs of valves.
Further, and in the same manner as for the extraction method, it has been recognized that once a first cycle has been carried out, the number of chambers carrying out the defrosting step in the extraction system is equal to N′, where N′ is an integer that depends on the value of N.
More particularly, N′ is such that the ratio N′/N is equal to a value in the range one-third to one-half, said value being a function of the value of N.
It has been shown, for example, that the ratio N′/N is equal to the minimum value ⅓ when N=3. Similarly, it has been shown, for example, that the ratio N′/N is equal to the maximum value ½ when N=4.
In a particular embodiment, the extraction system of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to N/2 if N is equal to a power of two
In another embodiment, the extraction system of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to (N/2)−1 if N is even and is not equal to a power of two.
In another embodiment, the extraction system of the invention is such that after a first cycle, the number of chambers carrying out the defrosting step is equal to (N−1)/2 if N is odd.
As with the extraction method, the number of chambers carrying out the recover step and the number of chambers carrying out the temperature-reduction step are always selected so as to complement the number of chambers carrying out the defrosting step, i.e. so as to conserve the equality between the number of chambers carrying out the frosting step and the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps.
When the integer N is equal to a power of 2 (N then being 4 or more), the ratio N′/N is equal to ½ and a constructal distribution of the three types of flow employed may be obtained, i.e. they may be divided by two.
In the particular circumstances explained above, it is not essential to adopt a constructal distribution of the steps over the series of the chambers of the extraction system. In particular, the choice depends on the various constraints imposed on the extraction system. However, it is vital that the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps remains equal to N.
In a particular embodiment of the invention, the duration of the frosting step is substantially equal to the cumulative duration of said defrosting, recovery, and temperature-reduction steps.
Further, the extraction system may include measurement means to carry out the preliminary step of determining the duration of the frosting step, the duration of the frosting step being determined from a measurement of a maximum pressure drop between the inlet and the outlet of the chamber during a frosting step.
Further characteristics and advantages of the present invention become apparent from the description below, made with reference to the accompanying drawings, which illustrate an embodiment that is not limiting in any way. In the figures
The present invention provides a system for extracting a substance present in a mixture of process gas or fumes, by bringing about anti-sublimation of that substance on the solid surface of a plurality of freezing heat-exchangers.
To this end, anti-sublimation of the substance to be extracted is carried out at a temperature and at a pressure lower than that defined by the triple point of the substance under consideration.
The extraction system of the invention comprises 2N heat-exchangers, N being an integer greater than or equal to three.
The eight heat-exchangers have been shown in
The extraction system of
Each freezing heat-exchanger comprises a circuit in which a refrigerant fluid (or a mixture of refrigerant fluids), a coolant fluid or a heat-transfer fluid may circulate. Said circuit typically comprises ribs associated with tubes in which the fluid in question can circulate.
Further, the flow rate of the refrigerant, or coolant/heat-transfer fluids circulating in the heat-exchangers is controlled by a series of valves described in more detail below.
By causing a refrigerant or coolant fluid to circulate at a given temperature, it is possible to control the temperature of the external surface of each heat-exchanger.
Thus, during the frosting step, it is possible to reduce the temperature of the gaseous mixture circulating over the heat-exchanger of a given chamber by causing a refrigerant fluid to circulate at low temperature and evaporate or by causing a coolant fluid to circulate and heat up. Thus, it is said that a refrigerant or coolant fluid “for frosting” circulates in the heat-exchanger.
Similarly, it is possible, during the defrosting step, to increase the temperature of the solid phase deposited on the heat-exchanger of a chamber. To this end, a refrigerant fluid is caused to circulate in a two-phase state at a relatively high temperature (10K [Kelvin] to 70K above the triple point temperature of the substance to be extracted) in the heat-exchanger circuit so that said fluid is condensed. Alternatively, a heat-transfer fluid may be caused to circulate in the heat-exchanger, which cools down.
During the defrosting step, it is said that a refrigerant fluid or a heat-transfer fluid “for defrosting” circulates in the heat-exchanger.
In the remainder of the description, it should be understood that when refrigerant fluids for frosting and refrigerant fluids for defrosting are used, it is possible to replace them with coolant fluids and heat-transfer fluids respectively.
In addition, in the remainder of the description attention is given to a single refrigerant fluid for frosting (or coolant fluid) and to a single refrigerant fluid for defrosting (or heat transfer) circulating in an alternating manner in the heat-exchangers. However, it should be understood that it is possible to cause mixtures of refrigerant fluids for frosting (or coolant fluids) or mixtures of refrigerant fluid for defrosting (or heat-transfer fluids) to circulate.
Further, the supply circuit 1000 can be used to route the gaseous mixture from which a substance is to be extracted inside the chambers AA, BB, CC, DD, EE, FF, GG, and HH.
Access by the gaseous mixture is controlled upstream of the chambers AA, BB, CC, DD, EE, FF, GG, and HH by valves A100, B100, C100, D100, E100, F100, G100, and H100 respectively, which are collectively termed the gas valves V100.
The gas mixture located inside the chambers AA, BB, CC, DD, EE, FF, GG, and HH may then be extracted. Said extraction is controlled using valves A101, B101, C101, D101, E101, F101, G101, and H101 respectively, which are collectively termed the gas valves V101.
The gaseous mixture extracted thereby may then be re-routed via the evacuation circuit 1010 to another chamber carrying out another functional step,
Further, evacuation from the chambers AA, BB, CC, DD, EE, FF, GG, and HH of the substance extracted from the gaseous mixture in the chambers and the residual gas phase is controlled by the valves A130, B130, C130, D130, E130, F130, G130, and H130 respectively, which are collectively termed the valves V130.
The substance that is extracted thereby, which is in the liquid state, is routed via the recovery circuit 130 to a reservoir R at the end of gas phase recovery.
Further, in a preferred implementation, the recovery circuit 130 is also connected to a vacuum pump P via a valve V200. Using said vacuum pump, it is possible to place the chambers of the system under vacuum. The importance of this pump and said vacuum step is described in more detail below,
Further, the refrigerant fluid circuit comprises two distinct supply circuits: a frosting circuit in which a refrigerant fluid for frosting (or a coolant fluid) circulates, and a defrosting circuit in which a refrigerant fluid for defrosting (or a heat-transfer fluid) circulates.
The frosting circuit comprises the supply circuit 1210, the branches 121 and 120 as well as the return circuit 1200.
The defrosting circuit comprises the supply circuit 1100, the branches 110 and 111 and the return circuit 1110.
More particularly, the supply circuit 1210 supplies the branch 121 with refrigerant fluid for frosting under high pressure. Said refrigerant fluid for frosting is sent to the heat-exchangers carrying out frosting or proceeding to the heat-exchanger temperature--reduction step.
Access by the fluid for frosting to the heat-exchangers A, B, C, D, E, F, G, and H is respectively controlled by the valves A121, B121, C121, D121, E121, F121, G121, and H121, which are collectively termed the valves V121.
Said valves V121 correspond to the expansion valves that can be used to change the refrigerant fluid for frosting from the high to the low pressure of the system. Said expansion valves can thus be used to evaporate the frosting fluid circulating in the heat-exchanger.
Alternatively, the valves V121 can be used to heat up the coolant fluid circulating in the heat-exchanger during the frosting step. In this particular configuration, the valves V121 are not expansion valves but are flow rate control valves.
In addition, extraction of the evaporated refrigerant fluid for frosting for heated coolant fluid) originating from the heat-exchangers A, B, C, D, E, F, G, and H is controlled respectively by the valves A120, B120, C120, D120, E120, F120, G120, and H120, which are collectively termed the valves V120.
The refrigerant fluid is then returned to a compressor (not shown) via the return branch 120 then the return circuit 1200.
Because 2N heat-exchangers (N≧3) are provided in the extraction system, the flow rate of the refrigerant fluid is constant over time and has constant thermodynamic properties, which means that the compressor for the system can function under steady state conditions. Such conditions mean that firstly the compressor can function under optimized compression conditions, and secondly that the heat-exchangers of the system can also function under steady state conditions. In addition, when mixtures of refrigerant fluids are used, the composition of said mixtures may then be optimized since the conditions for said fluids are steady.
When a coolant fluid is used to reduce the temperature of the heat-exchanger, it is then returned via the same branch 120 to a cooling heat-exchanger, not shown. This heat-exchanger can be used to cool the coolant fluid so that it can be re-introduced into the system. In the same manner, the steady flow rate of the coolant fluid means that the function of the heat-exchangers associated with cooling said coolant can be optimized.
Further, the circuit 1100 and the branch 110 supply the heat-exchangers with refrigerant fluid in the vapor phase or partial liquid-vapor phase under condensation conditions (i.e. with refrigerant fluid for defrosting).
Access by the refrigerant fluid for defrosting to heat-exchangers A, B, C, D, E, F, G, and H is respectively controlled by the valves A110, B110, C110, D110, B110, F110, G110, and H110, which are collectively termed the valves V110.
In addition, extracting the refrigerant fluid for defrosting originating from the heat-exchangers A, B, C, D, E, F, G, and H is respectively controlled by the valves A111, B111, C111, D111, E111, F111, G111, and H111, which are collectively termed the valves V111.
The collected refrigerant fluid for defrosting, the liquid content of which has been increased, is returned via the return branch 111 and the return circuit 1110 to a heat-exchanger or a series of heat-exchangers at a higher temperature.
Because the extraction system of the invention is arranged into 2N heat-exchangers (N≧3), the refrigerant fluid for defrosting has a constant mass flow rate in the circuits 1100, 110, 111, and 1110.
When a heat-transfer fluid is used during the defrosting step, the cooled heat-transfer fluid is returned to a heating heat-exchanger, not shown. Once heated up, said heat-transfer fluid may be re-introduced into the extraction system.
In the example described here, the series of valves identified above are configured so as to allow:
Reference is made to
As explained above, it has been shown that the extraction method hinges on a cycle of four successive functional steps.
In the example described here, a preliminary step (EX) is initially carried out before carrying out the various functional steps composing the cycle of the extraction process.
This preliminary step means that the duration of the subsequent frosting step can be ascertained.
As described above, this duration may be determined from a measurement of the pressure drop between the inlet and the outlet of the chamber AA during frosting. This pressure drop results from the gradual obstruction of the gas lines as well as gradual deposition of a solid layer on the surface of the heat-exchanger.
Next, the first functional step of the cycle is carried out: the frosting step (step FS).
This step requires that the gaseous mixture is moved in the chamber AA. To this end, the inlet and outlet valves A100 and A101 connecting the chamber AA to the supply circuit 1000 for the gaseous mixture are opened.
The gaseous mixture is then cooled during its passage over the external face of the heat-exchanger A. The gaseous mixture is cooled to a first temperature and to a first pressure so that the substance to be extracted solidifies on the heat-exchanger A: this constitutes anti-sublimation of the substance on the heat-exchanger A.
It should be noted that the first temperature and the first pressure are respectively lower than the temperature and pressure defined by the triple point of the substance to be extracted.
In order to cool the gaseous mixture, the valves A121 and A120 connecting the heat-exchanger to the refrigerant fluid for frosting or coolant fluid circuit are opened.
The refrigerant fluid for frosting circulating in the heat-exchanger evaporates, thereby creating the refrigerating power necessary to freeze the substance on the surface of the heat-exchanger A.
Alternatively, a coolant fluid circulates in the heat-exchanger and creates the necessary refrigerating power by heating up.
In the embodiment described here, a sub-step (denoted VSS) for placing the chamber AA under vacuum at the end of the frosting step is then carried out in order to extract the residual gases present in said chamber. To this end, the following is carried out in particular:
The valve V200 can be used to control the connection of the evacuation circuit 130 with either the vacuum pump P or the reservoir P. When the vacuum sub-step VSS is carried out, said valve V200 connects the vacuum pump P with the evacuation circuit 130.
This vacuum sub-step VSS can typically reduce the pressure in the chamber to approximately 50 Pa absolute. The duration of this vacuum step is of the order of 20 seconds, for example, but depends on various parameters such as the pumping power of the pump P in particular. The relative vacuum obtained means that the residual gaseous mixture contained in the chamber AA can be evacuated. Said residual gaseous mixture may, for example, be treated once recovered.
However, it should be noted that said vacuum sub-step VSS is optional. The advantage of said vacuum sub-step is described in more detail below.
The second functional step in the cycle corresponds to the defrosting step (step DS).
In this implementation, the valve A130 is closed at the start of defrosting step DS. However, it should be understood that said closure is only necessary because the valve A130 was open at the end of the frosting step in the example under consideration in order to carry out the vacuum sub-step VSS. In contrast, when the vacuum sub-step VSS is not carried out at the end of the frosting step, the valve A130 remains closed during the whole of the frosting step, and so the valve A130 is already closed when the defrosting step is commenced.
In addition, throughout the defrosting step, the valves A100 and A101 of chamber AA are closed, such that said chamber is no longer supplied with gaseous mixture. Thus, the step is carried out in a closed chamber.
Valves A121 and A120 are also closed such that the heat-exchanger A is no longer supplied with refrigerant fluid for frosting.
Further, the valves A111 and A110, connecting the heat-exchanger A to the refrigerant fluid for defrosting supply circuit, are open in order to reheat the heat-exchanger A.
The increase in temperature of the solid deposit of the substance present on the heat-exchanger A causes sublimation of the deposit, namely the direct passage of the substance from the solid phase to the gas phase.
The process of sublimation in a closed environment also causes an increase in the pressure in the chamber AA that, as explained above, was initially under vacuum at the start of the defrosting step.
Sublimation of the solid deposit still present on the heat-exchanger A then causes the pressure in the chamber AA to rise. When the pressure of the triple point, of the substance is reached in the chamber, the solid deposit undergoes a melting process such that the substance passes directly from the solid phase to the liquid phase.
To this end, the refrigerant fluid for defrosting is used in the heat-exchanger in the two-phase state and at a relatively high temperature, typically 10K to 70K above the temperature of the triple point of the substance.
The refrigerant fluid for defrosting condenses, releasing its heat to the heat-exchanger, thus allowing sublimation then melting of the frozen substance on the external surface of the heat-exchanger.
Alternatively, a heat-transfer fluid is used at a temperature of 10K to 70K above that of the triple point circulating in the heat-exchanger. On cooling, the heat-transfer fluid allows sublimation then melting of the substance frozen on the heat-exchanger.
The defrosting step is managed over time via the trio formed by the flow rate/temperature/vapor content of the refrigerant fluid for defrosting circulating in the heat-exchanger A, or via the duo formed by the flow rate/temperature for the incoming heat-transfer fluid.
The third functional step corresponds to the recovery step (step RS).
More particularly, this step comprises recovery of the liquid phase of the defrosted substance accumulated in the reservoir after the defrosting step.
This step also comprises, simultaneously with recovery of the liquid phase, recovery of the residual gas phase in the chamber before returning to the first pressure of the cycle of the extraction method.
The valve A130 is open, thus allowing the liquid phase and the residual gas phase to be evacuated. The valve V200 is configured so that the liquid and gas phases that are thus recovered are evacuated to the reservoir R.
It should be noted here that recovery of the residual gas phase is carried out until the pressure in the chamber AA returns to the pressure of the circuits 1000 and 1010.
Furthermore, during the recovery step, the valves A100, A101, A110, A111, A120, and A121 are closed. As a consequence, the gaseous mixture does not circulate in the chamber AA and no refrigerant fluid circulates in the heat-exchanger A.
It should be noted that when no vacuum sub-step has been carried out during the frosting step, residual gases are present in the chamber AA at the start of the defrosting step. These gases mainly include nitrogen and oxygen, for example. However, such gases are not capable of passing into the solid state during the defrosting step like the substance to be extracted (for example CO2). Thus, as indicated above, said vacuum sub-step (VSS) can advantageously be used to evacuate these undesirable residual gases by means of the vacuum pump P. Thus, at the end of the defrosting step, the chamber AA contains a very pure gas, i.e. a gas with a very high concentration of the substance to be extracted. In this manner, during the recovery step RS, it is possible to recover a high purity extracted substance, both in the liquid form and in the form of residual gases.
Recovery of a very pure residual gas is advantageous as that gas may have a significant commercial value. As an example, carrying out said vacuum sub-step VSS in the extraction method of the invention means that very pure CO2 can be extracted in the gaseous form; this is highly attractive commercially.
Finally, the fourth step corresponds to a temperature-reduction step of reducing the temperature of the heat-exchanger (step TS).
To this end, the valves A120 and A121 are opened in order to cause the refrigerant fluid for frosting to circulate in the heat-exchanger A.
When the temperature of the heat-exchanger A has reached a temperature close to the first temperature at the start of the cycle, a fresh cycle of the extraction method may he initiated by configuring the valves afresh to carry out a frosting step (opening the gas valves A100 and A101).
The extraction method of the invention also comprises a general sequencing step (not represented in
The sequencing is such that the number of chambers that carry out the frosting step, and also the total number of chambers carrying out the defrosting, recovery and temperature-reduction step are both always equal to N. This equality is, however, only reached once the first cycle has been carried out, so that the extraction system is in a steady state. As explained above, this equality means that the energy efficiency of the extraction method can be significantly improved.
Further, the sequencing mentioned above is such that after a first cycle, the following conditions are satisfied throughout the extraction method:
It should also be noted that the ratio of the number of chambers each carrying out the four functional steps throughout the extraction method also corresponds to the ratio of durations between each of these steps.
Thus, the cumulative duration of the defrosting, recovery, and temperature-reduction steps in an extraction system is always substantially equal to the duration of the frosting step. It should be noted that this equality is also satisfied when the vacuum sub-step VSS described above is carried out at the end of the frosting step. The duration of said sub-step is in fact negligible compared with the duration of the remainder of the frosting step (i.e. the time during which the substance is deposited in the solid form on the heat-exchanger). The duration of the frosting step may typically be of the order of 10 to 15 minutes, while the vacuum sub-step lasts approximately 20 seconds, for example. The vacuum sub-step VSS is thus carried out almost instantaneously compared with the frosting step as a whole.
Further, once a first cycle has been carried out, the number of chambers carrying out the defrosting step in an extraction system is equal to N′, N′ being an integer that depends on the value of N.
More particularly, N′ is such, that the ratio N′/N is equal to a value in the range from one third to one half, the value of the ratio being a function of the value of N.
This means that irrespective of the number of heat-exchangers 2N present in the extraction system (where N is three or more), the duration of the defrosting step is always between a third and half the duration of the frosting step.
As an example, it has been shown that the ratio N′/N is equal to the minimum value ⅓ when N=3.
Similarly, it has been shown that, for example, the ratio N′/N is equal to the maximum value when N=4.
Regarding the value of N, three distinct situations are envisaged:
Further, the number of chambers carrying out the recovery step and the number of chambers carrying out the temperature-reduction step are by definition always selected so as to complement the number of chambers carrying out the defrosting step.
This means that throughout the method, the number of chambers carrying out the recovery step and the number of chambers carrying out the temperature-reduction step are fixed so as to conserve the equality between the number of chambers carrying out the frosting step and the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps.
However, it should be noted that the above ratios in terms of the number of chambers each carrying out the functional steps can only be satisfied once a first cycle has been carried out in the extraction system under consideration. In this manner, it is possible to have, at any given instant, several chambers each carrying out a respective one of the four functional steps of the extraction method cycle.
Such distributions of the functional step, throughout an extraction method, over the chambers of an extraction system mean that continuous flows of refrigerant fluids for frosting and defrosting (or coolant and heat-transfer fluids) can be obtained over the series of heat-exchangers.
This continuity of the flows thus results in a steady state as regards the supply to the heat-exchangers and the compressor or compressors used in the system, which provides great opportunities for energy optimization.
Furthermore, the fixed duration for the defrosting step is a function of the flow rate, the initial quantity of vapor and the temperature of the refrigerant fluid for defrosting circulating in the heat-exchanger during the defrosting step or the temperature and flow rate of the heat transfer.
Similarly, the fixed duration for the recovery step is also a function of the recovery flow rate of the liquid phase and the residual gas phase, while the fixed duration for the temperature-reduction step is also a function of the flow rate of the refrigerant fluid for frosting (or coolant) for resetting the heat-exchanger to the first temperature of the cycle.
With reference to
More particularly,
In
Each of the eight heat-exchangers of the extraction system are indicated on the vertical axis.
At each time interval x1 to x8 under consideration, the heat-exchangers A to H carry out a particular functional step, which results in a specific configuration of the set of valves of the extraction system as described with reference to
During the first time interval x1, the heat-exchanger A carries out the frosting step (start of the step), the heat-exchanger B starts the temperature-reduction step, the heat-exchanger C starts the recovery step of the liquid phase of the substance to be extracted and the heat-exchanger D carries out the defrosting step (second half of the step).
The table below summarizes the opening or closing positions of the set of valves of the extraction system illustrated in
The “open” and “closed” positions of the various valves are indicated by the letters “O” and “C” respectively.
The four functional steps of the extraction method are carried out in the same manner on each of the eight heat-exchangers of the extraction system.
Thus, it is possible, from Table 1, to determine the configuration of the valves of the extraction system during each time interval x1 to x8. It should be noted that the above table does not include the configuration of the valves when the vacuum sub-step VSS is carried out at the end of the frosting step. This optional sub-step has been deliberately omitted since it does not have a significant impact on the general sequencing of the steps.
Further,
By studying the successive steps carried out in a cyclic manner for each heat-exchanger, it can be seen that for each heat-exchanger, the extraction method is carried out in two major time sequences: the frosting step followed by the other three functional steps, namely the defrosting, recovery, and temperature-reduction steps.
It is clearly seen here that throughout the extraction method, the number of chambers (or heat-exchangers) carrying out the frosting step is equal to the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps.
Further, in this particular situation. N is an even integer. Thus, throughout the method:
Further, the number of chambers carrying out the recovery step and the number of chambers carrying out the temperature-reduction step are each selected so that the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps is equal to 4.
In this particular situation, the number of chambers carrying out the recovery step and the number of chambers carrying out the temperature-reduction step are necessarily equal to 1.
As a consequence, when N=4, the duration of the defrosting step is equal to half the duration of the frosting step, while the durations of the steps of recovery and of temperature-reduction are each equal to a quarter of the duration of the frosting step.
Controlling the set of valves of the extraction system in accordance with
Thus, a constructal distribution of said three flow rates in the extraction system can be obtained, i.e. division of the flow rates by two.
However, it should be noted that in the situation in which N is an integer equal to a power of 2 and N is 8 or more, several configurations are possible concerning the number of chambers carrying out the steps of defrosting and temperature reduction (this is also true for other values of N).
As explained above, when several configurations are possible, it is not essential to select the configuration corresponding to a constructal sequencing of the functional steps in the chambers of the extraction system.
The choice of a configuration from those that are possible may be made in a random manner or as a function of certain constraints of the extraction system.
Further, it can be seen that when N=4, the ratio N′/N is equal to the maximum value ½.
An example of an extraction method of the invention in the situation in which. N=6 is described below with reference to
More particularly,
This situation differs from that of
In accordance with the invention, the number of chambers (and heat-exchangers) carrying out the frosting step is equal to the total number of chambers carrying out the defrosting, recovery, and temperature-reduction steps.
More particularly, in this particular situation, we have throughout the method:
Further, in this particular situation, the extraction system is configured so that throughout the method, there are two chambers carrying out the recovery step and two chambers carrying out the temperature-reduction step.
As a consequence, the durations of the defrosting, recovery, and temperature-reduction steps are each equal to one third of the duration of the frosting step.
As a consequence, N=3 and N is an odd integer.
More particularly, in this particular situation, we have throughout the method:
In this particular situation, the extraction system necessarily comprises one chamber carrying out the recovery step and one chamber carrying out the temperature-reduction step, throughout the extraction method.
This means that the durations of the defrosting, recovery, and temperature-reduction steps are each equal to one third of the duration of the frosting step.
Further, it can be seen that the ratio N′/N in this situation is equal to one third, i.e. the minimum possible value of the ratio N′/N.
In general, the number of heat-exchangers 2N (N being 3 or more) comprised in an extraction system of the invention is selected for specific design reasons linked to the dimensions of the facilities.
Further, it is possible to envisage programming a controller to control the opening or closing of the various valves of the extraction system of the invention.
The controller may be programmed to satisfy the sequencing of the functional steps as described, for example, with reference to
This controller may also control measuring means in order to carry out a preliminary step EX as described with reference to
| Number | Date | Country | Kind |
|---|---|---|---|
| 0955666 | Aug 2009 | FR | national |
| Filing Document | Filing Date | Country | Kind | 371c Date |
|---|---|---|---|---|
| PCT/FR2010/051685 | 8/9/2010 | WO | 00 | 4/2/2012 |
