Patent Application
20220234082
The present patent concerns the washing systems for industrial items, hereinafter simply referred to as industrial washing systems and/or industrial washing processes, and more specifically it concerns a new process with regeneration of the washing solvents and a system implementing said process.
1. State of the Art of the Industrial Washing Systems of the Single-Chamber and Vacuum Type
The industrial washing systems currently present on the international market are mostly of the single-chamber type. This means that the items and the material to be washed are introduced in a vacuum-tight washing chamber, in which the washing solvent is recirculated once or several times with increasing degree of purity as the process proceeds towards the last washing cycle.
Some variants exist, for example ultrasonic immersion washing, steam washing or other variant processes that in any case are all carried out inside a washing chamber.
At the end of the washing cycle, vacuum is created inside said washing chamber and in this way the residual solvent evaporates due to the very low pressure.
The washing liquids used in single chamber washing systems are mainly constituted by organic solvents, or aqueous solutions, or sometimes a combination of water and solvent. The most used solvents are modified alcohols whose boiling point exceeds 155° C., chlorinated solvents such as tetrachlorethylene and solvents with low boiling point such as methylene chloride, HFEs, HFOs, HFCs and Solstice™, solvents which at atmospheric pressure boil at a temperature between 15° C. and 60° C.
All the solvents are usually regenerated through distillation. This process constitutes an integral part of the washing process and is usually carried out in the same washing system.
The solvents with high boiling point are currently distilled, even under vacuum, with heating systems based on electric resistances or with hot water produced with electric resistances or fuels.
The vapor produced in this way is then condensed, generally using refrigerated water. Therefore, the solvents with high boiling point require a certain amount of energy, both when it comes to making them evaporate and when it is necessary to condense the vapors produced during distillation.
Solvents like HFEs, HFOs, HFCs and methylene chloride which, instead, have a boiling point under 40° C. under atmospheric pressure, can be distilled with the same systems used for modified alcohols, but also with heat pumps.
In this case, the heat pump recirculates the refrigerating fluid during the compression step, that is, when it is hot, inside coils immersed in the lower part of the distiller, and then the same refrigerating fluid, which during expansion cools down significantly, is recirculated in the upper part of the distiller.
In this way, the only energy involved is the mechanical energy necessary to carry out a refrigerating cycle, since the energy necessary to make the solvent evaporate is compensated for by the energy used for its condensation. Indicatively, distillation with a heat pump requires an amount of energy at least three times smaller than the amount of electric energy used for distillation with resistances and for condensation with refrigerated water.
A limitation of this last method using the heat pump lies in that, if the boiling temperature of the mixture constituted by the solvent and the dirt present in the distiller increases due to the presence of oil and dirt and approaches the temperature reached by the refrigerating fluid, the distillation capacity is reduced until it becomes equal to zero.
A variant of the method, which is applied very frequently, consists in distilling under negative pressure, so that the boiling temperature is lowered to several degrees less than the condensation temperature of the refrigerating fluid. This, however, is difficult to apply in case of distillation of modified alcohols, as their boiling temperature is generally around 170° C. under atmospheric pressure.
The technology of distillation through thermocompression or compression of the vapors is never used in industrial washing processes, while it is used in the chemical industry and above all in water distillation, both in the pharmaceutical sector and in the field of waste water treatment since, given the same amount of electric power absorbed, it has higher distillation capacity compared to other distillation systems.
However, a thermocompression system for water is generally very expensive, especially if it is going to be used to distil solutions that tend to dirty the heat exchangers with which the system is equipped.
This technology has never been taken in consideration in the field of industrial washing systems, due to the considerable cost of a thermocompression distillation system.
The patent document CN 2010610793 concerns a single chamber metal cleaning machine, schematically shown in the enclosed
Furthermore, the diagram of
The invention described below, instead, concerns a process for the industrial washing of industrially manufactured items in general, metallic or non-metallic, such as precision small parts, mechanical parts, printed circuits, lenses, watchmaking items, jewelry items, eyewear or similar items, in which the regeneration of the used solvents is obtained through a first distillation cycle, which does not require the supply of heat from an external source for boiling the solvents, and through the subsequent condensation of vapors, which does not require the use of an external refrigerant.
To sum up, in fact, said first distillation takes place thanks to the use of a first pump that compresses the distillation vapors, thus increasing their temperature and making it possible to use the liquid contained in the distiller, which is at a lower pressure and thus at a lower temperature, as exchange liquid for vapor condensation.
The object achieved by the process that is the subject of the present patent and by the system implementing said process is constituted by the fact that no external heat source and no refrigerator are required: the only energy supplied to the system is the mechanical energy necessary for the operation of the pump that draws the vapors from the distiller, and the energy necessary for the operation of a recirculation pump that recirculates the liquid solvent from the distiller to the condenser.
All the energy used to make the solvent evaporate is thus used to condense the vapors.
Said process using thermocompression distillation and the system implementing said process, a simplified form of which is schematically illustrated in
It is possible to use only one dry vacuum pump, as two of the three functions, meaning the drying of the pieces in the washing chamber and the distillation under vacuum, are used for a time fraction that is considerably short compared to the main function, which is the function of regenerating the solvent through distillation.
The invention can be especially and effectively applied in industrial washing systems of the type with a single chamber, with final vacuum drying, which use organic solvents for the washing cycle, wherein said organic solvents have a boiling point included between 15° C. and 60° C. under atmospheric pressure.
The application of the same method when solvents with a higher boiling point are used, instead, involves several drawbacks: a higher boiling point requires more attention during the heat exchange that takes place during the distillation process and may result in higher energy consumption, more overall complexity and thus more critical aspects. For example, when modified alcohols are used and the boiling temperature lowers below 100° C., the density of the vapors is very low, to the point that in order to obtain a sufficient quantity of distillate a compressor with very high flow rate is needed, which also results in high mechanical energy consumption.
On the contrary, the method described and claimed below, which uses solvents with a lower boiling point, can be applied in a simpler manner.
More specifically, the solvents like methylene chloride or other halogenated solvents, more precisely with chlorine and fluorine atoms, having a boiling temperature below 60° C. have also a very high vapor density, so that the application of the present process results to be very interesting from the energy point of view. Furthermore, said solvents are not soluble in water and therefore do not form salts. The boiling temperature inside the distiller does not exceed approximately 50° C. as boiling takes place under negative pressure and even if there were traces of water with salts, the latter would not be deposited on the walls of the exchanger because the temperature is relatively low.
As mentioned above,
The thermocompression distiller comprises a container DIST1 of the solvent to be distilled, hereinafter simply referred to as distiller DIST1, a first pump P1, an exchanger HEAT1 and a recirculation pump P2.
The system is thus without external heat sources and cold water sources for the condensation of vapors.
For the sake of simplicity, it is supposed that at the beginning of the distillation cycle the temperature T1 of the solvent is equal to 33° C.
By operating the first pump P1 it is possible to suck the vapors from the distiller DIST1 and convey them to the exchanger HEAT1 compressing them. Compression results in an increase of the temperature of the vapors from 33° to 50° C.
Inside the exchanger HEAT1, which is under negative pressure, more precisely at a pressure that is approximately 70 mbar less than the atmospheric pressure, the temperature of the vapors lowers until reaching the condensation temperature, which is approximately 38° C. The negative pressure, which is 70 mbar lower with respect to the atmospheric pressure, is not a binding condition for the principle of distillation through thermocompression. A slightly negative pressure compared to the atmospheric pressure has been suggested only because in washing systems with halogenated solvents it is preferable to maintain the system at a pressure below the atmospheric pressure in order to avoid small solvent leakages, for example through some critical points such as gaskets or valves.
The vapors come into contact with the surface of the exchanger HEAT1, inside which the solvent at the temperature of 33° C. coming from the distiller DIST1 is recirculated through said recirculation pump P2.
The thermal condensation energy is thus transferred to the solvent, which is conveyed back into the distiller DIST1, where it partly evaporates.
In simpler words, the system uses the same liquid to be distilled, contained in the distiller DIST1, to condense the vapors that have been compressed by the first pump P1 and that therefore have a higher condensation temperature than the liquid.
The process is self-regulating and the boiling temperature is automatically stabilized according to the pump flow rate, the exchange surface of the exchanger HEAT1 and heat dissipation towards the outside.
In particular, since the difference between the condensation temperature of the vapors and the temperature of the liquid is small, it is advisable that the heat exchange surface in the exchanger HEAT1 be sufficiently large and that the recirculation pump P2 have a very high flow rate, while on the contrary its head can even be very low.
Once stabilized, the process can thus proceed with no need for any external heat source or any refrigerant source.
The amount of energy used to carry out the distillation process can thus be from 5 to even 30 times smaller than the energy necessary to distil the same quantity of solvent in a distiller of the traditional type, similar to that schematically shown in
If at the beginning of the distillation cycle the solvent temperature is lower than the ambient temperature, the quantity of distillate will initially be very low. In any case, said pump P1 is able to extract and compress the vapors, even if very rarefied. Evaporation lowers the boiling temperature of the liquid, which therefore in the exchanger will have a lower temperature compared to that of the vapors. Therefore, the condensation process will take place in any case, even if the quantity of distillate obtained will initially be small. However, the mechanical energy of the pump P1 and of the pump P2 transferred to the system raise the temperature until reaching a balance point.
To conclude, the novelty of the present process and of the system implementing said process lies in the presence of the pump P1 which induces a difference in pressure between the liquid to be distilled and the vapors to be condensed.
It should also be noticed that the pump can be used also in a different way, maintaining the atmospheric pressure in the distiller and a higher pressure in the condenser, thus obtaining a high density of the sucked vapors and thus high efficiency.
In this first solution, the system comprises:
2. Description of the Distillation Function/Step Performed Through Thermocompression
Concisely, this function is performed by sucking the vapors from the top of said first distiller DIST1 through said first dry vacuum pump P1 which creates a certain negative pressure in said first distiller DIST1 and therefore lowers the boiling temperature of the solvent contained therein. The outlet of said first dry pump P1 is at atmospheric pressure or at a slightly lower pressure, if the system is under a slightly negative pressure with respect to the atmospheric pressure, as is often done to reduce random leakages of solvents with a low boiling point.
Said first distiller DIST1 can even be at atmospheric pressure and said first dry pump P1 can compress the vapors sucked from said first distiller DIST1 even exceeding the atmospheric pressure. In any case, whatever the pressure in said first distiller DIST1, by sucking and compressing the vapors it is possible to obtain a difference in pressure between the boiling liquid and the compressed vapors that must be condensed.
The difference in pressure, as is known from physical chemistry, causes a difference in temperature. Thus, the liquid, at a lower pressure than the vapors compressed by said first dry pump P1, has a lower temperature than the condensing vapor downstream of the first pump P1 itself.
The thermocompressors of the known type work as follows: instead of using an external cold source, to condense the vapors the liquid contained in a distiller, whose temperature is a few degrees lower than the vapor condensation temperature, is conveyed to an exchanger. The liquid, flowing into the exchanger and coming into contact with the hotter wall touched by the vapors, warms up and partially evaporates while flowing back into said distiller, where the pressure is lower. Therefore, the total quantity of energy required to condense the vapors is equal to the quantity of energy supplied to create them in said distiller.
With reference to the hydraulic diagram shown in
In said exchanger HEAT1, the pressure of the vapors is always higher than the pressure inside said first distiller DIST1, since said first dry pump P1 behaves like a vapor compressor, even if with a very limited compression ratio.
The difference in pressure between said first distiller DIST1 and the vapor side of said exchanger HEAT1 created by said first dry pump P1 causes the solvent to boil in the first distiller DIST1, but at a lower temperature than the condensation temperature, since condensation takes place at a higher pressure. The solvent in the liquid phase is colder than the vapors compressed by said first dry pump P1 and is thus used as a liquid for condensing vapors. When the system reaches the balance conditions, a thermal and pressure regime is established upstream and downstream of said first dry pump P1, said regime depending on the capacity of said exchanger HEAT1, the mechanical power transmitted to the vapors during the compression process, and the heat exchange of the entire system (distiller DIST1, first dry pump P1, recirculation pump P2, pipes etc.) with the environment.
If all of these components are well insulated, the distillation capacity is equal to the flow rate of said first dry pump P1 expressed in kg/m3, slightly increased due to the fact that the mechanical energy of the motor of said first dry pump P1, transferred to the vapors, contributes to the distillation process, too, as mechanical energy is transformed into heat.
In the field of solvents with boiling point included between 15° C. and 60° C., the heat exchange with the environment is limited and therefore the distillation capacity is only slightly affected by the environmental conditions.
However, if when said first distiller DIST1 is started the solvent temperature is several degrees lower than the boiling temperature, the solvent starts boiling at a much lower temperature and therefore more rarefied vapors are generated, which results in a decidedly lower distillation capacity, expressed in Kg/h.
The mechanical energy of said recirculation pump P2 and the energy transmitted to the vapors by said first dry pump P1 slowly increase the distillation temperature, until reaching a balanced situation.
In order to reach the balance conditions more quickly, at the beginning of the distillation cycle or step it is possible to activate a small heating system constituted, for example, by a coil with hot water flowing therethrough or by small heating resistances which, through the bottom or the walls of said first distiller DIST1, heat the fluid to be distilled. Once the balance conditions have been reached, the heating process can be interrupted.
Said first dry pump P1, however, is used also to dry the washed pieces under vacuum, so that a condenser COND1, which has the purpose of condensing the vapors extracted from the washing chamber W of the washing system, is installed in series with said exchanger HEAT1.
Sometimes a certain quantity of water is introduced in said distiller DIST1 together with the pieces to be washed and a small part of this water is distilled, too. Therefore, the distillate obtained may be constituted by a mixture of solvent and small traces of water, which is not soluble in the solvent if not in a very limited percentage.
Therefore, downstream of said condenser COND1 there is a water-solvent separator SEP1 which, exploiting the difference in density between water and solvent and the fact that the two components are actually not mixable, allows a distillate without water to be obtained.
The diagram of
A pipe T that draws from the bottom of said separator SEP1 then allows the solvent without water to flow out, except for a very small percentage of water, which is due to the solubility of water in solvent at a molecular level. The solvent separated from the water is recirculated in a distillate storage tank ACC.
During the thermocompression distillation process, said first distiller DIST1, or main distiller, is connected to a second distiller DIST2 through a valve VPS. Said second distiller DIST2 is thus arranged in parallel to said first distiller DIST1 but is fed by a small heat source S, for example constituted by hot water contained in a jacket or in heating resistances, which allows a small quantity of solvent to be distilled.
Thus, clean solvent in the vapor phase flows out of said second distiller DIST2, while solvent in the liquid phase, coming from said first distiller DIST1 and containing dirt or oil, flows into said second distiller DIST2.
Since oil and dirt do not evaporate, as the clean solvent flows out in the form of vapors, the concentration of dirt in said second distiller DIST2 increases and consequently also the distillation temperature increases. When the distillation temperature reaches a value that is close to the temperature of the heat source S, the distillation process stops. At this point it is necessary to start the vacuum distillation process described below.
3. Description of the Vacuum Drying Step Carried Out in the Washing Chamber at the End of the Washing Cycle.
This function is activated when requested by the program that manages the system's washing cycle. Said drying step is started by closing a first valve VP1 that connects said dry pump P1 to said first distiller DIST1 and stopping said recirculation pump P2. At this point a second valve VP2 is opened, which connects said dry pump P1 to said washing chamber W.
Said dry pump P1 sucks the vapors from said washing chamber W and said vapors flow through said exchanger HEAT1 without condensing. Said vapors, instead, are condensed in said condenser COND1, which is fed by refrigerated water. The condensed vapors pass into said separator SEP1 and from there they flow into said distillate storage tank ACC.
The material drying step carried out in said washing chamber W generally ends when an absolute pressure of just a few mbar is reached, a value which is set based on the washing program and the characteristics of the material to be washed. Said drying step can last from less than one minute to maximum a few minutes. The washing cycles generally last between 10 and 20 minutes, so the period during which said first dry pump P1 is used for said drying step is significantly shorter than the period during which it is used for said thermocompression distillation step described above.
4. Description of the Step of Solvent Distillation Under Vacuum Performed to Minimize the Percentage of Solvent in Distillation Waste.
The industrial washing equipment and systems serve the function of removing dirt from the materials to be washed, dirt which is generally constituted by processing residues, chips, emulsifiable oil, neat oil and dirt of various kinds. The corpuscular part of the dirt is generally blocked by the filters inserted in the washing circuit, which are not indicated in the attached drawings to simplify the hydraulic diagram, while the liquid part coming from the washing chamber W ends first into said first distiller DIST1 and then into said second distiller DIST2, where it is most concentrated. Thus, sooner or later it is necessary to remove the oil/dirt residues, by distilling thoroughly, meaning under high vacuum, the liquid contained in said second distiller DIST2.
Said operation is carried out by:
In an alternative solution, between said first and said second distiller DIST1 and DIST2 there is a transfer pump, not indicated in the figures, wherein said transfer pump is suited to transfer the liquid to be distilled under vacuum from said first distiller DIST1 to said second distiller DIST2, when necessary.
The vacuum generated by said first dry pump P1 and the heat generated by said heat source S with which said second distiller DIST2 is equipped make it possible to continue the distillation process in said second distiller DIST2 itself, until the solvent evaporates almost completely, leaving only the dirt in said second distiller DIST2.
For example, using hot water at 80° C. as heat source S and setting a maximum boiling temperature of 80° C., since the boiling temperature of the solvents used in this system does not exceed 60° C., the combination of the very low absolute evaporation pressure due to said first dry pump P1 with the heat transmitted to the liquid to be distilled makes it possible to obtain a distillation residue with a very low solvent percentage, even markedly below 1%, at the end of the process.
The absolute temperature and pressure necessary to conclude the vacuum distillation process must be defined by the user based on the type of residue, which may be simply constituted by oil, or may contain cleaning pastes or have a muddy consistency that makes it difficult to drain. The shape of said second distiller DIST2 and the distillation residue draining mode must be decided according to the type of pollutant to be removed.
In a washing system in which the quantity of dirt and oil is negligible, the addition of the second distiller DIST2 in parallel to the main distiller DIST1 can be avoided. In this case, when the distillation capacity tends to decrease due to the increase in the quantity of oil and dirt that gets into said main distiller DIST1, it is possible to carry out the vacuum distillation process in the main distiller DIST1 itself, which therefore must be equipped with a heat source or heating means to reach approximately 80° C. and must be structured in such a way as to resist high vacuum.
5. Calculation of the Cost of Thermocompression Distillation of a Solvent
The calculation concerns only the function of distillation through thermocompression, as the function of distillation under vacuum and the vacuum drying of the washed pieces require a negligible amount of energy compared to that necessary to regenerate the solvent.
The solvent taken in consideration for the calculation is methylene chloride, which has a boiling temperature of 40° C. under atmospheric pressure and is among the solvents suited to be effectively used in the new system.
As to chlorinated solvents, according to several national standards the whole system should remain under a slightly negative pressure with respect to the atmospheric pressure, in such a way that if the degree of tightness is insufficient due to a faulty gasket or valve, the solvent does not leak out and, instead, airs flows in. A system is provided to ensure that no abnormal air inflow takes place.
The solvents with low boiling point, which evaporate easily, do not form drops in the points with any leakages, in fact evaporation takes place immediately, unless the leakage is severe. In the case where the system is not under negative pressure, therefore, there is the risk of losing a high quantity of solvent even if no considerable leakage can be observed visually. Consequently, it is advisable to always keep the system under negative pressure, 24/7.
Inevitably, during some steps of the cycle the pressure in some pipe sections exceeds the atmospheric pressure. They are, for example, the liquid recirculation pipe of the distiller DIST1 and the delivery pipe of the washing pump P3. Depending on the type of washing cycle, there may also be other parts of the system at positive pressure. The rest of the system always remains under negative pressure.
Calculation data concerning the new system as described above:
6. Calculation of the Cost of Solvent Distillation Carried out Through a Traditional Distiller with Electrical Heating and Successive Condensation with Refrigerated Water
The energy required for the evaporation or condensation of 1 kg of methylene chloride is equal to 330 kjoule.
This energy must be added to that necessary to produce refrigerated water by means of a refrigerator. Generally, the electric energy consumed by a refrigerator amounts to 30% of the energy yielded as thermal energy, so the value of 330 kjoule/kg must be increased by 30%.
Therefore, 429 kjoule, corresponding to a power of 0.120 KW applied for 1 hour, are needed in total to distil 1 kg of methylene chloride.
Therefore, with 1 KW it is possible to distil and condense 8.33 Kg of solvents against the 84 Kg obtained with the new method employing thermocompression.
The calculations presented above concerning thermocompression have been made considering a washing system always under negative pressure, for evident safety reasons; the calculations change in the case where the system is at atmospheric pressure or, even better, if the part located downstream of said first dry pump P1, including said heat exchanger HEAT1, is under positive pressure, for example at 200 mbar.
In this last case, the solvent vapors are drawn from said first distiller DIST1 under atmospheric pressure and therefore their density is higher. Consequently, the quantity of distillate produced is higher, too.
Finally, if the condensation process takes place at a higher pressure and therefore with a difference in temperature between the cooling liquid in said exchanger HEAT1 and the condensing vapors at a pressure exceeding the atmospheric pressure, a lower flow rate of said recirculation pump P2 is necessary, with consequently lower energy consumption and a smaller exchange surface, therefore with a further reduction in operating and energy costs.
Indicatively, if the thermocompression distillation process according to the new method takes place at atmospheric pressure or at a pressure slightly higher than the atmospheric pressure, the distillation capacity, given the same amount of power, can be even 20-30% higher compared to the value calculated above.
7. Construction Variant in Which Said Exchanger HEAT2 is Installed on Said First Distiller DIST1, is Preferably of the Type with Tube Bundle and is Immersed in Said First Distiller DIST1, Thus Obtaining Even Higher Energy Efficiency (
A variant embodiment is constituted by a tube bundle exchanger provided in the lower part of said first distiller DIST1. The tubes of said exchanger HEAT2 are thus immersed in the liquid to be distilled while the vapors are conveyed into the space outside the tubes by the dry pump.
Even if a tube bundle exchanger located inside the distiller is generally more expensive than an external exchanger, this configuration offers the great advantage of avoiding the use of said recirculation pump.
To clean the exchanger HEAT2, if necessary, it will be sufficient to open and empty said first distiller DIST1.
8. Construction Variant for High Distillation Flow Rates and Even Higher Energy Efficiency, Carried Out with Two Dry Pumps P1, P4 in Series (
This variant is equal to that shown in
The flow rate of said second dry pump P4 can be even three times smaller than that of said first dry pump P1, since it sucks vapors that are already partially compressed. The advantage of this configuration lies in that the thermocompression cycle does not require the use of a compressor capable of creating high vacuum, rather it requires only a compressor with a high flow rate and a low compression ratio, which therefore needs less compression energy.
Said two dry pumps P1, P4 together thus constitute the best combination for obtaining very large quantities of distillate, with low energy consumption and at the same time the ability to create high vacuum when necessary.
According to a further construction variant, a liquid ring pump is used instead of a dry pump P4. This type of pump does not reach a high degree of vacuum due to the vapor tension of the operating liquid, unless the latter is cooled with an external refrigerator in such a way as to reduce the vapor tension to a very low value. In this case, instead of using water as operating fluid, which is common practice in most of the applications with liquid ring pumps, it is possible to use the washing solvent itself. In the event that water, which cannot be mixed with the solvents considered above, is used, it is necessary to provide a suitable system for separating water from solvent, similar to said separator SEP1 but properly sized. For the sake of simplicity, the recirculation tank of the liquid ring pump and the water-solvent separator, if any, are not indicated, as these solutions are known to the operators who normally use this kind of pumps.
The configuration with the first dry vacuum pump P1 only, as shown in
9. Other Functions Performed by the Same Vacuum Pump Used for Thermocompression Distillation
A washing machine does not consist only of a distiller to regenerate the solvent but is made up of several other components suited to perform the functions necessary to carry out a washing cycle.
The main functions performed by a washing machine with a single chamber based on vacuum technology, therefore, are the following:
A washing cycle can last from just a few minutes to 1 hour, according to the material to be washed and to the capacity of the machine. By way of example, it can be supposed that 3 washing cycles are performed every hour. A small quantity of oil and dirt is removed from the washing chamber at every cycle and enters the main thermocompression distiller.
Oil and dirt increase the boiling temperature of the solvent, while on the contrary the condensation temperature remains constant because the condensate does not contain oil. Therefore, in the presence of oil that increases the boiling temperature, the heat exchanger automatically reduces the passage of condensation energy into the liquid, as the difference in temperature between liquid and vapor has decreased. A part of the vapors is thus condensed in a small condenser containing cold water, which is installed in series with the main exchanger.
The vacuum pump, however, continues to draw the vapors from the distiller and this lowers the boiling temperature of the liquid, so that a new condition of balance is automatically established, as the colder liquid allows all the vapors sucked by the pump to be condensed. The lower boiling temperature consequently reduces also the density of the vapors and, since the volumetric flow rate of the dry pump is constant, the quantity of distilled solvent expressed as weight decreases. Slowly, as the quantity of oil introduced in the distiller reaches a high concentration, the boiling temperature and the density of the vapors become so low that it is not convenient to continue the thermocompression distillation process any longer.
Therefore, the value of oil concentration in the distiller must not be excessively high. This can be obtained by installing—in parallel to the thermocompression distiller—a small classical distiller equipped with a small independent heat source. Indicatively, this distiller indicated by DIST2 should not contain more than 10% of the solvent contained in the main distiller DIST1.
With a small source of thermal energy, obtained, for example, with a heating element on the bottom, this distiller can produce one tenth of the solvent compared to the main distiller. The mixture of solvent and low concentration oil thus flows into the distiller DIST2 while, on the contrary, only vapors of pure solvent flow out of this distiller, so that the quantity of oil remaining in the distiller DIST2 slowly increases and so does also the boiling temperature, until the latter reaches a maximum value established during the design step.
At this point the oil must be removed from the distiller DIST2, which is isolated from the rest of the system and maintained in operation by carrying out a vacuum distillation process, connecting it to the dry pump P1 used for the thermocompression.
This vacuum distillation in the secondary distiller DIST2 is obviously carried out when the machine is at rest regarding the washing of the pieces. Vacuum distillation indicatively requires 10-30 minutes and largely depends on the quantity of oil brought inside the machine by the pieces to be washed.
Vacuum distillation in the distiller DIST2 can be carried out when the operator who manages the machine deems it convenient, for example at the end of the work shift, or during weekends. The distillation capacity of the distiller DIST2 depends on the quantity of oil and dirt removed by the washing process daily. Indicatively, this capacity is included between 5% and 10% of the distillation capacity of the thermocompression distiller DIST1.
The dry pump P1, when connected to the vacuum distiller DIST2, must be able to create absolute vacuum, meaning very few mbar, while, on the contrary, when it works as a thermocompressor it compresses the vapors by approximately 200-300 mbar with respect to the boiling pressure.
The absolute pressure of just a few mbar in the distiller DIST2 can be achieved by one or more vacuum pumps arranged in series, while if production is very high it is possible to use a small vacuum pump capable of reaching an absolute pressure of a few mbar in the distiller DIST2 only, as shown in
10. Vacuum Drying
This step requires that vacuum be created inside the washing chamber in order to dry the pieces, until reaching an absolute pressure of just a few mbar. For this operation it is possible to use the same vacuum pump P1 used for thermocompression in the distiller DIST1.
A vacuum drying cycle in the washing chamber lasts a few minutes, during which thermocompression distillation is suspended.
The quantity of solvent removed for the drying step in the washing chamber, performed using the pump P1, is very low and therefore, even if a few minutes are dedicated to this operation for each washing cycle, the thermocompression distillation capacity is only slightly affected.
Once the solvent has been drained at the end of the washing cycle, a washing chamber having an inner volume of 1 cubic meter contains approximately 3-5 kg of solvent, while the thermocompression distillation capacity obtained with the same pump P1 having, for example, a flow rate of 350 m3/h is in the order of 15 l/min.
In the case of a very large washing system requiring a large quantity of regenerated solvent, a dry pump P1 can be used for thermocompression distillation while a second vacuum pump P6 can be dedicated to the drying step in the washing chamber and a third vacuum pump P5 can be dedicated to vacuum distillation, as shown in
The first dry pump intended for thermocompression, which requires that the vapors be compressed by no more than 500 mbar, is less expensive than a pump capable of reaching an absolute pressure of just a few mbar.
For most applications, only one dry pump capable of reaching an absolute pressure of 1 mbar is thus sufficient to carry out the three most important functions of a washing machine, that is:
11. Additional Refrigerated Water Condenser
The complete hydraulic diagram attached to the patent (
This condenser COND1 is necessary to condense the vapors removed from the washing chamber while the pieces are being dried and to condense the vapors produced by the small distiller DIST2.
Independently of the type of distillation, a machine that uses vacuum to dry the pieces and carry out a vacuum distillation process needs this condenser COND1.
However, the average quantity of solvent removed every hour to dry the pieces and carry out a vacuum distillation process is negligible compared to the quantity of solvent regenerated through thermocompression distillation, as indicated in the previous chapters.
Finally, this condenser COND1 serves the function of condensing any excess solvent vapors in the presence of severe environmental conditions, for example if the temperature inside the machine exceeds 30° C.
Obviously, if the ambient temperature is high, also the quantity of solvent produced increases, being the sum of what has been produced through thermocompression and what is due to the mechanical energy dissipated in the system.
The energy necessary to operate the washing machine installed in a room at a temperature below 20° C. is dissipated by the walls. However, if the room temperature is high, the energy dissipated by the thermocompression pump P1 and by the recirculation pump P2 must be removed by a cold water condenser or in any case by a refrigeration system.
12. Conclusion
The washing machine that is the subject of the present invention uses solvents with a boiling point included between 15° C. and 60° C., the most significant of which is methylene chloride, and is characterized by the presence of a system for regenerating the solvent through thermocompression which, to produce the same quantity of distillate produced by a distiller similar to those used in the currently known washing machines, requires much less energy, as all the energy used to condense the vapors is recovered to evaporate the solvent.
According to the size of the machine and the type of solvent, the energy consumption of the new machine can be from 5 to 30 times smaller compared to that required by a standard distiller.
Furthermore, the three main functions of the machine can be carried out in the simplest configuration by one dry pump only or by two dry pumps in series, thus making it possible to obtain a system with a limited number of components, and thus less expensive than traditional machines. The three main functions can be performed also by independent vacuum pumps, on the only condition that one of these pumps must be dedicated to the regeneration of the solvent through vapor compression.
No washing machine in the world currently uses thermocompression to regenerate solvent.
These are the schematic outlines that are sufficient to the expert in the art to carry out the invention, consequently on practical application variants may be developed which do not affect the substance of the innovative concept introduced herewith.
Therefore, with reference to the above description and the attached drawings, the following claims are expressed.
| Number | Date | Country | Kind |
|---|---|---|---|
| 102019000007257 | May 2019 | IT | national |
| Filing Document | Filing Date | Country | Kind |
|---|---|---|---|
| PCT/IB2020/054970 | 5/26/2020 | WO | 00 |
