DESCRIPTION HYBRID MEMBRANE AND CATHODIC REDUCTION SYSTEM FOR RHODIUM ENRICHMENT AND RECOVERY Technical Field of the Invention The present invention relates to a hybrid membrane electro recovery system (1) for the recovery of rhodium from jewellery industry wastewater, comprising membrane filtration and cathodic reduction of rhodium. Prior Art The applications for platinum group metals are growing as a result of changing environmental regulations and technological advancements. Platinum group metals (PGM) are used in many areas of industry due to their high corrosion resistance and non-oxidation even at high temperatures. PGMs are primarily used in catalytic converters, which reduce harmful emissions from automobiles. The jewelry industry is the other most common use of rhodium (Rh). Sulphate-based solutions containing 2 g/l Rh ³⁺ are used for decorative coating of gold jewelry, particularly in the jewelry sector. When the solution baths reach a Rh ³⁺ content of 0.2 - 0.7 g/l, the bath solution is replaced with a new one due to both the decrease in rhodium ion concentration and the darkening of the coating colour due to the acid excess in the bath composition. Therefore, waste bath solutions are generated from large and small enterprises in the industry. These industrial wastewaters contain high levels of precious metals such as rhodium. These wastes are sources of precious metal-containing secondary (PGM) raw materials for our industry. It is crucial to recover PGMs from used catalysts as well as from other sources of usage, including the jewelry industry, because natural sources of PGMs are rare and the production of high purity PGMs from these sources is difficult. There are a limited number of methods for the recovery of such effluents in the state of the art. Hydrometallurgical methods (dissolution and precipitation processes) and thermal pyrometallurgical methods are widely used in the recovery and enrichment of rhodium from waste rhodium baths. Precipitation is the oldest and most widely used method for recovering rhodium from rhodium wastes. Metals in the waste solution are precipitated with reductants such as zinc powder, copper powder, iron powder and rhodium recovery is aimed. Furthermore, rhodium wastes are classified as solid or liquid according on their industrial use. The most common rhodium wastes are solid as the catalytic converter catalyst in the automobile industry is the most significant area of application. The majority of liquid rhodium wastes are rhodium plating bath wastes from the jewelry sector. Rhodium can not be produced pyrometallurgically due to its high melting point and noble metal characteristics. Rhodium is recovered using a variety of physical and chemical separation techniques, including solvent extraction (Sümer, 2009; Yılmaz, 2005), ion exchange (Kononova et. al., 2010a; Kononova et. al., 2010b; Beamish, 1966; Blokhin vd., 2009; Borbat et. al., 2010), adsorption (Losev et. al., 2010; Tüylüoğlu, 2008), precipitation (Güven, 2002), cementation (Yavuz, 2008; Aktas, 2011; Aktas, 2012; Morcalı et. al., 2013), electrodialysis (Akça, 2017), and electro-recovery (Yu et. al., 2014). In the United States patent document numbered US4155750 (A), which is in the known state of the art, metallurgical processes for the recovery or purification of rhodium are mentioned. In the said document, respectively, firstly (i) a solution of a soluble anionic rhodium complex is treated to precipitate insoluble penta amino-chloro rhodium dichloride (in the presence of a catalyst capable of producing hydrate (aqueous) ions and ammonia), (ii) rhodium is redissolved as the equivalent hydroxo complex cation ((Rh(NH3)5OH)2 ⁺ ) and (iii) the solution is treated to precipitate the nitrate salt of the penta amino-nitro rhodium complex. Then (iv) the precipitate is converted to penta amino-chloro rhodium dichloride and finally (v) calcined to form rhodium metal. This approach demonstrates that one of the most challenging difficulties in the platinum group metal refining indusrty is the separation and purification of rhodium in such waste solutions. In the international patent document numbered WO2006/013568A2, which is in the known state of the art, the recovery of precious metals from electronic scrap by hydrometallurgical processing is mentioned. The method in the said document is a process for the recovery of non-ferrous precious metals from raw materials, which includes mechanical grinding, initial settling and disintegration, etc. with the method in question, an increase in the efficiency of electrochemical reduction activity at the cathode was observed by enrichment instead of dissolution- solutionizing-precipitation- solution etc. processes. The United States patent document numbered US4097347 (A), which is in the known state of the art, relates to a technique for the recovery of metals, and more particularly gold. According to the technique, gold in solution is electrolytically collected on a cathode and must then be extracted from the cathode. The titanium cathode was first coated with nickel and then gold deposition was accomplished in the procedure described in patent document numbered US4097347 (A). The gold deposited on the cathode at the desired level was then removed by immersion in gold king water. However, in this process, nickel was also added to the solution in addition to gold. The United States patent document numbered US3857763 (A) relates to the recovery of rhodium from electrolyte by deposition method. The invention is applicable to the recovery of rhodium from aqueous waste solutions containing fission products obtained in the processing of fuel elements containing neutron irradiated uranium. In the said invention, the acidic solution containing rhodium is electrolysed in an electrolytic cell. Rhodium is reduced on a titanium cathode in the presence of a controlled potential against a platinised titanium anode. At this stage, the electrolysis current value is around 40 mA while the potential against the Ag/AgCl reference electrode is kept at -25 V. The electrolysis time is approximately 4 hours. Rhodium metal is removed from the cathode by contacting with dilute hydrofluoric acid. The said invention relates to the recovery of Purex alkaline waste solutions. In the United States patent document numbered US3567368 (A) releates to rhodium concentrate production methods. The procedure described in the paper includes recovering rhodium concentrate, passing a solution containing rhodium through an anion exchange column, precipitating the cationic rhodium until a zone of cationic recovered rhodium is created, and eluting the cationic rhodium from this zone. The said technique is designed to recover rhodium from wash baths and rinse baths following galvanic rhodium plating baths in jewelry workshops, large gold processing facilities, or laboratory scale electroplating baths. Product wash and rinse waters are discharged to sewers without recovery of rhodium. However, this method cannot be utulized in industrial practice for the recovery of rhodium from waste solutions because the low rhodium concentration and acidity of the solution results in low and unsatisfactory efficiencies in rhodium recovery and therefore recovery is uneconomical. The present invention discloses a hybrid system designed to recover rhodium from jewellery industry wash and rinse baths. The present invention discloses the electrolytic recovery of rhodium from acidic solutions in the jewellery industry, as well as rhodium enrichment by pre-membrane treatment. In the hybrid method of the present invention, the concentration enrichment of the metal by pre-membrane filtration reduces the volume of the solution and thus reduces the volume of the electrolyte cell. With this pre-treatment, an improvement in cathodic reduction efficiency was observed. Since the cathodic deposition of rhodium in the method of the present invention does not involve stripping with acidic treatment such as king water etc., it will not cause blackening and low gloss problems that may be caused by unwanted metals such as nickel in coatings. Technical Problem that the Invention Aims to Solve The object of the present invention is to develop a method that eliminates acidic dissolution/solutionizing processes and the associated environmental and occupational health risks, does away with the use of chemicals, and allows on-site reuse and/or recovery of waste. Another aim of the present invention is to create a hybrid membrane-electro recovery system that enables the recovery of rhodium from secondary sources (wastewater) by concentrating it by membrane process and reducing it on the cathode surface by electrochemical method. When rhodium is pyrometallurgically dissolved in acid, highly toxic and corrosive gases are released. The present innovation offers the electrochemical enrichment of rhodium from waste sources by membrane filtration without subjecting it to acidic operations, followed by solid recovery. Another difference of the present invention from the state of the art is that it offers an environmentally friendly approach compared to existing conventional methods. There are no secondary pollutants produced by the present innovation. In conventional methods such as precipitation-solubilisation or solvent removal, the transition from one medium to another medium causes a new problem to arise. With the present invention, two different technological methods are combined to provide an environmentally friendly recovery method. These methods are membrane filtration method and electro recovery method. The present invention involves enriching rhodium from the solution medium using the porous structure of the membrane and then separating it using the oxidation/reduction property of rhodium without the the use of additional acid-base, etc. chemicals. The term molecular weight cut off (MWCO, molecular weight cut off, Da) is also used instead of "pore diameter" in membranes. The pore diameters of nanofiltration (NF) membranes vary between 0.005 and 0.001 µm (200 - 1000 Da). Due to the anionic rhodium sulphate complex in the waste bath solutions having a molecular radius of 0.90-0.95 nm, approximately 10% of the rhodium in the waste bath solution passes to the filtrate in the commercial nanofiltration membranes (NF90 and NP030) used in the membrane filtration stage described in the present invention. Thus, some rhodium loss occurs with the passage of 10% rhodium to the filtrate. In the present invention, without precipitation of rhodium in rhodium wastes, rhodium in soluble form in wastewater is enhanced in concentration by membrane technique and then recovered by reduction on the cathode surface by electrodeposition technique. The present invention is particularly efficient for rhodium. The ambient conditions will need to be modified if the system of the present invention is utilized to recover other platinum group metals. For example; membrane type, operating conditions of the membrane system, anode-cathode material type and system operating conditions will change. Therefore, the system in the present invention is unique to rhodium chemistry. In the present invention, the behaviour of rhodium against the pH of wastewater, the electrochemical behaviour of rhodium as a result of voltammetric studies and the compatibility of properties such as conductivity and pH of wastewater in the membrane system against the recovery system are in question. Description of the Figures Figure 1: Schematic view of the hybrid membrane electro-recovery system (1) Figure 2: Flow chart of the hybrid membrane electro-recovery system (1) Descriptions of the References in the Figures 1: Hybrid membrane electro-recovery system 2: Waste water feed tank 3: pH meter 4: Conductivity meter/ probe 5: Level sensor 6: Valve 7: Pump 8: Manometer 9: Flowmeter/flow sensor 10: Membrane module 11: Filtrate line 12: Filtrate tank 13: Feedback line (Concentrated line) 14: Two-way valve 15: Electrodeposition line 16: Electrolysis unit/cell 17: DC (Direct Current) power supply 18: Anode 19: Cathode 20: Control unit 100: Pre-Filtration A: Filtration of wastewater with pre-filtration (100) B: Taking the pre-filtered wastewater into the wastewater feed tank (2) by manual transfer C: Operating the system from the system control panel (20) for the hybrid membrane electro-recovery system (1) to operate. D: Filtering the wastewater taken into the wastewater feed tank (2) in the membrane module (10) E: Taking the wastewater filtered in the membrane module (10) into the permeate tank (12) via the permeate line (11) F: Measuring the rhodium concentration values of the wastewater in the wastewater feeding tank (2), the permeate tank (12) and the concentrate line (13) and the quantitative follow-up of the liquid volumes with appropriate measuring cups (grade drum, measuring cup, beaker, etc.) G: If the wastewater in the permeate tank (12) after the F treatment step is not at least 70% of the total volume of the wastewater taken into the wastewater feed tank (recovery rate), the wastewater is fed back to the waste water feed tank (2) via the concentrate line (13) and continuing the membrane filtration process until it reaches at least this rate. H: If the wastewater in the permeate tank (12) after the treatment step G is at least 70% of the total volume of the wastewater taken into the wastewater feed tank (2) (when the return rate is reached), the enriched wastewater in the wastewater feed tank (2) directing the water to the electrodeposition line (15) through the double-acting valve (14) positioned on the concentrate line (13) I: Connecting the anode (18) plates to the positive (+) output pole of the DC power supply (17) in the electrolysis unit (16), and connecting the cathode (19) plates to the negative (-) output pole of the DC power supply (17). J: Initiation of electrodeposition process with the help of DC power supply (17) after receiving the enriched wastewater to the electrolysis unit (16) in the H process step. K: Operating the electrolysis unit (16) until the rhodium concentration reaches at least 30 mg Rh/l. L: Completion of electrolysis process by turning off the DC power supply (17) M: Removing the anode (18) and cathode (19) plates and drying them at a temperature of at least 105 °C for at least 24 hours N: After the drying process in the M process step, in order for the anode (18) and cathode (19) plates to cool, the electrodes should be placed in a cabinet isolated from moisture and external environment for at least two hours. O: Determination of weight losses and gains in the anode (18) and cathode (19) plates after the cooling process is completed with the help of analytical balance P: After the determination of the weight loss and gains on the anode (18) cathode (19) plates in the O process step, stripping the metallic coating deposited on the plate surface from the cathode (19) plates with a thin brush and/or a dilute acidic solution (5- 10% sulfuric acid). R: Obtaining metallic powder after stripping step S: Washing the metallic powder with distilled water, hot water or a dilute acid (HCl, CH3COOH, H2SO4) to remove unwanted salts and metals and then filtering to purify the powder T: Drying the metallic powder at a temperature of at least 105 °C for at least 24 hours after washing U: Obtaining rhodium powder after the drying process in the T process step. Disclosure of the Invention The hybrid membrane electro-recovery system (1) described in the present invention is a two-stage system, and the membrane module (10) filtration is the first stage of the system. The aim of the first stage is to reach the rhodium concentration that will provide high efficiency for the electrodeposition stage. The second stage of the hybrid membrane electro-recovery system (1) of the present invention is the electrodeposition or electrolysis cell (16). The hybrid membrane electro-recovery system (1) used in rhodium recovery in the present invention, in its most basic form comprises - at least one wastewater feed tank (2), at least one pH meter (3) placed in the wastewater supply tank (2), at least one conductivity meter (4) and at least one level sensor (5), - at least one main pipe connected to the wastewater feed tank (2) and at least one valve (6) connected on said main pipe, - at least one pump (7) placed/connected to the main pipe to ensure the flow of water in the wastewater feed tank (2), - one manometer (8) connected on the main pipe following the pump (7), followed by at least one flow meter (9), - at least one 25x40 membrane module (10) for concentrating the desired metal in the wastewater, - at least one membrane module permeate line (11) outlet and at least one permeate tank (12), - at least one feedback (concentrate) line (13) coming out of the membrane module (10) and at least one flow meter (9) connected on the feedback line (13), -at least one double-acting valve (14) located on the feedback line (13) and at least one electrodeposition feed line (15) which will allow the passage of the feedback line (13) (concentrated) to the electrolysis cell (16) when desired, - at least one DC power supply (17) to power the electrolysis cell, - at least one anode (18), at least two cathodes (19), at least one pH meter (3) and at least one conductivity meter (4) in the electrolysis cell (16), - a system control software on at least one computer or one panel, - at least one control unit (20) where the entire flow is controlled, In the hybrid membrane electro-recovery system (1) of the present invention, rhodium wastewater from the jewelry industry is subjected to a pre-filtration (100) process before being taken into the wastewater feed tank (2). The wastewater, which is subjected to pre-filtration (100), is then taken to the wastewater feed tank (2) (Figure 1). Wastewater taken into the wastewater supply tank (2) is pumped to the membrane module (10) by a pump (7) along the main pipe coming out of the wastewater feed tank (2), and the wastewater is filtered in the membrane module (10) which is the first stage of the hybrid membrane electro-recovery system (1). A nanofiltration (NF) membrane is used in the membrane module (10), which is the first stage of the present invention. In order to not pass through the membrane for the rhodium sulfate compound with a molecular radius of 0.95 nm, the pore diameter of the NF membrane should be below 0.90-0.95 nm. Since the rhodium sulphate compound in the wastewater with a molecular diameter greater than 0.90-0.95 nm cannot pass through the membrane surface, the rhodium sulphate compound returns to the wastewater supply (2) tank with the water dissolved in the water. Although it varies according to the conductivity value of the bath solution taken into the waste water feed tank (2), the hybrid membrane electroplating membrane is at a pressure range of 4-15 bar, at room temperature and at a pH of less than 1.2, until it reaches a recovery rate of at least 70%. The membrane module (10) system, which is the first stage of the hybrid membrane electro-recovery system (1), is operated in a cycle. For example, the membrane module (10) system, which is the first stage of the hybrid membrane electro- recovery system (1), is maintained until at least 70 liters of the 100 liters of liquid taken into the waste water feed tank (2) passes into the filtrate (12). While the wastewater is filtered in the membrane module (10), the filtered (passing) wastewater from the membrane goes to the permeate tank (12). The filtrate tank (12) refers to the tank containing all kinds of small compounds (iron, calcium, magnesium, zinc, etc.) that can pass through the membrane (<0.90 -0.95 nm, <500 Da). Therefore, the wastewater passing into the permeate tank (12) should be at least 70% of the total wastewater taken into the wastewater feed tank (2) after the pre-filtration (100). This rate can be increased according to the user's request, but cannot be less. The concentrated wastewater is the water in the wastewater feed tank (2). After the filter process is completed in the membrane module (10), the double-acting valve (14) is opened and the concentrated wastewater in the wastewater supply tank (2) is sent to the electrolysis unit (16) with the help of the feed line (15). The rhodium values and liquid volumes of the solution in the waste water feed tank (2), the permeate line (11) and the concentrate line (13) are quantitatively measured with suitable measuring cups (scaling drum, measuring cup, beaker, etc.), and the return rate is at least 70% should be provided. After the filtering process with the membrane module (10), the wastewater whose volume decreases by at least 70% is taken to the electrolysis cell (16) for the second stage of electrodeposition process via the feedback line (13). The electrolysis cell (16) consists of a platinum anode (18) and a platinum or platinized-titanium or gold cathode (19). With a DC power supply (17), the wastewater is subjected to electrodeposition until the rhodium concentration reaches <0.30 mgRh/l depending on the rhodium concentration in the wastewater in the range of 0.70 - 0.90 volts. This voltage range is the value at which rhodium is reduced (accumulated on the cathode plate surface) from solution form (Rh ⁺³ (in wastewater)) to solid form (Rh ⁰ (solid)). As a result, rhodium metal is reduced at the cathode. The size of the membrane module (10) in the hybrid membrane-electro recovery system (1) in the present invention may vary, and 20x20-40x40 modules may be more ideal for the jewelry industry. Specific to rhodium chemistry, rhodium in the rhodium sulfate compound precipitates as rhodium hydroxyl at pH higher than 3.2. Therefore, in the membrane enrichment process, the pH value of the waste bath water in the waste water feeding tank (2), the pH value at the time of operation with the membrane method and the pH value at the time of operation with the electro recovery method should always be less than 2.0. In the hybrid membrane-electro recovery system of the present invention (1), pH meter (3) and conductivity meter (4) are installed in order to control the acidity and conductivity of the wastewater in the wastewater feed tank (2). The level sensor (5) mounted on the wastewater feed tank (2) both controls the level of the water level in the wastewater feed tank (2) and protects the pump (7) from being dehydrated. The pump (7) should preferably be a high pressure pump capable of providing a pressure of at least 15 bar. The level sensor (5) may preferably be the lower level sensor. In the hybrid membrane electro-recovery system (1), which is the subject of the invention, the water in the wastewater supply tank (2) is pumped to the membrane module (10) by means of a pump (7). Before the pump (7), the pressure of the pump (7) can be adjusted with the valve (6) placed on the main pipeline connected to the wastewater feed tank (2). In addition, pressure and flow rate can be displayed via the control system (20) with a manometer (8) and flow meter (9) after the pump (7). There is a manometer (8) on the main pipe coming out of the wastewater supply tank (2). The main pipe represents the piping line between the wastewater supply tank (2) and the membrane module (10). The main pipe may preferably be made of plastic, PVC or stainless steel (316L, 304L). There is a control unit (20) adapted to operate the hybrid membrane electro-recovery system (1) and the pump (7). There is at least one computer for collecting and evaluating the data sent to the control unit (20). The pressure sensor (8) transmits data about the inlet pressure values of the wastewater entering the membrane module (10) on the main pipe to the control unit (20). At least one flow sensor (9) is connected to the main pipe and the flow sensor (9) transmits data about the flow values of the wastewater entering the membrane module (10) to the control unit (20). In addition, there are flow sensors (9) at the output of the membrane module (10), which transmit data about output conductivity and output flow values to the control unit (20). Considering the safety of the system due to the high working pressure and internal osmotic pressure of the wastewater, the membrane module (10) sheath was chosen to be resistant to 1000 PSI (pound per square inch) pressure (Aqualine FRP pressure vessel 1000 PSI 2540). All piping lines (pipes) entering the membrane module (10) are made of stainless steel AISI 316L, since the operating pressure range can exceed 15 bar. The lines used in the hybrid membrane electro-recovery system (1) of the present invention, from the pressure pump (7) to the membrane module (10), must be stainless steel due to the extremely acidic corrosive property of the wastewater and high sulfate acid content post-pump treatment in high pressure environment (> 15 bar) will continue, so the main line with the liquid flow should be stainless steel pipe instead of the plastic pipe, otherwise the plastic pipe cannot withstand this pressure. The main pipe where there is no pressure medium and other liquid flow can be made of plastic orpvc material. The membrane module (10) has two output lines, the filtrate line (11) output and the feedback line (13). Mentioned permeate line (11) exits to a permeate tank (12) with the help of a pipeline. The feedback line (13) (concentrated line), which is another output line coming out of the membrane module (10), is also connected as a feedback (concentrated line) (13) with the help of a pipeline. By connecting a bidirectional valve (14) to the end of the feedback line (13), the concentrated wastewater in the feedback line (13) can be fed directly to the electrolysis unit (16) with the help of the electrodeposition line (15) if desired. In cases where the feedback needs to be continued, the water in the feedback line (13) coming out of the membrane module (10) is returned to the waste water supply tank (2) with the help of the bidirectional valve (14). Returning the water in the feedback line (13) coming out of the membrane module (10) back to the wastewater feed tank (2) with the help of a two-way valve (14), it continues as a cycle until it reaches a recovery rate of at least 70%. In case the target concentration is reached, the electrolysis unit (16), which is the second part of the hybrid membrane electro-recovery system (1), is activated by the the two-way valve (14) and the electrodeposition line (15) connection. Concentrated wastewater in the feedback line (13), which is brought to the electrolysis unit (16) with the help of a feed line (15), is taken to the electrolysis cell (16). The power required to operate the cell is supplied from a DC power supply (17) connected to the cell. There is anode (18) and cathode (19) plates placed in the cell. A minimum distance of 0.5 cm should be left between the anode (18) and the cathode (19) plates. The anode (18) must be selected from the appropriate material (gold, platinum, platinized titanium). First of all, the electrochemical behavior of the anode material is determined for the metal to be recovered. According to the results obtained, the limit current-voltage values are determined. At these values, an inert material is determined. The anode plate must be made of this material so that an oxidation reaction does not occur at the anode at the applied current-voltage values (0.70 – 0.90 volts, 0.1-1.0 ampers). The cathode material (gold, platinum, platinized titanium, titanium, nickel, stainless steel) is also determined using similar techniques. Platinum and/or platinum anode plates (18) and cathode plates (19) made of titanium are used in the hybrid membrane electro- recovery system (1). One of the important aspects of the invention is the anode and cathode materials. At least one pH meter (3) and at least one conductivity meter (4) mounted in the electrolysis unit (16) are placed. In the electrolysis process, the electro-recovery, that is, the operating time, is decided by periodically taking samples from the electrolysis cell (16) and monitoring the metal concentration with the ICP (Inductively coupled plasma spectrometer) device. When the metal concentration in the electrolysis cell (16) reaches below the desired limit values (for example, <30 µl/l), the DC power supply (17) is turned off and the electrolysis process is completed. Then, the anode (18) and cathode (19) plates are carefully removed and subjected to drying. When sufficient drying (at least 12 hours and 120 °C) is achieved, the electrodes are kept in a cabinet (such as a vacuum desiccator) to cool down in a cabinet isolated from moisture and external environment. The weight losses and gains in the electrodes whose cooling process is completed are determined. The metallic coating accumulated on the surface from the cathode plates (19) is peeled off with the help of a thin brush and/or with the help of a dilute acidic solution (5-10% sulfuric acid). The metallic powder is then washed with pure water, hot water and a dilute acid to remove unwanted salts and metals. The powder after drying is subjected to a grinding process. With the help of the mass difference between the initial metal concentration and the obtained metal powder, the efficiency of the hybrid membrane electro recovery system (1) is calculated. The operating method of the hybrid membrane electro-recovery system in the present invention comprises process steps; a) Entering the control unit (20) with the system control software on the 10-30 hertz frequency panel with a pressure value of 4-15 bar, b) The control unit (20) operates the pump (7) in line with the entered pressure- frequency values of 4-15 bar and 10-30 hertz, c) The system control software on the computer processes the data it receives from the pH meter (3), conductivity meter/probe (4) and flow/flow measuring sensor (9) connected to the main pipe, located in the wastewater feeding tank (2), d) With the activation of the pump (7), the fluid in the main pipe (wastewater) moves and the pressure and velocity and flow rate data change in the flow line (main pipe), e) Transmitting the mentioned changing data from the pH meter (3), conductivity meter (4) and the flow/flow measuring sensor (9) to the computer via the control unit (20), f) Processing the data transmitted to the computer by the computer and recording the data in the form of waste pressure, waste flow, raw water conductivity, product water conductivity, product water flow and high pressure pump pressure determined by the user, g) If the values (m ³ /h or l/h) are within the target range determined by the user (although it varies according to the wastewater characteristics, it is generally ideal in the range of 0.1-0.3 m ³ /h); operation of the hybrid membrane electro- recovery system (1) at the same pressure (hertz) setting, h) If the values (m ³ /h or l/h) are not within the target range determined by the user (although it varies according to the wastewater characteristics, it is generally ideal in the range of 0.1-0.3 m ³ /h); operation of the membrane module (10) system by changing the target range (pressure (hertz)) via the control unit (20) or the pump (7) or by moving the valve (6), i) Activating the electrolysis unit (16) with the double-acting valve (14) and the electrodeposition line (15) connection, in case a recovery rate of at least 70% is achieved, j) Operating the electrolysis unit (16) in accordance with the input of the desired values to the DC power source (17), k) If the values (cathodic reduction ratio) are within the target range (100 mg Rh/hr deposit); operation of the electrolysis unit (16) at the same current-voltage setting, l) If the values (cathodic reduction ratio) are not within the desired range; Operating the electro recovery system (1) by changing the current and voltage value ranges over the DC power supply (17) The user transmits the pressure-frequency values on the panel to the control unit (20) on the system control software, in which the hybrid membrane electro-recovery system (1) is used. The control unit (20) operates the pump (7) in accordance with the desired values. The system control software on the computer activates the pressure pump (7) located on the wastewater main pipe according to the desired values. By activating the pressure pump (7), the fluid wastewater moves and the pressure, flow and conductivity values in the main pipe change. The data related to the desired values are transmitted to the computer via the control unit (20). The transmitted values are controlled by the computer and if they are within the value range specified by the user, the hybrid membrane electro recovery system (1) operates at this specified setting. Data is transmitted to the control unit (20) every 1 second from the conductivity meter (4), the pressure sensor (8) and the flow rate sensor (9), and the data is recorded by computer processing and also outputs graphically. The present invention is also described in more detail and specifically with an example. The claims cannot be construed as being limited to the examples given in this specification to narrow the scope of the invention. Application Example Experimental studies related to the present invention were carried out with the hybrid membrane electro-recovery system (1) in two stages. In the first stage, the metal content enrichment of the wastewater by membrane filtration (A) and in the second stage the metal recovery from the concentrated electrolyte water on the cathode surface by electrodeposition technique (A,B,C). A. Pilot System Enrichment Studies The enrichment studies were carried out using a 25x40 spiral wound NF90 membrane. At pH greater than 3.2, rhodium in the rhodium sulfate complex precipitates as rhodiumhydroxyl. As a result, the pH value of waste bath water should be 2.0 throughout the membrane enrichment process. Enrichment studies were carried out using waste rhodium baths and NF90 type polymeric membrane in the pilot system. Wastewater inlet to the membrane module (10) is between 15-20 L, and the filtrate returns for 0.1 m ³ /h, 0.2 m ³ /h and 0.3 m ³ /h are 56%, 47% and 55%, respectively. Concentrate recovery is 44%, 53% and 45% for 0.1 m ³ /h, 0.2 m ³ /h and 0.3 m ³ /h, respectively. Table 1. Operating conditions of pilot scale-I with NF-90 (Input rhodium concentration values A: 70.78 mg/L, B: 548.9 mg/L, C: 606.9 mg/L, inlet pH:2.0, Input conductivity values A: 62.5 mS/cm , B:51.9 mS/cm, C: 93.5 mS/cm), HPP: High pressure pump (7) All studies in Table 1 were carried out at pH 2.0, the minimum working pH of the NF polymeric membrane. All 3 studies (A,B,C) were conducted using 20 L of wastewater. In the pilot system, the residual wastewater volume in the high pressure pump (7), all the piping lines and the membrane module (10) is 10 L on average. Therefore, the return (% Recovery) in studies numbered A, B, and C was between 47% and 56%. In case of working with 50 or 100 L capacity, the return (% Recovery) can be increased to very high levels depending on conductivity, internal osmotic pressure and pollution on the membrane surface. In this case, it will provide highly concentrated enrichment, especially in medium-concentration wastewater (400 - 800 mg/L Rh ³⁺ -containing wastewater) and high-concentration wastewater (>800 mg/L Rh ³⁺ -containing wastewater) at 70-80% return rates. Table 2. Operating conditions of pilot scale-II with NF-90 (Input rhodium concentration values D: 256.5 mg/L, E: 589.9 mg/L, F: 862.7 mg/L, inlet pH:2.0, Input conductivity values D: 36.0 mS/cm , E:41.3 mS/cm, F: 72.1 mS/cm), HPP: High pressure pump In all studies (D, E, F) in Table 2, the pH of the wastewater is approximately 2.0. In studies D, E, and F, the recovery (% Recovery) ranged between 34% and 48%. B. Electrochemical reduction(electrodeposition) study of rhodium at the cathode Electrowinning studies were carried out using different anode-cathode electrode pairs. The most important parameter to be effective in electrowinning is the applied current and the electrolysis time. Studies Carried Out with Platinum and Gold (Pt-Au) Anode-Cathode Pairs Gold (Au) plate electrodes were used as cathode, and platinum (Pt) plate electrodes were used as anode in electrowinning studies. As the distance between the anode and the cathode increases (d) (Table 3), the electrolytic deposition efficiency of rhodium decreases. During the 48-hour electrolysis period, the residual rhodium concentration in the wastewater at d = 0,5 cm is 38,17 mg/L, while the rhodium concentration at d = 2 cm is 83,15 mg/L. It is seen from Table 3 that as the electrolysis time increases, the rhodium electrolytic recovery efficiency also increases. Another important issue is current efficiency. The current efficiency is calculated from the ratio of experimental and theoretical amounts of rhodium associated with electrowinning. This ratio is not very dependent on d. It is seen that the current efficiency (%) varies between 4,2-16,7 and has the highest value at d = 1 cm (Table 3a). It is mentioned in the literature that the current efficiency is at the level of 60-80% even in real sulfate-based rhodium baths. Table 3b shows the rhodium deposited on the cathode surface and the energy consumed for the Pt-Au (platinum-gold) anode-cathode pair. Table 3 (a) Results obtained for the Pt-Au anode-cathode pair Note: C0: inlet rhodium concentration (mg/L), Ct: rhodium concentration (mg/L) at time t, Re: rhodium recovery efficiency (%), :final pH Table 3 (b). Results obtained for Pt-Au anode-cathode pair Note: : experimental amount, : theoretical amount, : anode change amount, : current efficiency, : energy consumption amount According to the results obtained, the obtained powder composition is 14,13% O (Oxygen), 1,68% Fe (Iron), 70,69% Rh (Rhodium), 6,99% Na (Sodium), 19,76% S. (Sulphur), 2,7% P (Phosphorus), and 1,01% Al (aluminum). It is observed that the metals deposited on the Au cathode surface are oxidized due to contact with air. Studies with Gold-Titanium (Au-Ti) Anode-Cathode Pairs Two electrode pairs, a gold plate anode, and a titanium plate cathode, were used in the electrowinning studies (Tables 4a and 4b). The cathode electrode titanium plate was weighed before each experiment, and it was dried in an oven and weighed again after each experiment, then washed with distilled water, placed in the oven for drying and used for the next experiment. Table 4 (a). Results obtained for Au-Ti anode-cathode pair Note: C0: inlet rhodium concentration (mg/L), Ct: rhodium concentration (mg/L) at time t, Re: rhodium recovery efficiency (%), :final pH Table 4 (b). Results obtained for Au-Ti anode-cathode pair Note: : experimental amount, : theoretical amount, : anode change amount, : current efficiency, : energy consumption amount Studies with Platinum and Titanium (Pt-Ti) Anode-Cathode Pairs Two electrode pairs, a platinum plate anode, and a titanium plate cathode, were used in the electrowinning studies. The cathode electrode titanium plate was weighed before each experiment, and after each experiment, it was dried in an oven and weighed again, then washed with distilled water, placed in the oven for drying and used for the next experiment. The experimental amount was calculated by weighing the metallic rhodium stripped from the cathode surface and given in Table 5 (a-b). Table 5 (a). Results obtained for the Pt-Ti anode-cathode pair Note: C0: inlet rhodium concentration (mg/L), Ct: rhodium concentration (mg/L) at time t, Re: rhodium recovery efficiency (%), :final pH. Table 5 (b). Results obtained for the Pt-Ti anode-cathode pair Note: : experimental amount, : theoretical amount, : anode change amount, : current efficiency, energy consumption amount C. Electrodeposition studies under high current Studies with Platinum and Titanium (Pt-Ti) anode-cathode Pairs Two electrode pairs, a platinum plate anode, and a titanium plate cathode, were used in the electrowinning studies. The cathode electrode titanium plate was weighed before each experiment, and after each experiment, it was dried in an oven and weighed again, then washed with distilled water, placed in the oven for drying and used for the next experiment. The experimental amount was calculated by weighing the metallic rhodium stripped from the cathode surface and given in Table 6 (a-b). To drive a reaction in a non-spontaneous direction, a voltage that is at least as large as the generated voltage must be applied. For example, the standard reduction potential of rhodium is +0,758 volts, as given in Reaction 1. In the recovery of rhodium from the wastewater system by electro-deposition method, a voltage of at least 0,758 volts should be applied so that the Rh ³⁺ ions in the system can migrate to the cathodic region with the driving force and be reduced to metallic rhodium on the cathode surface. The value of 0,758 volts given in reaction 1 is a measured value against the standard hydrogen electrode. Of course, this value may deviate in real wastewater systems. Another important point is overvoltage (limiting current). Applying an excessive voltage can cause ion migration from the anodic material as well as ion migration. ) (1) ) (2) In Pt anode studies at 0.05 and 0.1 A, gold (Au) in the effluent wastewater was found (Table 6). The average reduction voltage in electro-deposition studies is 2,0, 2,81 and 2,40 Volts for 0,01, 0,05 and 0,1 A, respectively. It was calculated experimentally that the anode material decreased in mass in the studies of 0,05 and 0,1 A above 0,01 A. The limiting current value in Pt-Au, Pt-Graphite and Pt-Ti anode-cathode pairs is above 0,01 Amps. In low current 0,01 A operations, the average voltage for Pt-Graphite is 2,4 V, and the average voltage for Pt-Ti is 2,1 Volts. Table 6. Results obtained at different electrolysis times and currents In the recovery of rhodium from the wastewater system by electrodeposition method, a voltage of at least 0.758 volts should be applied (driving force) so that the Rh ³⁺ ions in the system can migrate to the cathodic region and be reduced to metallic rhodium on the cathode surface. 0,758 is a measured value against a standard hydrogen electrode. Of course, this value may deviate in real wastewater systems. Another important point is overvoltage (limiting current). Applying an excessive voltage can cause ion migration from the anodic material as well as ion migration. In the studies, where we used platinum as the anode, it was seen that the anode material did not change in mass in the studies of 0,05 and 0,1 A above 0,01 A. It was determined that the limiting current value in Pt-Au, Pt-Graphite and Pt-Ti anode-cathode pairs was above 0,01 amperes, and its average potential was above 2.3 volts compared to the theoretical value (Tables 7a and 7b). Table 7 (a). Results obtained for the Pt-Ti anode-cathode pair Note: C0: inlet rhodium concentration (mg/L), Ct: rhodium concentration (mg/L) at time t, Re: rhodium recovery efficiency (%), :final pH Table 7 (b). Results obtained for the Pt-Ti anode-cathode pair Note: : experimental amount, : theoretical amount, : anode change amount, : current efficiency, energy consumption amount Studies with Gold and Titanium (Au-Ti) Electrode Pairs Two electrode pairs, a gold plate anode, and a titanium plate cathode, were used in the electrowinning studies. The cathode electrode titanium plate was weighed before each experiment, and after each experiment, it was dried in an oven and weighed again, then washed with distilled water, placed in the oven for drying and used for the next experiment. The experimental amount was calculated by weighing the metallic rhodium stripped from the cathode surface and given in Table 8 (a-b). In Au anode studies at 0,05 A and 0,1 A, gold was found in the effluent. The average reduction voltage in electro-deposition studies is 2,35, 2,13, 2,40 and 2,67 Volts for 0,02, 0,03, 0,05 and 0,1 A, respectively. It was calculated experimentally that the anode material decreased in mass at 0,03, 0,05 and 0,1 A studies over 0,02 A. The limiting current value in Au-Cu, Au-Pt- Au-Ti anode-cathode pairs is 0,01 Amps. The average voltage for Au-Cu is 1,98 V, and the average voltage for Au-Ti is 2,1 V. ) (3) Table 8. Results obtained with Au-Ti anode pair at different electrolysis times and currents However, as seen in the reduction-oxidation equation of gold, Reaction 3, the value is 1,498 volts. This theoretical voltage value is 2.4 V in practice. Anodic gold tends to dissolve when the limiting voltage exceeds <2.4 V. Because every potential is measured against a standard Hydrogen electrode. The fact that the real systems do not fully correspond to the theoretical values is due to the fact that the waste bath/wastewater system is not limited to an ion. Real systems contain many cation and anion groups, especially in the case of industrial waste bath/wastewater systems. This causes each metal to deviate from the reduction-oxidation potential it shows against the hydrogen electrode. Table 9 (a). Results obtained for Au-Ti anode-cathode pair Note: C0: inlet rhodium concentration (mg/L), Ct: rhodium concentration (mg/L) at time t, Re: rhodium recovery efficiency (%), :final pH. Table 9 (b). Results obtained for Au-Ti anode-cathode pair Note: : experimental amount, : theoretical amount, : anode change amount, : current efficiency, energy consumption amount. In studies where gold is used as an anode, the limit current value of 0,01 amperes has been determined. The data in Table 9 showed that gold undergoes anodic dissolution in all studies of 0,02 Amps and above. In EDX (Scanning Electron Microscopy) analyzes, a decrease was observed in the weight recovery of rhodium deposited on the cathode surface by 55,84%, 22,06% and 16,39%, respectively, with an increasing current value of 0,01, 0,02 and 0,05 amperes. In Table 10, EDAX-EDS analysis results of the metallic powder accumulated at the cathode from electrochemically enriched concentrated baths, when different anode and cathode pairs and different currents are used, are given. Table 10. EDS analyzes of all electrochemical rhodium recovery studies When the EDS (Energy Distribution Spectroscopy) analysis results of the powders accumulated on the cathode in Table 10 are examined, the highest rhodium recovery was obtained at the values of gold anode-Pt cathode 0.1 ampere and Pt anode-Ti cathode 0,001-0,05-0,1A, respectively. However, it is more advantageous to use platinum as an anode instead of gold in electro recovery/deposition studies. Because, as seen in experimental studies, the limiting current value of platinum is higher than gold. This gives the opportunity to work at higher voltage values. It can be seen from the results of Au-Ti anode pair studies in Table 9 that gold dissolves cathodic when operating at 0,1 Amperes in Pt anode and gold cathode pairs. Industrial Applicability of the Invention Rhodium plating solutions are formulated for the jewelry industry and used in baths suitable for the products to be coated. After a certain lifetime, the ion concentration of rhodium in the plating baths decreases. This affects the brightness, homogeneity, and thickness quality on the products. As a result, the bathroom has become a waste and must be replaced with a new one. Therefore, raw material and economic losses are experienced with the discharge of industrial wastewater containing precious metals. The economical and environmentally friendly recovery of rhodium from the jewelry industry's waste rhodium plating baths has become a necessity for the country's economy. Gases and waste acid solutions released in acidic dissolution processes of rhodium by hydrometallurgical method are highly toxic and corrosive. The method of the present invention offers the enrichment of rhodium from waste sources by membrane filtration without exposure to acidic treatments, followed by electrochemical recovery. In addition, the present invention has an environmentally friendly approach over the present conventional method. It does not create a secondary pollutant. The invention can be applied to industry both in terms of its technological level and in terms of material supply. The hybrid membrane electro-recovery system (1) is designed to allow two different characteristics/types of recovery. In the first stage, low-concentration water taken from the wastewater supply tank (2) can be enriched with the desired metal by membrane filtration until it reaches the desired concentration value. Thus, an enriched rhodium plating solution is obtained. Under certain conditions, this enriched solution may be considered in the industry as a recycled coating product. The present invention is applicable in the treatment of baths containing acidic and corrosive solutions.