Membrane filtration treatment device, system and process for commercial and industrial textile care application

Abstract

Membrane filtration treatment device comprising ceramic membrane modules. The modules comprise 220 to 1500 individual ceramic hollow fibres made from aluminium oxide (Al2O3). The fibres may have an in

Description

Technical Field Described embodiments relate generally to a fluid treatment device. Particular embodiments relate to a commercial and industrial laundry effluent treatment skid mounted device, including process components such as sensors, metering and control software. Thus processing effluent from such application for the purpose of reuse as clean water. The removal of contaminants both organic and inorganic, including specific functionally and design is the key feature of this invention. This invention is uniquely designed to incorporate individual hollow fiber ceramic membranes, bundled together by epoxy, ceramic or glass endcaps to form a membrane module. Summary The embodiments relate to an effluent treatment skid mounted device including a unique process design and skid configuration, being a skid system requiring only three fluid pump units to undertake methods or process as described below, including individual or multiple membrane modules in a stacked configuration, either vertical or horizontal forming a column. a hollow fiber ceramic membrane module; which includes multiple hollow fibres bundled together by ceramic, epoxy of glass material end caps to form a complete membrane module. Additionally, a complete hollow fiber membrane module, comprises of multiple nominal 2.0 to 4.00 millimetres inside diameter symmetric individual hollow fibres, made of aluminium oxide (AI2O3) substrate material. The geometry of the individual ceramic hollow fiber walls also being nominal 1.00 to 2 millimetres in thickness, known as the membrane wall. Such ceramic hollow fibres shall comprise of selective membranes pores including a range of nominal 1 nanometre to 1400 nanometres. Additionally, the ceramic hollow fibres shall comprise of selective membranes pores including a range of nominal 1 nanometre to 1400 nanometres which may include individual or multiple separating layers attached to the fiber walls of nominal 1 to 100 nanometres. and a skid mounted effluent treatment device, operable to pass water through an individual hollow fiber ceramic membrane module or multiple membrane modules in series known as a membrane loop, via a process known as inside to out flow filtration. The device is also operable to pass water through the hollow fiber ceramic filter module or multiple membrane modules in an outside to in flow direction, so as to remove material from the separation layer of the hollow fiber ceramic membrane fibres, a process known as backwashing or back flushing, whereby contaminant materials having been deposited during inside-out filtration of the commercial &industrial laundry effluent is removed. Such embodiments allow for the provision of a maintenance regime for the hollow fiber ceramic filter membrane modules such as membrane cleaning which can be built-in the control logic, and particularly suited for implementation in the commercial and industrial commercial laundry application. The process device may include a heater or steam injector and diffuser, operable to heat effluent to pass through the hollow fiber ceramic membrane module or membrane modules in series, including the skid mounted effluent treatment device. This aspect provides a controlled and improved flux and yield of recycled water known as permeate and synergistically improved flux longevity and maintenance of the hollow fiber ceramic membrane modules, which provides further improvements in yield and throughput. The device may include a program logic controller or software operable to control the flow device to pass effluent through the hollow fiber ceramic membrane modules according to a determined operating schedule. The controller may be operable to collect and read data defining a maintenance schedule for the skid mounted effluent treatment device. The device includes a forward-flow function, operable to provide the inside to out filtration process through the hollow fiber ceramic membrane wall. The device includes a left and right flow function, operable to provide effluent feed to either the left or right membrane module loop. The device may include a reverse-flow function operable to provide the outside to in process through the hollow fiber ceramic membrane wall, known as backwashing or back flushing The device may include a membrane cleaning program operable to provide periodical chemical cleaning as required, known as membrane clean-in-place The device may include an ancillary permeate or back wash tank operable to receive permeate water from the device to provide water to the reverse-flow process. The device may include an inlet conduit operable to receive commercial or industrial laundry effluent to be filtered by passing through the hollow fiber ceramic membrane modules in a forward direction. The device may include a fluid flushing process via an actuated controlled valve using program logic, at the inlet conduit operable to receive city water and commercial or industrial laundry effluent to be filtered by passing through the hollow fiber ceramic membrane module in a forward direction. The device may include an inlet conduit operable to receive commercial or industrial laundry recycled fluid known as permeate, in addition to a water supply derived from local city sources, to be passed through the hollow fiber ceramic membrane module in a reverse direction, known as backwashing or back flushing The device may include an actuated valve, operated by logic, controlling the volume of permeate flow, from the membrane module conduit. The device may include hollow fiber membrane modules to operate individually or in series, stacked in multiple creating one vertical column. The device may include hollow fiber membrane modules to operate individually or in series, stacked in multiple creating one horizontal column. The stacking of the membrane modules consisting of multiple hollow fiber membrane provides a compact configuration and high filtration surface area which may reduce overall device footprint. The device may include conduits connected to the membrane module or multiple modules in series to channel effluent or fluid into the membrane module or multiple modules in series alternatively, suitably known within the effluent treatment skid mounted device as conduits right and left. The device may include a conduit connected to the membrane module or multiple modules in series to evenly channel effluent or fluid known as retentate within the effluent treatment skid mounted device. The device may include a hollow fiber ceramic membrane module; which holds multiple hollow fibres bundled together by ceramic material or epoxy material end caps to form a complete membrane module. Additionally, a complete hollow fiber membrane module, comprises of multiple nominal 2.0 to 4.0 millimetres inside diameter symmetric individual hollow fibres, made of aluminium oxide (AhOs) substrate material. The geometry of the individual ceramic hollow fiber walls also being nominal 1 to 2 millimetres in thickness, known as the membrane wall. Such ceramic hollow fibres shall comprise of selective membranes pores including a range of nominal 1 nanometre to 1400 nanometres. The device may include a hollow fiber membrane module; which includes nominal 220 to 1500 individual ceramic hollow fibres made of aluminium oxide (AI2O3) substrate material; the fiber geometry being nominal 2 to 4 millimetres inside diameter, 4.00 to 6.00 millimetres outside diameter, effective nominal length 360 to 1000 millimetres, bundled together with either epoxy, ceramics or glass end caps to provide excellent thermal stability and a wide range of pH stability and the ability to operate at high operating temperature of 40 to 80 degrees centigrade. The device may include individual or multiple hollow fiber membrane modules; which includes nominal 220 to 1500 individual ceramic hollow fibres made of aluminium oxide (AI2O3) substrate material; as stated above; including but not limited to selective pore sizes of the aluminium oxide substrate material (AbO3) being nominal 50 to 1400 nanometres, also but not limited to selective pore sizes of the aluminium oxide substrate material (AI2O3) being nominal 50 to 1400 nanometres, including nominal 1 to 100 nanometres ceramic or polymeric coating or multiple separate ceramic polymeric coatings, acting as a separating layer attached to the membrane fiber wall. Advantageously, the compact hollow fiber membrane module with selective membrane pores including a range of 1 to 1400 nanometres to separate undesirable matters in the industrial commercial laundry effluent such as and not limited to fine suspended particulates, microbes, bacteria, colouring matter and dissolved solids and producing clean permeate for reuse in the laundering process. Some embodiments relate to a water treatment device comprising: a hollow fiber ceramic membrane module operable to filter effluent passed through the hollow fiber ceramic membrane module; and a heater or steam injector and diffuser operable to heat fluid to be filtered by the hollow fiber ceramic membrane module. The device of any of the above paragraphs may include a heater or steam injector and diffuser operable to heat effluent to be passed through the hollow fiber ceramic membrane module in a forward direction. The heater may be operable to heat the effluent to 40 degrees centigrade or more. The heater may be operable to heat the water to about 50 degrees centigrade or more. The heater may be operable to heat the effluent to within a temperature range of 50 to 80 degrees centigrade. The device may include a feed pump, referred to as the feed pump, a circulation pump, referred to as circulation pump and backwash pump, referred to as a backwash pump. The device of any of the above paragraphs may include a preliminary filter to filter effluent prior to it being passed through the hollow fiber ceramic membrane module and device, such as a drum filter or vibrating screen, to remove organic or inorganic material such as lint or fibres. The device of any of the above paragraphs may include multiple actuated solenoid valves, operable by program logic control. The device of any of the above paragraphs may include a pH adjustment device operable to adjust the pH level of permeate water from the device and operable by the program logic control. The device of any of the above paragraphs may include a conductivity measuring and adjustment device, operable to adjust the analyse and control the level of conductivity in the permeate water from the device and operable by the program logic control with set-points correlated to the effluent quality. The device of any of the above paragraphs may include a turbidity measuring, operable to analyse the level of turbidity in the permeate water from the device. Some embodiments relate to a method, processing industrial or commercial laundry effluent including: The commercial and industrial laundry effluent treatment skid mounted device, may include a feed pump, referred to as the feed pump and circulation pump, referred to as circulation pump. The method may comprise of pumping fluid either clean or contaminated in a controlled manner by way of program logic into the inlet conduit of the skid mounted. Pumping commercial or industrial effluent, firstly in a forward direction into a stainless steel conduit [Conduit right], being a nominal diameter of nominal 100 to 250 millimetres into the hollow fiber ceramic membrane module or modules in series, so as to enable the hollow fiber ceramic membrane surface through a phenomena known as “cross-flow”, remove contaminants from the effluent, whilst forcing water know as permeate, through the fiber wall. The method may comprise or pumping effluent in a second forward direction, alternately, via program logic control, into a stainless steel conduit [Conduit left], being a nominal diameter of nominal 100 to 250 millimetres into the hollow fiber ceramic membrane module or modules in series, so as to enable the hollow fiber ceramic membrane surface through a phenomena known as “crossflow”, remove contaminants from the effluent, whilst forcing water know as permeate, through the fiber wall. The method of pumping through the inlets right and left may be carried out on an alternating cycles with a pre-determined filtration or backwash timing. The disclosed method of pumping and distributing the contaminated fluid to the inlet conduits right or left may substantially improve the separation efficiency through every membrane loops with optimised cross-flow rate and lower operating pressure possible. The method may comprise of pumping permeate water from a permeate storage tank into the inlet conduit, to conduits right and left, flushing the skid mounted effluent treatment device in a third direction with permeate water, controlled by program logic. The method may comprise of pumping permeate water from a permeate storage tank, into the backwash inlet conduit in a reverse direction, to conduits connected to the hollow fiber ceramic membrane module or modules in series, dislodging contaminants by way of back washing or flushing the hollow fiber ceramic membrane fibres or module or modules in series, lodged on the hollow fiber ceramic membrane surface, during pumping effluent either in the first or second forward directions. The method may comprise of a short backwash timing of nominal 5 to 60 seconds using permeate water with a tangential flow suited for the plurality of the membrane modules and thin membrane separating layer structure. As such, the disclosed method advantageously help to preserve the efficiency of the membrane separating layers of the hollow fiber ceramic membrane modules and increase its resistance to fouling. In turn preserving the service life of the membrane significantly and reducing the requirement for membrane chemical cleaning. Advantageously, the membrane filtration water treatment process may operate on continuous basis, therefore improving permeate recovery rate and minimizing the loss of thermal energy in the commercial laundry effluent. In turn, providing potential water and energy savings for the industrial commercial laundry application. The method may comprise of multiple actuated solenoid valves, operated by program logic control The method may include heating effluent to be forced in the first and second forward directions. Some embodiments relate to a process to treat commercial and industrial laundry effluent including: heating water to be treated to provide heated water; and forcing the heated water through a hollow fiber ceramic membrane module, or multiple modules in series known as membrane loop. Some embodiments relate to a process to treat water including: filtering water through a pre-filter such as a drum filter or vibrating screen device; and subsequently pumping the effluent through a hollow fiber ceramic membrane module Embodiments may involve any of the methods of paragraphs above applied to commercial or industrial effluent, so as to recycle or recover the encompassed water within the effluent. Some embodiments relate to a computer readable carrier medium, carrying computer executable code, the code operable when executed to configure a configurable device to control a water or effluent treatment device, to carry out the method of one of the paragraphs above. Some embodiments relate to a computer system including: a code memory operable to store processor executable code; a processor operable to execute code stored in the code memory; and a data memory operable to store data, a cloud-based system operable to collect and store data points from the programmable logic control or controls software from the effluent treatment device, wherein the code memory stores code, which when executed, causes the computer to control an effluent treatment device to perform the method of one of the paragraphs above or causes the computer to configure a configurable device to control an effluent treatment device to perform the method of one of the paragraphs above. Some embodiments use the computer system as part of a computer-controlled effluent treatment system configured to perform the functions described herein. Brief Description of the Drawings Figure 1 is a piping and instrumentation drawing of the commercial or industrial laundry effluent treatment system skid process, Figure 2 is a front perspective view of a commercial or industrial laundry effluent treatment recycling according to embodiments. Figure 3 is a rear perspective view of the commercial or industrial laundry effluent treatment recycling shown in figure 2. Detailed Description Described embodiments relate to methods, systems and processes for the commercial or industrial effluent treatment system and computer readable logic code or storage configured to control the performance of such methods, systems and processes. For example, embodiments may be used as part of small or large commercial or industrial water usage laundry process, such as for laundering laundry articles, where high throughput of water is required. Embodiments are not, however, limited to such use. The commercial and industrial laundry effluent treatment skid mounted device is described not-withstanding the functions of ancillary components as detailed in the drawing. Figure 1 Diagram - P&ID The diagram demonstrates the commercial or industrial laundry effluent treatment system process, operable by program logic control as described below. It is critical that the skid process is completely vented of air [Step 1], encapsulated within the commercial and industrial laundry effluent treatment skid. Trapped air within the associated skid conduits and membrane module or modules, combined with the introduction of fluid flow and pressure, will compromise the integrity and performance of the individual or bundled hollow fiber ceramic membrane fibres. As the commercial or industrial laundry effluent treatment system process, is designed and configured for such application, understanding the nature of the feed effluent containing an excessive volume of lint and fiber material, so as to not excessively plug or block the inlet of the hollow fiber membrane conduit with such lint or fiber material; the process by way executable program logic control intermittently alternates fluid [step 2] to the right hand side membrane loop conduit, then [step 4] to the left hand side membrane loop conduit. Relative the steps as stated below, unless otherwise, it is assumed the commercial or industrial laundry effluent treatment device is in “standby mode” being all method or process components are deactivated to either closed or off. So to alleviate the operable risk as stated above relative to ceramic hollow fiber membrane damage, an air venting process [Stepl] is included; Step 1: Device venting of air Program logic activates valves AV 3.2, AV 3.3, AV 3.4, AV 3.5, AV 3.6, AV 3.8 and AV 3.10 to open position. AV 3.3 enables city water and commercial or industrial laundry effluent to be drawn into the system by way of the encompassed feed pump P 3.1 for a nominal time period of 60-180 seconds. At the end of this time period, feed pump P 3.1 stops, once stopped program logic de-activates valves AV 3.2, AV 3.3, AV 3.4, AV 3.5, AV 3.6, AV 3.8 and AV 3.10 to close position. The commercial and industrial laundry effluent treatment skid mounted device is now free of encapsulated air. As described in the embodiment related to a method, processing industrial or commercial laundry effluent, the commercial and industrial laundry effluent treatment skid mounted device is designed and capable of processing commercial and industrial laundry effluent, for the purpose of reuse known as recycling, through a specific process known as filtration. The key functionality of the filtration and backwash process prescribed below is performed through program logic executable code, relative to the unique design and configuration of the pumps, valves, modules and associated conduits. The innovative know-how detailed in this invention is through enabling and deactivating specific components in a specific order or process, relative to the unique design and configuration of the components including pumps, valves, modules and associated conduits. The filtration and backwash process consists of alternating cycles of filtration and backwash via the right or left hand side conduits as described in Steps 2 to 5. Step 2: Filtration - Conduit, Right hand side The process includes heating effluent held in a storage tank, as indicated T3, feed tank, by way of an actuated control valve, heater or steam injector including diffuser, as indicated by component AV 3.14. This method may be operable may to heat the effluent to 40 degrees centigrade or more. The heater may be operable to heat the water to about 50 degrees centigrade or more. The heater may be operable to heat the effluent to within a temperature range of 50 to 80 degrees centigrade. The heater may be operable to heat the effluent to an optimum of 60 degrees centigrade. The method described above provides a controlled and improved flux and yield of recycled water known as permeate and synergistically improved flux longevity and maintenance of the hollow fiber ceramic membrane modules, which provides further improvements in yield and throughput. Once effluent is at nominal temperature, program logic executable code activates components AV 3.2, AV 3.3, AV 3.6, AV 3.7 and AV 3.10 to open, then feed pump P 3.1 is enabled to nominal set point of 1-10 bar, pumping fluid into the inlet conduit of the device to the right hand circulation loop conduit, including membrane modules either individual or stacked to forming a vertical or horizontal column generating the internal operating pressure, in addition to supplementing fluid lost during the method by way of permeate and retentate. After nominal 10-30 seconds at set point, circulation pump P 3.2 is enabled to flow set point 50-500m3 / hr, generating flow and velocity of nominal 2 meters per second to 8 meters per second, within the circulation loop conduit feeding the hollow fiber ceramic membrane modules. During this method, the phenomena known as “crossflow” occurs, separating contaminated effluent channelled to both the retentate conduit and clean fluid conduit known as permeate to the permeate to clean tank, being the encompassed method known as filtration. The above filtration method shall operate for a time period of nominal 5 or more minutes than stop. Once Step 2 is complete, the program logic executable code enables step 3 of the process as referred to the embodiment related to a method, processing industrial or commercial laundry effluent, back washing or back flushing. Step 3: Backwash and / or Backflush, Left hand side The commercial or industrial laundry effluent treatment system process, activated by program logic control executable code, enables a unique method of backwashing or back flushing the hollow fiber ceramic membrane using a backwash pump P3.3 and circulation pump P 3.2. Step 3 method requires feed pump P3.1 and circulation pump P 3.2. to ramp down to minimum run speed. Then deactivate AV3.7 and AV 3.9 to close position, simultaneously activate AV 3.10, AV 3.11 and AV 3.12 to open position. Then activate backwash pump P 3.3 to frequency setpoint 0-100% and circulation pump P 3.2 to run at lower frequency of 1 to 2 m / s. This method channelling clean fluid being permeate or city water into the hollow fiber ceramic membrane module and subsequent ceramic fiber wall in a reverse direction of outside to in filtration referred to as back washing or back flushing. The nominal cycle time of the above mentioned method shall be scheduled by the program logic executable code, nominal every 5 to 120 minutes including a nominal process duration time of 10 to 60 seconds. Once step 3 process time complete program logic executable code deactivates valve components AV 3.2, AV 3.4, AV 3.11 and AV 3.12 to close position, backwash pump P 3.3 to stop, then enables step 4. Step 4: Filtration - Conduit, Left hand side Assuming effluent is at nominal temperature as stated above in step 2, program logic executable code activates components AV 3.4, AV 3.5, AV 3.7 and AV 3.10 to open, then feed pump P 3.1 is enabled to nominal set point of nominal 1 to 10 bar, pumping fluid into the inlet conduit of the device to the left hand circulation loop conduit, including membrane modules either individual or stacked to forming a vertical or horizontal column generating the internal operating pressure, in addition to supplementing fluid lost during the method by way of permeate and retentate. After nominal 10 to 30 seconds at set point, circulation pump P 3.2 is enabled to flow nominal set point 5-500m3 / hr, generating flow and velocity of nominal 2 meters per second to 8 meters per second, within the circulation loop conduit feeding the hollow fiber ceramic membrane modules. During this method, the phenomena known as “crossflow” occurs, separating contaminated effluent channelled to both the retentate conduit and clean fluid conduit known as permeate to the permeate to clean tank, being the encompassed method known as filtration. The above filtration method shall operate for a time period of nominal 5 or more minutes than process or method stops. Step 5: Backwash and / or Backflush - Conduit, Left hand side The commercial or industrial laundry effluent treatment system process, activated by program logic control executable code, enables a unique method of backwashing or back flushing the hollow fiber ceramic membrane using a backwash pump P3.3 and circulation pump P 3.2. Step 5 method requires feed pump P3.1 and circulation pump P 3.2. to ramp down to minimum run speed. Then deactivate AV3.7 and AV 3.9 to close position, simultaneously activate AV 3.10, AV 3.11 and AV 3.12 to open position. Then activate backwash pump P 3.3 to frequency setpoint 0-100% and circulation pump P 3.2 to run at lower frequency of 1 to 2 m / s. This method channelling clean fluid being permeate or city water into the hollow fiber ceramic membrane module and subsequent ceramic fiber wall in a reverse direction of outside to in filtration referred to as back washing or back flushing. The nominal cycle time of the above-mentioned method shall be scheduled by the program logic executable code, nominal every 5 to 120 minutes including a nominal process duration time of 10 to 60 seconds. Once step 5 process time complete program logic executable code deactivates valve components AV 3.5, AV 3.4, AV 3.11 and AV 3.12 to close position, backwash pump P.3.3 &circulation pump P 3.2 to stop. Once process is complete Step 1 is restarted. Step 6 - Flush Step 6 is an individual method or process from steps 1 to 4, as described in the embodiments related the systems and processes for the commercial or industrial effluent treatment system. This method or process shall include the external injection from the commercial or industrial effluent treatment device of city water or permeate into the feed tank, labelled T3. The method or process relation to flush, is operable by executable program logic control to remove any industrial laundry effluent from the commercial or industrial laundry effluent treatment system, being either individual or multiple hollow fiber membranes; which includes nominal 220 to 1500 individual ceramic hollowfibres made of aluminium oxide (AI2O3) substrate material; as stated above; including but not limited to selective pore sizes of the aluminium oxide substrate material (AI2O3) being nominal 50 to 1400 nanometres, also but not limited to selective pore sizes of the aluminium oxide substrate material (AI2O3) being nominal 50 to 1400 nanometres, including nominal 1 to 100 nanometres ceramic or polymeric coating or multiple separate ceramic or polymeric coatings, acting as a separation layer attached to the membrane fiber wall. The executable program logic control from “inactive” shall activate components AV 3.11 to open position, draining feed tank, labelled T3, of effluent or fluid for a nominal time period of 60 to 1200 seconds. Then deactivate AV 3.11 to close position. Then activate AV 3.13 to open position to activate city water fill of feed tank, labelled T3, of city water to nominal level setpoint of 40-90%. Then deactivate AV 3.13. Then activate AV 3.14 to open position to activate steam injection of feed tank, labelled T3, of steam to nominal temperature setpoint 40-80 degree centigrade. Then deactivate AV 3.14. Then activate AV 3.2, AV 3.9 and AV 3.12 to open position and activate feed pump P 3.1 to set point until nominal level setpoint of feed tank, labelled T3, is reached. Then activate AV 3.4 to open position and AV 3.2 is deactivated to close position to nominal level setpoint of feed tank, labelled T3, is reached. Then activate AV 3.11 to open position and AV 3.12 is deactivated to close position to nominal level setpoint of feed tank, labelled T3, is reached. Then activate AV 3.5 to open position and AV 3.4 is deactivated to close position to nominal level setpoint of feed tank, labelled T3, is reached. Then activate AV 3.6 to open position and AV 3.5 is deactivated to close position to nominal level setpoint of feed tank, labelled T3, is reached. Once final nominal level in feed tank, labelled T3, has been reached, feed pump P 3.1 ramps down via frequency and deactivates. Then deactivate AV 3.3, AV 3.6, and AV 3.11 to close position. Step 7 - Clean in Place [CIP] Step 7 is an individual method or process from steps 1 to 4, as described in the embodiments related the systems and processes for the commercial or industrial effluent treatment system. This method or process shall include the external injection from the commercial or industrial laundry effluent treatment device, of an alkali or acidic solution into the feed tank, labelled T3, mixed with clean water being city or permeate. The method or process relative to CIP, is operable by executable program logic control to preserve, maintain or restore the clean fluid permeation flow through the ceramic hollow fiber wall, being either individual or multiple hollow fiber membranes; which includes nominal 220 to 1500 individual ceramic hollow fibres made of aluminium oxide (AI2O3) substrate material; as stated above; including but not limited to selective pore sizes of the aluminium oxide substrate material (AI2O3) being nominal 50 to 1400 nanometres, also but not limited to selective pore sizes of the aluminium oxide substrate material (Ai2O3) being nominal 50 to 1400 nanometres, including nominal 1 to 100 nanometres ceramic or polymeric coating or multiple separate ceramic or polymeric coatings, acting as a separation layer attached to the membrane fiber wall. The process includes heating city water or permeate held in a storage tank, as indicated T3, feed tank, by way of an actuated control valve, heater or steam injector including diffuser, as indicated by component AV 3.14. This method may be operable may to heat the city water or permeate to 40 degrees centigrade or more. The heater may be operable to heat the water to about 50 degrees centigrade or more. The heater may be operable to heat the effluent to within a temperature range of 50 to 80 degrees centigrade. The heater may be operable to heat the effluent to an optimum of 60 degrees centigrade. The executable program logic control from “inactive” shall activate components AV 3.2, AV 3.3, AV 3.6, AV 3.8 and AV 3.10 to open position and activate feed pump P 3.1 and circulation pump P 3.2 to set point for a nominal period of 5 minutes to 180 minutes. Then feed pump P 3.1 and circulation pump P 3.2 ramps to 0% frequency and stops. Deactivate AV 3.2, AV 3.3, AV 3.6, AV 3.8 and AV 3.10 to close position. Then activate step 6 before returning to “inactive”.

Claims

1. A membrane filtration device of individual or multiple hollow fiber ceramic membrane modules comprising of nominal 220 to 1500 individual ceramic hollow fibres made of aluminium oxide (AI2O3) substrate material; the fiber geometry being nominal 2.00 to 4.00 millimetres inside diameter, nominal 4.00 to 6.00 millimetres outside diameter, effective length nominal 360 to 1000 millimetres, bundled together with either epoxy, ceramics or glass end caps for commercial and industrial textile care effluent treatment.

2. A membrane filtration device consisting of multiple hollow fiber ceramic membrane modules with effective nominal length of 360 to 1000 millimetres that operate individually or stacked in series creating vertical or horizontal columns, thereby providing greater filtration surface area and permeate flow, per square meter of footprint area.

3. A membrane filtration device and process operable at cross-flow rate of nominal 2 metres per second to 8 meters per second and operating pressure of 1 to 10 bar relative to effluent profile and membrane fiber pore sizes from nominal 1400 nanometre’s down to nanofiltration phase of 1 nanometre including substrate material and separation layer coatings.

4. A continuous membrane filtration treatment method with alternate pumping of clean fluid and contaminated fluid through conduits right and left allowing greater control and dislodgement of lint or fiber material, that may build up at the membrane conduit inlet, causing blocking or plugging of compromising the integrity of the ceramic hollow fibre.

5. A continuous membrane filtration treatment method with filtration and backwash configurations through conduits right and left, operable by a programmable logic control or controls software to preserve theefficiency of the membrane separating layer and porous substrate during cross flow, therefore alleviating the operable risk of membrane fouling.

6. A membrane filtration treatment method consisting of backwash using fluid such as permeate water of 10 to 60 seconds for every 5 to 120 minutes to maintain hollow fiber membrane flux performance, membrane integrity and minimise chemical cleaning on the membrane separating layer.

7. A membrane filtration device with center retentate piping design and configuration in addition to left and right hand membrane inlet conduits, to evenly distribute fluid within the device and counteract internal pressure drop within the membrane loops allowing continuous collection of retentate between right and left conduits in an alternative process, controlled by a programmable control logic or controls software.

8. A membrane filtration device, including actuated solenoid valve operable by executable control logic on the permeate conduit, controlling high permeate flow during clean water flux, so as to, not damage or compromise the integrity of the hollow fibre ceramic membranes.

9. A membrane filtration device, including processed and methods [Steps1-5] detailed in the description of pumping industrial and commercial laundry effluent, using no more than three variable speed drive pumps, being a centrifugal the integrity or performance of the ceramic hollow fiber membrane, detailed in the embodiment and description.

10. A membrane filtration device and process including executable program logic control, that controls effluent temperature in a specific manner, so as to improve the performance and permeate yield of the hollow fiberceramic membrane and so as to not compromise the integrity or performance of the ceramic hollow fiber membrane through thermal shock + / -10 degrees centigrade of the nominal effluent temperature, detailed in the embodiment and description.511 .A membrane filtration treatment method consisting of flush using city water or permeate fluid to remove effluent from the membrane filtration device to increase performance of chemical cleaning on the membrane separating layer.1012. A membrane filtration treatment method consisting of clean in place using alkali or acidic solution to return hollow fiber membrane flux performance and membrane integrity.

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