CN1024323C - Turndown control method for membrane separation systems - Google Patents
Turndown control method for membrane separation systems Download PDFInfo
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- CN1024323C CN1024323C CN 88106632 CN88106632A CN1024323C CN 1024323 C CN1024323 C CN 1024323C CN 88106632 CN88106632 CN 88106632 CN 88106632 A CN88106632 A CN 88106632A CN 1024323 C CN1024323 C CN 1024323C
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Abstract
The present invention relates to an osmotic membrane technical process which is effectively implemented by reducing feed flow quantity and pressure division driving force which penetrates through an osmotic membrane under the condition of requirement reduction. The surface area of the installed osmotic membrane is sufficiently used in the process of requirement condition reduction. The driving force is reduced by reducing feed flow pressure and/or increasing pressure on one side of an osmotic object of the osmotic membrane. The product flow reduction and/or the product purity reduction can be easily achieved during the requirement reduction. Meanwhile, the opening/ stopping operation of an osmotic membrane system is avoided, and the reliability of the whole system is increased.
Description
The present invention relates to the permeable membrane system.More specifically say and relate under different demand conditions, use this kind system.
The permeable membrane method and system is known in the present technique field, and is just using in various gases and liquid separation or considering to be applied.In this generic operation, incoming flow is contacted with the surface of permeable membrane, and the component of easier infiltration in this incoming flow is reclaimed as permeate stream.And the component that is difficult for infiltration is just emitted from this permeable membrane system as non-penetrant or remaining logistics.
The easy characteristics of this kind fluid separation operation institute's inherent are impelled the present technique field to enlarge in the industrial operation of reality and are used permeable membrane.Certainly, the selectivity of a kind of permeable membrane system and thoroughly oozing property must meet total production requirement in a kind of specific end use.In addition, also must constantly improve the efficient of permeable membrane system, run into the feasibility of advantageously using the permeable membrane system under the operational condition in the art so that improve.
Design for the permeable membrane system is to finish a kind of given permeable membrane surface-area that separates required by task with the factor that total efficiency plays an important role, and for obtaining the needed partial pressure difference that passes this film of desired product quality and quantity, that is needed perviousness and selectivity, perhaps separating factor.In actual permeable membrane system design, need between permeable membrane surface-area and described partial pressure difference, carry out best trading off.Therefore, the partial pressure difference (or the impellent of passing permeable membrane) that passes film is big more, and the required permeable membrane surface-area of then a certain given lock out operation is just more little.At this moment just need to use more expensive pumping equipment and higher pump operated cost, but can make permeable membrane equipment keep lower cost.Otherwise,, just need the relative cost of the each side of bigger permeable membrane surface-area so total system and operation also will change if use less impellent thereupon.
The permeable membrane system normally designs and determines the performance of the best by full throughput, stable base runoff condition (that is design conditions, these design conditionss always do not make full use of) in practicality.Under the operational condition that is not design conditions, for the relation of permeable membrane surface-area and partial pressure difference, the multiple different combination of optimum operation condition all is feasible.For the permeable membrane system is the fluid separation purposes that meets the requirements, and does not generally operate under the regime flow condition.According to the quantity and/or the quality of product, the demand of permeable membrane system is changed through regular meeting.For example, according to nitrogen flow and/or desired degree of purity,, very big variation can be arranged in during 24 hours to the demand of the product of the nitrogen from air separation permeable membrane system, separated.
During low demand, or turn down under the condition so-called, generally there are three kinds of operating method in the permeable membrane system.First kind, do not take to turn down the reduction that adapts to the product demand.In this case, feed rate and partial pressure difference keep constant.As a result, the quality of product will be increased on the design level, and the power requirement also remains on full designed capacity level.So this mode is imperfect, because can not realize saving power, and the quality of products therefrom surpasses desired level.
The second way, change is used for isolating permeable membrane area.Under the condition that demand reduces, a part of permeable membrane area is cut off need not.So just reduce inlet amount in order to processing with the reduction of adaption demand.The shortcoming of this method is can make full use of the permeable membrane area that is provided with the end to be associated.This factor has determined be lower than under the condition of turning down of designed capacity, the compromise optimization that do not reach between permeable membrane area and partial pressure difference.
The third mode that is used for low demand condition is permeable membrane to be operated under design conditions, and used a buffering basin to deal with the requirement of changes in demand.When surge tank is filled, or make the permeable membrane system zero load, promptly allow fresh feed pump dally, or termination of pumping is to save energy.This mode also has the shortcoming of failing to make full use of the permeable membrane area of being installed, because when device idle running or shut-down, these permeable membrane areas do not use fully.Often open/stop the shortcoming that the formula operation also has the wearing and tearing of aggravation relevant devices.
Therefore, needing a kind of turning down under the condition can be fully and utilize the method for the separating power of the permeable membrane area of being installed expeditiously in the art really.Such method can make the permeable membrane system of being installed all operate with the efficient of the best from start to finish, and can provide than above-mentioned opening/the stop higher working method of operating method reliability.
Therefore, an object of the present invention is to provide and a kind ofly turning down under the condition improving one's methods of operation permeable membrane system.
Another object of the present invention provides a kind of method that can utilize whole separating powers of the permeable membrane system of being installed under the condition that the product demand reduces expeditiously.
At these and other purposes, be described in detail the present invention hereinafter, and in claims, specifically indicate novel feature of the present invention.
Lowering under the demand condition, can realize the improved control of turning down by reducing feed rate with the reduction partial pressure driving force, and under all operations condition, all can make full use of the permeable membrane area of being installed simultaneously.Therefore turning down under the condition, owing to reduced machine utilization, thereby can reach the quantity of desired product and quality expeditiously and improve the reliability of permeable membrane device, and avoid opening under the changes in demand condition/the stop caused wearing and tearing aggravation of operating method.
Further narrate the present invention with reference to accompanying drawing hereinafter, this figure is a synoptic diagram of turning down permeable membrane system used in the general preferred embodiment of control method of the present invention.
Purpose of the present invention can reach by adopting a kind of control method of turning down, and in the method, when demand lowers, feed rate and the partial pressure driving force of passing permeable membrane is all reduced. This partial pressure driving force is the function of the dividing potential drop of this component in charging and the permeate stream. Can carry out this kind and subtract low-energy operation, and simultaneously not only under design condition, and lower under the operating condition of demands at all, can both take full advantage of institute The permeable membrane area of installing. Turning down condition and lowering in the situation of load because can be constant, operating equipment stably, so can reach more efficient operation, and can prevent from operating the wearing and tearing that aggravate because opening/stopping.
Method for turning down sound of the present invention is to begin by the desired signal of indicating requirement to be lower than design condition. Sort signal can be that indication is lower than the product stream flow measurement signal of design discharge, or is equally the purity input signal that indication requires to be lower than design condition. Usually during this permeable membrane system, adopt a process computer in design, its program is based on existing permeable membrane area in the system of taking full advantage of and the operating pressure ratio on permeable membrane both sides is reduced to new optimum condition. The reduction of required pressure ratio is by to pumping equipment, and transmissions such as compressor, vavuum pump, liquor pump is a kind of turns down that signal finishes.
Accompanying drawing is that the general vote of turning down control method of the present invention is implemented in explanation, and with reference to this figure, feeding pipe 1 is to be used for carrying feeding gas to compressor 2, and the feeding gas of pressurization just sent pipeline 3 and arrived permeable membrane device 4 from compressor.Desired product stream, promptly penetrant or non-permeate gas are to emit by product pipeline 5.Other gas stream (not shown)s of removing from permeable membrane device 4, or throw aside, or be used for the purposes of some needs.The accurate product under meter of one station symbol is arranged on pipeline 5, on described under meter, have a conventional formula product flow signal transmitter, and a kind of input signal (generally representing with number 8) is sent to process computer/controller 9 through connecting.So product under meter 6 is to be used for monitoring the product flow, transmitter 7 is to be used for process variable signal (promptly with the proportional signal of this product flow) is sent to process computer 9.Also have a purity set point (by number 10 expressions) in addition also as the signal of the described computer of input, this set point can change according to the requirement to product purity in the operation.
Process computer 9 used programs are that an output signal (by number 11 expressions) is sent to working ability control device 12, this device is to connect (by number 13 expressions) by suitable machinery or electrician to turn down compressor 2, it is by regulating suitable recirculation (egr) valve, admission air valve, variable bit rate motor or the like, making its pressure and flow condition be suitable for indicated demand condition.Method of the present invention has high degree of flexibility, because, when design conditions changed owing to process applications difference, permeable membrane improvement in performance etc., this process computer can be regrouped program soon, to cooperate the new design conditions of process applications different or that revised.
In another kind of process program, product purity can be triggered the control of turning down of permeable membrane system as a kind of process variable.In this case, monitor degree of purity of production rather than monitoring flow, and handle is sent to process computer/controller 9 with the proportional signal of product purity.In the case, the program of this computer should be worked out into adjusting the ability and the pressure of compressor, to keep desired degree of purity.
Those skilled in the art will recognize that desired product purity usually can be from downstream process process gas or product liquid.When this product flow reduces, product purity will begin to rise, and process computer will perceive this rising simultaneously, and compressor load is reduced.But should be noted that, because product purity analysis and data gathering related inherent retardation time, so when using product purity, can cause certain labile factor in some cases as main measurement index.On the contrary, the fluctuations in discharge of immediately monitoring product can be accomplished at an easy rate.
Carrying out air separation below by the application permeable membrane comes the example of production nitrogen product to further specify the present invention.Adopt a kind of typical permeable membrane system, this kind permeable membrane material can separate oxygen as more meable component in the air, just can understand that the required product gas flow that is rich in nitrogen is that remaining gas reclaims as non-penetrant.In this case, the infiltration gas of oxygen enrichment is as a kind of off-gas flows.Feeding air be compressed to be higher than barometric point, with the product nitrogen gas stream of non-infiltration from the permeable membrane system, to emit a little less than feed pressure.Generally speaking, permeate gas is emitted with normal pressure.The manufacturing of this permeable membrane system and use are with design conditions, be that required all-round power is operating as the basis, and according to the price of required product flow and purity, pressure size and desired partial pressure driving force, water, electricity and gas for example expenditure on power be used for carrying out optimization all sidedly.
For any given pressure ratio of passing permeable membrane, gas or the operation of other fluid separation are feature with two key parameters, i.e. area factor and compressor factor.Area factor is to produce per hour standard cubic foot of 1ncfh(in this example) the required permeable membrane surface-area of product nitrogen.The compressor factor is to produce the required charging tolerance of the described product of 1ncfh.After the product of determining given purposes requires, can determine immediately the best of passing permeable membrane or desired pressure ratio and corresponding area factor and compressor factor.
Be understood to include in the compromise optimization between higher compression machine cost and the power expense that under higher-pressure ratio, is associated for the optimization of these process variables, and under this kind higher-pressure ratio, can produce big product flow.In the air separation purposes, bigger product flow be associated with higher feed pressure because permeate pressure generally be to be fixed under the normal pressure.
As mentioned above, for the operation of constant product purity and constant permeable membrane area, when feed pressure was higher, the product flow generally also increased, and vice versa.Similarly, for the fixedly operation of purity, when feed pressure increased, area factor generally can reduce.In addition, for fixedly product purity and the fixedly operation of permeable membrane area, when feed pressure is higher, feed rate then, promptly compressor flowrate generally can increase, and vice versa.In definite design conditions, that is during full demand condition, take above these relations into account, best is with above-mentioned trade-off relation optimization, so that reach the desired optimized design condition of the production of concrete permeable membrane system and given purposes.
In a kind of illustrative air separation operation, one cover permeable membrane device is issued to optimization at full demand condition, making it is 200psig(pound/square inch gauge in feed gas pressure) under operate, and produce 98% nitrogen 10000ncfh as non-infiltration gas.If the product demand is reduced to 7000ncfh, in enforcement of the present invention, can keeps the permeable membrane area that is provided is provided fully by intake pressure being reduced to 145psig, and product purity be remained essentially in the design purity level simultaneously.Except reducing feed gas pressure, also reduced and produced the required feeding air flow of 7000ncfh nitrogen product.When low feed gas pressure was 145psig, the permeate gas amount of passing permeable membrane was less, just needed more a spot of feeding gas to reach the desired production of turning down.Above-mentioned turning down in the example, product needs to turn down to 7000ncfh from 10000ncfh, and feeding air pressure is reduced to 145psig from 200psig, the result, and compressor flowrate, the feed rate that promptly flows through the permeable membrane system is 72% of design full flow.Therefore, when turning down, keep making full use of the permeable membrane area that is provided, and the condition of making the product that reaches the design purity level simultaneously, should comprise the described impellent that reduces to pass this permeable membrane, for example by reducing feed gas pressure, adopt simultaneously and describedly turn down from the feeding gas design discharge.
The energy saving amount that is reached when turning down will depend on the type of used gas booster compressor in the invention process.Be understandable that,,, can provide many kinds of compressed capability control device according to the type of used gas booster compressor in the art.According to the present invention, the various available apparatus that can be used to turn down gas booster compressor are, for example variable speed motor, internal recycle valve and sniff valve load reducer.
When this gas booster compressor, promptly has the reciprocation compressor of sniff valve load reducer, the oil spilling formula spiral-lobe compressor that has the internal recycle valve that is circulated back to inspiratory point or other this type of commercially available equipment, receive when turning down signal, its feed rate will reduce with the pressure ratio of passing permeable membrane, consequently reduces the power consumption.In self acting embodiment of the present invention, above-mentioned process computer can automatically set up gas booster compressor by programming and mechanism is turned down in control, be valve load reducer, variable speed motor or the like, so that make optimal flow rate and the pressure ratio of passing permeable membrane be used for given desired signal, i.e. flow signal or purity signal.
In the embodiment of above-mentioned illustrative, adopted the screw type compression system that has the internal recycle valve, when when 10000ncfh nitrogen is turned down 7000ncfh, the power consumption is 77% of a design load.When feed gas pressure was reduced to 145psig, the power consumption was 85% of a design load.The total output consumption is reduced by above-mentioned two factors, it is the reduction of the feed gas pressure that reduces and produce the impellent that a kind of reduction passes permeable membrane of feeding gas volume, so the total output consumption be design load 77% 85%, or design conditions power consumption 65%.
Should be noted that and of the present inventionly turn down that control method can be used for effectively that product purity is turned down in requirement but not the embodiment of turning down the product flow.If require fixedly lowering product purity under the product flow condition, can reduce feed pressure with the pressure difference of reduction, and the product flow is remained on the design conditions level by this permeable membrane.In such embodiments, total permeable membrane area of being provided remains in turning down operating process and makes full use of.Those skilled in the art can understand, and above-mentioned process computer also is easy to the operation of regulating compression system automatically by programming so that carry out the control of turning down of product purity and product flow simultaneously.In this purposes, the pressure difference that produces the impellent of passing permeable membrane will change according to the change of product purity and flow, and can carry out optimization according to given gas or relevant general requirements and the operational condition of other fluid separation operation.
Will be understood that, the efficient that this kind turned down control be depend on the compression system design that is used for given permeable membrane lock out operation and effectively controlling flow to the ability of the feed rate of this permeable membrane.Should also be noted that the efficient of turning down control method of the present invention will submit to the product pressure requirement that is purposes.In the example of above-mentioned air separation with recovery nitrogen, if the product minimal pressure that requires is 100psig, the limit of then turning down then is 45% of the maximum product flow of this compression system.But in most of the cases, this factor should not have influence on total efficient of turning down, because the optimum design working pressure of permeable membrane will be higher than required product pressure significantly generally speaking.Therefore in most of purposes, implementation method of the present invention is feasible, also is the most effective control method of turning down.Those skilled in the art will be understood that the method for turning down of the present invention will reasonably be optimised to by in the whole technological process of being controlled this and turn down the degree that importance guaranteed of operation.Selection compressor assembly and design operation pressure turn down efficient for decision in the industrial actually operating and rangeability is an important parameters.What it is further to be understood that is, the present invention merely relates to from design conditions turning down one group of concrete low feed rate and Impetus Condition, but relate in described design conditions and various adjusting of hanging down the described condition between the demand condition, or the adjusting between each different low demand conditions, and be to require to be lower than design flow and/or purity reclaims product in described low demand condition.What be also pointed out that is, for desired product flow and purity, though design conditions is the all-round power of a kind of given permeable membrane system of expression, but in general be to be higher than operation permeable membrane system under its designed capacity, be higher than the product of design quantity so that can have to produce under the condition of some declines, or having at the product yield to produce under the condition of some declines is higher than the product that designs purity in product purity.Be higher than operation under the design conditions at above-mentioned these, being interpreted as mainly is to constitute the design conditions of turning down feature of the present invention.From above explanation, be appreciated that, if product traffic requirement or product purity require or these two kinds of requirements all are when being lower than the design product flow of given permeable membrane system and purity level, then this to turn down condition be feasible.
Scope of the present invention is included in the fluid separation operation of broad variety and implements the as herein described and claimed method of turning down, and the embodiment of wherein above-mentioned air separation production nitrogen is exactly a kind of illustrative example that relates to the condition of turning down.These operations comprise can effectively utilize the permeable membrane system with the easier infiltration component in the fluid mixture be difficult for the isolating any operation of infiltration component.For example the hydrogeneous waste gas from desulfurizer is that another is fit to use permeable membrane operation and the feed stream example of turning down control method of the present invention.The typical flue gas of this class can contain the 45%(mole of having an appointment) hydrogen, 25% methane, 25% ethane and a small amount of other hydrocarbon.The permeable membrane systems approach can be used for described hydrogen is purified to qualified purity level, and for example about 90%.From the ammonia sweep gas, reclaim hydrogen, and carbonic acid gas and methane separation are suitably can use the illustrative example of turning down other industrial fluids lock out operation of method of the present invention under the situation.Though be also pointed out that the top air separation operation of having narrated the Oxygen Flow that discharges infiltration under normal pressure easily, in other various embodiments of the present invention, other suitable and preferred pressure conditions also will be fit to.In some occasion, may preferably utilize at the existing feed pressure of turning down under the condition, and by the raising seepage water pressure, rather than reduce feed gas pressure and reduce the impellent of passing permeable membrane.Certainly, product purity that is reached and/or product yield will have some variations along with the general requirements of any given permeable membrane lock out operation.
The control method of turning down of the present invention can be applied to any needed permeable membrane system.Therefore, employed permeable membrane material can be any suitable material that can optionally see through easier infiltration component in a kind of gas or other fluid mixtures, derivatived cellulose for example, as cellulose ethanoate, cellulose acetate butyrate or the like, polymeric amide and polyimide, comprise polyarylamide and poly-aryl imide, polysulfones, polystyrene or the like.Be also pointed out that the scope of the invention comprises the permeable membrane of using any required configuration.Therefore, can be the permeable membrane of composite form, promptly on a kind of porousness bearing bed, determine the separating layer of characteristics such as the selectivity of this film and perviousness with one deck.Also can use the permeable membrane of unsymmetric form, promptly in the permeable membrane of this kind unsymmetric form, have a dense surface region to determine that characteristics such as the selectivity of this film and perviousness and the district than porousness provide the carrying effect.Other forms of permeable membrane, for example Zhi Mi permeable membrane also is applied to specific purposes.Being used for permeable membrane of the present invention, can be any needed shape, planar sheet for example, hollow fiber, spiral wound or other shapes that needs, general preferred employing be hollow fibers permeable membrane cartridge.It generally is to be fitted to the permeable membrane module that hollow fiber or other need the penetration material of shape, comprising hollow fiber bundle, rivel sheet permeable membrane assembly, perhaps helical coil around the permeable membrane tube, they have the oral-lateral of being fed into and permeant outlet side, and conduit means are housed the non-penetrant part and the penetrant of incoming flow are partly emitted respectively.All these systems all can turn down effectively by the present invention, and can both utilize the permeable membrane surface-area of being installed fully under all operations condition.
Therefore, the invention provides a kind of height practicality and the high efficiency control method of turning down, not only can make full use of the permeable membrane system capability of being installed, and avoid changing or turn down condition and go to adopt out/stop the operation of mode in order to respond different demand.The result can still use the permeable membrane system to reach desired product quality and quantity turning down in the usual way under the condition, and improves the reliability of permeable membrane system under the condition of turning down that reduces to load by the stable and quiet run of equipment.
Claims (12)
1, in a kind of permeable membrane technological process, wherein under the design operation condition, a kind of feed fluid fed with required feed rate and pressure and contact with the feeding side of a kind of permeable membrane system, this permeable membrane system has a kind of mounted permeable membrane surf zone, this surf zone can optionally make and contain a kind of easily infiltration component infiltrate that relatively is difficult for the described incoming flow of infiltration component, simultaneously the described infiltration component that relatively is difficult for of aequum is discharged as non-penetrant under the design pressure level that is this incoming flow basically, the easily infiltration component of aequum is then discharged as penetrant under lower pressure levels, and provide the impellent of described permeable membrane centrifugation by the partial pressure difference that described incoming flow component is passed this permeable membrane, the improved control method of turning down of this kind comprises:
(a) partial pressure driving force that keeps this feed stream flow and pass this permeable membrane makes penetrant and the quantity of non-penetrant and the quantity and the purity level that purity all reaches this design of gained, and makes full use of the surf zone of the permeable membrane system of being installed simultaneously;
(b) detect product stream, i.e. penetrant or non-permeate stream are from quantity and/or purity in the product flow line downstream of this permeable membrane system;
(c) will be sent to the technological process computer system with the technological process variable signal that product flow in the described product flow line and/or product purity are directly proportional, to send a kind of corresponding output signal to the working ability control device, be controlled under design and the variable demand condition, arrive the feed rate and/or the pressure condition of permeable membrane;
(d) reducing product stream, be penetrant or non-permeate stream, quantity and/or the demand of purity during, this feed rate and described impellent of passing permeable membrane are reduced, continue to keep making full use of the permeable membrane surf zone that this system installs simultaneously, with response from the output signal of described working ability control device, thereby during the turning down of described attenuating demand, product stream is turned down quantity and/or quality is emitted from this permeable membrane system with required; With
(e) (wherein can obtain to reach the product stream of this design quantity and purity level in design conditions by the step (a) of design requirements, be penetrant or non-permeate stream) and low feed rate and less Impetus Condition (the wherein recyclable product stream that is lower than the quantity and/or the purity level of described design level) during by low demand condition steps performed (d) between, regulate this feed rate and described impellent of passing this permeable membrane, with response from the described output signal of described working ability control device and response and the described technological process variable signal that is directly proportional from the needed product flow in the product flow line of permeable membrane system and/or product purity, thereby under the variable demand condition, the permeable membrane surf zone that provides by making full use of improves the efficient of this permeable membrane technological process.
2, according to the method for turning down of claim 1,, make at steps performed (d) wherein by during the reduction demand, reducing feed stream pressure, the time reduce the impellent pass this permeable membrane.
3, according to the method for turning down of claim 1, wherein this permeate stream is needed product stream.
4, according to the method for turning down of claim 1, wherein this non-permeate stream is needed product stream.
5, according to the method for turning down of claim 1, comprise during the wherein said reduction demand this demand wherein be a kind of product that is lower than design quantity that reaches the design purity level of supply during.
6, according to the method for turning down of claim 1, comprise during the wherein said reduction demand this demand wherein be a kind of product that is lower than design purity that reaches the design quantity level of supply during.
7, according to the method for turning down of claim 1, wherein, make when steps performed (d), reduce the impellent of passing this permeable membrane by during the reduction demand, increasing this permeate stream pressure.
8, according to the method for turning down of claim 3, wherein said incoming flow comprises a kind of hydrogenous streams, and described product permeate stream comprises the hydrogen of purification.
9, according to the method for turning down of claim 4, wherein said incoming flow comprises air, and the non-permeate stream of described product comprises a kind of streams of rich nitrogen.
10, the method for turning down according to Claim 8 wherein by increase this permeate pressure during the reduction demand, makes when steps performed (d), reduces the impellent of passing this permeable membrane.
11, according to the method for turning down of claim 9,, make when steps performed (d), reduce the impellent of passing this permeable membrane wherein by during the reduction demand, reducing feed stream pressure.
12, according to the method for turning down of claim 1, wherein this permeable membrane system comprises the permeable membrane module that contains hollow-fiber film.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
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| CN 88106632 CN1024323C (en) | 1988-09-09 | 1988-09-09 | Turndown control method for membrane separation systems |
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| CN 88106632 CN1024323C (en) | 1988-09-09 | 1988-09-09 | Turndown control method for membrane separation systems |
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| CN1040929A CN1040929A (en) | 1990-04-04 |
| CN1024323C true CN1024323C (en) | 1994-04-27 |
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