CN103508422A - Membrane-separation oxygen supply method and system capable of providing oxygen enrichment with stable purity or stable flow - Google Patents
Membrane-separation oxygen supply method and system capable of providing oxygen enrichment with stable purity or stable flow Download PDFInfo
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Abstract
The invention belongs to the technical field of air separation and particularly relates to a membrane-separation oxygen supply method and system. On the basis of the existing membrane-separation oxygen supply system, a regulating loop connected in parallel to a vacuum pump is added to continuously monitor the pressure at the inlet of the vacuum pump. In the case of temperature reduction, the external air can be led in or oxygen enrichment at the outlet of the vacuum pump is circularly returned through the regulating loop, so as to regulate the vacuum degree at the inlet of the vacuum pump and then to regulate the trans-membrane pressure ratio of a membrane separator, and the oxygen enrichment with stable purity and flow can be obtained. In the case of temperature rise, the system is emptied through the regulating loop. When the system runs normally, the purpose of low-load start-up can be achieved through the regulating loop, so as to avoid overflow of the vacuum pump to ensure stable running. The membrane-separation oxygen supply method and system provided by the invention can effectively avoid the fluctuation of components or flow of the prepared oxygen enrichment due to environmental change and temperature change during the membrane separation process, so that the membrane separation system provides oxygen enrichment with stable purity or stable flow to support the oxygen enrichment combustion in a furnace or kiln with a relatively-low manufacturing cost.
Description
Technical field
The invention belongs to air separation technology field, be specifically related to a kind of membrane sepn method for supplying oxygen and assembling system.
Background technology
Membrane oxygen enrichment technology is a kind of new separation method growing up gradually from the end of the seventies, it utilizes organic polymer dense film to nitrogen, the selection perviousness difference of oxygen, while there is pressure difference or pressure ratio in Dang Mo both sides, in mixed gas, the fast gas of infiltration rate is as water vapor, hydrogen, helium, oxygen, carbonic acid gas etc. become oxygen-rich air (depending on the oxygen nitrogen separation factor difference of mould material through the low-tension side enrichment at film after film, single-stage separation can obtain the oxygen enrichment that purity is about 23-60%), and the relatively slow gas of infiltration rate is as nitrogen, argon gas, methane and carbon monoxide etc. are oxygen deprivation (or rich nitrogen) air in the delay side of film by enrichment, membrane separating method is that a new way has been opened up in oxygen enrichment extraction, because there is not phase transformation in it in the concentrated whole process of separation, normal temperature is separated, especially the negative pressure flow process separation system building with board-like film, there is equipment simple, low cost of manufacture, energy consumption is little, output is adjustable, start rapidly, easy and simple to handle, static system operation, the high outstanding advantages that waits of reliability, it is a kind of separation method of economy, at present, adopt membrane separating method to produce oxygen enrichment and be widely used in oxygen-enriched combustion-supporting, oxygen enrichment ventilates, the fields such as water treatment, especially for glass, metallurgical, cement rotary kiln, the oxygen-enriched combustion-supporting of Industrial Boiler etc. Thermal Power Engineering Field.
Single with regard to constituent of air membrane sepn oxygen preparation, after once type selecting has been determined the separating area and power-equipment of separation membrane, mould material, because of the intrinsic performance of parting material,, the ability of power-equipment is definite, the temperature of the feeding air that the oxygen components that membrane sepn process obtains in air is main and separated with the stability of flow is relevant.For an oxygen-rich combustion-supporting system being likely applied under various ambient temperature conditions, the different envrionment temperatures that application scenario is installed can be different, and even same place causes the difference of envrionment temperature because of the variation in season.Therefore, for stove oxygen-enriched combustion-supporting provides the film separating system Hui Yin different location, Various Seasonal of oxygen, even between the morning, noon and afternoon, the variation of separated air themperature causes flow, the oxygen purity of the oxygen-rich air separated to produce huge fluctuation.Because membrane sepn provides the flow of oxygen enriched air system, the stable effect of oxygen-enriched combustion-supporting process and the accessibility that stove heat power engineering system regulates of directly having determined of oxygen purity, so, in a sense, if the oxygen enrichment of stablizing purity or regime flow can not be provided, with the application of the oxygen-rich combustion-supporting system of this separation method, serious restriction will be subject to.
Summary of the invention
The object of the present invention is to provide a kind ofly provides membrane sepn method for supplying oxygen and the assembling system of stablizing the oxygen enrichment of purity or the oxygen enrichment of regime flow for terminal by oxygen point.
The invention provides membrane sepn method for supplying oxygen, be different from the simple barrier sepn process of prior art, specifically, on the basis of existing membrane sepn oxygen system, increase a regulating loop in parallel with vacuum pump, the pressure of continuous monitoring vacuum pump inlet; When temperature reduces, can pass through regulating loop, introduce the oxygen enrichment that vacuum pump outlet is returned in extraneous air or circulation, to adjust the vacuum tightness of vacuum pump inlet, and then adjust membrane separation apparatus transmembrane pressure ratio, thereby obtain the oxygen enrichment of stablizing purity or regime flow; When temperature raises, can pass through this regulating loop emptying; When system is normally moved, also can realize Low loading start up by this regulating loop, avoid vacuum pump overcurrent with steady running.
Corresponding to above-mentioned membrane sepn method for supplying oxygen, membrane sepn oxygen system of the present invention, as shown in Figure 2, is on the basis of existing membrane sepn oxygen system, increases a regulating loop in parallel with vacuum pump, specifically comprises:
(1) preferred but non-essential at least one strainer AF01;
(2) at least one device A B01 that boosts, in order to boost to unstripped gas certain pressure; After this equipment that boosts also can be placed on membrane separation apparatus, in order to scavenge;
(3) at least one group of membrane separation apparatus M0n (n=1,2 ... N, N is at least 1), while organizing membrane separation apparatus, each is organized membrane separation apparatus and is connected in parallel more;
(4) preferred but non-essential at least one group of regulated valve V0n1, V0n2, n=1,2, N, N is at least 1, when envrionment temperature is too high, for switching, isolate, regulating, enters the air to be separated of membrane separation apparatus M0n and the flow that enters vacuum pump from membrane separation apparatus per-meate side;
(5) a preferred but non-essential pressure monitoring devices PE01, in order to monitor vacuum pump inlet pressure;
(6) at least one vaccum-pumping equipment AB02, in order to set up membrane separation apparatus both sides transmembrane pressure ratio;
(7) at least one regulating loop in parallel with vacuum pump, this regulating loop is by 3 variable valve V101, V102, V103 forms, as schema method of attachment, wherein, the second variable valve V102 can be from the outside introducing air of system to vacuum pump inlet, the first variable valve V101 can introduce vacuum inlet by the oxygen-rich air circulation of vacuum pump outlet, the 3rd variable valve V103 can be that the oxygen-rich air of vacuum pump outlet leads to system outside (emptying) by internal system, the tie point access vacuum pump inlet of the second variable valve V102 and the first variable valve V101, the tie point access vacuum pump outlet of the first variable valve V101 and the 3rd variable valve V103,
(8) the preferred but inessential vacuum pump inlet pressure feedback regulating and controlling valve V101 monitoring with pressure monitoring devices PE01, V102, the control of V103 aperture and the topworks of comprising;
(9), as known technology, system also needs to comprise necessary control unit so that system dynamic equipment can move, by-pass valve control can switch etc. as requested.
The present invention can response environment temperature variation and is at least guaranteed that membrane sepn oxygen can provide the oxygen enrichment of stablizing purity or regime flow, can effectively avoid membrane sepn process to cause the oxygen enrichment component produced or the fluctuation of flow because of application variation of ambient temperature, thereby make take film separating system as stove oxygen-enriched combustion-supporting provides the oxygenant of stablizing purity or regime flow, to carry out oxygen-enriched combustion-supporting in lower manufacturing cost.
Accompanying drawing explanation
Fig. 1 is existing membrane sepn method for supplying oxygen and system diagram.
Fig. 2 is membrane sepn method for supplying oxygen of the present invention and system diagram.
Number in the figure: AF01 is air filter, V0n1, V0n2 are valves, V101, V102, V103 are variable valve, AB01, AB02 are the equipment of boosting, and PE01 is pressure monitoring devices, and M01～M0N is membrane separation apparatus, A0 is that the feed side entrance of membrane separation apparatus is also gas inlet, A1 is that retained gas outlet is also waste gas outlet, and A2 is that membrane separation apparatus suction side is also per-meate side outlet, i.e. oxygen-rich air outlet.
Embodiment
Below in conjunction with drawings and Examples, comparison the present invention is different from prior art, and further describes the present invention.
In accompanying drawing:
AF01, it is air filter, can be various forms of strainers, comprise fibers form, filtrate form, bag type filtering, preferably employing can automatically cleaning form or the strainer of various array configurations, for filtering, clean the raw air that enters membrane separation apparatus, guarantee the degree of cleaning requirement of membrane separation apparatus to raw air.
V0n1, V0n2 is valve, can be various forms of valves, as various manual, automatically control, the stopping valve regulating, butterfly valve, gate valve etc., preferably adopt various forms of automatic regulating valves, can be pneumatic, electronic, surge, for switching, isolation, adjusting enters the air to be separated of membrane separation apparatus and the flow that enters vacuum pump from membrane separation apparatus per-meate side, wherein, if automatic regulating valve door, they can be opened or close and carry out flow according to the temperature of monitoring according to predefined logic, control of purity regulates, these valves can be pneumatic controls, also can be electronic, the self-acting valve of hydrostatic control.
V101, V102, V103, it is variable valve, V101, V102 is for regulating the negative pressure before vacuum pump, variable valve V102 is used for compensating normal atmospheric and enters vacuum pump inlet, variable valve V101 is for returning to the oxygen enrichment circulation of exporting after vacuum pump to vacuum pump inlet, these valves can be various forms of valves, as various manual, automatically control, the stopping valve regulating, butterfly valve, gate valve etc., preferably adopt various forms of automatic regulating valves, can be pneumatic, electronic, surge, they can be according to predefined logic, as carried out regulating and controlling according to the temperature of monitoring, also can regulate according to the pressure before monitoring vacuum pump, V103 is for emptying when vacuum pump superpressure, open valve when V102 also can be used as vacuum pump Low loading start up.
AB01, AB02, the equipment of boosting, can be various forms of gas booster compressors, as piston-type, centrifugal, screw rod, vortex, Roots, pendular ring etc. compressed format, gas is boosted to suitable pressure, and AB01 is for component to be separated is boosted to and enters the required separating pressure of separator, and AB02 is for being decompressed to the required separating pressure of separator by membrane separation apparatus suction side and overcoming the resistance that follow-up fluid is carried.
PE01, is pressure monitoring devices, for monitoring the pressure of vacuum pump inlet, can be arranged on all and can reflect in real time the optional position that enters vacuum pump gaseous tension, and can be the pressure monitoring devices of pressure-sensitive or other arbitrary form.
M01 ~ M0N, is membrane separation apparatus, can be board-like film, rolled film, hollow-fibre membrane, wherein, A0 is that the feed side entrance of membrane separation apparatus is also gas inlet, A1 is that retained gas outlet is also waste gas outlet, and A2 is that membrane separation apparatus suction side is also per-meate side outlet, oxygen-rich air outlet.
Membrane separation apparatus and the membrane sepn oxygen of explaining for convenience membrane sepn process, as shown in Figure 1, lexical or textual analysis is as follows:
M01 ~ M0N is as shown in Figure 1 a kind of 3 mouthfuls of membrane separators, each membrane separator is at least by 1 unstripped gas entrance A0,1 retained gas outlet A1,1 oozes vent outlet A2 composition, and the separation membrane in membrane separation apparatus has at least been divided into both sides, one side is malleation side, one side is suction side, and malleation side is also the unstripped gas side of membrane separation apparatus, also referred to as high-tension side, retained gas side, suction side is also the infiltrating gas side of membrane separation apparatus, also referred to as low-tension side, suction side;
That prior art be take membrane oxygen enrichment technology and provided the process of oxygenant as stove oxygen-enriched combustion-supporting as shown in Figure 1, wherein, gas filters out the malleation side that enters membrane separation apparatus from the A0 of membrane separation apparatus entrance after the impurity such as dust boost by AB01 through AF01, in membrane separation apparatus, gas is penetrated into low-tension side through membrane sepn rear portion, per-meate side enrichment becomes oxygen enrichment to export from A2, in addition a part of enrichment be difficult to infiltration oxygen deprivation nitrogen-rich gas be excluded from membrane separation apparatus from being detained side outlet A1, membrane sepn process for separating oxygen enrichment in air, general, the oxygen nitrogen separation factor (being called alpha value) of the purity of membrane sepn oxygen producing and separation membrane, gas is more relevant than the ratio of (being called separating pressure ratio) and unstripped gas and oxygen enriched product gas (being called sky oxygen ratio) with the absolute pressure of suction side by membrane separation apparatus malleation side, oxygen nitrogen separation factor is higher, mean and can than under isolate more highly purified oxygen rich gas at lower separating pressure ratio and less empty oxygen, for identical separation membrane, separating pressure is than higher, can obtain more highly purified oxygen enrichment, empty oxygen is than larger, can obtain more highly purified oxygen enrichment, and on the other hand, the flow that membrane sepn is produced oxygen enrichment is the infiltration capacity of separation membrane, main relevant with temperature and the pressure of unstripped gas, for identical separation membrane, separation temperature is higher, infiltration capacity is larger, separating pressure is higher, infiltration capacity is larger,
In a typical membrane sepn process that rolling or board-like separator carry out as adopted, AB01 mainly take to meet provides fresh air as main purpose, overcome the resistance that fluid is carried, typically, adopt rolling diaphragm separator, 1～10KPa boosts, preferably, set up the gas communication resistance that the blast of 2～5KPa has to overcome rolled film itself, and adopt board-like film, even only need to set up tens of blast to hundreds of handkerchief, more have AB01 is placed on after board-like film to the way as exhaust gas emission blower fan, object is also only used to overcome resistance that raw air enters membrane separation apparatus so that the object of fresh air to be constantly provided, for avoiding concentration polarization phenomenon, popular saying be to need constantly to meet separated required fresh air, the air quantity of AB01 is looked the alpha value of parting material and required oxygen-enriched purity requirement, typically, as the rolled film made from the separation membrane of alpha value 2～3, board-like film, in order to obtain the oxygen enrichment of 30% left and right, typically, through AB01, enter the required air quantity of membrane separation apparatus M01 ~ M0N and be approximately 8～20 times of oxygen-rich air flow, more typical, for 10～15 times of required oxygen enrichment flow, simultaneously, AB02 mainly take that to meet separated required pressure ratio be main purpose, the separating pressure ratio of setting up skinning both sides is 2～10, more typical, the rolled film of making at 2～3 separation membrane at the alpha value that adopts parting material, board-like film, when required oxygen-enriched purity is 30% left and right, the separating pressure ratio that approximately needs to set up skinning both sides is 4 left and right, , as the malleation wall pressure of the film blast that is 1～5KPa, absolute pressure is normal atmosphere (101.325KPa)+(1～5KPa), suction side should be set up the vacuum tightness of be equivalent to-75KPa of about 25Kpa(gauge pressure) absolute pressure, like this, separating pressure is than being 4 times of [101.325+ (2～5KPa)]/25 ≌, can obtain approximately 30% oxygen-enriched purity,
As accompanying drawing 1, with reference to above-mentioned, professional and technical personnel can understand, unstripped gas enters the isolated waste gas of M01 ~ M0N through AB01 and gets rid of from A1, oxygen enrichment is collected to send into through AB02 and is used gas point, in order to obtain stable oxygen purity, oxygen flow, air quantity, the blast of AB01 in this process, because of type selecting, have been determined, the air quantity of AB02, blast, also type selecting has been determined membrane separation apparatus M01 ~ M0N, the oxygen nitrogen separation factor of its parting material and separating area are all definite, when applied environment temperature variation, will change according to following trend:
When 1, envrionment temperature raises, the temperature that enters membrane separation apparatus raises, and will strengthen, simultaneously for its infiltration capacity of membrane separation apparatus of determining area and material assertive evidence characteristic, the rising of separation temperature, also will cause the decline of separation factor, what is more important, because the increasing of infiltration capacity, the pumping speed of the vacuum pump AB02 that directly causes arranging can not be met and is drawn into predetermined separating pressure, this is all by the reduction of the oxygen-enriched purity that causes separating, and meanwhile, the oxygen enrichment flow of separating will rise;
When 2, envrionment temperature declines, the temperature that enters membrane separation apparatus declines, and for its infiltration capacity of membrane separation apparatus of determining area and material assertive evidence characteristic, will reduce, simultaneously, the rising of separation temperature, also will cause the rising of separation factor, what is more important, because reducing of infiltration capacity, the pumping speed of the vacuum pump AB02 that directly causes arranging is excessive, until surpass predetermined separating pressure, this is all by the rising of the oxygen-enriched purity that causes separating, meanwhile, the oxygen enrichment flow of separating will decline;
Above, because the change of envrionment temperature all produces significantly fluctuation by directly causing for oxygen-rich combustion-supporting system provides oxygen enrichment flow or the oxygen-enriched purity that the film separating system of oxygenant is produced, be unfavorable for carrying out oxygen-enriched combustion-supporting;
Membrane sepn method for supplying oxygen provided by the invention and system are as shown in Figure 2.Different from original technology, the present invention is by a regulating loop in parallel with vacuum pump, the pressure of continuous monitoring vacuum pump inlet, when envrionment temperature reduces, by adjusting the variable valve on this loop, the oxygen enrichment returning as the extraneous air to supplement or circulation compensates the inlet pressure of vacuum pump, Indirect method transmembrane pressure ratio, thereby can obtain stable oxygen-enriched purity or stable oxygen enrichment flow; When envrionment temperature raises, by adjusting the variable valve on this loop, by unnecessary oxygen enrichment emptying, thereby can will meet in the scope that oxygen-enriched combustion-supporting requires because temperature variation causes the fluctuation of purity or flow to eliminate or be relieved to.
As accompanying drawing 2, by a regulating loop in parallel with vacuum pump, can carry out vacuum pump inlet pressure compensation, by adjusting the V102 on this regulating loop, V101 variable valve, can Indirect method film separating system transmembrane pressure ratio, the film separating system (the former oxygen-rich air that produces approximately 30% purity) according to 4 times of pressure ratio designs of take is example, in the situation that other separation condition is all constant, as typically, the air quantity of AB01, blast, the pumping speed of AB02, vacuum tightness, the parting material of membrane separation apparatus is determined and separating area is determined, in these conditions above all under definite condition, the present invention is because having designed this regulating loop, can avoid film separating system because of variation of ambient temperature (the different envrionment temperature differences that application scenario is installed, even same place is because of the spring, summer, autumn and winter, the flow of the oxygen-rich air envrionment temperature difference of morning, noon and afternoon) causing, oxygen purity produces huge variation, this variation is eliminated or is relieved in the scope that meets oxygen-enriched combustion-supporting requirement, the oxygen enrichment flow that at least can reduce purity but can be stable or reduced flow but the oxygen-rich air output that can stablize purity, concrete operations are as follows:
(1) raw air is through filter AF01, after being held back, the corpuscular property impurity such as dust that contain in gas enter rear class separation system, this strainer, as known technology is described, can be the strainer of arbitrary form, comprises the strainer that can adopt complex method, automatically cleaning form;
(2) gas is sent into the device A B01 that boosts after filtering, the device A of boosting B01 enters membrane separation apparatus after air is boosted to the pressure that at least can overcome membrane separation apparatus high-tension side resistance, membrane separation apparatus can be grouped into n group, evenly accept raw air, n organizes the infiltration side joint vacuum pump of membrane separation apparatus in parallel, from vacuum pump outlet output oxygen-rich air, membrane separation apparatus can adopt valve V0n1, V0n2 isolation;
(3) typical, when operating ambient temperature low, as in winter operation or evening temperature compared with normal design temperature when low, as temperature is down to freezing point, now, conventionally because inlet air temperature is low, the infiltration capacity of film significantly reduces, as system is not made to any change, the vacuum tightness of vacuum pump inlet can continue to rise, this will cause vacuum pump overcurrent, and system will be shut down because of protection, and this is obviously inappropriate concerning a stove oxygen-rich combustion-supporting system;
Now, if kiln needs can accept stable flow in other words, but allow lower oxygen-enriched purity, so, can be by opening V102 variable valve to certain aperture, by introducing a part of normal air (containing oxygen approximately 21%), with the inlet pressure of holding vacuum pump, the oxygen enrichment flow that can keep vacuum pump outlet is substantially constant and be only purity drop;
Now, if kiln needs can accept stable purity in other words, but allow the oxygen enrichment of lower flow, so, can be by opening V101 variable valve to certain aperture, oxygen enrichment (containing oxygen approximately 30%) by introducing vacuum pump pump discharge is with the inlet pressure of holding vacuum pump, and the oxygen-enriched purity that can keep vacuum pump outlet is substantially constant and be only that rate of discharge declines;
(4) typical, when operating ambient temperature is high, as in summer operation or the normal design temperature of temperature correction at noon when high, as temperature rises to 45 ℃, now, conventionally because inlet air temperature is high, the infiltration capacity of film significantly increases, the vacuum tightness meeting continuous decrease of vacuum pump inlet, vacuum pump outlet will be discharged more low-purity but the larger oxygen enrichment of flow, if not any change in addition, this will cause follow-uply with gas point pressure, continue rising and causing the excessive and overcurrent of vacuum pump back pressure, system also will be shut down because of protection, this is obviously inappropriate concerning a stove oxygen-rich combustion-supporting system, now, by V103 variable valve, oxygen enrichment is emptying, continuous operation that can holding vacuum pump, stable supply follow-up with gas point regime flow the oxygen enrichment of purity drop,
(5) at vacuum pump, start, shut down, or during in normal course of operation as because of situations such as client's gas consumption minimizings, also can avoid calmly overload, overcurrent even to cause the situations such as accident, frequent shutdown by above-mentioned regulating loop, typically, while starting as vacuum, can, by opening V102, V103, open the bypass of vacuum pump, avoid starting overload, shut down also right; When reduced by the interim gas consumption of client, can open V101 circulation by this loop and return, or directly open V103 emptying, thereby can avoid interim overcurrent, even shutdown.
The present invention is by a regulating loop in parallel with vacuum pump, also can automatically adjust by the pressure of continuous monitoring vacuum pump inlet, when envrionment temperature is reduced to when low compared with design load, by automatically adjusting the variable valve on this loop, as the oxygen enrichment returning with air or circulation compensates the inlet pressure of vacuum pump, Indirect method transmembrane pressure ratio, thereby can obtain stable oxygen-enriched purity or stable oxygen enrichment flow; When envrionment temperature is increased to when high compared with design load, by adjusting the variable valve on this loop, intrasystem unnecessary gas is led to system outside emptying, thereby can, by because temperature variation causes the fluctuation of purity or flow to eliminate or be relieved to be met in the scope that oxygen-enriched combustion-supporting requires, keep the stable of vacuum pump operation.
And, can be by the design's loop, when vacuum pump starts, can be by opening V102, the loop that V103 forms, the load reduction that vacuum pump is started, when follow-up terminal use gas point gas consumption changes, also can make purity or the flow of the oxygen-rich air that obtains more stable relative to existing technologies by method of the present invention, especially comparatively stable when variation of ambient temperature, power-equipment is operated steadily, and, method of the present invention has solved the key technical problem that oxygen-enriched combusting requisite oxygen agent is provided with membrane separating method with relatively inexpensive laid down cost, strengthened the stability of system, the total efficiency of raising system operation.
Priority application of the present invention provides oxygenant in constituent of air membrane sepn process for stove oxygen-enriched combustion-supporting, but disclosed fundamental principle can be used for a lot of other separated occasions.By method of the present invention, can realize separation, the separation of titanium dioxide carbon/nitrogen gas, the separation of hydrogen/nitrogen and olefin/paraffin separated of separation that separated representative instance comprises oxygen/nitrogen, gas drying, carbonic acid gas/methane.
Separation factor mentioned herein, as oxygen nitrogen separation factor, it is commonly defined as:
α (alpha) value, oxygen nitrogen separation factor=(Q
n2/ Q
o2)
Q in formula
n2and Q
o2be respectively under unit time, pressure pure component nitrogen and oxygen by the infiltration capacity of certain films material.
specific examples:
A board-like membrane separation apparatus that adopts Shanghai YvonneDa Fu material Science and Technology Ltd. separation membrane to produce, design unimodule oxygen enrichment flow 5000Nm
3/ hr, can be by commercially available acquisition, and the separation factor of the oxygen nitrogen separation membrane material that this separator adopts under 25 ℃ of conditions is 2.044, and oxygen penetration is 5.068 Nm
3/ hrbarm
2, nitrogen infiltration capacity is 2.479 Nm3/hrbarm
2, 5000Nm
3/ hr. unimodule separator has adopted 1381.1 m altogether
2mould material, design selection 21352.9 Nm at a set of 25 ℃
3the vacuum pump of/hr pumping speed has been obtained the rich 5256.2Nm of 29.61% purity under 25 ℃ of conditions
3/ hr, meets the requirement of user's oxygen-enriched combusting:
During actual motion, vacuum pump and separator are all under constant condition, and when envrionment temperature reaches 3 ℃ of conditions, because temperature declines, the infiltration capacity of film declines to a great extent to 4014.5 Nm
3/ hr, this will directly cause vacuum pump overcurrent, system-down, although separating pressure ratio rises to 4.6 under this separate condition, oxygen-enriched purity can rise to 31.44%, because vacuum pump overcurrent will cause system-down, can not meet the requirement of user's oxygen-enriched combusting:
| Envrionment temperature | 3.0 | ℃ |
| Ambient moisture | 70.0% | |
| Operation ground height above sea level | 100.0 | m |
| Operation ground normal atmosphere | 100.1 | KPa |
| Oxygen penetration | 3.871 | Nm 3/hr.bar.m 2 |
| Nitrogen infiltration capacity | 1.678 | Nm 3/hr.bar.m 2 |
| Separation factor | 2.307 | |
| Empty oxygen ratio | 10.0 | |
| Total membrane area | 1381 | m 2 |
| Design separating pressure (absolute pressure) | 25.032 | KPa |
| Per-meate side flow (oxygen enrichment) | 4014.5 | Nm 3/hr. |
| Output pressure requirement | 1.0 | KPa |
| Total pressure head | 76.10 | KPa |
| The required pumping speed of actual motion ground pump | 18294.8 | m 3/hr. |
| Separating pressure ratio | 4.6 | |
| Oxygen purity | 31.44% |
From above-mentioned, the variation of envrionment temperature has caused oxygen enrichment flow 5256.2-4014.5=1241.7 Nm
3the minimizing of/hr, amplitude reaches 20%, and huge on the impact of system operation, will have a strong impact on combustion-supporting effect because of the great variety of the oxidizer flow rate that film oxygen enriching system provide in this extreme weather conditions as can be seen here;
As now adopted the present invention, by opening V102, supplement 1241.7 Nm
3the oxygen purity of/hr is 21% air, and film separating system cross-film separating pressure is than being still down under 4.2 following condition, the separable oxygen enrichment that goes out purity approximately 30.90%.
| Envrionment temperature | 3.0 | ℃ |
| Ambient moisture | 70.0% | |
| Operation ground height above sea level | 100.0 | m |
| Operation ground normal atmosphere | 100.1 | KPa |
| Oxygen penetration | 3.871 | Nm 3/hr.bar.m 2 |
| Nitrogen infiltration capacity | 1.678 | Nm 3/hr.bar.m 2 |
| Separation factor | 2.307 | |
| Input purity | 21.00% | |
| Output purity | 30.90% |
Under following condition when 3.0 ℃ of envrionment temperatures, unimodule membrane area 1381 m
2oxygen penetration is 4014.5 Nm
3/ hr.
| Envrionment temperature | 3.0 | ℃ |
| Ambient moisture | 70.0% | |
| Operation ground height above sea level | 100.0 | m |
| Operation ground normal atmosphere | 100.1 | KPa |
| Oxygen penetration | 3.871 | Nm 3/hr.bar.m 2 |
| Nitrogen infiltration capacity | 1.678 | Nm 3/hr.bar.m 2 |
| Separation factor | 2.307 | |
| Empty oxygen ratio | 10.0 | |
| Output purity | 30.90% | |
| Total membrane area | 1381 | m 2 |
| Design separating pressure (absolute pressure) | 25.032 | KPa |
| Per-meate side flow (oxygen enrichment) | 4014.5 | Nm 3/hr. |
| Output pressure requirement | 1.0 | KPa |
| Total pressure head | 76.10 | KPa |
Therefore, 1241.7 Nm
3/ hr oxygen level is 21% air and 4014.5 Nm
3the oxygen-rich air of/hr oxygen level 30.90% mixes can export 5256.2 Nm from vacuum pump outlet
3/ hr contains the oxygen-rich air of oxygen 28.56%, stability of flow, and it is few that purity declines, and can substantially meet the requirement of user's oxygen-enriched combusting.
Same, as now adopted the present invention, by opening V101, circulation is returned as 1241.7 Nm
3at least a portion oxygen enrichments such as/hr, vacuum pump is unlikely to overcurrent because obtaining certain pressure compensation, and the amount of oxygen that exports client terminal to is to have reduced, but that purity can be adjusted to is substantially constant.
Implementation method described above is only set forth key characters more of the present invention, professional and technical personnel will be appreciated that, although the present invention has carried out partly describing by reference to the accompanying drawings, but this is only an application example of the present invention or a kind of method, all other variations of not violating the essence of the present invention's elaboration also belong to category of the present invention, and scope of the present invention is limited by appending claims scope only.
Claims (3)
1. a membrane sepn method for supplying oxygen, is characterized in that, on the basis of existing membrane sepn oxygen system, increases a regulating loop in parallel with vacuum pump, the pressure of continuous monitoring vacuum pump inlet; When temperature reduces, by regulating loop, introduce the oxygen enrichment that vacuum pump outlet is returned in extraneous air or circulation, to adjust the vacuum tightness of vacuum pump inlet, and then adjust membrane separation apparatus transmembrane pressure ratio, thereby obtain the oxygen enrichment of stablizing purity or regime flow; When temperature raises, can pass through this regulating loop emptying; When system is normally moved, also can realize Low loading start up by this regulating loop, avoid vacuum pump overcurrent with steady running.
2. a membrane sepn oxygen system, specifically comprises:
(1) at least one strainer (AF01);
(2) at least one equipment that boosts (AB01), in order to boost to unstripped gas certain pressure; After this equipment that boosts also can be placed on membrane separation apparatus, in order to scavenge;
(3) at least one group of membrane separation apparatus (M0n), n=1,2 ... N, N is at least 1, and while organizing membrane separation apparatus, each is organized membrane separation apparatus and is connected in parallel more;
(4) at least one group of regulated valve (V0n1, V0n2), n=1,2, N, N is at least 1, when envrionment temperature is too high, for switching, isolate, regulating, enters the air to be separated of membrane separation apparatus (M0n) and the flow that enters vacuum pump from membrane separation apparatus per-meate side;
(5) pressure monitoring devices (PE01), in order to monitor vacuum pump inlet pressure;
(6) at least one vaccum-pumping equipment (AB02), in order to set up membrane separation apparatus both sides transmembrane pressure ratio;
It is characterized in that, also comprise:
(7) at least one regulating loop in parallel with vacuum pump, this regulating loop is by 3 variable valve (V101, V102, V103) form, wherein, the second variable valve (V102) from the outside introducing air of system to vacuum pump inlet, the first variable valve (V101) is introduced vacuum inlet by the oxygen-rich air circulation of vacuum pump outlet, the oxygen-rich air that the 3rd variable valve (V103) is vacuum pump outlet by internal system leads to system outside, the second variable valve (V102) accesses vacuum pump inlet with the tie point of the first variable valve (V101), the first variable valve (V101) accesses vacuum pump outlet with the tie point of the 3rd variable valve (V103),
(8) control and the topworks of vacuum pump inlet pressure feedback regulating and controlling valve (V101, V102, the V103) aperture monitoring with pressure monitoring devices (PE01).
3. the oxygen supplying control method based on membrane sepn oxygen system described in claim, is characterized in that, concrete operations are as follows:
(1) raw air, through filter (AF01), enters rear class separation system after the corpuscular property impurity such as dust that contain are held back in gas;
(2) gas is sent into the equipment of boosting (AB01) after filtering, boost after equipment (AB01) boosts to the pressure that at least can overcome membrane separation apparatus high-tension side resistance by air and enter membrane separation apparatus, membrane separation apparatus is grouped into n group, evenly accept raw air, n organizes the infiltration side joint vacuum pump of membrane separation apparatus in parallel, from vacuum pump outlet output oxygen-rich air, membrane separation apparatus adopts valve (V0n1, V0n2) isolation;
(3) when operating ambient temperature reduces,
If kiln needs or can accept stable flow, but allow lower oxygen-enriched purity, so, by opening the second variable valve (V102) to certain aperture, introduce a part of normal air, with the inlet pressure of holding vacuum pump, the oxygen enrichment flow that keeps vacuum pump outlet is substantially constant and be only purity drop;
If kiln needs or can accept stable purity, but allow the oxygen enrichment of lower flow, so, by opening the second variable valve (V101) to certain aperture, introduce the oxygen enrichment of vacuum pump pump discharge, with the inlet pressure of holding vacuum pump, the oxygen-enriched purity that keeps vacuum pump outlet is substantially constant and be only that rate of discharge declines;
(4) when operating ambient temperature raises, by opening the 3rd variable valve (V103), oxygen enrichment is emptying, the continuous operation of holding vacuum pump, stably supply with follow-up with gas point stability of flow the oxygen enrichment of purity drop;
(5) at vacuum pump, start, shut down, or while occurring in normal course of operation that client's gas consumption reduces situation, by above-mentioned regulating loop, avoid calmly overload, overcurrent even to cause accident, frequent shutdown situation, specifically comprise: while starting as vacuum, by opening the second variable valve (V102), the 3rd variable valve (V103), open the bypass of vacuum pump, avoid starting overload, shut down also right; When reduced by the interim gas consumption of client, by opening the first variable valve (V101), circulation is returned, or directly opens the 3rd variable valve (V103) emptying, thereby avoids interim overcurrent, even shutdown.
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| CN109381973A (en) * | 2017-08-09 | 2019-02-26 | 中国石油化工股份有限公司 | Modified embrane method petroleum vapor recovery packet control process |
| CN110078032A (en) * | 2019-05-23 | 2019-08-02 | 昆山伊普乐净化科技有限公司 | Formula nitrogen separating equipment for purification can be filtered with magnetic film |
| CN111594446A (en) * | 2020-05-14 | 2020-08-28 | 上海利方达真空技术有限公司 | Dynamic pressure accurate control system for continuous charging of working gas into low-vacuum system |
| CN114183694A (en) * | 2021-11-04 | 2022-03-15 | 北京卫星制造厂有限公司 | Gas circuit pressure regulating device |
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