CN202390202U - Device for supplying oxidant with stable flow and purity to oxygen-enriched combustion supporting of kiln - Google Patents

Abstract

The utility model belongs to the technical field of air separation and particularly provides a device for supplying an oxidant with stable flow and purity to oxygen-enriched combustion supporting of a kiln. The device comprises a membrane separator, an air filter, boost equipment, vacuum equipment and the like. According to the device provided by the utility model, a first heat exchanger is additionally arranged between the air filter and the boost equipment, and a corresponding adjusting valve is arranged between the air filter and the boost equipment; a second heat exchanger is arranged behind the vacuum equipment; the heat exchangers supply stable oxidant for the oxygen-enriched combustion supporting of the kiln according to the flow and the purity of stably-separated oxygen-enriched air by introducing low-grade heat energy, pre-heating raw material air and heating permeated air when the environment temperature is changed or fluctuates. The device sufficiently uses the heat energy of the waste gas, so as to reduce construction and operation costs. Meanwhile, the system stability can be enhanced, and the overall efficiency of the system is improved.

Description

A kind of device that the oxygenant of regime flow and purity is provided for the stove oxygen-enriched combustion-supporting

Technical field

The utility model belongs to the air separation technology field, is specifically related to a kind of device that adopts membrane oxygen enrichment technology that oxygenant is provided for the stove oxygen-enriched combustion-supporting.

Background technology

Oxygen enrichment is widely used in combustion-supporting and energy-saving and environmental protection such as various fuel oils, combustion gas, coal-fired furnace (glass, cement, pottery), various boiler, process furnace, incinerator, heating agent stove, hotblast stove, smelting furnace, aircraft engine, marine engine; Catalytic cracking, desulfurization, wastewater treatment, mover synergy, oxygen enrichment are made fields such as (coal) gas, each kinds of oxidation reaction, fermentation and are also used oxygen enrichment technology and obtained favorable economic benefit; In addition; Oxygen enrichment also number of applications relates to fields such as petrochemical industry, chemical industry, medicine, light industry, electric power, building materials, metallurgy, coal, communications and transportation, aquaculture and national defense and military in aspects such as health care, the ventilation of large-scale oxygen enrichment, plateau oxygenation, aquacultures.

Contain about 21% oxygen and 78% nitrogen in the air; Be that raw material extracts in the method for oxygen enrichment with the air, the method that the most extensively adopts in the industry is cryogenic rectification method and pressure swing adsorption process, but the oxygen enrichment system that these two kinds of methods make up all exists investment big; Power consumption is high; Technical sophistication need special messenger's operation, and working cost is higher; In addition; Also have such as oxygen separation methods such as electrolytic process, chemical methods; But because of it realizes oxygen separation with consume water, consumption chemical raw material; Exist raw material to obtain drawbacks difficult, aspects such as energy consumption is high, manufacturing cost is high, use cost height,, only adopt at some special occasions for industrial client can not accept.

Membrane oxygen enrichment technology is a kind of new separation method that grows up gradually from the end of the seventies; It utilizes the selection perviousness difference of organic polymer dense film to nitrogen, oxygen; When having pressure difference or pressure ratio in the film both sides; Fast gas of infiltration rate such as water vapor, hydrogen, helium, oxygen, carbonic acid gas etc. see through behind the film low-tension side enrichment at film in the mixed gas becomes oxygen-rich air (the oxygen nitrogen separation factor of looking mould material is different; Single-stage is separated can obtain the oxygen enrichment that purity is about 23-60%), and slow relatively gas such as nitrogen, argon gas, methane and the carbon monoxide etc. of infiltration rate 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 the oxygen enrichment extraction; Because of there is not phase transformation in it in separating spissated whole process; Normal temperature separates, and the negative pressure flow process separation system that especially makes up with board-like film has that equipment is simple, low cost of manufacture, energy consumption are little, output adjustable, start rapid, easy and simple to handle, the static operation of system, the high outstanding advantage of safety; It is a kind of separation method of economy; At present, adopt membrane separating method to produce oxygen enrichment and be widely used in fields such as oxygen-enriched combustion-supporting, oxygen enrichment ventilation, water treatment, especially be directed against the oxygen-enriched combustion-supporting of glass, metallurgy, cement rotary kiln, Industrial Boiler or the like Thermal Power Engineering Field; Because of the series of advantages that membrane separating method has, can be each energy unit a kind of relatively inexpensive, on-the-spot air supply method and extensively being adopted flexibly is provided.

Along with the research and development of separation membrane and the breakthrough of flow process; The organic membrane parting material isolating α of its oxygen nitrogen (alpha-acetol) value that is applied to air separation is mostly between 2～7; Can directly in air, obtain the oxygen of about 60% following purity; Adopt the system of multistage membrane sepn process can obtain purity even greater than 90% oxygen; Single with regard to constituent of air membrane sepn oxygen preparation, in case type selecting confirmed after the separating area and power-equipment of separation membrane, mould material, because of the intrinsic performance of parting material definite; The ability of power-equipment is definite, and the oxygen components that the membrane sepn process obtains in air is mainly relevant with the temperature of separated feeding air with the stability of flow.To an oxygen-enriched combustion-supporting system that might be applied under the various ambient temperature conditions; The envrionment temperature of different installation application occasions is different; Even same place is because of the envrionment temperature of spring, summer, autumn and winter is different, and the film separating system that oxygen is provided for the stove oxygen-enriched combustion-supporting produces huge variation because of flow, the oxygen purity of the oxygen-rich air that will be caused by the separated air temperature variations of different location, Various Seasonal separating.And obviously; Membrane sepn provides the flow of the oxygen system of oxygen-rich air, the stable effect that has directly determined the oxygen-enriched combustion-supporting process of purity; In a sense; If can not solve stable oxygenant method is provided, will receives serious restriction with the application of the oxygen-enriched combustion-supporting system of this separation method.

Summary of the invention

It is the basis with the membrane oxygen enrichment technology that the purpose of the utility model is to propose a kind of, produces the device of the oxygen rich gas of regime flow and purity, so that the response environment temperature variation, for the stove oxygen-enriched combustion-supporting provides flow and the stable oxygenant (oxygen rich gas) of purity.

Common membrane oxygen enrichment technology provides the device of the stable oxygenant (oxygen rich gas) of flow and purity as shown in Figure 3 for the stove oxygen-enriched combustion-supporting.When winter or envrionment temperature were lower, the oxygen permeable membrane flux reduced with temperature and reduces.Membrane separation process process for the vacuum pump of common use rated output; The pressure reduction of oxygen permeable membrane both sides will be with the reducing and increase of membrane flux, and oxygen concn can rise but the oxygen enriched product airshed can decline to a great extent so that influence the use of back segment oxygen rich gas in the oxygen enriched product gas like this.The present invention adopts furnace flue gas or other cheap thermal source that raw air is carried out thermal pretreatment, makes mould material separation of air under suitable temperature through temperature regulation, thereby obtains the oxygen enriched product gas of regime flow and purity.

The separation method that the utility model adopts is different from the simple barrier sepn process of prior art; Can effectively avoid the membrane sepn process in response to the oxygen enrichment component that causes adopting membrane sepn to be produced with variation of ambient temperature and the fluctuation of flow through reclaim using low-grade heat source to the method for raw air thermal pretreatment; Thereby making that be that the stove oxygen-enriched combustion-supporting provides and stablize oxygenant and carries out oxygen-enriched combustion-supporting with film separating system in low manufacturing cost, is a kind of simple, very suitable required oxygenant supply method of stove oxygen-enriched combustion-supporting process; Simultaneously, reduced oxygen rich gas and got into the required heat energy that heats up behind the kiln, the combustion-supporting effect of oxygen rich gas has been played promoter action through reclaim using low-grade heat source that oxygen enriched product gas is carried out heat treated.

But based on the method for the oxygenant of above-mentioned regime flow and purity, the utility model provides corresponding membrane separation unit.This membrane separation unit is that original membrane separation unit that is used to prepare oxygen enriched product gas is improved and obtains.Original membrane separation unit that is used to prepare oxygen enriched product gas, its structure is as shown in Figure 3, comprising: a kind of membrane separator M01, air filter AF01, the device A of boosting B01, vacuum apparatus AB02; Each membrane separator has a virgin gas inlet A0 at least, a retained gas outlet A1, an infiltration gas outlet A2; Separation membrane in the membrane separation apparatus (being separatory membrane) has been divided into both sides at least, and a side is the malleation side, and a side is a suction side; The malleation side also is the virgin gas side of membrane separation apparatus; Be also referred to as high-tension side, retained gas side, suction side also is the infiltrating gas side of membrane separation apparatus, is also referred to as low-tension side, suction side; Air filter AF01, the device A of boosting B01 connect the back successively through pipeline and are connected with the virgin gas inlet A0 of membrane separator M01; Vacuum apparatus AB02 is connected with the infiltration gas outlet A2 of membrane separator M01 through pipeline; The improvements of this device are; At air filter AF01 and boost and set up the first interchanger TC01 between the device A B01; And between the air filter AF01 and the first interchanger TC01, valve V02 is set; At air filter AF01 and boost valve V01 is set between the device A B01, between the virgin gas inlet A0 of boost device A B01 and membrane separator M01, temperature monitor TE01 is set; The second interchanger TC02 is set after vacuum apparatus AB02.The first interchanger TC01 is through introducing low grade heat energy, preheating material air; The second interchanger TC02 is through introducing low grade heat energy, adds thermoosmosis gas (promptly separate oxygen rich gas), and it is combustion-supporting to send into stove as oxygenant.Specifically see shown in Figure 1.

In this device, also can the second interchanger TC02 be connected with the first interchanger TC01, respectively infiltration gas (promptly separate oxygen rich gas) be heated with raw air through introducing stove flue hot gas (waste gas).Specifically see shown in Figure 2.

In this device; Raw air filters out impurity such as dust through air filter AF01; AF01 can be various forms of strainers, comprises fibers form, filtrate form, bag type filtering, but preferably adopts the strainer of automatically cleaning form or various array configurations; Be used to filter, clean the raw air that gets into membrane separation apparatus, guarantee the degree of cleaning requirement of membrane separation apparatus raw air.

Raw air after the filtration is divided into two portions, and a part is through the direct air inlet of valve V01, and a part is mixed with fore portion gas after valve V02 gets into interchanger TC01 elevated temperature; When needs are regulated the raw air temperature, can realize through adjusting V01, V02 aperture; V01, V02 can be various forms of valves; Like various manual, automatic controls, the stopping valve of regulating, butterfly valve, gate valve etc., preferably adopt various forms of program control variable valve, can be air operated, electronic, liquid-operated; Be used to switch, regulate and treat that separation of air gets into membrane separation apparatus fluid before and distributes; Wherein, if program control regulated valve, they can according to predefined logic open or close and according to the temperature of monitoring carry out flow, control of purity is regulated; These valves can be pneumatic controls, also can be self-acting valves electronic, hydrostatic control.

Filter and temperature adjustment after air boost through the device A B01 that boosts, the device A of boosting B01 can be various forms of gas booster compressors, like piston-type, centrifugal, screw rod, vortex, Roots, pendular ring or the like compressed format, gas is boosted to suitable pressure.

Air after the filtration through after get into membrane separation apparatus from the A0 of membrane separation apparatus M01 inlet the malleation side; In membrane separation apparatus; Gas through a part behind the membrane sepn be penetrated into low-tension side, the per-meate side enrichment becomes oxygen enrichment to export from A2, in addition a part of enrichment the oxygen deprivation nitrogen-rich gas that is difficult to permeate then be excluded out membrane separation apparatus from being detained side outlet A1, M01 can be board-like film; Rolled film, hollow-fibre membrane; Low-tension side provides power by vacuum apparatus AB02; Vacuum apparatus AB02 can be various forms of like piston-type, centrifugal, screw rod, vortex, Roots, pendular ring etc., and the membrane separation apparatus suction side is decompressed to the required separating pressure of separator and overcomes the resistance that follow-up fluid is carried.

Before vacuum apparatus AB02 output oxygen rich gas entering kiln is combustion-supporting, can pass through interchanger TC02 elevated temperature; Wherein temperature parameter can be implemented monitoring by temperature monitor TE01; Interchanger TC01, interchanger TC02 can be various forms of interchanger, like shell and tube, and plate-fin etc.; Interchanger TE01 is used to monitor the gas temperature that gets into membrane separation apparatus, can be installed in the optional position that all can reflect the gas temperature that gets into membrane separation apparatus in real time, can be resistance-type, electric thermo-couple temperature sensing or temperature monitoring conditioning equipment.

Be convenient membrane separation apparatus and the membrane sepn oxygen preparation of explaining the membrane sepn process, lexical or textual analysis is following:

Shown in accompanying drawing 3, M01 be a kind of 3 mouthfuls of membrane separators, each membrane separator is at least by 1 virgin gas inlet A0; 1 retained gas outlet A1,1 infiltration gas outlet A2 forms, and the separation membrane in the membrane separation apparatus has been divided into both sides at least; One side is the malleation side, and a side is a suction side, and the malleation side also is the virgin gas side of membrane separation apparatus; Be also referred to as high-tension side, retained gas side, suction side also is the infiltrating gas side of membrane separation apparatus, is also referred to as low-tension side, suction side.

It shown in accompanying drawing 3 process that the membrane sepn of prior art is produced oxygen-rich air; Wherein, Gas filters out the impurity malleation sides that the back gets into membrane separation apparatus from the virgin gas inlet A0 of membrane separation apparatus after the device A B01 that boosts boosts such as dust through AF01; In membrane separation apparatus; Gas through a part behind the membrane sepn be penetrated into low-tension side, the per-meate side enrichment becomes oxygen enrichment from permeating gas outlet A2 output, in addition a part of enrichment the oxygen deprivation nitrogen-rich gas that is difficult to permeate then be excluded out membrane separation apparatus from being detained side outlet A1.To the membrane sepn process of separating oxygen enrichment in air, general, it is more relevant than the ratio (being called sky oxygen ratio) of (being called the separating pressure ratio) and virgin gas and oxygen enriched product gas with the absolute pressure of suction side through membrane separation apparatus malleation side with oxygen nitrogen separation factor (being called alpha value), the gas of separation membrane that membrane sepn is produced the purity of oxygen; Oxygen nitrogen separation factor is high more, means than under to isolate more highly purified oxygen rich gas at lower separating pressure ratio and littler empty oxygen, to identical separation membrane; Separating pressure is higher than more, can obtain more highly purified oxygen enrichment, and empty oxygen is bigger than more; 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 the temperature and the pressure of unstripped gas; To identical separation membrane, separation temperature is high more, and infiltration capacity is big more; Separating pressure is high more, and infiltration capacity is big more.

Therefore, when adopting different separation systems, have different separation mechanisms; The purpose of the power-equipment that is provided with is also different, and as adopting in the membrane sepn process that rolling or board-like separator carry out, mainly fresh air is provided is main purpose to the device A of boosting B01 to satisfy; Overcome the resistance that fluid is carried, typical, adopt rolling diaphragm separator; 1～the 10KPa that boosts, preferred, 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 set up tens of blast to the hundreds of handkerchief, and more having the device A B01 that boosts is placed on after the board-like film way as the exhaust gas emission blower fan, purpose also only is in order to overcome resistance that raw air gets into membrane separation apparatus so that the purpose of fresh air constantly to be provided.Simultaneously, vacuum apparatus AB02 is a main purpose to satisfy the required pressure ratio of separation mainly then, and the separating pressure ratio of promptly setting up the skinning both sides is 3～10; More typical, rolled film, the board-like film made at 2～3 separation membrane at the alpha value that adopts parting material are when required oxygen-enriched purity is 30% left and right sides; The separating pressure ratio that need set up the skinning both sides approximately is about 4, that is, be the blast of 2～5KPa like the malleation wall pressure of film; Absolute pressure is normal atmosphere (101.325 KPa)+(2～5KPa); Then suction side should be set up the absolute pressure of the about 25kpa vacuum tightness of 75KPa gauge pressure (be equivalent to-), and like this, separating pressure is than being 4 times of [101.325+ (2～5KPa)]/25 ≌; Can obtain about 30% oxygen-enriched purity; Obviously, in this process, the device A of boosting B01 is for keeping separating pressure than being about 4 to provide the blast of fresh air more limited than contributing to separating pressure; Be main to satisfy the required resistance that overcomes of conveying only, the vacuum power of about 25kpa that vacuum apparatus AB02 provides is only the major impetus source of satisfying the separating pressure ratio.

And carry out with hollow-fibre membrane in the oxygen nitrogen separating process another kind of, typical, boost like the employing device A B01 that boosts; Its effect the more important thing is in order to obtain to separate required absolute pressure then not only in order to overcome the resistance of membrane separation apparatus M01, is improved the separating pressure ratio of film both sides; Common way can only boost to suitable pressure with the device A B01 that boosts, and after keeping separating required pressure ratio, omits vacuum apparatus AB02; Typically, when the hollow fiber membrane separator of making at 5～7 separation membrane at the alpha value that adopts parting material separates, when required oxygen-enriched purity is 30～60% left and right sides; The separating pressure ratio that need set up the skinning both sides approximately is more than 4, that is, be the pressure of 300～1300KPa like the malleation wall pressure of film; Absolute pressure is that normal atmosphere (101.325 KPa)+(400～1300KPa), suction side or per-meate side then only need keep normal atmosphere discharging (vacuum tightness that is equivalent to 0 KPa gauge pressure), like this; Separating pressure can obtain about 30～60% oxygen-enriched purity than for 4～14 times of [101.325+ (300～1300KPa)]/101.325 ≌, obviously; In this process; The device A of boosting B01 is that fresh air is provided about 4～14 times for keeping the separating pressure ratio, and to the separating pressure that keeps sepn process compared with conclusive effect, not only to carry the required resistance that overcomes be main to satisfy; After satisfying the required absolute pressure ratio of separation, vacuum apparatus AB02 then need not to be provided with because of only keeping normal pressure.

Simultaneously, no matter adopt which kind of membrane separation apparatus form, a membrane sepn oxygen preparation all need satisfy suitable empty oxygen ratio; To avoid the concentration polarization phenomenon, popular saying promptly is to need to satisfy constantly to separate required fresh air, and air quantity is looked the alpha value of parting material and required oxygen-enriched purity requirement; Typically, like the rolled film made from the separation membrane of alpha value 2～3, board-like film, in order to obtain the oxygen enrichment about 30%; Typically, get into the required air quantity of membrane separation apparatus M01 through the device A B01 that boosts and be approximately 8～20 times of oxygen-rich air flow, more typical; Be 10～15 times of required oxygen enrichment flow, and for example hollow-fibre membrane is typical; Like the hollow-fibre membrane made from the separation membrane of alpha value 5～7,, typical in order to obtain the oxygen enrichment about 30%; Get into the required air quantity of membrane separation apparatus M01 through the device A B01 that boosts and be approximately 2～5 times of oxygen-rich air flow, more typical, be 2.5 times of required oxygen enrichment flow; The purity that needs is high more, requires big more at the constant space-time oxygen ratio of other conditions.

Like accompanying drawing 3, with reference to above-mentioned, the professional and technical personnel can understand; Virgin gas gets into membrane separation apparatus M01 separated waste gases through the device A B01 that boosts to be got rid of from A1, and oxygen enrichment is collected to send into through AB02 and used the gas point, in order to obtain stable oxygen purity, oxygen flow; In this process because of type selecting confirmed to boost air quantity, the blast of device A B01; The air quantity of AB02, blast, also type selecting has been confirmed membrane separation apparatus M01, the oxygen nitrogen separation factor of its parting material and separating area are all definite; When the applied environment temperature variation, will change according to following trend:

When 1, envrionment temperature raise, the temperature that gets into membrane separation apparatus raise, and will strengthen to its infiltration capacity of membrane separation apparatus of confirming area and material assertive evidence characteristic; Simultaneously, the rising of separation temperature also will cause the decline of separation factor; What is more important because the increasing of infiltration capacity, can not satisfy the pumping speed of the vacuum pump AB02 that directly causes being provided with to be drawn into predetermined separating pressure; The reduction of the oxygen-enriched purity that this all will cause separating, simultaneously, the oxygen enrichment flow of separating will rise;

When 2, envrionment temperature descended, the temperature that gets into membrane separation apparatus descended, and will reduce to its infiltration capacity of membrane separation apparatus of confirming area and material intrinsic property, simultaneously; The decline of separation temperature, separation factor will increase, but what is more important; Because reducing of infiltration capacity is excessive with the pumping speed of the vacuum apparatus AB02 that directly causes being provided with, until surpassing predetermined separating pressure; The rising of the aforementioned oxygen-enriched purity that these all will cause separating, but simultaneously, total oxygen enrichment flow of separating will descend.

More than, because the change of envrionment temperature will directly cause all producing significantly fluctuation for oxygen enrichment flow and purity that the oxygen-enriched combustion-supporting system provides the film separating system of oxygenant to produce, be unfavorable for carrying out oxygen-enriched combustion-supporting.

The utility model is just in order to address the above problem; Propose a cover and installed the film separating system that inlet air temperature compensates additional; Shown in accompanying drawing 1, can exchange the low grade heat energies such as waste gas that kiln burning produces through interchanger when getting into and obtain stable virgin gas separation temperature, under all constant situation of other separation condition because of virgin gas; As typically; Air quantity, the blast of the device A of boosting B01, the pumping speed of vacuum apparatus AB02, vacuum tightness, the parting material of membrane separation apparatus is confirmed and separating area is confirmed; Under the condition that these conditions are all confirmed in front; The present invention can avoid flow, the oxygen purity of the oxygen-rich air that film separating system causes because of variation of ambient temperature (envrionment temperature of different installation application occasions is different, even same place is different because of the envrionment temperature of spring, summer, autumn and winter) to produce huge variation, and this variation is eliminated or being relieved in the scope that meets the oxygen-enriched combustion-supporting requirement:

1, raw air is through strainer AF01; The corpuscular property impurity such as dust that contain in the gas are held back the back get into back level separation system; This strainer can be the strainer of arbitrary form as known technology is described, comprises the strainer that can adopt complex method, automatically cleaning form;

2, gas can divide two-way to send into the device A B01 that boosts after filtering, and one the tunnel directly sends into from V01; Other one the tunnel sends into interchanger TC01 from V02 carries out sending into after the heat exchange, and two bypasses are regulated flow with variable valve V01, V02 respectively, regulates through the Temperature Feedback that receives the TE01 monitoring; With the stable gas temperature that gets into membrane separation apparatus, keep the gas temperature that gets into the device A B01 that boosts and tend towards stability, typical; When operating ambient temperature low; As moving in winter, temperature is reduced to-20 ℃, can be through reducing the circulation of variable valve V01; The circulation that strengthens variable valve V02 realizes stable virgin gas temperature with preheating of air, finally guarantees the flow of oxygen-rich air and the stablizing of purity of separation system outlet;

3, simultaneously, preferred but non-essentially carry out an oxygen-rich air preheating, from the oxygen-rich air of vacuum apparatus AB02 outlet output preferentially with low grade heat energies such as interchanger TC02 exchange stove waste gas with the preheating oxygen enrichment;

4 and, typical adopt the utilizing on the mode of low grade heat energy at one, preferably exchange the heat energy from waste gas that the kiln chimney is discharged, and, like accompanying drawing 2, at first with countercurrent direction preheating oxygen enrichment again with countercurrent direction preheating material air.

Different with prior art; Through temperature stabilizer system to raw air; The present invention can continous-stable obtain oxygen rich gas with membrane separating method, its purity, the relative prior art of flow are comparatively stable when variation of ambient temperature, and; Method of the present invention has fully reclaimed heat energy from waste gas; Solve the key technical problem that the required oxygenant of oxygen-enriched combusting is provided with membrane separating method with simple method, relatively inexpensive laid down cost and running cost, not only strengthened the stability of system, also improved system total efficiency.

The utility model priority application is that oxygen-enriched combusting provides oxygenant in constituent of air membrane sepn process, but disclosed fundamental principle can be used for much other separation occasions.Can realize that through method of the present invention isolating representative instance comprises the separation, gas drying, the separation of carbonic acid gas/methane, separation, the separation of hydrogen/nitrogen and the separating of olefin/paraffin of titanium dioxide carbon/nitrogen gas of oxygen/nitrogen.

Shown in accompanying drawing 1, a complete membrane sepn process synoptic diagram which comprises at least:

1, at least one strainer AF01;

2, at least two are connected on AF01 parallelly connected flow cycle afterwards; Wherein, the one tunnel only forms another road by variable valve V01 with necessary connecting tube; TC01 forms with necessary connecting tube by variable valve V02 serial connection heat exchanger, and two bypasses compile parallel-series and connect the device A B01 that boosts;

3, at least one device A B01 that boosts is in order to boost to virgin gas certain pressure;

4, at least one temperature monitoring equipment TE01, in order to monitoring virgin gas temperature, control V01, the control of V02 aperture and topworks preferred but inessential comprising with this Temperature Feedback;

5, at least one group of membrane separation apparatus M01, they can be connected in parallel or be connected in series;

6, the device A B02 that boosts;

7, preferred but non-essential interchanger TC02 is used to exchange heat energy from waste gas preheating oxygen-rich air;

8, like known technology, system also need comprise the necessary control assembly so that system dynamic equipment can move, by-pass valve control can switch etc. as requested.

The said separation factor of this paper like oxygen nitrogen separation factor, is defined as as the one of which:

α (alpha-acetol) value, oxygen nitrogen separation factor=(Q N2/Q O2)

Q N2 and Q O2 are respectively under unit time, the pressure pure component nitrogen and oxygen through the infiltration capacity of certain films material in the formula.

Description of drawings

Fig. 1 is the device diagram of utilizing the stove low grade heat energy and oxygenant being provided for the stove oxygen-enriched combustion-supporting with the membrane oxygen enrichment technology.

Fig. 2 is the device diagram of utilizing stove stack gas heat energy and oxygenant being provided for the stove oxygen-enriched combustion-supporting with the membrane oxygen enrichment technology.

Fig. 3 provides the device diagram (prior art) of oxygenant for adopting membrane oxygen enrichment technology for the stove oxygen-enriched combustion-supporting.

Embodiment

Embodiment 1

One uses Oxylead Plate membrane separator provided for the cement kiln enriched combustion oxidant system designed for a single membrane separator plate assembly oxygen flow 5000Nm3/hr., Oxylead Membrane separator plate by the Shanghai Industrial Miho Sugimoto Co., Ltd., can be obtained commercially, is used in the separation of oxygen and nitrogen separation membrane material under the conditions at 25 ℃ separation factor of about 2.05, the oxygen permeation amount of 5.068 Nm3/hr.bar.m2, permeation amount of nitrogen 2.479 Nm3/hr.bar.m2, 5000Nm3/hr. single component separator uses a 1381 m2 membrane material, in this case the design chosen 20 ℃ under 22186 Nm3/hr pumping speed of the vacuum pump, at 25 ℃ under the conditions obtained 29.61 % purity oxygen 5256.2 Nm3/hr: <tables num="0001"> <table > <tgroup cols="3"> <colspec colname =" c001 "colwidth =" 48% " /> <colspec colname="c002" colwidth="19%" /> <colspec colname =" c003 "colwidth =" 31% " /> <tbody > <row > <entry morerows="1"> design ambient temperature </entry> <entry morerows = "1"> 25.0 </entry> <entry morerows="1"> ℃ </entry> </row> <row > <entry morerows = "1 "> Design Environment Humidity </entry> <entry morerows="1"> 70.0% </entry> <entry morerows="1"> </entry> </row> < row > <entry morerows="1"> run to altitude </entry> <entry morerows="1"> 100.0 </entry> <entry morerows =" 1 "> m </entry> </row> <row > <entry morerows="1"> run to atmospheric pressure </entry> <entry morerows =" 1 "> 100.1 </entry> <entry morerows="1"> KPa </entry> </row> <row > <entry morerows = "1"> oxygen permeation amount </entry> <entry morerows="1"> 5.068 </entry> <entry morerows="1"> Nm3/hr.bar. m2 </entry> </row> <row > <entry morerows="1"> nitrogen permeation </entry> <entry morerows="1"> 2.479 </entry> <entry morerows="1"> Nm3/hr.bar.m2 </entry> </row> <row > <entry morerows = "1"> membrane material separation factor </entry> <entry morerows="1"> 2.05 </entry> <entry morerows="1"> </entry> </ row > <row > <entry morerows="1"> empty oxygen ratio </entry> <entry morerows="1"> 10.0 </entry> <entry morerows = "1"> </entry> </row> <row > <entry morerows="1"> separation pressure ratio requirements </entry> <entry morerows = "1"> 4.0 </entry> <entry morerows="1"> </entry> </row> <row > <entry morerows =" 1 "> Design Oxygen purity </entry> <entry morerows="1"> 29.43% </entry> <entry morerows="1"> </entry> </row> <row > <entry morerows="1"> single-component membrane area </entry> <entry morerows="1"> 1381 </entry> <entry morerows="1"> m2 </entry> </row> <row > <entry morerows="1"> design separation pressure (absolute pressure) </entry> <entry morerows="1"> 25.032 </entry> <entry morerows="1"> KPa </entry> </row> <row > <entry morerows="1"> permeate side flow (oxygen) </entry> <entry morerows="1"> 5256.2 </entry> <entry morerows = "1"> Nm3/hr. </entry> </row> <row > <entry morerows="1"> output pressure requirements </entry> <entry morerows = "1"> 1.0 </entry> <entry morerows="1"> KPa </entry> </row> <row > <entry morerows = "1"> Total pressure </entry> <entry morerows="1"> 76.10 </entry> <entry morerows="1"> KPa </entry> </row> <row > <entry morerows="1"> run to vacuum pumping speed requirements </entry> <entry morerows = "1" > 21025.0 </entry> <entry morerows="1"> Nm3/hr. </entry> </row> <row > <entry morerows = "1 "> Selection pumping speed (20 ℃) </entry> <entry morerows="1"> 22564.4 </entry> <entry morerows="1"> Sm3/hr. </entry> </row> <row > <entry morerows="1"> actual operation to pump pumping speed </entry> <entry morerows = "1 "> 22186.0 </entry> <entry morerows="1"> m3/hr. </entry> </row> <row > <entry morerows =" 1 "> actual separation pressure ratio </entry> <entry morerows="1"> 4.2 </entry> <entry morerows="1"> </entry> </row> <row > <entry morerows="1"> actual oxygen purity </entry> <entry morerows="1"> 29.61% </entry> <entry morerows = "1"> </entry> </row> </tbody> </tgroup> </table> </tables>

When envrionment temperature drops under 8 ℃ of conditions, still adopt 20 ℃ of vacuum pumps of 22186 Nm3/hr pumping speed down, membrane separation apparatus does not change, and under 8 ℃ of conditions, has only obtained oxygen enrichment 4444.6 Nm3/hr of 31.31% purity;

Envrionment temperature	8.0	℃
			Ambient moisture	70.0%
Operation ground height above sea level	100.0	m
			Operation ground normal atmosphere	100.1	KPa
Oxygen penetration	4.143	Nm3/hr.bar.m2
			The nitrogen infiltration capacity	1.860	Nm3/hr.bar.m2
The mould material separation factor	2.227
			Empty oxygen ratio	10.0
The unimodule membrane area	1381	M2
			Separating pressure (absolute pressure)	22.447	KPa
Per-meate side flow (oxygen enrichment)	4444.6	Nm3/hr.
			The output pressure requirement	1.0	KPa
Total pressure head	78.68	KPa
			Actual motion ground pump pumping speed	22186.0	M3/hr.
Pressure ratio is checked	4.9
			Oxygen purity	31.31%

By above-mentioned visible; The variation of envrionment temperature has caused the minimizing of oxygen enrichment flow 5256.2-4444.6=811.6 Nm3/hr; Amount of decrease reaches 15.4%, explains that the influence that system is moved is huge, especially is reduced to-20 ℃ in extreme weather conditions such as envrionment temperature; Under-40 ℃ even the lower condition, the great variety of the oxidizer flow rate that will provide because of the film oxygen enriching system and have a strong impact on combustion-supporting effect.

Through after the above-mentioned analysis, the technology shown in accompanying drawing 2 is adopted in this case, will divide 2 bypass air inlets for the supply raw materials inlet mouth of the device A B01 (gas blower) that boosts of gas of membrane separation apparatus; And variable valve V01, V02 have been installed respectively, and the interchanger TC01 that in the bypass of install adjustment valve V02, connected, exchange is from the heat energy from waste gas of flue gas; And the oxygen enrichment of seeing off to vacuum apparatus AB02 (vacuum pump) has also carried out preheating, and interchanger TC02 as shown in the figure has been installed; And flue gas at first gets into interchanger TC02 with countercurrent direction preheating oxygen-rich air, gets into interchanger TC01 again with the countercurrent direction preheated air; Under extreme low temperature conditions such as winter, open big variable valve V02, reduce the circulation of variable valve V01, regulate V01, V02 automatically through the feedback of device for detecting temperature TE01; With the stable virgin gas temperature that gets into membrane separation apparatus; Obtained the oxygen-rich air of regime flow, and, because of having carried out preheating to oxygen enrichment from AB02 output; Better meet oxygen-enriched combustion-supporting, obtained great economic benefit.

Above described implementation method only set forth key characters more of the present invention; The professional and technical personnel will be appreciated that; Although the present invention combines accompanying drawing to carry out partly describing; But this only is an application example of the present invention or a kind of method, and all other variations of not violating the essence of this patent elaboration also belong to category of the present invention, and scope of the present invention is limited by the appending claims scope only.

Claims (2)

1. one kind for the stove oxygen-enriched combustion-supporting provides the device of the oxygenant of regime flow and purity, comprising: a kind of membrane separation apparatus M01, air filter AF01, the device A of boosting B01, vacuum apparatus AB02; Each membrane separation apparatus has a virgin gas inlet A0 at least, a retained gas outlet A1, an infiltration gas outlet A2; Separatory membrane in the membrane separation apparatus is divided into both sides at least, and a side is the malleation side, and a side is a suction side; Air filter AF01, the device A of boosting B01 connect the back successively through pipeline and are connected with the virgin gas inlet A0 of membrane separator M01; Vacuum apparatus AB02 is connected with the infiltration gas outlet A2 of membrane separator M01 through pipeline; It is characterized in that:

At air filter AF01 and boost and set up the first interchanger TC01 between the device A B01; And between the air filter AF01 and the first interchanger TC01, variable valve V02 is set; At air filter AF01 and boost variable valve V01 is set between the device A B01, between the virgin gas inlet A0 of boost device A B01 and membrane separator M01, temperature monitor TE01 is set; The second interchanger TC02 is set after vacuum apparatus AB02; The first interchanger TC01 is used to introduce low grade heat energy, the preheating material air; The second interchanger TC02 is used to introduce low grade heat energy, adds thermoosmosis gas, and it is combustion-supporting to send into stove as oxygenant.

2. according to claim 1 it is characterized in that: the second interchanger TC02 is connected with the first interchanger TC01 for the stove oxygen-enriched combustion-supporting provides the device of the oxygenant of regime flow and purity, is used to introduce stove flue hot gas heating infiltration gas and raw air.

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