CN100567810C - Be used to produce the method and apparatus of the steam that is suitable for the oxygen burning - Google Patents
Be used to produce the method and apparatus of the steam that is suitable for the oxygen burning Download PDFInfo
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- CN100567810C CN100567810C CNB2005800232436A CN200580023243A CN100567810C CN 100567810 C CN100567810 C CN 100567810C CN B2005800232436 A CNB2005800232436 A CN B2005800232436A CN 200580023243 A CN200580023243 A CN 200580023243A CN 100567810 C CN100567810 C CN 100567810C
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/003—Methods of steam generation characterised by form of heating method using combustion of hydrogen with oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
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Abstract
The present invention relates to a kind of boiler (30) that is suitable for the oxygen burning, comprising: combustion chamber (31), water preheater (33) and evaporimeter (38,40), wherein combustion chamber is made up of water preheater (33) at least in part.The invention still further relates to a kind of oxygen combustion method that produces hot water, comprise the liquid that cold water is heated into heat with the oxygen combustion flame.Method of the present invention preferably uses device of the present invention to implement.
Description
Technical field
Theme of the present invention relates to the method that a kind of generation is suitable for the steam of oxygen burning (oxycombustion), that is, a kind of generation is suitable for as the oxygen of oxidant or is rich in the air of oxygen and the method for the steam of the burning of fossil fuel.Theme of the present invention also relates to the device of implementing this method.
Background technology
The burning of use oxygen or oxygen burning are current being used for to continue to use fossil fuel and limit CO
2Enter one of the most noticeable mode in the atmosphere.In fact, the burning of these fuel and air causes forming CO
2, described CO
2Highly watered down in the nitrogen of combustion air, this forms a significant inertia matter (ballast): this CO usually
2Only account for the 10-15% of combustion product.CO
2To reinject be current one of the technology of discharging to atmosphere that is used for limiting.For air burning, be used for separating or capturing (capture) CO in order to satisfy
2Energy requirement, one ton of reflooded CO
2Produce 0.3-0.5 ton additional C O
2(based on fuel kind) is essential, and efficient approximately is 50%.For using oxygen combustion, at the CO of oxygen production generation
2Obviously discharge the necessary CO of gas than above-mentioned separation
2Under few situation, efficient approximately improves 30-50%.Like this, under the situation of oxygen burning, after the steam condensation that burning produces, CO
2Usually account for greatly and discharge 90% of gas, remaining comprises residual nitrogen, is included in as the argon gas in the oxygen of oxidant, for excessive oxygen that makes fuel completing combustion introducing and other gas (NO that forms in combustion process
x, SO
x).After separating all or part of noncondensable gas, purity is more than or equal to 95% CO like this
2Can easily be reinjected.
With purity oxygen or highly be rich in the subject matter that the air burning of oxygen causes and be high flame temperature.In fact, this can surpass 3000 ℃, and for aerial standard burning, temperature is typically about 2000 ℃.
This high flame temperature causes and the unaccommodated high radiant heat flux of the operation of conventional boiler.In fact, in conventional boiler, combustion chamber by pipe around, evaporation of water and/or overheatedly in this pipe, carry out.If hot-fluid is too high, the situation of water evaporate to dryness from pipe can take place.The liquid that contacts with hot wall is steam, and the thermal capacitance of the heat capacity ratio water of steam is obviously low, and therefore, cooling effectiveness obviously reduces.Because overheated, such situation causes pipe destroyed rapidly.This phenomenon is being also referred to as " parching (dry out) " or " (burn out) burnouts " in the art.
First kind of scheme comprises with the CO that produces
2Water down flame gas.Yet this kind recirculation needs substantial equipment, therefore need seek a kind of CO that do not need
2The scheme of recirculation.
" parch " phenomenon and be the hot-fluid accepted and the function (steam is many more, the approaching more condition that parches) of the quality of steam in the mixture.Control must absorbed hot-fluid be very difficult on wall.A kind of scheme of controlling these hot-fluids comprises that the material with infusibility covers tube wall.Yet this scheme has reduced the efficient of swap table area in the combustion chamber slightly and has increased installation cost.
" parch " phenomenon for fear of this, it also is known using water under high pressure in nuclear industry, and high pressure prevents the boiling at pipe/shell interface.Yet this is the problem of a control conduction phenomenon (on the pipe side), and this conduction phenomenon is followed and the proportional rule of temperature contrast, and the shell temperature is relatively low.
In a distinct mode, under the situation of flame boiler, this is the problem of a control radiation phenomenon, and this radiation phenomenon is followed the Stefan-Bolzmann rule, and is proportional and comprise emissivity and absorption factor with the bipyramid of absolute temperature.In addition, the oxygen burning that is converted to 3000 ℃ from 2000 ℃ ignition temperature of standard causes 1000 ℃ temperature difference,, has raise about 50% that is.Then, photothermal difference has surpassed 4 times.Therefore, under the situation of oxygen burning, the surface power density of being accepted by wall can easily surpass 1000kW/m
2
No. 6619041 patents of the U.S. described a kind of do not have recirculation oxygen combustion boiler with and component devices.Described boiler is in " cold " flue gas (flue gas) part rather than be provided with a water preheater in stove.
The patent disclosure relevant that does not have other with the oxygen burning water preheater is installed in stove.
Therefore, prior art is not described or hint the present invention.
Summary of the invention
The present invention is based on the idea opposite, combustion product (liquid of heat) is circulated to water and steam (cold liquid) substantially with conventional boiler.
The invention provides a kind of boiler that is suitable for the oxygen burning, comprising: combustion chamber, water preheater and evaporimeter, wherein combustion chamber is made up of water preheater at least in part; Wherein, described preheater comprises that first restraints independently pipe, and the spacing p/d of pipe is 2-3, and wherein p represents the centre distance between the pipe, and d represents the external diameter of pipe; And described evaporimeter comprises second beam tube, and in described combustion chamber, the described evaporimeter of second beam tube that comprises is arranged on around the described preheater that comprises first beam tube with one heart.
According to an embodiment, described combustion chamber is made up of preheater fully.
According to an embodiment, described preheater comprises the inner reeded pipe of first bundle.
According to first kind of optional mode, described evaporimeter is the radiation evaporimeter.
According to second kind of optional mode, described evaporimeter comprises radiation evaporimeter and convection current evaporimeter.
According to the third optional mode, described evaporimeter is the convection current evaporimeter.
According to an embodiment, described boiler comprises that also water/steam separates flask, and this boiler is supplied water by preheater, and this boiler is supplied water to evaporimeter, and evaporimeter is to this boiler supplying steam.
According to an embodiment, described water preheater is arranged on the inside of combustion chamber.
According to an embodiment, the operation of the combustion product adverse current of described water preheater and combustion chamber.
According to an embodiment, described boiler also comprises superheater.
The present invention also provides a kind of method of using aforementioned boiler by oxygen burning generation hot water, comprises by oxygen combustion flame preheating cold water to produce hot water (liquid of preheating).
According to an embodiment, this method also comprises the gasifying stage of preheated liquid product.
According to first kind of optional mode, the gasifying stage of described preheated liquid is implemented by radiation.
According to second kind of optional mode, the gasifying stage of described preheated liquid is implemented by convection current.According to the third optional mode, the gasifying stage of described preheated liquid is implemented by radiation and convection current.
According to an embodiment, the described stage by oxygen combustion flame preheating cold water implements by adverse current.
According to an embodiment, the temperature of described oxygen combustion flame between 2000-3300 ℃, preferred 2500-3000 ℃.
According to an embodiment, the temperature of described cold water is between 105-170 ℃, and the pressure of this cold water is between the 8-500 crust.
According to an embodiment, described preheated liquid comprises water and steam, and the scope of water/quality of steam ratio is 100/0-50/50, is preferably 100/0-70/30, more preferably 95/5-80/20.
According to an embodiment, the temperature of described preheated liquid is between 170-600 ℃, and the pressure of this preheated liquid is between the 8-500 crust.
According to an embodiment, the vapor (steam) temperature of generation is between 170-600 ℃, and the pressure of this steam is between the 8-500 crust.
According to an embodiment, this method also comprises the stage of the steam superheating that makes generation.
According to an embodiment, the temperature of described water preheat stage rear pass gas is between 1200-600 ℃.
According to an embodiment, the temperature of described gasifying stage rear pass gas is between 250-150 ℃.
Description of drawings
Fig. 1 is the schematic diagram of liquid circulation in the conventional boiler;
Fig. 2 is the schematic diagram according to liquid circulation in the boiler of the present invention;
Fig. 3 is the schematic diagram according to liquid circulation in the boiler of an embodiment;
Fig. 4 A, 4B are respectively the part cross sectional representation according to the boiler of prior art and another embodiment.
The specific embodiment
With reference to Fig. 1, the figure shows a kind of boiler 10 of routine, this boiler comprise one with the contacted water preheater of burning gases 11 of cooling, an evaporimeter 12 and a superheater 13, these members are according near the order setting that is in the flame in the combustion chamber 14.The heat exchange of Chan Shenging is maximized like this, carries out between the liquid and stream or adverse current and temperature difference minimum.The temperature of the steam that superheater produced is above 600 ℃.
With reference to Fig. 2, the figure shows a kind of according to the boiler that is suitable for the oxygen burning of the present invention.In this kind boiler, cold liquid contacts with the hottest combustion product.Term " oxygen burning " refers to be rich in greater than the burning as oxidant of the air of the oxygen of 22 (volume) %.The hot-fluid of radiation is at 200-3000kW/m on the pipe of combustion chamber
2Between change preferred 300-1000kW/m
2
Can use any fuel, for example gas, oil, various petroleum residue (particularly heavy residue) or coal.
The present invention is used for various fields, and it can be used for producing electricity from fossil energy, like this will be no longer because discharging CO
2And bear punishment.The present invention can be used for producing heavy oil by the mode of steam being injected deposit (with steam activation heavy oil field) (activation of heavy-oil fields by steam) in the activation framework of product, for example according to (SAGD) technology of so-called SAGD (steam-assisted gravity drainage).The present invention especially is suitable for activating the production of the high steam in heavy oil field.In fact, steam pressure is high more, and the enthalpy that will offer preheating water before evaporation is big more, and the heat of evaporation is low more.This combustion chamber that makes design high-vapor-pressure and only being used to add hot water becomes possibility.
The present invention also can be used for for clear well or in improving oil recovery (EOR) technological architecture CO
2Refilled the situation of well.In order to utilize the downstream product of oil product, the present invention will allow to use various oil products.
Usually, boiler according to the present invention comprise one on the horizontal plane of combustion chamber preheater and at the evaporimeter in this preheater downstream.Term " downstream " and " upstream " refer to the flow direction (or in other words, referring to the gradient of the temperature in the boiler) of combustion product.Cold water enters preheater, and the liquid after the preheating leaves preheater, and the mass ratio of water/steam can change between 100/0-50/50 in the exit of preheater, preferably changes between 100/0-70/30, more preferably changes between 95/5-80/20.As needs,, can be provided with a superheater is installed, particularly under the situation that produces electric current in order to produce superheated steam.
In the embodiment shown in Figure 2, boiler 20 comprises a combustion chamber 21, a preheater 22 of installing along the combustion chamber wall.The liquid that leaves preheater 22 is transported in the flask, and this flask separates the gaseous state part with liquid part.Liquid part is transported to evaporimeter 23, and this evaporimeter also is positioned partially in the combustion chamber.Liquid is evaporated in so-called primary evaporator.If the quantity of steam deficiency that produces also can in parallelly be used a secondary evaporimeter that is connected with flask 24.This secondary evaporimeter absorbs the heat that convection current transmitted by the gas of heat, and this mainly absorbs by the heat of radiation transmission different with primary evaporator.If preheater has produced the very high liquid of quality of steam, even can only produce steam with secondary evaporimeter 24.Under the situation that needs the superheater (not shown), this superheater is arranged on the position of secondary evaporimeter usually, that is, in the positive upstream of secondary evaporimeter or with secondary evaporimeter at same horizontal plane or randomly in the downstream of primary evaporator.
With reference to Fig. 3, according to one embodiment of the invention, shown boiler is set to vertical with one or more flames towards the bottom.Boiler 30 comprises a combustion chamber 31, and this combustion chamber is provided with the burner of 32 fuel supplying from the source, for example gas or heavy oil product.For example, the temperature of flame is approximately 2000-3000 ℃ in the combustion chamber.One preheater 33 is connected with combustion chamber 31.Be this preheater supply cold water by pipe 34.For example, the temperature of cold water under the pressure of about 180 crust is approximately 136 ℃.Usually, be used for the characteristic such as the following scope of cold water of the present invention: temperature is between 105-170 ℃, and pressure is between the 8-500 crust.
Liquid after the preheating leaves preheater by pipe 35, and this liquid is approximately 337 ℃ in the temperature that pressure is approximately under 180 crust.Usually, be used for the characteristic such as the following scope of heating of the present invention back liquid: temperature is between 170-600 ℃, and pressure is between the 8-500 crust.
Liquid after the heating is transported to water/steam and separates flask 36.Water in flask 36 bottoms is delivered to primary evaporator 38 by pipe 37.Steam produces in this evaporimeter and leaves this evaporimeter in order to be transported to flask 36 by pipe 39.This steam is approximately 357 ℃ in the temperature that pressure is approximately under 180 crust.Usually, the characteristic such as the following scope of the steam that the present invention produces: temperature is between 170-600 ℃, and pressure is between the 8-500 crust.
In the exit of combustion chamber, that is, in the exit of primary evaporator, the temperature of gas is greatly about 1000-1300 ℃.Can obtain a lower outlet temperature so that the amount of the steam that further increases primary evaporator and produced.Optimization is economically depended in the selection of this temperature, and this optimization economically considers to compare the extra swap table area on the elementary and secondary evaporimeter essential in order to obtain identical steam product.
Yet for the optimized reason of above-mentioned economy, 000-1300 ℃ of the temperature stuck-at-of radiation areas opening part in order to improve the output of steam, under this kind situation, can use a main secondary evaporimeter 40 by Convective Heating.The water of flask 36 bottoms is delivered to secondary evaporimeter 40 by pipe 41.In this evaporimeter, produce steam, and for this steam is delivered to flask 36 and leaves this evaporimeter by pipe 42.The temperature of this steam under about 180 bar pressures is approximately 357 ℃.Flue gas finally leaves boiler through chimney 43.
Selectively, for gas of will discharge and the water that forms in combustion process, particularly the aqueous phase separation that forms by condensation can be provided with a separator 44.Then, dry basically CO
2Air communication is crossed pipe 45 and is discharged from.
Hereinafter, some members according to boiler of the present invention have been described in more detail, that is, and water preheater, primary radiation evaporimeter, secondary convection current evaporimeter and superheater.
Water preheater
As previously mentioned, combustion chamber particularly in the combustion zone, is made up of water preheater basically.This water preheater generally includes straight tube, and the outer surface of this straight tube is preferably level and smooth.These pipes are preferably independently of one another.If consider the outside diameter d of this pipe and the centre distance p between the pipe, can obtain a ratio p/d, this ratio is pipe " spacing ".For example, this spacing is 2-3.The inner surface of these pipes can be reeded (" ripple ") or smooth, and perhaps as a kind of distortion, inner surface is smooth but have insert.These pipes all be arranged on combustion chamber around, this combustion chamber can the part (in section) circular or rectangle.Is these pipe supplying cold water by the bottom from gatherer, and hot water is discharged by the top.Therefore, the local evaporation that may exist can not hinder flow usually (the general movement) of liquid.Thickness and/or the raising internal heat transfer coefficient of forming the preferred minor diameter of pipe of this preheater with confinement tube.Also can cocurrent cooling operation (co-current operation), but in this situation, burner is arranged on the base plate, also can put in lateral location.
The water evaporation component comprises primary radiation evaporimeter and two independent evaporimeters of another one secondary convection current evaporimeter.
The primary radiation evaporimeter
If burner is positioned at the top of combustion chamber, the radiation evaporimeter be positioned at just water preheater below, if burner is positioned at the bottom of combustion chamber, the radiation evaporimeter be positioned at just water preheater above.This evaporimeter comprises straight tube, the outer surface smoother of this straight tube, and inner surface is fluted or level and smooth.Descending (amply dimensioned descending) water piping system by the size abundance and gatherer are to the hot water of evaporimeter source of supply from flask.The steam that produces in these pipes returns flask by the gatherer that is positioned near this evaporimeter top outlet.By Natural Circulation or randomly under pressure recirculation can produce water-steam emulsion circulation.
Also can cocurrent cooling operation.The optimization between the abundant circulation of the good absorption of hot fluid and emulsion is especially depended in the selection of pipe diameter.The assembling of water preheater and radiation-evaporimeter form required size so that the temperature of the flue gas in combustion chamber exit between 1000-1300 ℃.The energy distribution that is sent to two each interchangers in the interchanger is the function that Boiler Steam is pressed.
Secondary convection current evaporimeter
Replenishing gasification carries out at the counter current exchanger that is arranged in the combustion chamber downstream.Via with the irrelevant following flowing tube of waterpipe that be equipped with to give the radiation evaporimeter or via identical pipeline, from flask to evaporimeter bundle (vaporizer bundle) hot-water supply.This evaporimeter bundle can be vertical, or relatively horizontal plane tilts, and in this kind situation, water-steam emulsion can Natural Circulation; Or horizontal relatively pipe tilts, in this kind situation, and can be with a pump or randomly use the same pump of supplying with the primary radiation evaporimeter under pressure, to recycle independently.If the quality of combustion products and non-existent in fact dust allow, blade (blade) can be arranged in the arranged outside of the coldest pipe.For example, the temperature that allows to enter this evaporimeter is cooled to above gasification temperature 10-20 ℃ at 1000-1300 ℃ flue gas.
Superheater
The superheater (not shown) is arranged on the front of convection current evaporimeter usually or in the first row back of this convection current evaporimeter pipe, this superheater can comprise two or three beams.Between every bundle, can control the temperature of superheated steam by the device that injects water for cooling.
With reference to Fig. 4 A, the figure shows the part of conventional boiler combustion chamber.It comprises an outside (watertightness) fence 51, pipe 52a, 52b etc., and water-steam emulsion circulates in pipe, and pipe is connected to each other to form the fence of a watertightness by blade 53a, 53b etc.In this situation, these pipes form standard pan.
With reference to Fig. 4 B, show a part according to embodiment of the invention boiler combustion chamber.It comprises that one is coated with the outside watertightness fence 51 of refractory material.For example, be used for pipe 54a, the 54b etc. of cold water circulation concentricity be arranged on direction around heating furnace.In this kind situation, these pipes 54a, 54b etc. form preheater.This kind arrangement makes these pipes can accept its whole lip-deep hot-fluid, accepts the radiation of being sent again by the infusibility wall with the flame facing surfaces.
Below this preheater, primary evaporator can be to design with the similar mode of this preheater, makes the infusibility wall be in the back of pipe, or design in more conventional mode, make the pipe longitudinal blade become an integral body each other, form a dividing plate and guarantee the watertightness of combustion chamber.
In Fig. 4 B, as an example, combustion chamber comprises an outside watertightness fence 51, pipe 52a, 52b etc., and pipe is connected to each other to form the fence of a watertightness by blade 53a, 53b etc.In this situation, these pipes 52a, 52b etc. form evaporimeter.For example, the sub-54a of other cool water circulating pipe, 54b etc. are arranged on the direction around heating furnace with one heart.In this situation, these pipes 54a, 54b etc. form preheater, and this kind alternative especially is fit to hot-fluid and keeps restricted situation.The direct radiation of this design on can restrain evaporation organ pipe is particularly in the high zone of quality of steam.
For some boiler is converted into according to boiler of the present invention, this kind alternative also allows these boilers are transformed, and satisfies the demand because will insert as the other pipe of water preheater in the existing combustion chamber that has been provided with the evaporimeter bundle.
The favorable factor of these transformations is that relevant boiler has been configured to the burning of air as oxidant at first, so the surface area of wall is relatively large.
Compare with conventional boiler, the present invention has following advantage:
Compare with the burner of supplying with atmosphere.
Significantly reduced with purity oxygen burning and to have helped to collect CO
2Nitrogen inertia matter (ballast).
The minimizing of this nitrogen inertia matter has following advantage:
The direct radiant flux of flame increases, and the radiant flux of flue gas increases.First kind of effect is because the rising of ignition temperature, and second kind of effect is relevant with following factor: use the thickness of impartial gaseous layer, higher CO
2+ H
2O concentration has improved the emissivity (in fact, triatomic gas is radiation, is different from diatomic gas) of flue gas.Therefore, essential swap table area significantly reduces.
The volume of the flue gas that produces reduces.This minimizing causes the minimizing of convective exchange, thereby causes the minimizing of counter current exchanger surface area.
According to oxygen combustion boiler of the present invention, have similar power and productive rate, its combustion chamber is littler than the combustion chamber of the burner that uses atmosphere, and a fluid stream is reduced significantly.Therefore, reduced cost and weight, at sea under the situation that (offshore) installs, second characteristic in these characteristics has basic importance.
With supply with oxygen and have CO
2The boiler of recirculation relatively.
High temperature for fear of oxygen combustion causes fault, and a solution is the CO by the boiler downstream is produced
2Recirculation and flame is diminished.
Like this, the hot-fluid from the direct radiation in combustion zone will be littler.Yet because the combustion chamber surface area has the identical order of magnitude with the combustion chamber surface area of the burner that uses atmosphere, the advantage of compactness has not just had.
Flue gas or CO
2Recirculation require a kind of relatively effectively recirculation network, and have the extra energy consumption that is used for recycling fan.The recirculation of sample whatsoever always causes non-existent defective in framework of the present invention:
If the flue gas of recirculation is directly discharged from the outlet of boiler, this recirculation can not influence the hot output of boiler, and on the other hand, because the temperature and the volume of recycle gas, extra energy consumption is significant.In addition, if the temperature of recycled liquid and dew-point temperature are approaching, must consider sulfur corrosion.
If absorb CO in the cooling of acid condensation thing and after separating
2, because its temperature is obviously lower, extra energy consumption can reduce, and condensation takes place at low temperatures, on the other hand, and by with CO
2Be heated to the boiler export temperature and can influence the productive rate of boiler.
The method according to this invention can be implemented the boiler of chamber (band pressure combustion) under pressure, the CO that reinjects and produced when needs
2The time this method have advantage.
The present invention is not limited to described specific embodiment, but has contained the various variations for the easy understanding of those of ordinary skills.
Claims (27)
1. one kind is suitable for the boiler (20,30) that oxygen burns, and comprising: combustion chamber (21,31), water preheater (22,33) and evaporimeter (23,24,38,40), and wherein combustion chamber (21,31) is made up of water preheater (22,33) at least in part;
Wherein, described preheater (33) comprises that first restraints independently pipe (54a, 54b), and the spacing p/d of pipe is 2-3, and wherein p represents the centre distance between the pipe, and d represents the external diameter of pipe; And
Described evaporimeter comprises second beam tube (52a, 52b), in described combustion chamber, the described evaporimeter that comprises second beam tube (52a, 52b) be arranged on one heart comprise first beam tube (54a, 54b) described preheater (33) on every side.
2. boiler according to claim 1 is characterized in that described combustion chamber is made up of preheater fully.
3. boiler according to claim 1 is characterized in that, described preheater (33) comprises the first bundle reeded pipe (54a, 54b).
4. boiler according to claim 1 is characterized in that, described evaporimeter is the radiation evaporimeter.
5. boiler according to claim 1 is characterized in that, described evaporimeter comprises radiation evaporimeter and convection current evaporimeter.
6. boiler according to claim 1 is characterized in that, described evaporimeter is the convection current evaporimeter.
7. boiler according to claim 1 is characterized in that, comprises that also water/steam separates flask, and described boiler is supplied water by preheater, and described boiler is supplied water to evaporimeter, and evaporimeter is to described boiler supplying steam.
8. boiler according to claim 1 is characterized in that, described water preheater (22,33) is arranged on the inside of combustion chamber (21,31).
9. boiler according to claim 1 is characterized in that, described water preheater (22,33) moves with the combustion product adverse current of combustion chamber (21,31).
10. boiler according to claim 1 is characterized in that, also comprises superheater.
11. a method of using boiler according to claim 1 by oxygen burning generation hot water comprises by oxygen combustion flame preheating cold water to produce hot water.
12. method according to claim 11 is characterized in that, also comprises the gasifying stage of the preheated liquid of generation.
13. method according to claim 12 is characterized in that, the gasifying stage of described preheated liquid is implemented by radiation.
14. method according to claim 12 is characterized in that, the gasifying stage of described preheated liquid is implemented by convection current.
15. method according to claim 12 is characterized in that, the gasifying stage of described preheated liquid is implemented by radiation and convection current.
16., it is characterized in that the described stage by oxygen combustion flame preheating cold water implements by adverse current according to the described method of one of claim 11-15.
17. method according to claim 11 is characterized in that, the temperature of described oxygen combustion flame is between 2000-3300 ℃.
18. method according to claim 17 is characterized in that, the temperature of described oxygen combustion flame is between 2500-3000 ℃.
19. method according to claim 11 is characterized in that, the temperature of described cold water is between 105-170 ℃, and the pressure of this cold water is between the 8-500 crust.
20. method according to claim 12 is characterized in that, the temperature of described preheated liquid is between 170-600 ℃, and the pressure of this preheated liquid is between the 8-500 crust.
21. method according to claim 12 is characterized in that, described preheated liquid comprises water and steam, and the scope of water/quality of steam ratio is 100/0-50/50.
22. method according to claim 21 is characterized in that, the scope of described water/quality of steam ratio is 100/0-70/30.
23. method according to claim 22 is characterized in that, the scope of described water/quality of steam ratio is 95/5-80/20.
24. method according to claim 12 is characterized in that, the temperature of the steam of described generation is between 170-600 ℃, and the pressure of this steam is between the 8-500 crust.
25. method according to claim 12 also comprises stage of the steam superheating that makes generation.
26. method according to claim 11 is characterized in that, the temperature of described water preheat stage rear pass gas is between 1200-600 ℃.
27. method according to claim 12 is characterized in that, the temperature of described gasifying stage rear pass gas is between 250-150 ℃.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0407700A FR2872886B1 (en) | 2004-07-09 | 2004-07-09 | METHOD AND DEVICE FOR GENERATING WATER VAPOR ADAPTED TO OXY-COMBUSTION |
| FR0407700 | 2004-07-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101002053A CN101002053A (en) | 2007-07-18 |
| CN100567810C true CN100567810C (en) | 2009-12-09 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005800232436A Expired - Fee Related CN100567810C (en) | 2004-07-09 | 2005-07-06 | Be used to produce the method and apparatus of the steam that is suitable for the oxygen burning |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US20070227145A1 (en) |
| EP (1) | EP1774223A1 (en) |
| JP (1) | JP2008506088A (en) |
| KR (1) | KR20070033418A (en) |
| CN (1) | CN100567810C (en) |
| CA (1) | CA2573254A1 (en) |
| FR (1) | FR2872886B1 (en) |
| WO (1) | WO2006016042A1 (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7849692B2 (en) * | 2006-07-31 | 2010-12-14 | Caterpillar Inc | Segmented heat exchanger |
| CA2684817C (en) | 2008-12-12 | 2017-09-12 | Maoz Betzer-Zilevitch | Steam generation process and system for enhanced oil recovery |
| US9315734B2 (en) | 2008-05-12 | 2016-04-19 | Ex-Tar Technologies, Inc. | System and method for minimizing the negative environmental impact of the oilsands industry |
| JP2011099598A (en) * | 2009-11-05 | 2011-05-19 | Kawasaki Thermal Engineering Co Ltd | Fluid heating device |
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-
2004
- 2004-07-09 FR FR0407700A patent/FR2872886B1/en not_active Expired - Fee Related
-
2005
- 2005-07-06 CN CNB2005800232436A patent/CN100567810C/en not_active Expired - Fee Related
- 2005-07-06 WO PCT/FR2005/001745 patent/WO2006016042A1/en active Application Filing
- 2005-07-06 CA CA002573254A patent/CA2573254A1/en not_active Abandoned
- 2005-07-06 KR KR1020077000562A patent/KR20070033418A/en not_active Application Discontinuation
- 2005-07-06 US US11/571,736 patent/US20070227145A1/en not_active Abandoned
- 2005-07-06 EP EP05826778A patent/EP1774223A1/en not_active Withdrawn
- 2005-07-06 JP JP2007519840A patent/JP2008506088A/en active Pending
Also Published As
| Publication number | Publication date |
|---|---|
| FR2872886A1 (en) | 2006-01-13 |
| EP1774223A1 (en) | 2007-04-18 |
| CN101002053A (en) | 2007-07-18 |
| US20070227145A1 (en) | 2007-10-04 |
| KR20070033418A (en) | 2007-03-26 |
| FR2872886B1 (en) | 2006-09-22 |
| CA2573254A1 (en) | 2006-02-16 |
| WO2006016042A1 (en) | 2006-02-16 |
| JP2008506088A (en) | 2008-02-28 |
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