CN108680017A - Reheat furnace system and furnace apparatus - Google Patents
Reheat furnace system and furnace apparatus Download PDFInfo
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- CN108680017A CN108680017A CN201810528743.4A CN201810528743A CN108680017A CN 108680017 A CN108680017 A CN 108680017A CN 201810528743 A CN201810528743 A CN 201810528743A CN 108680017 A CN108680017 A CN 108680017A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27B—FURNACES, KILNS, OVENS, OR RETORTS IN GENERAL; OPEN SINTERING OR LIKE APPARATUS
- F27B17/00—Furnaces of a kind not covered by any preceding group
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F27—FURNACES; KILNS; OVENS; RETORTS
- F27D—DETAILS OR ACCESSORIES OF FURNACES, KILNS, OVENS, OR RETORTS, IN SO FAR AS THEY ARE OF KINDS OCCURRING IN MORE THAN ONE KIND OF FURNACE
- F27D17/00—Arrangements for using waste heat; Arrangements for using, or disposing of, waste gases
- F27D17/004—Systems for reclaiming waste heat
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
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Abstract
The present invention provides a kind of reheat furnace system and furnace apparatus, belong to heating furnace technical field.The reheat furnace system includes reduction reactor first entrance, reduction reactor second entrance, reduction reactor first outlet, reduction reactor second outlet, heating furnace first entrance, heating furnace second entrance, heating furnace first outlet, heating furnace second outlet, separator first entrance, separator second entrance, separator first outlet, separator second outlet, separator third exports, oxidation reactor first entrance, oxidation reactor second entrance, oxidation reactor first outlet, oxidation reactor second outlet, heat exchanger first entrance, heat exchanger second entrance, heat exchanger first outlet and heat exchanger second outlet.Above system can solve the problems, such as to generate pollutant in traditional heating stove operational process and the thermal efficiency is low, realizes heating furnace high efficiency and low emission operation.Including the furnace apparatus of above system is efficient, operating cost is relatively low.
Description
Technical field
The present invention relates to heating furnace technical fields, and more particularly to a kind of reheat furnace system and furnace apparatus.
Background technology
Heating furnace heating process medium by the way of fuel and air catalytic combustion at present, high-temperature flue gas is through waste heat recovery
It is discharged after system.This heating furnace method of operation will produce environmental contaminants, and the thermal efficiency is difficult to further increase, and specifically has
Following problem.1) fuel is in direct contact burning with air and will produce NOx、CO2Equal pollutants；2) due to low-temperature dew point corrosion
Presence, heating furnace exhaust gas temperature all at 120 DEG C or more, the low temperature exhaust heat of flue gas can not depth recycling, constrain heating furnace heat
The raising of efficiency；3) combustion process excess air coefficient is big, and flue gas loss is larger；4) most of to add in order to reduce environmental pollution
Hot stove uses gas fuel combustion, operating cost higher.
Therefore, existing heating furnace need to be improved.
Invention content
An object of the present invention includes providing a kind of reheat furnace system, which can solve traditional heating stove and run
Pollutant is led to the problem of in journey and the thermal efficiency is low, realizes heating furnace high efficiency and low emission operation.
Another object of the present invention includes providing a kind of furnace apparatus, and it includes above-mentioned reheat furnace systems.
The present invention solves its technical problem and is realized using including following technical scheme：
The embodiment of the present invention proposes a kind of reheat furnace system comprising separator, heat exchanger, oxidation reactor, reduction
Reactor and heating furnace.
Reduction reactor includes for being passed through the reduction reactor first entrance of fuel, for being passed through oxidation state oxygen carrier
Reduction reactor second entrance, the reduction reactor first outlet for exporting reduction-state oxygen carrier and for exporting high temperature cigarette
The reduction reactor second outlet of gas.
Heating furnace includes the heating furnace first entrance being connected to reduction reactor second outlet, the heating being connected to heat exchanger
Stove second entrance, the heating furnace first outlet for exporting low-temperature flue gas and the heating furnace second for exporting heat medium go out
Mouthful.
Separator includes the separator first entrance being connected to heating furnace first outlet, the separation for inputting high temperature air
Device second entrance, the separator first outlet being connected to oxidation reactor, for export the separator second outlet of condensed water with
And for exporting high concentration CO2Separator third outlet.
Oxidation reactor include the oxidation reactor first entrance being connected to separator first outlet, with reduction reactor the
The oxidation reactor second entrance of one outlet, the oxidation reactor first outlet being connected to heat exchanger and and reduction reaction
The oxidation reactor second outlet of device second entrance connection.
Heat exchanger includes the heat exchanger first entrance being connected to oxidation reactor first outlet, for inputting processing medium
Heat exchanger second entrance, the heat exchanger first outlet being connected to heating furnace second entrance and for exporting low temperature oxygen denuded air
Heat exchanger second outlet.
Further, in a preferred embodiment of the present invention, oxidation reactor further includes the first collection chamber, the first cyclonic separation
Device, the first distribution grid and return inclined tube, the first distribution grid are set to the bottom of the cavity of oxidation reactor and separate cavity
At first chamber and second chamber, the first collection chamber is set to one end of the separate second chamber of first chamber and and oxidation reaction
Device first outlet is connected to, and the first cyclone separator is set between the first collection chamber and the first distribution grid, is returned to inclined tube and is set to
One end of the close second chamber of first chamber and return the both ends of inclined tube respectively with oxidation reactor second outlet and reduction
Reactor second entrance is connected to.
Further, in a preferred embodiment of the present invention, reduction reactor further includes the second collection chamber, the second cyclonic separation
Device, the second distribution grid, tedge, expansion chamber and regenerator sloped tube, one end of tedge are connected to the cavity of reduction reactor, separately
One end is equipped with the second distribution grid and tedge is separated into the first tube chamber and the second tube chamber, reduction reactor second by the second distribution grid
Entrance is set to one end of close second tube chamber of the first tube chamber, one end of separate first tube chamber of the second tube chamber and reduction reaction
Device first entrance is connected to, and the second collection chamber is set to the top of the cavity of reduction reactor and connects with reduction reactor second outlet
Logical, cyclone separator is set between the second collection chamber and tedge, and regenerator sloped tube is set to the remote of the cavity of reduction reactor
The both ends of one end and regenerator sloped tube from the second collection chamber respectively with reduction reactor first outlet and oxidation reactor second
Entrance is connected to.Expansion chamber is set to one end of close first tube chamber of the cavity of reduction reactor.
Further, in a preferred embodiment of the present invention, one end of close second tube chamber of the first tube chamber is additionally provided with solid
The entry position of fuel inlet, solid fuel import is divided higher than the position that return inclined tube is connect with reduction reactor second entrance
It exports from device third and is connected to reduction reactor first entrance.
Further, in a preferred embodiment of the present invention, heating furnace is directly-firing heating furnace.
Further, in a preferred embodiment of the present invention, oxygen carrier includes metal oxygen carrier or nonmetallic oxygen carrier, metal
Oxygen carrier includes that copper-based oxygen carrier, iron-based oxygen carrier or manganese base load oxysome, nonmetallic oxygen carrier include GaSO4Oxygen carrier or calcium titanium
Mine oxygen carrier.
Further, in a preferred embodiment of the present invention, include solid fuel, liquid combustion into the fuel of reduction reactor
Material or fuel gas, solid fuel include coal or biomass, and liquid fuel includes crude oil or heavy oil, and fuel gas includes natural
Air-liquid gas or refinery gas.
Further, in a preferred embodiment of the present invention, the reaction temperature of oxidation reactor and reduction reactor is
600-1000℃。
Further, in a preferred embodiment of the present invention, the excess air coefficient of reheat furnace system is 1-1.05.
The embodiment of the present invention also proposed a kind of furnace apparatus comprising above-mentioned involved reheat furnace system.
The advantageous effect of reheat furnace system and furnace apparatus includes in the embodiment of the present invention：
First, present pre-ferred embodiments can reduce heating furnace exhaust gas temperature, and thermal efficiency of heating furnace is greatly improved.Discharge
Smoke components are CO2And H2The high-temperature flue gas and oxygen deprivation high temperature air, heat transmission equipment of O compositions will not occur low-temperature dew point corrosion and ask
Topic, using heat exchanger can abundant Mist heat recovering, make flue-gas temperature by 120 DEG C of sinkings to 50 DEG C hereinafter, promoted heating furnace heat
3-4 percentage points of efficiency.
Second, NO can be greatly reduced in present pre-ferred embodimentsxContent.In common process, fuel directly connects with air
Burning is touched, under the flame temperature more than 1200 DEG C, will produce thermal NOx, Quick-type NOx, nitrogenous liquid, solid fuel can also
Generate fuel type NOx.Fuel is not contacted with air in present pre-ferred embodiments, belongs to flameless combustion mode, ignition temperature
It is relatively low, generally below 1000 DEG C, eradicate Quick-type NOxAnd thermal NOxGeneration.In the reducing atmosphere of oxygen carrier and hypoxemia
Under, the nitrogen in solid, liquid fuel generates fuel type NOxProcess it is suppressed, it is most of with N2Discharge, fuel type NOx50% can be reduced
More than.
Third, present pre-ferred embodiments can realize CO2Efficient trapping.The flue gas of traditional heating stove is due to CO2Concentration pole
It is low, carry out concentration trapping energy consumption it is larger, be generally directly discharged in air.That present pre-ferred embodiments generate is only CO2
And H2The flue gas of O, flue gas pass through separator condensation of water steam, may separate out 95% or more concentration without additionally consuming energy
CO2。
4th, combustion process excess air coefficient is small in present pre-ferred embodiments, and flue gas loss is few.Traditional heating stove mistake
For surplus air coefficient between 1.05-1.3, oxygen decouples chemical chain burning technology (CLOU) since oxygen carrier specific surface area is very big and has
There is catalytic action, quickly, fully, excess air coefficient can react fuel combustion process completely in 1-1.05, and exhaust gas volumn can subtract
Few 10% or more.
Description of the drawings
In order to illustrate the technical solution of the embodiments of the present invention more clearly, below will be to needed in the embodiment attached
Figure is briefly described, it should be understood that the following drawings illustrates only certain embodiments of the present invention, therefore is not construed as pair
The restriction of range for those of ordinary skill in the art without creative efforts, can also be according to this
A little attached drawings obtain other relevant attached drawings.
Fig. 1 is the first structural schematic diagram of reheat furnace system provided in an embodiment of the present invention；
Fig. 2 is second of structural schematic diagram of reheat furnace system provided in an embodiment of the present invention；
Fig. 3 is the first structural schematic diagram of furnace apparatus provided in an embodiment of the present invention；
Fig. 4 is second of structural schematic diagram of furnace apparatus provided in an embodiment of the present invention.
Icon：10- reheat furnace systems；1- separators；101- separator first entrances；102- separator second entrances；
103- separator first outlets；104- separator second outlets；105- separator thirds export；2- heat exchangers；201- heat exchangers
First entrance；202- heat exchanger second entrances；203- heat exchanger first outlets；204- heat exchanger second outlets；3- oxidation reactions
Device；The first collection chambers of 301-；The first cyclone separators of 302-；The first distribution grids of 303-；304- returns to inclined tube；305- oxidation reactions
Device first entrance；306- oxidation reactor second entrances；307- oxidation reactor first outlets；308- oxidation reactors second go out
Mouthful；309- first chambers；310- second chambers；4- reduction reactors；The second collection chambers of 401-；The second cyclone separators of 402-；
The second distribution grids of 403-；404- tedges；405- expansion chambers；406- regenerator sloped tubes；407- reduction reactor first entrances；408-
Reduction reactor second entrance；409- reduction reactor first outlets；410- reduction reactor second outlets；411- first is managed
Chamber；The second tube chambers of 412-；413- solid fuel imports；5- heating furnaces；501- heating furnace first entrances；502- heating furnaces second enter
Mouthful；503- heating furnace first outlets；504- heating furnace second outlets；20- furnace apparatus；21- collection portions.
Specific implementation mode
In order to make the object, technical scheme and advantages of the embodiment of the invention clearer, below in conjunction with the embodiment of the present invention
In attached drawing, technical scheme in the embodiment of the invention is clearly and completely described, it is clear that described embodiment is
A part of the embodiment of the present invention, instead of all the embodiments.The present invention being usually described and illustrated herein in the accompanying drawings is implemented
The component of example can be arranged and be designed with a variety of different configurations.
Therefore, below the detailed description of the embodiment of the present invention to providing in the accompanying drawings be not intended to limit it is claimed
The scope of the present invention, but be merely representative of the present invention selected embodiment.Based on the embodiments of the present invention, this field is common
The every other embodiment that technical staff is obtained without creative efforts belongs to the model that the present invention protects
It encloses.
In the description of the present invention, it should be noted that the orientation or position of the instructions such as term "upper", "lower", "inner", "outside"
Set relationship be based on the orientation or positional relationship shown in the drawings or the invention product using when the orientation or position usually put
Relationship is set, is merely for convenience of description of the present invention and simplification of the description, device is not indicated or implied the indicated or element is necessary
With specific orientation, with specific azimuth configuration and operation, therefore be not considered as limiting the invention.In addition, term
" first ", " second " etc. are only used for distinguishing description, are not understood to indicate or imply relative importance.
In addition, the terms such as term " vertical " are not offered as requiring component absolute upright, but can be slightly tilted.As " hung down
Directly " to refer to only its direction more vertical with respect to for "horizontal", be not indicate the structure have to it is completely vertical, but can
To be slightly tilted.
In the description of the present invention, it is also necessary to which explanation is unless specifically defined or limited otherwise, term " setting ",
" installation ", " connection " shall be understood in a broad sense, for example, it may be being fixedly connected, may be a detachable connection, or integrally connect
It connects；It can be mechanical connection, can also be electrical connection；It can be directly connected, can also indirectly connected through an intermediary, it can
To be the connection inside two elements.For the ordinary skill in the art, it can understand above-mentioned term with concrete condition
Concrete meaning in the present invention.
It is specifically described with reference to embodiments.
Embodiment
Please with reference to Fig. 1 to Fig. 2, the embodiment of the present invention provides a kind of reheat furnace system 10, includes mainly separator
1, heat exchanger 2, oxidation reactor 3, reduction reactor 4 and heating furnace 5.
Reduction reactor 4 includes for being passed through the reduction reactor first entrance 407 of fuel, for being passed through oxidation state oxygen carrier
Body is (with M in the present embodimentxOyIndicate) reduction reactor second entrance 408, for exporting reduction-state oxygen carrier (the present embodiment
In with MxOy-1Indicate) reduction reactor first outlet 409 and reduction reactor second outlet for exporting high-temperature flue gas
410。
Under certain temperature, oxidation state oxygen carrier releases oxygen in reduction reactor 4, after being converted into reduction-state oxygen carrier
From the output to oxidation reactor 3 of reduction reactor first outlet 409.
Fuel enters reduction reactor 4 by reduction reactor first entrance 407, is released with oxidation state oxygen carrier pure
Oxygen reacts, and generates CO2And H2The high-temperature flue gas of O compositions is simultaneously exported by reduction reactor second outlet 410 into heating furnace 5, simultaneously
Discharge heat.
Optionally, for example may include solid fuel, liquid fuel or fuel gas into the fuel of reduction reactor 4.
Wherein, solid fuel may include coal, biomass or sludge etc., such solid fuel price is more cheap, and liquid fuel may include
Crude oil or heavy oil etc., fuel gas may include natural gas, liquefied gas or refinery gas etc..
Above-mentioned oxygen carrier refers to that can discharge oxygen at the reaction temperatures, energy oxidation by air regeneration, and as reactor heat
Measure the carrier of transmission.Optionally, oxygen carrier used for example may include metal oxygen carrier or nonmetallic oxygen carrier.Wherein, golden
Belong to oxygen carrier and may include copper-based oxygen carrier, iron-based oxygen carrier or manganese base load oxysome etc., nonmetallic oxygen carrier may include GaSO4Oxygen carrier
Body or perovskite oxygen carrier etc..Preferably copper-based oxygen carrier.
Heating furnace 5 includes the heating furnace first entrance 501 being connected to reduction reactor second outlet 410, connects with heat exchanger 2
Logical heating furnace second entrance 502, the heating furnace first outlet 503 for exporting low-temperature flue gas and for exporting heat medium
Heating furnace second outlet 504.The high-temperature flue gas that reduction reactor second outlet 410 exports enters heating furnace 5 and is come from heating
The processing medium of heat exchanger 2, then enters downstream after processing medium is heated to target temperature, and flue-gas temperature obtains after reducing
Low-temperature flue gas is drawn by heating furnace first outlet 503 and is introduced into separator 1 by separator first entrance 101.It is worth explanation
, the heat medium that heating furnace second outlet 504 exports is to reach the processing medium of target temperature.
Optionally, above-mentioned heating furnace 5 can be directly-firing heating furnace 5, such as tubular heater 5, metallurgical furnace or rotary kiln
Deng preferably tubular heater 5.
Separator 1 includes the separator first entrance 101 being connected to heating furnace first outlet 503, for inputting high temperature sky
The separator second entrance 102 of gas, the separator first outlet 103 being connected to oxidation reactor 3, point for exporting condensed water
From device second outlet 104 and for exporting high concentration CO2Separator third outlet 105.When the low temperature introduced by heating furnace 5
Flue gas isolates high concentration CO in separator 12After condensed water, high concentration CO2It is cold by 105 output of separator third outlet
Condensate is exported by separator second outlet 104, and the heat of release is for heating the sky introduced by separator second entrance 102
Gas.
Oxidation reactor 3 includes the oxidation reactor first entrance 305 being connected to separator first outlet 103 and reduction
The oxidation reactor second entrance 306 of the connection of reactor first outlet 409, the oxidation reactor first being connected to heat exchanger 2 go out
Mouth 307 and the oxidation reactor second outlet 308 being connected to reduction reactor second entrance 408.
The air (being referred to as preheated air) that separator 1 preheats is delivered to oxidation reaction by separator first outlet 103
Device first entrance 305 simultaneously inputs in oxidation reactor 3, the reduction-state oxygen carrier (M with high temperaturexOy-1) reaction, and reduction-state is carried
Oxysome is oxidized to oxidation state oxygen carrier (MxOy), it discharges heat and generates high temperature oxygen denuded air.
Oxidation state oxygen carrier (MxOy) pass through oxidation reactor second outlet 308 and the return of reduction reaction second entrance successively
It is reacted to continuing to participate in reduction reactor 4.
Heat exchanger 2 includes the heat exchanger first entrance 201 being connected to oxidation reactor first outlet 307, for inputting work
It the heat exchanger second entrance 202 of skill medium, the heat exchanger first outlet 203 being connected to heating furnace second entrance 502 and is used for
Export the heat exchanger second outlet 204 of low temperature oxygen denuded air.The high temperature oxygen denuded air that oxidation reactor first outlet 307 exports is logical
It crosses in 201 input heat exchanger 2 of heat exchanger first entrance, processing medium is entered by heat exchanger second entrance 202 in heat exchanger 2, work
Skill medium obtains the low temperature oxygen denuded air after pre-heating technique medium is reduced with temperature by exchanging heat with high temperature oxygen denuded air, wherein
By heat exchanger first outlet 203, heated stove second entrance 502 inputs in heating furnace 5 pre-heating technique medium again, low temperature oxygen deprivation
Air is then exported by heat exchanger second outlet 204.In the program, burner is no longer set in heating furnace 5, by oxidation reaction
The high-temperature flue gas that the high temperature oxygen denuded air and reduction reactor 4 that device 3 generates generate heats the processing medium into stove.
It holds, oxidation reactor 3 and reduction reactor 4 constitute burning chemistry chains reaction system, and oxygen carrier is using cycle
The mode of fluidisation realizes cycle.Fuel combustion decouples chemical chain burning technology using fuel and the oxygen of air non-direct contact
(CLOU), the oxidation state oxygen carrier (M in reduction reactor 4xOy) pure oxygen is directly discharged at the reaction temperatures.
The oxygen that fuel enters reduction reactor 4 with oxygen carrier discharges directly reacts release heat.
Reduction-state oxygen carrier (MxOy-1) enter oxidation reactor 3 and air reaction regeneration at a certain temperature.
In said program, oxygen carrier oxidating and fuel combustion belong to exothermic reaction, and the process of oxygen carrier release oxygen belongs to
The endothermic reaction, burning chemistry chains react total thermal discharge and are more than total caloric receptivity, and net thermal discharge is the calorific value of fuel, oxidation reactor
3 and 4 reaction temperature of reduction reactor can be at 600 DEG C -1000 DEG C.
Further, above-mentioned oxidation reactor 3 may also include the first collection chamber 301, the first cyclone separator 302, first
Distribution grid 303 and return inclined tube 304.First distribution grid 303 is set to the bottom of the cavity of oxidation reactor 3 and divides cavity
It is divided into first chamber 309 and second chamber 310, the first collection chamber 301 is set to the separate second chamber 310 of first chamber 309
One end and be connected to oxidation reactor first outlet 307, the first cyclone separator 302 is set to the first collection chamber 301 and
Between one distribution grid 303, return inclined tube 304 is set to one end of the close second chamber 310 of first chamber 309 and returns to inclined tube
304 both ends are connected to oxidation reactor second outlet 308 and reduction reactor second entrance 408 respectively.
Wherein, the first cyclone separator 302 is mainly used for carrying out gas solid separation.The surface of first distribution grid 303 is provided with
It is multiple to be on the one hand used to be filtered the preheated air in input oxidation reactor 3 in the equally distributed through-hole in surface, it is another
Aspect can make the preheated air into first chamber 309 more uniform, avoid all concentrating on same position.Preheated air and load
The mixed airflow of oxysome in first chamber 309 after 302 gas solid separation of the first cyclone separator, the high temperature oxygen denuded air of gained
It is then collected in the first collection chamber 301 and for being passed through into heat exchanger 2.
It is returned it is worth noting that, the position of above-mentioned return inclined tube 304 being connect with oxidation reactor second outlet 308 is higher than
Go back to the position of inclined tube 304 being connect with reduction reactor second entrance 408.
Reduction reactor 4 further includes the second collection chamber 401, the second cyclone separator 402, the second distribution grid 403, tedge
404, one end of expansion chamber 405 and regenerator sloped tube 406, tedge 404 is connected to the cavity of reduction reactor 4, and the other end is set
There is the second distribution grid 403 and tedge 404 is separated into the first tube chamber 411 and the second tube chamber 412 by the second distribution grid 403, restores
Reactor second entrance 408 be set to the first tube chamber 411 close to one end of the second tube chamber 412, the second tube chamber 412 far from the
One end of one tube chamber 411 is connected to reduction reactor first entrance 407, and the second collection chamber 401 is set to the chamber of reduction reactor 4
It the top of body and is connected to reduction reactor second outlet 410, cyclone separator 1 is set to the second collection chamber 401 and tedge
Between 404, regenerator sloped tube 406 is set to one end far from the second collection chamber 401 of the cavity of reduction reactor 4 and regenerator sloped tube
406 both ends are connected to reduction reactor first outlet 409 and oxidation reactor second entrance 306 respectively.Expansion chamber 405 is set
It is placed in one end of close first tube chamber 411 of the cavity of reduction reactor 4.
Wherein, the second cyclone separator 402 is also mainly used for carrying out gas solid separation.The surface of second distribution grid 403 is also set
Be equipped with it is multiple in the equally distributed through-hole in surface, on the one hand be used for input reduction reactor 4 in fuel be filtered, it is another
Aspect can make the fuel into tedge 404 more uniform, avoid all concentrating on same position.The mixing of fuel and oxygen carrier
For object in the cavity of reduction reactor 4 after 402 gas solid separation of the second cyclone separator, the high-temperature flue gas of gained is then collected in
In two collection chambers 401 and for being passed through into heating furnace 5.
It is worth noting that, the position of above-mentioned regenerator sloped tube 406 being connect with oxidation reactor second entrance 306 is less than again
The position of raw inclined tube 406 being connect with reduction reactor first outlet 409.
The method of operation of above-mentioned reheat furnace system 10 can refer to following (by taking oxygen carrier is copper-based oxygen carrier as an example)：
1) before reheat furnace system 10 starts, it is passed through high-temperature flue gas into the tedge 404 of reduction reactor 4, makes to enter upper
The copper-based oxygen carrier of oxidation state (CuO) fluidisation of riser 404 rises and discharges oxygen, after oxygen carrier is ciculation fluidized, from return inclined tube
When the 304 oxygen carrier temperatures for entering tedges 404 reach 800 DEG C of temperature, it is passed through fuel gas and cuts off high-temperature flue gas.
2) fuel gas enters the fluidisation oxygen carrier of tedge 404 (CuO) through the second distribution grid 403, and is released with oxygen carrier (CuO)
The oxygen put fully reacts in uphill process, releases heat, maintains the temperature of reactor and oxygen carrier, and generates 800-
850 DEG C of high-temperature flue gas.
3) mixed airflow of high-temperature flue gas and oxygen carrier enters the second cyclone separator 402 in expansion chamber 405 into promoting the circulation of qi
Gu separation, high-temperature flue gas enters heating furnace 5 through the second collection chamber 401, discharges the reduction-state oxygen carrier (Cu of oxygen2O) from sedimentation
405 lower part of room enters oxidation reactor 3 through regenerator sloped tube 406.
4) air (preheated air) heated from separator 1 enters the fluidisation of oxidation reactor 3 also through the first distribution grid 303
Ortho states oxygen carrier (Cu2O), reacted with it in uphill process, by reduction-state oxygen carrier (Cu2O) it is oxidized to oxidation state oxygen carrier
(CuO), heat is released, maintains oxidation reactor 3 and oxygen carrier temperature, and generate 850 DEG C of high temperature oxygen denuded airs.
5) mixed airflow of high temperature oxygen denuded air and oxygen carrier enters first cyclone separator on 3 top of oxidation reactor
Carry out gas solid separation in 302, high temperature oxygen denuded air enters heat exchanger 2 through the first collection chamber 301, oxidation state oxygen carrier (CuO) from
Into tedge 404, the reaction was continued with fuel gas through returning to inclined tube 304 for 3 bottom of oxidation reactor.
6) processing medium enters heat exchanger 2 and exchanges heat with the high temperature oxygen denuded air from oxidation reactor 3 out, high temperature
Oxygen denuded air temperature is expelled directly out after being reduced to 50 DEG C, and the processing medium being preheated, which enters heating furnace 5, to be continued to heat.
7) the pre-heating technique medium for entering heating furnace 5 is added in heating furnace 5 by the high-temperature flue gas drawn from reduction reactor 4
Heat flows out heating furnace 5 after reaching target temperature.
8) heating process medium temperature is reduced to 120 DEG C of flue gas in heating furnace 5, and CO is contained only in flue gas2And H2O, will
It introduces separator 1 and carries out CO2With the separation of vapor, be used in combination condensation heat heat normal temperature air, isolated concentration 95% with
On CO2, CO can be carried out without additionally consuming energy2Trapping, seal up for safekeeping.
With 5 technics comparing of traditional heating stove, above-mentioned 10 exhaust gas temperature of combustion gas tubular type reheat furnace system is reduced to 50 by 120 DEG C
DEG C, excess air coefficient is reduced to 1-1.05, exhaust gas volumn to reduce by 10% by 1.15, and 5 thermal efficiency of heating furnace improves 4 percentages
Point, and do not contain NO in discharging fumexAnd CO2, pollutant emission is almost nil.
In addition, can also the fuel gas of above-mentioned tubular heater 5 be changed to solid fuel, reheat furnace system in the present embodiment
10 as shown in Fig. 2, the first tube chamber 411 is additionally provided with solid fuel import 413, solid fuel close to one end of the second tube chamber 412
The entry position of import 413 is higher than the position that return inclined tube 304 is connect with reduction reactor second entrance 408, separator third
Outlet 105 is connected to reduction reactor first entrance 407.Namely it is additionally arranged one on the tedge 404 in reduction reactor 4
Solid fuel import 413, solid fuel particle entry position return to what inclined tube 304 was connect with reduction reactor 4 higher than oxygen carrier
Position.The high concentration CO being partially separated out2It is introduced into tedge 404 and fluidizes oxygen carrier and solid fuel particle, oxygen carrier enters
Part of oxygen is first discharged in tedge 404, then with solid fuel particle hybrid reaction, other flows of system and said program
All same.When fuel is changed to solid fuel by fuel gas, 10 operating cost of reheat furnace system can reduce 10% or more.
Please with reference to Fig. 3 and Fig. 4, the present embodiment additionally provides a kind of furnace apparatus 20, which includes above-mentioned
Reheat furnace system 10, and further include multiple and different collection portion 21, to collect the high concentration CO exported by separator 1 respectively2With
And condensed water, the low temperature oxygen denuded air exported by heat exchanger 2 and the target temperature processing medium etc. exported by heating furnace 5.
From the above, it includes below that the reheat furnace system 10 and furnace apparatus 20 that the embodiment of the present invention is provided, which have,
Effect：
First, present pre-ferred embodiments can reduce by 5 exhaust gas temperature of heating furnace, and 5 thermal efficiency of heating furnace is greatly improved.Discharge
Smoke components be CO2And H2Low-temperature dew point corrosion will not occur for the high-temperature flue gas and oxygen deprivation high temperature air, heat transmission equipment of O compositions
Problem, using heat exchanger 2 can abundant Mist heat recovering, make flue-gas temperature by 120 DEG C of sinkings to 50 DEG C hereinafter, promoted heating furnace
5 3-4 percentage points of the thermals efficiency.
Second, NO can be greatly reduced in present pre-ferred embodimentsxContent.In common process, fuel directly connects with air
Burning is touched, under the flame temperature more than 1200 DEG C, will produce thermal NOx, Quick-type NOx, nitrogenous liquid, solid fuel can also
Generate fuel type NOx.Fuel is not contacted with air in present pre-ferred embodiments, belongs to flameless combustion mode, ignition temperature
It is relatively low, generally below 1000 DEG C, eradicate Quick-type NOxAnd thermal NOxGeneration.In the reducing atmosphere of oxygen carrier and hypoxemia
Under, the nitrogen in solid, liquid fuel generates fuel type NOxProcess it is suppressed, it is most of with N2Discharge, fuel type NOx50% can be reduced
More than.
Third, present pre-ferred embodiments can realize CO2Efficient trapping.The flue gas of traditional heating stove 5 is due to CO2Concentration
It is extremely low, carry out concentration trapping energy consumption it is larger, be generally directly discharged in air.What present pre-ferred embodiments generated is to only have
CO2And H2The flue gas of O, flue gas pass through 1 condensation of water steam of separator, may separate out 95% or more concentration without additionally consuming energy
CO2。
4th, combustion process excess air coefficient is small in present pre-ferred embodiments, and flue gas loss is few.Traditional heating stove 5
Excess air coefficient between 1.05-1.3, oxygen decouple chemical chain burning technology (CLOU) since oxygen carrier specific surface area is very big and
With catalytic action, quickly, fully, excess air coefficient can react fuel combustion process completely in 1-1.05, and exhaust gas volumn can
Reduce 10% or more.
5th, the solid fuels fictitious hosts such as cheap coal, biomass, sludge can be used in fuel in present pre-ferred embodiments
Higher gaseous fuel reduces by 5 operating cost of heating furnace.Oxygen in present pre-ferred embodiments decouples chemical chain burning technology
(CLOU) it can directly be reacted with solid fuel, 5 gases used fuel of heating furnace, which is changed to solid fuel, can substantially reduce operating cost.
To sum up, the reheat furnace system 10 and operation method of high efficiency low emission provided in an embodiment of the present invention, using oxygen solution
Coupling chemical chain burning technology (CLOU) realizes the contactless burning of fuel and air；Avoid low-temperature dew point corrosion, depth recycling
Fume afterheat；And the CO in flue gas is trapped in a manner of condensation2.It solves in 5 operational process of traditional heating stove, generates pollutant
And the problem that the thermal efficiency is low, realize 5 high efficiency of heating furnace and low emission operation.
The foregoing is only a preferred embodiment of the present invention, is not intended to restrict the invention, for the skill of this field
For art personnel, the invention may be variously modified and varied.All within the spirits and principles of the present invention, any made by repair
Change, equivalent replacement, improvement etc., should all be included in the protection scope of the present invention.
Claims (10)
1. a kind of reheat furnace system, which is characterized in that including separator, heat exchanger, oxidation reactor, reduction reactor and add
Hot stove；
The reduction reactor includes for being passed through the reduction reactor first entrance of fuel, for being passed through oxidation state oxygen carrier
Reduction reactor second entrance, the reduction reactor first outlet for exporting reduction-state oxygen carrier and for exporting high temperature cigarette
The reduction reactor second outlet of gas；
The heating furnace includes the heating furnace first entrance being connected to the reduction reactor second outlet, connects with the heat exchanger
Logical heating furnace second entrance, the heating furnace first outlet for exporting low-temperature flue gas and the heating for exporting heat medium
Stove second outlet；
The separator includes the separator first entrance being connected to the heating furnace first outlet, for inputting high temperature air
Separator second entrance, the separator first outlet being connected to the oxidation reactor, the separator for exporting condensed water
Two export and for exporting high concentration CO2Separator third outlet；
The oxidation reactor includes the oxidation reactor first entrance being connected to the separator first outlet and the reduction
The oxidation reactor second entrance of reactor first outlet connection, the oxidation reactor first outlet that is connected to the heat exchanger with
And the oxidation reactor second outlet being connected to the reduction reactor second entrance；
The heat exchanger includes the heat exchanger first entrance being connected to the oxidation reactor first outlet, is situated between for inputting technique
The heat exchanger second entrance of matter, the heat exchanger first outlet being connected to the heating furnace second entrance and poor for exporting low temperature
The heat exchanger second outlet of oxygen air.
2. reheat furnace system according to claim 1, which is characterized in that the oxidation reactor further includes the first gas collection
Room, the first cyclone separator, the first distribution grid and return inclined tube, first distribution grid are set to the oxidation reactor
The bottom of cavity and the cavity is separated into first chamber and second chamber, first collection chamber is set to first chamber
Room far from the second chamber one end and be connected to the oxidation reactor first outlet, first cyclone separator is set
It is placed between first collection chamber and first distribution grid, the close institute for returning to inclined tube and being set to the first chamber
State one end of second chamber and it is described return inclined tube both ends respectively with the oxidation reactor second outlet and the reduction
Reactor second entrance is connected to.
3. reheat furnace system according to claim 2, which is characterized in that the reduction reactor further includes the second gas collection
Room, the second cyclone separator, the second distribution grid, tedge, expansion chamber and regenerator sloped tube, one end of the tedge with it is described
The cavity of reduction reactor is connected to, and the other end is equipped with the second distribution grid and the tedge is separated into the by second distribution grid
One tube chamber and the second tube chamber, the reduction reactor second entrance are set to close second tube chamber of first tube chamber
One end, second tube chamber are connected to far from one end of first tube chamber with the reduction reactor first entrance, and described the
Two collection chambers are set to the top of the cavity of the reduction reactor and are connected to the reduction reactor second outlet, the rotation
Wind separator is set between second collection chamber and the tedge, and the regenerator sloped tube is set to the reduction reactor
Cavity far from second collection chamber one end and the regenerator sloped tube both ends respectively with the reduction reactor first
Outlet and oxidation reactor second entrance connection, the expansion chamber are set to the close of the cavity of the reduction reactor
One end of first tube chamber.
4. reheat furnace system according to claim 3, which is characterized in that close second tube chamber of first tube chamber
One end be additionally provided with solid fuel import, the entry position of the solid fuel import is higher than the returns inclined tube and the reduction
The position of reactor second entrance connection, the separator third outlet are connected to the reduction reactor first entrance.
5. reheat furnace system according to claim 1, which is characterized in that the heating furnace is directly-firing heating furnace.
6. reheat furnace system according to claim 1, which is characterized in that the oxygen carrier includes metal oxygen carrier or non-gold
Belong to oxygen carrier, the metal oxygen carrier includes copper-based oxygen carrier, iron-based oxygen carrier or manganese base load oxysome, the nonmetallic oxygen carrier
Including GaSO4Oxygen carrier or perovskite oxygen carrier.
7. reheat furnace system according to claim 1, which is characterized in that enter the fuel packet of the reduction reactor
Solid fuel, liquid fuel or fuel gas are included, the solid fuel includes coal, biomass or sludge, the liquid fuel packet
Crude oil or heavy oil are included, the fuel gas includes natural gas, liquefied gas or refinery gas.
8. reheat furnace system according to claim 1, which is characterized in that the oxidation reactor and the reduction reactor
Reaction temperature be 600-1000 DEG C.
9. reheat furnace system according to claim 1, which is characterized in that the excess air coefficient of the reheat furnace system is
1-1.05。
10. a kind of furnace apparatus, which is characterized in that the furnace apparatus includes such as claim 1-9 any one of them
Reheat furnace system.
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| CN201810528743.4A CN108680017B (en) | 2018-05-28 | 2018-05-28 | Reheat furnace system and furnace apparatus |
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Cited By (1)
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| CN110131725A (en) * | 2019-05-21 | 2019-08-16 | 中石化炼化工程（集团）股份有限公司 | A kind of heating means, heating device and its flue gas processing method |
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| CN108680017B (en) | 2019-10-18 |
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Effective date of registration: 20230626 Address after: 100000 22 Chaoyangmen North Street, Chaoyang District, Beijing. Patentee after: CHINA PETROLEUM & CHEMICAL Corp. Patentee after: Sinopec Engineering (Group) Co.,Ltd. Address before: No.6, Heluo Avenue, Sanshan science and Technology Industrial Park, Luoyang high tech Industrial Development Zone, Luoyang, Henan Province Patentee before: SINOPEC (LUOYANG) TECHNOLOGY Co.,Ltd. Patentee before: Sinopec Engineering (Group) Co.,Ltd. |