CN1981122A - Waste heat recovery apparatus, waste heat recovery system, and method of recovering waste heat - Google Patents
Waste heat recovery apparatus, waste heat recovery system, and method of recovering waste heat Download PDFInfo
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- CN1981122A CN1981122A CNA2005800217953A CN200580021795A CN1981122A CN 1981122 A CN1981122 A CN 1981122A CN A2005800217953 A CNA2005800217953 A CN A2005800217953A CN 200580021795 A CN200580021795 A CN 200580021795A CN 1981122 A CN1981122 A CN 1981122A
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- fuel
- heat exchanger
- dimethyl ether
- waste heat
- heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
- F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/12—Improving ICE efficiencies
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Abstract
A heat exchanger packed with a catalyst for reforming DME is installed in the discharge line of a combustion apparatus such as a furnace, an internal combustion engine or electric power generation facilities. A mixed gas from DME and H<SUB>2</SUB>O is passed through the heat exchanger, to thereby pyrolyze DME and recover the sensible heat of the exhaust gas from a furnace or an internal combustion engine as an H<SUB>2</SUB> fuel. Since waste heat is recovered as an H<SUB>2</SUB> fuel or an H<SUB>2</SUB> and CO fuel, not simply as steam, warm water, hot air or the like, the energy recovered by the above method is not limited in the use thereof.
Description
Technical field
The present invention relates to reclaim the method for the used heat of being discharged by various industrial departments, particularly recovery is by the waste heat recovery plant and the method for the used heat of the exhaust of firing units such as stove, internal-combustion engine or power generating equipment discharge.
Background technique
It is the used heat of the firing units such as various stoves, internal-combustion engine or power generating equipment of the representative exhaust of emitting that people are devoted to reclaim by the combustion furnace with combustion fuel always, to reach energy-conservation actual effect.
As the recovery method of the used heat of exhaust, implement sensible heat with exhaust usually and reclaim method as heat energy.Particularly, on the vent systems of firing unit, heat exchanger is set, makes the heat recovery medium by this heat exchanger,, the sensible heat of exhaust is reclaimed as heat energy by the heating of exhaust to the heat recovery medium.For example the waste heat boiler water is as heat exchange medium, and the sensible heat of exhaust is reclaimed heat energy as low pressure steam, hot water.Recuperator, reheating furnace use air as heat exchange medium, and the sensible heat of exhaust is reclaimed heat energy as the heated air of preheating.
As the feature of the used heat that influences the waste heat recovery technology, it is low to list energy density.The temperature of exhaust reaches the situation of low temperature below 300 ℃ in addition, at this moment, if in heat exchanger, carry out then can only reclaiming 200～250 ℃ heat energy at most from being vented to the heat exchange of heat exchange medium.The heat energy that energy density is low can only be as the heating source of low temperature.In order to overcome this problem, reclaim used heat efficiently, then often need the big heat exchanger of heat transfer area, it is big that waste heat recovery plant also becomes thereupon.
In addition, issue as the waste heat recovery technology, the purposes of waste heat recovery technology is limited on heating source of combustion air, low temperature etc., the use position also be limited at reclaim thermal source neighbouring (when with pipeline etc. when heated air, steam are carried in the distant place, it is big that heat radiation becomes, and can not effectively utilize the heat of recovery).Because like this, particularly when the temperature of exhaust is hanged down, finish very difficulty of waste heat recovery technology cost-effectively.
On the other hand, make H in recent years
2Oxygen generation electrochemical reaction in fuel and the atmosphere and the fuel cell of the direct generation of electricity just is being tending towards practicability.As the H that obtains fuel cell
2The method of fuel discloses the C that contains in the coke-stove gas with iron works
nH
mComposition is reformed with the sensible heat of coke oven gas itself and is reclaimed H
2Method (opening the 2002-212575 communique) with CO with reference to the spy.But in this method, if there is not coke oven then can not obtain H
2Fuel can widely used H so can not become the future of the fuel of the battery that acts as a fuel etc.
2The source takes place in fuel.
Summary of the invention
The objective of the invention is to, provide and the sensible heat of the exhaust of being discharged by firing units such as stove, internal-combustion engine or power generating equipments can be reclaimed as being H
2New waste heat recovery plant, Waste Heat Recovery System (WHRS) and the waste recovery method of fuel such as fuel.
In order to achieve the above object, the invention provides following waste heat recovery plant, Waste Heat Recovery System (WHRS) and waste recovery method.
(1) a kind of waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
(2) according to (1) described waste heat recovery plant, it is characterized in that,, in described vent systems, drop into dimethyl ether for the temperature that makes described firing unit exhaust raises.
(3) a kind of waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
(4) according to (3) described waste heat recovery plant, it is characterized in that, the CO that contains of described firing unit
2Exhaust dehydration and deoxidation, the mixed gas that makes the exhaust of this dehydration and deoxidation and dimethyl ether is by described heat exchanger.
(5) a kind of waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel, on described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
(6) according to (5) described waste heat recovery plant, it is characterized in that, for the temperature that makes the described firing unit exhaust that drops into described the 2nd heat exchanger raises, with the H that reclaims in described the 1st heat exchanger
2And CO fuel drops into the vent systems between described the 1st heat exchanger and described the 2nd heat exchanger.
(7) according to (5) or (6) described waste heat recovery plant, it is characterized in that the H that reclaims in separation and described the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 1st heat exchanger.
(8) according to each described waste heat recovery plant in (1)～(7), it is characterized in that described firing unit is gas turbine, gas engine or diesel engine, with the described H that reclaims
2Fuel or described H
2Use with the fuel of CO fuel as described gas turbine, described gas engine or described diesel engine.
(9) according to each described waste heat recovery plant in (1)～(7), it is characterized in that, the described H that reclaims
2Fuel or described H
2Use as the alternative fuel of the manufacture gas of iron works with CO fuel.
(10) according to each described waste heat recovery plant in (1)～(7), it is characterized in that, the described H that reclaims
2Fuel or described H
2Use with the act as a fuel fuel of battery of CO fuel.
(11) a kind of Waste Heat Recovery System (WHRS), it is characterized in that, be provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaim the waste heat recovery plant of the sensible heat of this firing unit exhaust, described waste heat recovery plant, on the vent systems of described firing unit, be provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
(12) a kind of Waste Heat Recovery System (WHRS), it is characterized in that, be provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaim the waste heat recovery plant of the sensible heat of this firing unit exhaust, described waste heat recovery plant, on the vent systems of described firing unit, be provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
(13) a kind of Waste Heat Recovery System (WHRS), it is characterized in that, be provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaim the waste heat recovery plant of the sensible heat of this firing unit exhaust, described waste heat recovery plant, on the vent systems of described firing unit, be provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel, on described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel, the H that reclaims in separation and described the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 1st heat exchanger.
According to each described Waste Heat Recovery System (WHRS) in (11)～(13), it is characterized in that (14) described firing unit uses LNG (LNG Liquefied natural gas) to act as a fuel.
According to each described Waste Heat Recovery System (WHRS) in (11)～(14), it is characterized in that (15) described Waste Heat Recovery System (WHRS) also is provided with the described H that burning is reclaimed
2Oven or firing unit with CO fuel.
(16) according to each described Waste Heat Recovery System (WHRS) in (13)～(15), it is characterized in that, described Waste Heat Recovery System (WHRS) also is provided with described the 2nd heat exchanger waste heat boiler in downstream side more that is arranged on described vent systems, and the water vapour that this waste heat boiler is reclaimed offers described the 2nd heat exchanger.
(17) a kind of waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
(18) a kind of waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
(19) a kind of waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel, on described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel, the H that reclaims in separation and described the 1st heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 2nd heat exchanger.
(20) a kind of waste recovery method, it is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, fill the catalyzer of reformation dimethyl ether, by dimethyl ether being blown into described vent systems, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
(21) a kind of waste recovery method, it is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, fill the catalyzer of reformation dimethyl ether, by dimethyl ether being blown into described vent systems, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
According to each described invention in (1)～(7) and since not only with the waste heat recovery of firing unit as steam, hot water, heated air etc., also reclaim as H
2Fuel or H
2With CO fuel, so the purposes of the energy that reclaims unrestricted (that is, owing to reclaim the ignition heat that acts as a fuel, even to carrying at a distance, the energy of recovery does not reduce yet).In addition, because utilize the sensible heat of exhaust that dimethyl ether is restructured as H
2Fuel is so can improve dimethyl ether to H
2Energy conversion efficiency during conversion (for example, even the temperature of exhaust is low to moderate 250～300 ℃, energy conversion efficiency also can reach more than 90%).And, because can be with waste heat recovery as the high fuel of surcharge, so even delivery temperature low (for example, the temperature of exhaust is below 300 ℃), the also heat recovery that can have an economic benefit.In addition, as long as because exhaust, dimethyl ether and H are arranged
2O or CO
2, just can produce H
2Fuel is so can obtain general H
2The fuel generating means realizes consuming in large quantities H
2The social system of fuel.
According to (8) described invention, can be with H
2Fuel or H
2Use with the fuel of CO fuel as gas turbine, gas engine or diesel engine.
According to (9) described invention, because the H that obtains
2Fuel or H
2Close with the composition and the heating value of the manufacture gas of CO fuel and iron works, so with its as manufacture gas in the blast furnace blowing-out etc. the manufacture gas alternative fuel when not enough, not existing fuel-burning equipment can be used, the utilization ratio of iron works manufacture gas can also be improved through transforming.
According to (10) described invention, can be with the H that obtains
2Fuel or H
2Use with the act as a fuel fuel of battery of CO fuel.
According to (11) or (12) described invention, can obtain can be with the waste heat recovery of firing unit as H
2Fuel or H
2Waste Heat Recovery System (WHRS) with CO fuel.
According to (13) described invention, the H that reclaims in separation and the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, and with the CO that separates
2Offer the 1st heat exchanger, so CO
2Circulation get up, so can reduce CO
2Discharge capacity.
According to (14) described invention,, can reduce CO by using the carbon discharge capacity than the fuel of dimethyl ether LNG still less as firing unit
2Discharge capacity.
According to (15) described invention, can be with the H that reclaims
2Use with the fuel of CO fuel as firing units such as oven or boilers.
According to (16) described invention, can reclaim the water vapour that offers the 2nd heat exchanger with waste heat boiler.
According to (17) or (18) described invention and since not only with waste heat recovery as steam, hot water, heated air etc., also reclaim as H
2Fuel or H
2With CO fuel, so the purposes of the energy that reclaims unrestricted (that is, owing to reclaim the ignition heat that acts as a fuel, even to carrying at a distance, the energy of recovery does not reduce yet).
According to (19) described invention, the H that reclaims in separation and the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, and with the CO that separates
2Offer the 1st heat exchanger, so CO
2Circulation get up, so can reduce CO
2Discharge capacity.
As described in (20) or (21), also can directly dimethyl ether be blown into vent systems.
Description of drawings
Fig. 1 is the figure of the waste heat recovery plant of expression the 1st mode of execution of the present invention.
Fig. 2 is the figure of the heat exchanger (recuperator) of expression tubular type.
Fig. 3 is the figure of the heat exchanger (switching type) of expression heat accumulating type.
Fig. 4 is the figure of the heat exchanger (rotary) of expression heat accumulating type.
Fig. 5 is the figure of the circulating heat exchanger of expression fluid bed type and thermal medium, and Fig. 5 a represents the heat exchanger of fluid bed type, and Fig. 5 b represents the heat exchanger that thermal medium is circulating.
Fig. 6 is the figure of the hydrogen reformation characteristic of expression DME.
Fig. 7 is that expression estimation DME is to H
2The figure of an example of the energy conversion efficiency during conversion.
Fig. 8 is the figure of the waste heat recovery plant of expression the 2nd mode of execution of the present invention.
Fig. 9 is the figure of the waste heat recovery plant of expression the 3rd mode of execution of the present invention.
Figure 10 is the figure of the waste heat recovery plant of expression the 4th mode of execution of the present invention.
Figure 11 is the procedure operation precedence diagram (Waste Heat Recovery System (WHRS) of LNG and DME and usefulness) of the Waste Heat Recovery System (WHRS) of the 1st mode of execution of the present invention.
Figure 12 is the procedure operation precedence diagram that all uses the Waste Heat Recovery System (WHRS) of LNG.Figure 12 a is to use the procedure operation precedence diagram of LNG as the Waste Heat Recovery System (WHRS) of the fuel of oven, Figure 12 b is to use the procedure operation precedence diagram of LNG as the Waste Heat Recovery System (WHRS) of the fuel of gas electricity generator, and Figure 12 c is the procedure operation precedence diagram that uses the Waste Heat Recovery System (WHRS) of LNG in reformer.
Figure 13 is the procedure operation precedence diagram of the Waste Heat Recovery System (WHRS) of the 2nd mode of execution of the present invention.
Embodiment
The following describes embodiments of the present invention.Fig. 1 represents the waste heat recovery plant of the 1st mode of execution of the present invention.The vent systems 4 of combustion furnace 1 is provided with heat exchanger 2, and (following note is made H with water vapour to make dimethyl ether (following note is made DME)
2O) mixed gas is by this heat exchanger 2.By carry out the heat exchange of exhaust and DME in heat exchanger 2, making the DME thermolysis is H
2, the sensible heat of exhaust is reclaimed as H
2Fuel.
Heat exchanger 2 can use tubular type, board-like, enlarge various structures such as heat transfer surface, heat accumulating type, fluid bed type, thermal medium be circulating.Fig. 2 represents an example (being known as recuperative recovery heat exchanger) of the heat exchanger of tubular type, and Fig. 3 and Fig. 4 represent the heat exchanger of heat accumulating type, and Fig. 5 represents fluid bed type and the circulating heat exchanger of thermal medium.
In recuperator shown in Figure 2, exhaust and DME and H
2The heat-transfer pipe 3 that the mixed gas of O is used as solid walls separates.DME and H as cryogen
2The mixed gas of O flows through the inboard of heat-transfer pipe 3, crosses the outside of heat-transfer pipe 3 as the blast air of high temperature fluid, they are contacted indirectly and carries out heat exchange.The sensible heat of exhaust is transferred to DME and H by radiation, conduction through heat-transfer pipe 3
2In the mixed gas of O.
Fig. 3 represents the heat regenerator of switching type.For easy to understand, the using method of this heat regenerator is described.At first, make the high temperature fluid blast air cross the heat retainer A that constitutes by alumina balls, cellular material etc., thereby heat retainer A is heated up.When heat retainer A was raised to certain temperature, switch valve made cryogen DME and H
2The mixed gas of O flows through the heat retainer A of intensification.Meanwhile, switch valve stops blast air to cross heat retainer A, and makes it flow through heat retainer B.When heat retainer B was raised to certain temperature, switch valve repeated identical operations again.The switching of valve is carried out once every scheduled time.
Fig. 4 represents revolving heat regenerator.In this heat exchanger, the runner in two outsides is divided into runner and the cryogen DME and the H of high temperature fluid exhaust
2The runner of the mixed gas of O.Middle heat retainer can rotate, and through after the rotation of stipulated time, the part that is heated by high temperature fluid moves to the cryogenic flow side.Cryogen flows through the part that heat retainer heats up, so exhaust and DME and H
2The heat exchange of the mixed gas of O can be carried out.
In the exhaust downstream side of heat exchanger shown in Figure 2, allocation plan 3 or heat exchanger shown in Figure 4 also can be with DME and the H after heating up
2The mixed gas of O imports heat exchanger shown in Figure 2.The sensible heat that can reclaim exhaust thus efficiently is up to being warming up to the temperature province that DME can thermolysis.
Flow through DME and H at heat exchanger 2
2One side of the mixed gas of O is filled the catalyzer that DME is restructured as hydrogen.This catalyzer can use known catalyzer such as aluminium oxide, silica, titanium dioxide.There is no particular limitation for the kind of catalyzer, as long as DME can be restructured as hydrogen, no matter which kind of catalyzer can use.
And, can also use DME and CO
2Mixed gas replace DME and H
2The mixed gas of O is by heat exchanger 2, and making the mixed gas thermolysis is H
2And CO, the sensible heat of the exhaust of combustion furnace 1 is reclaimed as H
2With CO fuel.For with DME and CO
2Be restructured as H
2With the reaction of CO fuel, discuss in detail with the 2nd mode of execution shown in Figure 8.
Fig. 5 a represents the heat exchanger of fluid bed type, and Fig. 5 b represents the heat exchanger that thermal medium is circulating.In the heat exchanger of the fluid bed type shown in Fig. 5 a, DME and H
2O or CO
2Mixed gas in fluidized bed 2a internal flow.The blast air of high temperature is crossed the outside of fluidized bed 2a, carries out the heat exchange of exhaust and mixed gas by the wall of fluidized bed 2a.The inner catalyst filling 2b of fluidized bed 2a, catalyzer 2b flows along with flowing of mixed gas.Mixed gas by fluidized bed 2a is restructured as H under the effect of catalyzer 2b
2Or CO+H
2
In the circulating heat exchanger of the thermal medium shown in Fig. 5 b, DME and H
2O or CO
2Mixed gas (among the figure note do flowing medium) in circulation layer 2c internal flow.The inner 2c of circulation layer is catalyst filling 2e also.Mixed gas and catalyzer 2e pass through heat-transfer pipe 2d in circulation layer 2c inner loop.The blast air of high temperature is crossed the outside of heat-transfer pipe 2d, carries out the heat exchange of exhaust and mixed gas by the wall of fluidized bed 2d.Mixed gas by circulation layer 2a is restructured as H under the effect of catalyzer 2e
2Or CO+H
2
In aforesaid heat exchanger 2, reaction CH
3OCH
3+ 3H
2O+29kcal 6H
2+ 2CO
2Under catalyst action, carry out.By this reaction, can make the DME thermolysis is H
2, the sensible heat of exhaust is reclaimed as H
2Fuel.
Fig. 6 represents the hydrogen reformation characteristic of DME.To the DME+3H before reacting
2O increases heat, and after the reaction, DME is restructured as 6H
2+ 2CO
2Only increase by 9% this moment is the heat of 29kcal, low-temperature waste heat can be reclaimed as hydrogen fuel as can be known.
When the temperature of exhaust is low (for example below 300 ℃ time), be difficult to cause DME and H
2The mixed gas of O resolves into H
2Reaction.In addition, because DME and H
2O resolves into H
2And CO
2Reaction be heat absorption reaction, so the temperature of exhaust might be more and more lower.Therefore, as shown in Figure 1, in order to increase heat of exhaust (temperature of exhaust is elevated to more than 300 ℃), a part of DME that will be used for heat recovery drops into vent systems (so-called overheated).And, also can utilize the ignition heat thermal exhaust of the DME of input.
When the temperature of exhaust is 350 ℃～400 ℃, because DME and H
2The mixed gas of O resolves into H
2Be reflected at and carry out, so there is no need to make DME overheated.In addition, if use high efficiency heat exchanger, even then the temperature of exhaust also can make the DME thermolysis below 300 ℃.
Fig. 7 represents to estimate that DME is to H
2An example of the energy conversion efficiency during conversion.In this example, the temperature of supposing exhaust 7 is 300 ℃.If make 300 ℃ exhaust 7 be 20Nm
3/ h, then the heat of exhaust 7 is 2100kcal/h.
In this example, for the temperature that makes exhaust 7 remains on more than 300 ℃, on vent systems 4, carrying out the Overheating Treatment of 0.1kg/h (688kcal/h) as the DME 5 of thermal source.In order only to provide necessary heat, make the input amount of overheated DME 5 become to replenish the DME5 thermolysis is become H to reaction
2The amount of the reaction heat of the heat absorption reaction of fuel.By the Overheating Treatment of DME5, the temperature of exhaust 10 reaches 394 ℃.
DME6 and H with 30 ℃ of normal temperature
2O8 offers heat exchanger 2.Utilize the sensible heat of exhaust 7 to make DME6 and H
2The temperature of O8 is elevated to 300 ℃.The temperature of the exhaust 11 of being discharged by heat exchanger is 248 ℃, so about 50 ℃ of exhaust 11 [=300 ℃ (temperature of exhaust 7)-248 ℃ (temperature of exhaust 11)] are used to make DME6 and H
2O8 heats up.
In heat exchanger 2, make exhaust 1O and DME6 and H
2The mixed gas of O8 carries out heat exchange, and DME6 is restructured as H
2Fuel 9.DME6 is dropped into heat exchanger 2 with 1.05kg/h (7224kcal/h).The H that obtains
2Fuel 9 is 2.91Nm
3/ h (7499kcal/h).
In utilizing this example of exhaust 7 of 300 ℃, change into H if calculate DME6
2Energy conversion efficiency during fuel 9 then is 7499/ (7224+688) * 100=94.5%, and it is changed with the higher thermal efficiency as can be known.Even delivery temperature is 250～300 ℃, energy conversion efficiency also can reach more than 90%.At this moment, energy conversion efficiency η is defined as: the η=(H that obtains
2The burning energy of fuel)/(the burning energy of the DME of use).
According to this energy conversion efficiency, 95% of the ignition heat that DME had becomes H
2Ignition heat.For example, work as H
2When fuel is used for fuel cell, if the generating efficiency of fuel cell itself is about 60%, then it can be using at H
2Generation on the total efficiency generating of energy in being also contained in, promptly with total efficiency [=generated energy/fuel (DME) energy] generating of 60% * 95%=about 57%.Therefore, can obtain the same generating efficiency of large-scale gas turbine power generating plant that had with existing power company.
Thermal efficiency when as a comparative example, estimation does not utilize 300 ℃ exhaust.At this moment, remedy heat 2788kcal whole of the exhaust 10 that drops into heat exchanger 2 with the ignition heat of DME.That is, the heat itself with the DME burning makes the DME thermolysis.Result's energy conversion efficiency at this moment is 7499/ (7224+2788) * 100=74.9%, is reduced to below 80%.This is to be the cause that obtains by other the DME of burning because be used to make the thermal source of DME thermolysis.
Can also use DME and CO
2Mixed gas replace DME6 and H
2The mixed gas of O8 is by heat exchanger 2, and making the DME thermolysis thus is H
2And CO, the sensible heat of the exhaust of combustion furnace is reclaimed as H
2With CO fuel.For DME is restructured as H
2With the reaction of CO fuel, discuss in detail with the 2nd following mode of execution.
Fig. 8 represents the waste heat recovery plant of the 2nd mode of execution of the present invention.In this embodiment, waste heat recovery plant is arranged on the vent systems of combustion turbine combined system.Combustion turbine combined system is meant compressed fuel gas in compress fuel gas machine 13, and its air with compression in air compressor 14 is burnt in burner 15.The fuel gas of the High Temperature High Pressure by making generation expands in gas turbine I6 and to generator 17 output powers of outside.
The exhaust high temperature and the flow of gas turbine 16 are big.The vent systems of this gas turbine 16 is provided with heat exchanger 18.By with DME and CO
2Mixed gas by heat exchanger 18, make the DME thermolysis, the sensible heat of exhaust is reclaimed as H
2With CO fuel.The H that reclaims
2With CO fuel, the fuel that for example can mix with the manufacture gas of iron works as gas turbine 16 uses.
Fill in the heat exchanger 18 DME is restructured as H
2Catalyzer with CO fuel.Catalyzer can use known catalyzer such as ruthenium, nickel.There is no particular limitation for the kind of catalyzer, as long as DME can be restructured as H
2And CO, no matter which kind of catalyzer can use.
In heat exchanger 18, carrying out CH
3OCH
3+ CO
2+ 58kcal 3H
2The reaction of+3CO.With input DME and H
2The mixed gas of O and obtain H
2The reacting phase ratio of fuel is because the reaction heat of heat absorption reaction is big, so the temperature of necessary rising exhaust.The temperature of the exhaust of gas turbine 16 is for example because up to 600 ℃, so be fit to use this exhaust to make the DME thermolysis.Certainly, can also utilize CH
3OCH
3+ CO
2+ 58kcal 3H
2The reaction of+3CO promptly for example replaces heat exchanger 18 with heat exchanger shown in Figure 12.
The exhaust of being discharged by heat exchanger 18 is provided for waste heat boiler 19.Waste heat boiler 19 is with H
2O (water) heats, and the sensible heat of exhaust is reclaimed as H
2O (water vapour).The H that obtains
2O (water vapour) is used to make the steam turbine 20 with gas turbine 16 combinations to rotate.If gas turbine 16 and steam turbine 20 rotations, then motor 17 generatings.
Fig. 9 represents the waste heat recovery plant of the 3rd mode of execution of the present invention.The waste heat recovery plant of this mode of execution is the same with the waste heat recovery plant of above-mentioned the 2nd mode of execution, is provided with heat exchanger 18 on the vent systems of gas turbine 16 firing units such as grade, by with DEM and CO
2Mixed gas by this heat exchanger 18, make the DME thermolysis, the sensible heat of the exhaust of firing unit is reclaimed as H
2With CO fuel.On the other hand, what the waste heat recovery plant of this mode of execution was different with the waste heat recovery plant of above-mentioned the 2nd mode of execution is, with the CO that contains of firing unit
2Exhaust at dewatering unit with take off O
2Dewater, take off O in the device 21
2, make this dehydration, take off O
2Exhaust by heat exchanger 18.The CO that is used to reform
2Concentration to there is no need be 100%, even contain the CO about 10%
2Gas also can be used as 1000Kcal/Nm
3About fuel gas reform, reclaim.
Figure 10 represents the waste heat recovery plant of the 4th mode of execution of the present invention.In this embodiment, be provided with at the upstream side of the vent systems of combustion furnace DME is reclaimed as H
2With the 1st heat exchanger 25 of CO fuel, the downstream side is provided with reclaims DME as H
2The 2nd heat exchanger 26 of fuel.As mentioned above, the reaction heat of the heat absorption reaction of the 1st heat exchanger 25 is bigger than the reaction heat of the heat absorption reaction of the 2nd heat exchanger 26.For each heat absorption reaction is carried out reposefully, preferably with the 1st and the 2nd heat exchanger 25,26 arranged in series, and make the 1st heat exchanger 25 be configured in upstream side, the 2nd heat exchanger 26 is configured in the downstream side.
Fill in the 1st heat exchanger 25 DME is restructured as H
2Catalyzer with CO fuel.With DME and CO
2Mixed gas drops into the 1st heat exchanger 25.Then the 1st heat exchanger 25 reclaims the sensible heat of exhaust as H
2With CO fuel.The H that reclaims
2With CO fuel, for example be provided for the manufacture gas system of iron works etc.For the temperature that makes the exhaust that drops into the 2nd heat exchanger 26 raises, also a part of DME can be thrown into the vent systems between the 1st heat exchanger 25 and the 2nd heat exchanger 26 and make its burning (what is called is overheated).
Fill in the 2nd heat exchanger 26 DME is restructured as H
2The catalyzer of fuel.With DME and H
2The mixed gas of O drops into the 2nd heat exchanger 26.Then the 2nd heat exchanger 26 reclaims the sensible heat of exhaust as H
2Fuel.Will with H
2The CO that fuel is discharged by the 2nd heat exchanger 26 simultaneously
2In segregating unit 28, separate.The CO that separates
2Offer the 1st heat exchanger 25 as raw material.Because the CO that separates
2The concentration height is so needn't make CO in the 1st heat exchanger 25
2Gas heating in addition can carry out the decomposition reaction of DME efficiently.Relative therewith, if DME and exhaust are dropped into the 1st heat exchanger 25 simultaneously, then owing to also will make CO
2The N that contains in the remainder in addition
2, O
2Heat up, so the reuse efficiency of used heat reduces.This device also can replace with the heat exchanger 18 of combustion turbine combined system shown in Figure 8.
The H that obtains by present embodiment
2Close with the composition and the heating value of the manufacture gas of CO fuel and iron works, so with its as manufacture gas in the blast furnace blowing-out etc. the manufacture gas alternative fuel when not enough, not existing fuel-burning equipment can be used, the utilization ratio of iron works manufacture gas can also be improved through transforming.Be described as follows.
Manufacture gas is a coke-stove gas: 4500kcal/Nm
3, blast furnace gas: 750kcal/Nm
3, coal gas of converter: 2000kcal/Nm
3Mixed gas, with H
2With CO be main body.The fuel gas that obtains in the present embodiment is H
2With CO fuel: 2800kcal/Nm
3, H
2Fuel: 1800～2580kcal/Nm
3The composition of the fuel gas of manufacture gas and present embodiment and calorie are close, therefore are fit to present embodiment is applied to the vent systems of iron works combustion furnace, if with the H that obtains
2Fuel, H
2Sneak in the manufacture gas system with CO fuel, then can not transform existing fuel-burning equipment, its alternative fuel as manufacture gas is used.
As the iron works of the representative of high energy-consuming industry, waste heat is big, and about 40% of the energy that produces in each manufacturing process becomes manufacture gas and is discharged from.But, because the variation of manufacture gas is violent, so be difficult to use the high generating gas turbine of efficient that manufacture gas is acted as a fuel at iron works.Replace it, in order to remedy the part that manufacture gas changes, make the productive rate of steam stable, use steam turbine power generation by combusting heavy oil etc.If with the H that obtains in the present embodiment
2Fuel, H
2Sneak in the manufacture gas system with CO fuel, then can make the productive rate of manufacture gas stable, therefore introduce easily and generate electricity, thereby can improve the utilization ratio of iron works manufacture gas with the high machinery of efficient such as gas turbine.
Figure 11 is the procedure operation precedence diagram of the Waste Heat Recovery System (WHRS) of expression the 1st mode of execution of the present invention.This Waste Heat Recovery System (WHRS) uses gas electricity generator 31 as firing unit, is provided with 1st heat exchanger 25 and 2nd heat exchanger 26 identical with above-mentioned the 3rd mode of execution on the vent systems of gas electricity generator 31.
Fill in the 1st heat exchanger 25 DME is restructured as H
2Catalyzer with CO fuel.With DME and CO
2Mixed gas drops into the 1st heat exchanger 25.Then the 1st heat exchanger 25 reclaims the sensible heat of exhaust as H
2With CO fuel.On the other hand, filling is restructured as H with DME in the 2nd heat exchanger 26
2The catalyzer of fuel.With DME and H
2The mixed gas of O drops into the 2nd heat exchanger 26.Then the 2nd heat exchanger 26 reclaims the sensible heat of exhaust as H
2Fuel.Will with H
2Fuel is discharged CO by the 2nd heat exchanger 26 simultaneously
2In segregating unit 28, separate.The CO that separates
2Offer the 1st heat exchanger 25 as raw material.
The H that reclaims in the 1st heat exchanger 25
2Be used as the fuel of oven 32 with CO fuel.Also can use firing unit replacement oven 32 such as boiler.More downstream side at the 2nd heat exchanger 26 is provided with waste heat boiler 33, and the water vapour that reclaims in this waste heat boiler 33 is offered the 2nd heat exchanger 26.
In the Waste Heat Recovery System (WHRS) of this mode of execution, firing unit uses gas electricity generator 32, and the fuel of gas electricity generator does not use DME, and uses LNG (LNG Liquefied natural gas).At this,, use DME also can as the fuel of gas electricity generator because DME is offered the 1st and the 2nd heat exchanger 25,26.But, if the fuel of generator 31 uses DME, CO when then acting as a fuel burning owing to DME
2Discharge capacity Duo about 18% (the carbon emission coefficient of fuel is 64.06g-C/Mcal, and is relative therewith, and DME is 75.60g-C/Mcal) than LNG, so by the relation of the carbon emission coefficient of fuel as can be known the carbon discharge capacity of DME increase.Therefore, in order to reduce the carbon discharge capacity in this mode of execution, use the fuel of LNG as generator 31.
Below, more do not use DME and use LNG Waste Heat Recovery System (WHRS) (the following Waste Heat Recovery System (WHRS) that this Waste Heat Recovery System (WHRS) is called LNG and DME and usefulness) and the whole use LNG Waste Heat Recovery System (WHRS) (with reference to Figure 12) of fuel of the big generator 31 of consumption that acts as a fuel of fuel of the big generator 31 of consumption that act as a fuel, and be described.2 identical conditions of Waste Heat Recovery System (WHRS) are: generate electricity, obtain identical heat, make identical amounts of hydrogen with oven with identical output power with generator.
Figure 12 is the procedure operation precedence diagram that the system of LNG is all used in expression as a comparative example.In this system, use the fuel of LNG, and use the fuel of LNG, and LNG is reformed in reformer 43 as generator 42 as oven 41, obtain hydrogen.The vent systems of generator 42 is provided with waste heat boiler 44, with the waste heat recovery of generator 42 as steam.In oven, obtain the heat of 3278Mcal/hr, in generator, obtain the output power of 5500kw, make 666Nm
3The amounts of hydrogen of/hr.If will obtain heat, output power, the amounts of hydrogen of above-mentioned numerical value, then only need to consume the LNG of amount as shown in table 1 below, and discharge CO
2
Table 1
| The LNG consumption | CO 2Discharge capacity | |
| Oven fuel consumption hydrogen is made (666Nm 3) generator fuel consumption | 4058Mcal/h 2454Mcal/h 11129Mcal/h | 953Kg/h 576Kg/h 2614Kg/h |
| Add up to | 17641Mcal/h | 4144Kg/h |
Utilize the user of Waste Heat Recovery System (WHRS) to wish and not only to reduce fuel consumption but also reduce CO
2Discharge capacity.If can reduce fuel consumption, then can seek to reduce cost, since COP3 has ratified the Kyoto Protocol, also must reduce the CO of society
2Discharge capacity.From such background, designed the Waste Heat Recovery System (WHRS) of LNG shown in Figure 11 and DME and usefulness.In the Waste Heat Recovery System (WHRS) of LNG shown in Figure 11 and DME and usefulness, the fuel of the gas electricity generator 31 that fuel consumption is big uses LNG, and in addition, oven 32 uses DME for making hydrogen.So just obtain fuel consumption as shown in table 2 below and CO
2Discharge capacity.
Table 2
| Fuel consumption | CO 2Discharge capacity | ||
| DME | Oven fuel consumption hydrogen is made (666Nm 3) | 3302Mcal/h 1651Mcal/h | 915Kg/h 458Kg/h |
| LNG | Generator fuel consumes | 11129Mcal/h | 2614Kg/h |
| Add up to | 16082Mcal/h | 3987Kg/h | |
As shown in Table 2, compare, and more can reduce CO with LNG and DME with the technology of whole use LNG
2Discharge capacity, but also can reduce fuel consumption.Think and to reduce CO
2Thereby discharge capacity is to have reduced this partial C O because the used heat of gas electricity generator 31 is converted into fuel
2The cause of discharge capacity.That is, separate the CO that produces by the 2nd heat exchanger 26
2, offer the 1st heat exchanger 25, by making CO
2In the 1st heat exchanger 25, mix and obtain CO fuel once more, so in Waste Heat Recovery System (WHRS), carrying out CO with DME
2Circulation, so reduced CO
2Discharge capacity.
Relatively summing up of 3 pairs of above-mentioned 2 Waste Heat Recovery System (WHRS) of following table.Example 1 is all to use the Waste Heat Recovery System (WHRS) of LNG, and example 2 is and with the Waste Heat Recovery System (WHRS) of LNG and DME.Example 2 can make fuel reduction 9% as can be known, can also make CO
2Discharge capacity reduces 4%.
Table 3
| Example 1 (only using LNG) | Example 2 (and using LNG and DME) | ||
| Generating in the factory | Rock gas (11129Mcal/h) | Rock gas (11129Mcal/h) | |
| Oven | Rock gas (4058Mcal/h) | Rock gas (3302Mcal/h) | |
| Hydrogen produces | Rock gas (2454Mcal/h) | Rock gas (1651Mcal/h) | |
| Add up to | The fuel economy | Radix (17641Mcal/h) | -9％(16082Mcal/h) |
| CO 2Discharge slip | Radix (4144Kg-CO 2/h) | -4％(3987Kg-CO 2/h) | |
What is called can be reduced fuel consumption and is meant and can bring cost advantage to the user.If the cost that will reduce is used as the financial resources of the universal DME that is for example obtained by biomass, waste, petroleum residue, coal bed methane or coal (below be called from biomass DME), then can also be on economic base, the DME from biomass of some percentages is sneaked into from the form among the DME of rock gas make DME circulation from biomass.If popularize DME, then more can reduce all CO that produces of society from biomass
2DME from biomass temporarily is being gasificated into CO+H with biomass etc. in gasification oven
2After, make with the DME synthetic reaction of the well-known catalyzer of script.
Figure 13 is the procedure operation precedence diagram of the Waste Heat Recovery System (WHRS) of expression the 2nd mode of execution of the present invention.The Waste Heat Recovery System (WHRS) of this mode of execution be provided with existing fuel such as LNG, heavy oil act as a fuel generating power generating equipment 51 and reclaim the waste heat recovery hydrogen manufacturing installation 52 of sensible heat of the exhaust of power generating equipment 51.Waste heat recovery hydrogen manufacturing installation 52 is the same with above-mentioned waste heat recovery plant, and the DME that provides is restructured as H
2+ CO
2Or H
2+ CO fuel.The H that makes
2After fuel separates in hydrogen separation device 53, or fueling battery 54, or the fuel of the battery car that acts as a fuel uses.This Waste Heat Recovery System (WHRS) for example is subjected to following control.When the needs of electric power are higher (daytime), the hydrogen of making in the waste heat recovery hydrogen manufacturing installation 52 is all offered fuel cell 54, makes energy be converted to electric power.On the other hand, when the needs of electric power hang down (night), the hydrogen of making in the waste heat recovery hydrogen manufacturing installation 52 is used as the fuel reserve of fuel cell car.Like this, by the waste heat recovery of will generating electricity as hydrogen, can realize the having load adjustment ability power generation system of (promptly can select hydrogen manufacturing and generating).
And, waste heat recovery plant of the present invention is not limited to generating, mining industry field, also can be arranged on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment of various industrial fields such as petrochemistry, paper paper pulp, nonferrous metal, cement, ceramic industry, transportation, in addition, can also be arranged on the people's livelihood, commercial field air-conditioning, kitchen, provide on the vent systems of the fuel-burning equipment that hot water uses.In addition, though waste heat recovery plant of the present invention is preferred for the temperature of exhaust in the vent systems more than 300 ℃, also can be effectively applied to delivery temperature in the vent systems below 300 ℃.
In addition, waste heat recovery plant of the present invention is not limited to the situation of generator, oven, hydrogen reformation, as long as the vent systems of stove, internal-combustion engine or power generating equipment is provided with waste heat recovery plant, just can be applied to the Waste Heat Recovery System (WHRS) of various changes, also can not have waste heat boiler when for example not needing steam.And the oven of Waste Heat Recovery System (WHRS) of the present invention is except industrial heating furnace, can be air-conditioning, kitchen also, the fuel-burning equipment that provides hot water to use, can also be replaced into fuel cell.
And, in waste recovery method of the present invention, also heat exchanger can be set, directly DME is blown into the vent systems of having filled catalyzer, DME is restructured as H
2Fuel or H
2With CO fuel.
Claims (21)
1. a waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
2. waste heat recovery plant according to claim 1 is characterized in that, for the temperature that makes described firing unit exhaust raises, drops into dimethyl ether in described vent systems.
3. a waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
4. waste heat recovery plant according to claim 3 is characterized in that, with the CO that contains of described firing unit
2Exhaust dehydration and deoxidation, the mixed gas that makes the exhaust of this dehydration and deoxidation and dimethyl ether is by described heat exchanger.
5. a waste heat recovery plant is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel,
On described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
6. waste heat recovery plant according to claim 5 is characterized in that, for the temperature that makes the described firing unit exhaust that drops into described the 2nd heat exchanger raises, with the H that reclaims in described the 1st heat exchanger
2And CO fuel drops into the vent systems between described the 1st heat exchanger and described the 2nd heat exchanger.
7. according to claim 5 or 6 described waste heat recovery plants, it is characterized in that the H that reclaims in separation and described the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 1st heat exchanger.
8. according to each described waste heat recovery plant in the claim 1～7, it is characterized in that described firing unit is gas turbine, gas engine or diesel engine, with the described H that reclaims
2Fuel or described H
2Use with the fuel of CO fuel as described gas turbine, described gas engine or described diesel engine.
9. according to each described waste heat recovery plant in the claim 1～7, it is characterized in that, the described H that reclaims
2Fuel or described H
2Use as the alternative fuel of the manufacture gas of iron works with CO fuel.
10. according to each described waste heat recovery plant in the claim 1～7, it is characterized in that, the described H that reclaims
2Fuel or described H
2Use with the act as a fuel fuel of battery of CO fuel.
11. a Waste Heat Recovery System (WHRS) is provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaims the waste heat recovery plant of the sensible heat of this firing unit exhaust, it is characterized in that,
Described waste heat recovery plant on the vent systems of described firing unit, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
12. a Waste Heat Recovery System (WHRS) is provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaims the waste heat recovery plant of the sensible heat of this firing unit exhaust, it is characterized in that,
Described waste heat recovery plant on the vent systems of described firing unit, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
13. a Waste Heat Recovery System (WHRS) is provided with firing units such as stove, internal-combustion engine or power generating equipment and reclaims the waste heat recovery plant of the sensible heat of this firing unit exhaust, it is characterized in that,
Described waste heat recovery plant on the vent systems of described firing unit, is provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel,
On described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel,
The H that reclaims in separation and described the 2nd heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 1st heat exchanger.
14., it is characterized in that described firing unit uses LNG (LNG Liquefied natural gas) to act as a fuel according to each described Waste Heat Recovery System (WHRS) in the claim 11～13.
15., it is characterized in that described Waste Heat Recovery System (WHRS) also is provided with the described H that burning is reclaimed according to each described Waste Heat Recovery System (WHRS) in the claim 11～14
2Oven or firing unit with CO fuel.
16. according to each described Waste Heat Recovery System (WHRS) in the claim 13～15, it is characterized in that, described Waste Heat Recovery System (WHRS) also is provided with described the 2nd heat exchanger waste heat boiler in downstream side more that is arranged on described vent systems, and the water vapour that this waste heat boiler is reclaimed offers described the 2nd heat exchanger.
17. a waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
18. a waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
19. a waste recovery method is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, is provided with the 1st heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and CO
2Mixed gas by described the 1st heat exchanger, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel,
On described vent systems, be provided with the 2nd heat exchanger of the catalyzer of having filled the reformation dimethyl ether, by with dimethyl ether and H
2The mixed gas of O makes the dimethyl ether thermolysis by described the 2nd heat exchanger, and the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel,
The H that reclaims in separation and described the 1st heat exchanger
2The produced simultaneously CO of fuel
2, with the CO that separates
2Offer described the 2nd heat exchanger.
20. waste recovery method, it is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, fill the catalyzer of reformation dimethyl ether, by dimethyl ether being blown into described vent systems, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2Fuel.
21. waste recovery method, it is characterized in that, on the vent systems of firing units such as stove, internal-combustion engine or power generating equipment, fill the catalyzer of reformation dimethyl ether, by dimethyl ether being blown into described vent systems, make the dimethyl ether thermolysis, the sensible heat of described firing unit exhaust is reclaimed as H
2With CO fuel.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2004193249 | 2004-06-30 | ||
| JP193249/2004 | 2004-06-30 | ||
| JP116222/2005 | 2005-04-13 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1981122A true CN1981122A (en) | 2007-06-13 |
Family
ID=38131576
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNA2005800217953A Pending CN1981122A (en) | 2004-06-30 | 2005-06-29 | Waste heat recovery apparatus, waste heat recovery system, and method of recovering waste heat |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1981122A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102022747A (en) * | 2010-11-18 | 2011-04-20 | 昆明龙鑫洋塑料防腐设备制造有限责任公司 | Application of dimethyl ether in industrial boiler and gas supply device of dimethyl ether |
| CN102174339A (en) * | 2011-03-25 | 2011-09-07 | 天津华迈燃气装备股份有限公司 | Dimethyl ether gasification device |
| CN103194285A (en) * | 2012-01-05 | 2013-07-10 | 东莞市久能二甲醚应用技术专利有限公司 | Industrial combustion method of dimethyl ether used for replacing natural gas through conversion |
| CN103449366A (en) * | 2012-05-30 | 2013-12-18 | 杜伟良 | Method for converting dimethyl ether into gas mainly containing hydrogen and directly combusting gas in industry |
| CN110793092A (en) * | 2019-11-26 | 2020-02-14 | 国网江苏省电力有限公司南通供电分公司 | Heat transfer device based on energy internet |
-
2005
- 2005-06-29 CN CNA2005800217953A patent/CN1981122A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102022747A (en) * | 2010-11-18 | 2011-04-20 | 昆明龙鑫洋塑料防腐设备制造有限责任公司 | Application of dimethyl ether in industrial boiler and gas supply device of dimethyl ether |
| CN102022747B (en) * | 2010-11-18 | 2013-07-17 | 昆明龙鑫洋塑料防腐设备制造有限责任公司 | Application of dimethyl ether in industrial boiler and gas supply device of dimethyl ether |
| CN102174339A (en) * | 2011-03-25 | 2011-09-07 | 天津华迈燃气装备股份有限公司 | Dimethyl ether gasification device |
| CN103194285A (en) * | 2012-01-05 | 2013-07-10 | 东莞市久能二甲醚应用技术专利有限公司 | Industrial combustion method of dimethyl ether used for replacing natural gas through conversion |
| CN103449366A (en) * | 2012-05-30 | 2013-12-18 | 杜伟良 | Method for converting dimethyl ether into gas mainly containing hydrogen and directly combusting gas in industry |
| CN103449366B (en) * | 2012-05-30 | 2015-07-22 | 杜伟良 | Method for converting dimethyl ether into gas mainly containing hydrogen and directly combusting gas in industry |
| CN110793092A (en) * | 2019-11-26 | 2020-02-14 | 国网江苏省电力有限公司南通供电分公司 | Heat transfer device based on energy internet |
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