CN1029689C - Circulation fluidized-bed gas-steam combine producing process and device - Google Patents
Circulation fluidized-bed gas-steam combine producing process and device Download PDFInfo
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- CN1029689C CN1029689C CN 92100503 CN92100503A CN1029689C CN 1029689 C CN1029689 C CN 1029689C CN 92100503 CN92100503 CN 92100503 CN 92100503 A CN92100503 A CN 92100503A CN 1029689 C CN1029689 C CN 1029689C
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- Prior art keywords
- steam
- gas
- bed
- roasting kiln
- air
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- Expired - Lifetime
Links
- 238000000034 method Methods 0.000 title claims abstract description 14
- 239000000463 material Substances 0.000 claims abstract description 56
- 239000000446 fuel Substances 0.000 claims abstract description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 7
- 238000002485 combustion reaction Methods 0.000 claims description 27
- 238000002309 gasification Methods 0.000 claims description 25
- 239000007789 gas Substances 0.000 claims description 23
- 239000006200 vaporizer Substances 0.000 claims description 19
- 230000008676 import Effects 0.000 claims description 14
- 239000000567 combustion gas Substances 0.000 claims description 9
- 239000000126 substance Substances 0.000 claims description 9
- 238000005192 partition Methods 0.000 claims description 5
- 238000005243 fluidization Methods 0.000 claims description 4
- 235000003599 food sweetener Nutrition 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 239000003765 sweetening agent Substances 0.000 claims description 4
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000002245 particle Substances 0.000 claims 1
- 238000009423 ventilation Methods 0.000 claims 1
- 239000003795 chemical substances by application Substances 0.000 abstract description 6
- 239000000571 coke Substances 0.000 abstract 3
- 238000005422 blasting Methods 0.000 abstract 1
- 239000003034 coal gas Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 230000003009 desulfurizing effect Effects 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004043 dyeing Methods 0.000 description 1
- 239000003546 flue gas Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 229910052760 oxygen Inorganic materials 0.000 description 1
- 238000007639 printing Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 210000003296 saliva Anatomy 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 238000009941 weaving Methods 0.000 description 1
Images
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E20/00—Combustion technologies with mitigation potential
- Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
- Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
Landscapes
- Fluidized-Bed Combustion And Resonant Combustion (AREA)
Abstract
The present invention discloses a circulating fluidized bed process and device for co-producing gas and steam. The process comprises the steps: fuels are delivered into a gasifier by a feeding machine and are gasified to generate gas; gasifying semi-coke and low-temperature cycle materials in the gasifier are delivered into a burner by a material returning device; the gasifying semi-coke or the gasifying semi-coke and partial fuels are burned under the blasting action of air to generate heat to heat the low-temperature cycle materials, so that temperature is raised; then, the heated low-temperature cycle materials are delivered into the gasifier by the material returning device, a steam heat exchanger is heated to convert water into steam at the same time, and partial steam and the gas are used as gasifying agents for the gasifier. The device designed by the process has two types, namely an inner circulation type and an outer circulation type. The device has the advantages of wide applicability to the fuels, high utilizing rate and high gas heat value.
Description
The present invention relates to circulation fluidized-bed gas-steam combine producing process and device.
Existing burning boiler and vapourizing furnace can only produce steam and coal gas singlely, can only produce 1200Kcd/Nm as industrial widely used atmospheric air air blast vapourizing furnace such as normal pressure lurgi gasifier, Winkler stove etc.
3About low-heat value gas, can't satisfy civilian needs, its key reason is to adopt air continuous blast to make coal combustion produce heat, air feedization is with heat.Burn part coal gas on the one hand, 79% nitrogen is arranged in the air on the other hand, so caloric power of gas is very low.In order to address this problem, adopt air vapor to replace the blue-gas generator of air blast usually, thereby make technology become very complicated, the coal gas amount is unstable again.Need acquire simultaneously special-purpose steam boiler steam supply again.And adopt the pure oxygen air blast, and it is complicated more to increase oxygenerator, technology again, and the investment tool is big.Samll cities and towns' gas supply critical shortage in China and the vast rural area of the third world, and the large-scale producer gas plant of unable construction at present.
The purpose of this invention is to provide a kind of circulation fluidized-bed gas, steam co-producing technology and device.
Be illustrated below in conjunction with accompanying drawing.
Fig. 1 is the circulation fluidized-bed gas-steam combine producing process synoptic diagram;
Fig. 2 is an external circulation fluidized bed gas-steam combine producing device synoptic diagram;
Fig. 3 is inner circulation fluidized bed gas-steam combine producing device synoptic diagram;
Fig. 4 is inner circulation fluidized bed gas-steam combine producing device recycle stock mouth profile synoptic diagram.
Circulation fluidized-bed gas-steam combine producing process is: fuel 3 is sent into gasification furnace 1 through batcher and is taken place to supply outside the hot combustion gas 12 directly of pyrolytic gasification reaction generation. Or after cooling and dedusting washing, become clean combustion gas output. The part combustion gas is sent gasification furnace back to and is realized the combustion gas circulation, to increase steam decomposition rate, improves the combustion gas conversion ratio. Gasification char in the gasification furnace Deliver to combustion furnace 2 with low-temperature circulating material 10 through material returning device, gasification char or gasification char and part of fuel produce heat through air blast 4 burnings, and heating low-temperature circulating material makes it become high temperature circulation material 9, send into gasification furnace for gasifying with heat through material returning device. Simultaneously, steam heat-exchanger 8 makes water 6 become steam 7 outer confessions in the heating furnace. Part steam is made gasifying agent for gasification furnace. Part of fuel also can directly feed combustion furnace by batcher. Can add desulfurizing agent and replenishment cycles material 5 in the combustion furnace. Recycle stock can be inert material such as sand and multiple biomass fuel and the semicoke of coal after gasification etc. Gases Recirculation can pass through Venturi tube, pumps to realize with high steam.
External circulation fluidized bed gas-steam combine producing device, it has combustion furnace 13, gasification furnace 24, separator 27 and middle material returning device 21. The separator import communicates with the combustion furnace outlet, and the separator feed opening communicates with the gasification furnace bottom through tremie pipe. Middle material returning device communicates with gasification furnace bed top and combustion furnace bottom respectively. Separator import department is provided with steam heat-exchanger 31 makes water 28 become steam 30 outer confessions. Flue gas is discharged from exporting 29. Gasification furnace top also is provided with fuel inlet 25, gas outlet 26, and the gasification furnace bottom is provided with gasifying agent import 23 and communicates with steam heat-exchanger steam (vapor) outlet branch road. Combustion furnace also is provided with combustion furnace fuel inlet 14 and air intlet 19, and heat exchanger 18 makes water 17 become steam 16 outer confessions. Middle material returning device bottom air compartment communicates with air channel 22, and top is provided with vertical baffle 21, and middle material returning device is divided into feed space (linking to each other with gasification furnace), and with returning charge chamber (linking to each other with combustion furnace), bottom, two Room communicates. In returning charge chamber one side, have air vent on the dividing plate of air compartment. Also be provided with desulfurizing agent and replenishment cycles material inlet 15 in the combustion furnace. The gasifying agent import communicates with the gas outlet branch road, and Gases Recirculation can be pumped to realize with high steam by Venturi tube.
The roasting kiln of this device adopts air blast, the fast bed operation.Vapourizing furnace adopts steam and recirculation gas blast bubbling bed operating.During operation, the recycle stock that comes from middle material returning device is entered by the roasting kiln bottom, is carried secretly to the top outlet by air-flow and enters separator, separates the back recycle stock and delivers to the vapourizing furnace bottom through tremie pipe, and material returning device in the middle of overflowing to from vapourizing furnace bed top, thereby realize that material circulates between two stoves.General gasifier operation temperature is 700-800 ℃, and the roasting kiln operating temperature is 900-1000 ℃, so this device adopts solid heat carrier method to provide to gasify thermal source promptly to rely on the temperature difference between two, and utilizing material to circulate provides the gasification thermal source.
Reasonable operating mode through the advance copy device is:
1. the roasting kiln operating air velocity should be 1.1～1.6ut, and ut is an overall dimension particulate terminal settling velocity in the recycle stock.Could keep steady running and a large amount of recycle stock of fast bed to carry like this.
2. middle material returning device is the key part of this device, test shows to the various ways material returning device, adopt loop seals device form as shown in the figure to have the characteristic of start and stop Load Regulation preferably, the operation logic of this material returning device is the one side air blast of returning charge chamber, feed chamber one side material is the adhesion secondary flowage, enters the returning charge chamber through underclearance.Returning charge chamber material is the fluidized-bed operation, and returning charge wind is carried material secretly and delivered to roasting kiln through revert pipe, by regulating returning charge air quantity Control Circulation inventory easily, close returning charge wind, material returning device just stops returning charge, and the bottom gap height should guarantee that material does not flow automatically and be advisable, can be suitably more greatly.
3. vapourizing furnace is a low speed bubbling bed operating, high-temperature material is sent into from bed bottom one side through tremie pipe (can in stove), returning charge is then returned near the opposite side charge level, thereby guarantees temperature uniformity in the stove, and the blanking caliber can be 0.05～0.15m/s design by material flow.
Test shows that the circulation ratio of this device can reach 30-80 doubly, and air leakage is less than 1%.
Inner circulation fluidized bed gas-steam combine producing device characteristic is: be provided with vaporizer 44 side by side, combustion chamber 47, two Room separate with partition wall 43, and partition wall is provided with cocycle material mouth 40 and following recycle stock mouth 39 by the wall both sides, the oblique baffle plate 41 that is provided with of cocycle material mouth upside in the vaporizer.Bottom, two Room is respectively equipped with air distribution plate, air compartment, and communicate with air intlet 46 and vaporized chemical import 45 respectively.Vaporizer also is provided with vaporizer fuel inlet 38 and gas outlet 37, and the combustion chamber also is provided with combustion chamber fuel inlet 32, exhanst gas outlet 34.The combustor exit place is provided with steam heat exchanger 33, makes water 35 become steam 36, and steam heat exchanger vapour outlet branch road communicates with the vaporized chemical import.Roasting kiln also is provided with sweetening agent and replenishment cycles material inlet 51, and interchanger 49 makes water 48 become steam 50.Said vaporized chemical import also communicates with the gas outlet branch road.
This device vaporizer adopts steam and recirculation gas blast, and air blast is adopted in the combustion chamber, and vaporizer (low speed bed) wind speed is lower than combustion chamber (bed at a high speed).Because two wind speed is poor, causes the two bed operating height of bed, voidage difference.Produce from vaporizer to combustion chamber pressure reduction at following recycle stock mouth, promote material and flow to the combustion chamber, produce from the combustion chamber to vaporizer pressure reduction promotion material at top recycle stock mouth and flow to vaporizer from the combustion chamber, thereby the realization material circulates between two from vaporizer.The vaporizer operating temperature is 700-800 ℃, chamber temperature is 900-1000 ℃, rely on two between material temperature difference gasification heat absorption is provided, at cocycle material mouth upside one sloping baffle is set, stop combustion chamber gas to enter vaporizer, guarantees two between good resistance to air loss.Be provided with a dividing plate 42 perpendicular to partition wall in the middle of the recycle stock mouth up and down,, guaranteeing temperature homogeneity in the stove to prevent the recycle stock short circuit.
Through reasonable operation condition of advance copy device and scantlings of the structure be:
Decide on industrial application apart from the distance of air distribution plate following recycle stock mouth lower edge, the smaller the better.Last material mouth lower edge is near the quiet height of bed.Following recycle stock open height △ H
1, general △ H
1/ H
Mf=0.125～0.25, H
MfFor moving quiet bed of material height, cocycle material open height △ H
2Be △ H
2/ △ H
1=1～1.5.Two recycle stock mouth width △ L
1, △ L
2Decide by design.The horizontal saliva of two recycle stock mouths is flat to be decided on industrial application apart from △ L, big as far as possible.Two bed operating fluidising air velocity N
L＞2.2, N
h/ N
L=1.3～1.7(N
LBe low speed bed fluidization number, N
hBe high speed bed fluidization number), looking actual motion needs to regulate.
Test shows that this device circulation ratio can reach 70 times, and leak rate is less than 3%.
Advantage of the present invention is: 1. can produce steam simultaneously, produce industrial saturation steam or superheated vapour, combustion gas and generating.2. suitability of fuel is wide.Owing to adopt the fluidized-bed operation scheme, applicable multiple biomass fuel and coal.3. caloric power of gas height.Adopt the confession steam gasification, caloric power of gas can reach 2500～3000Kcal/Nm
3More than, do not need special oxygen generating plant, compare with similar vapourizing furnace, have characteristics such as simple in structure, reduced investment.4. fuel availability height.Gasification char after the vapourizing furnace gasification further burns through roasting kiln, and fuel availability is up to more than 90%.5. produce coal gas amount and stable components.Usually adopt continuous charging, the continuous discharging slag mode, vaporizer and combustion chamber parallel running have kept the stable of coal gas amount and composition.6. it is low to produce pollution.Because adopt the fluidized-bed mode to move, it is less to produce tar content, and adopts the desulfuration in furnace technology, thereby has simplified the afterbody treatment system.7. can be widely used in industries such as metal heat treatmet, weaving, printing and dyeing, food.
Claims (5)
1, a kind of circulation fluidized-bed gas-steam combine producing process is characterized in that:
A. fuel [3] is sent into the reaction of vapourizing furnace [1] generation pyrolytic gasification through feeding machine and is produced combustion gas [12], part of fuel is directly sent into roasting kiln [2] by feeding machine, the part combustion gas is sent vapourizing furnace back to and is realized the combustion gas circulation, in roasting kiln, add sweetening agent and replenishment cycles material [5], vaporizer adopts steam and recirculation gas blast, air blast is adopted in the combustion chamber, external circulation fluidized bed roasting kiln operating air velocity is 1.1～1.6ut, ut is the terminal settling velocity of largest particle in the recycle stock, Internal Circulating Fluidized Bed vaporizer (low speed bed) wind speed is lower than combustion chamber (bed at a high speed), two bed operating fluidising air velocity N
L＞2.2, N
h/ N
L=1.3～1.7 (N
LBe low speed fluidization number, N
hBe high speed bed fluidization number);
B. gasification char and the cold cycle material [10] in the vapourizing furnace delivered to roasting kiln [2] through material returning device, gasification char or gasification char and part of fuel produce heat through air blast [4] burning, heating low temperature follows material, make it become high temperature circulation material [9], send into the vapourizing furnace air feedization with hot through material returning device, simultaneously, heating steam interchanger [8] makes water [6] become steam [7], and part steam is made vaporized chemical for vapourizing furnace.
2, a kind of device according to the circulation fluidized-bed gas-steam combine producing process design, it is characterized in that: it has roasting kiln [13], vapourizing furnace [24], separator [27], and middle material returning device [21], the separator import communicates with the roasting kiln outlet, the separator feed opening communicates with the vapourizing furnace bottom through tremie pipe, middle material returning device communicates with vapourizing furnace bed top and roasting kiln bottom respectively, separator ingress is provided with steam heat exchanger [31], vapourizing furnace top also is provided with fuel inlet [25], gas outlet [26], the vapourizing furnace bottom is provided with vaporized chemical import [23] and communicates with steam heat exchanger vapour outlet branch road, and roasting kiln also is provided with roasting kiln fuel inlet [14] and air intlet [19].
3, a kind of device according to claim 2 according to the circulation fluidized-bed gas-steam combine producing process design, it is characterized in that said middle material returning device bottom air compartment communicates with air channel [22], top is provided with vertical baffle [20] middle material returning device is divided into feed chamber (linking to each other with vapourizing furnace) and returning charge chamber (linking to each other with roasting kiln), bottom, two Room communicates, on the dividing plate of one crosswind chamber, returning charge chamber, have ventilation hole, also be provided with sweetening agent and replenishment cycles material inlet [15] in the said roasting kiln, interchanger [18], said vaporized chemical import also communicates with the gas outlet branch road.
4, a kind of device according to the circulation fluidized-bed gas-steam combine producing process design, it is characterized in that being provided with side by side vaporizer [44], combustion chamber [47], two Room with partition wall [43] separately, partition wall is by the wall both sides, be provided with cocycle material mouth [40] and following recycle stock mouth [39], the oblique baffle plate [41] that is provided with of cocycle material mouth upside in the vaporizer, bottom, two Room is respectively equipped with air distribution plate, air compartment, and communicate with air intlet [46] and vaporized chemical import [45] respectively, vaporizer also is provided with vaporizer burning import [38] and gas outlet [37], the combustion chamber also is provided with combustion chamber fuel inlet [32], the combustor exit place is provided with steam heat exchanger [33], and steam heat exchanger vapour outlet branch road communicates with the vaporized chemical import.
5, a kind of device according to claim 4 according to the circulation fluidized-bed gas-steam combine producing process design, it is characterized in that said roasting kiln also is provided with sweetening agent and replenishment cycles material inlet [51], interchanger [49], said vaporized chemical import communicates with the gas outlet branch road.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92100503 CN1029689C (en) | 1992-01-23 | 1992-01-23 | Circulation fluidized-bed gas-steam combine producing process and device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 92100503 CN1029689C (en) | 1992-01-23 | 1992-01-23 | Circulation fluidized-bed gas-steam combine producing process and device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1074699A CN1074699A (en) | 1993-07-28 |
| CN1029689C true CN1029689C (en) | 1995-09-06 |
Family
ID=4938626
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 92100503 Expired - Lifetime CN1029689C (en) | 1992-01-23 | 1992-01-23 | Circulation fluidized-bed gas-steam combine producing process and device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1029689C (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN102099625B (en) * | 2008-07-15 | 2013-07-17 | 株式会社Ihi | Bed height controller for fluidized bed gasification furnace in gasification facility |
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| CN101294092B (en) * | 2007-04-25 | 2012-07-25 | 中国科学院过程工程研究所 | Combined thermal transition method and apparatus for solid fuel |
| JP5282465B2 (en) * | 2008-07-11 | 2013-09-04 | 株式会社Ｉｈｉ | Method and apparatus for controlling fluid medium residence time of fluidized bed gasifier in gasification facility |
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-
1992
- 1992-01-23 CN CN 92100503 patent/CN1029689C/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102099625B (en) * | 2008-07-15 | 2013-07-17 | 株式会社Ihi | Bed height controller for fluidized bed gasification furnace in gasification facility |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1074699A (en) | 1993-07-28 |
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Expiration termination date: 20120130 Granted publication date: 19950906 |