CN1869166A - Fluidized bed gasification furnace with solid-state aih discharge and its indnstrial application - Google Patents
Fluidized bed gasification furnace with solid-state aih discharge and its indnstrial application Download PDFInfo
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- CN1869166A CN1869166A CN 200610026335 CN200610026335A CN1869166A CN 1869166 A CN1869166 A CN 1869166A CN 200610026335 CN200610026335 CN 200610026335 CN 200610026335 A CN200610026335 A CN 200610026335A CN 1869166 A CN1869166 A CN 1869166A
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- cooling
- scrubbing
- vaporizer
- gasification furnace
- tube
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- 238000002309 gasification Methods 0.000 title claims abstract description 29
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 239000003034 coal gas Substances 0.000 claims abstract description 24
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 14
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 14
- 150000001875 compounds Chemical class 0.000 claims abstract description 11
- 238000001816 cooling Methods 0.000 claims description 46
- 239000006200 vaporizer Substances 0.000 claims description 30
- 238000005516 engineering process Methods 0.000 claims description 23
- 238000005406 washing Methods 0.000 claims description 11
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000000498 cooling water Substances 0.000 claims description 3
- 230000008676 import Effects 0.000 claims description 3
- 241001416181 Axis axis Species 0.000 claims description 2
- 239000003245 coal Substances 0.000 abstract description 11
- 229910052717 sulfur Inorganic materials 0.000 abstract description 3
- 239000011593 sulfur Substances 0.000 abstract description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 abstract description 2
- 238000007599 discharging Methods 0.000 abstract 1
- 239000000463 material Substances 0.000 abstract 1
- 238000002360 preparation method Methods 0.000 abstract 1
- 239000007787 solid Substances 0.000 abstract 1
- 238000005507 spraying Methods 0.000 abstract 1
- 239000002956 ash Substances 0.000 description 31
- 239000007789 gas Substances 0.000 description 17
- 150000001722 carbon compounds Chemical class 0.000 description 11
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 8
- 238000000034 method Methods 0.000 description 8
- 239000000428 dust Substances 0.000 description 7
- 239000012159 carrier gas Substances 0.000 description 6
- 239000003818 cinder Substances 0.000 description 6
- 239000002826 coolant Substances 0.000 description 6
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 5
- 230000000694 effects Effects 0.000 description 5
- 230000004927 fusion Effects 0.000 description 5
- 229910052760 oxygen Inorganic materials 0.000 description 5
- 239000001301 oxygen Substances 0.000 description 5
- 239000000843 powder Substances 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 238000006243 chemical reaction Methods 0.000 description 4
- 229910052757 nitrogen Inorganic materials 0.000 description 4
- 239000002002 slurry Substances 0.000 description 4
- 239000002893 slag Substances 0.000 description 3
- 239000007921 spray Substances 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 238000002844 melting Methods 0.000 description 2
- 230000008018 melting Effects 0.000 description 2
- 239000011819 refractory material Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 238000007664 blowing Methods 0.000 description 1
- 239000010883 coal ash Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000002498 deadly effect Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000000151 deposition Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 229910052742 iron Inorganic materials 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000013517 stratification Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
- C10J3/845—Quench rings
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
- C10K1/00—Purifying combustible gases containing carbon monoxide
- C10K1/08—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors
- C10K1/10—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids
- C10K1/101—Purifying combustible gases containing carbon monoxide by washing with liquids; Reviving the used wash liquors with aqueous liquids with water only
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/152—Nozzles or lances for introducing gas, liquids or suspensions
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
-
- 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
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Gasification And Melting Of Waste (AREA)
- Air Supply (AREA)
Abstract
The invention relates to a coal gas preparation facilities used carbon and ash containing compound as the material. It discloses entrained flow gasification furnace with solid state ash discharging and its industrial application. The gasification furnace is upright and has many nozzles. Its fireproof lining is conical surface. Its water spraying ring is set softening jam and two rows of holes. It can be applied to treat the coal with high ash fusing point, high ash content, and high sulfur and the big gasifier.
Description
Technical field
The present invention relates to a kind ofly contain device and the industrial application thereof that grey compound is a feedstock production coal gas, relate in particular to a kind of airflow bed gasification furnace with carbon containing.
Background technology
Gasification be carbon compound efficient, buy the main path that net profit is used.The primary product of gasification is a coal gas, and its component mainly comprises CO and H
2, can be used for producing NH
3, CH
3OH, (CH
3)
2Fields such as O, liquid fuel, generating (IGCC), sponge iron.
Modern big type coal gasification full scale plant generally adopts airflow bed gasification furnace, and the ash content in the carbon compound all adopts liquid discharge method.Hold the disclosed technology of patent ZL.98110616.1 as United States Patent (USP) 4637823 (GE-Texaco), Chinese patent 90103807.5 (shell) and applicant.
But objectively, a lot of coal ash content height, the ash fusion point height will adopt slag tap, and temperature of reaction is higher, and for example 1400～1700 ℃, under so high temperature, the refractory materials in the stove is difficult to anti-anti-.In case cooling just can cause the obstruction of cinder notch down again.Therefore, designing a kind of solid-state ash exhauster that can effectively utilize after the big gasification of ash fusion point height, ash content, will have great industrial application meaning, also is the problem that the gasification field is extremely paid close attention to.
Summary of the invention
The technical issues that need to address of the present invention are airflow bed gasification furnace and the industrial application thereof that disclose a kind of solid-state ash discharge, to overcome the above-mentioned defective that prior art exists.
Design of the present invention is such:
Reach the temperature that refractory materials can bear at reducing gasification temperature (being lower than following 50～200 ℃ of carbon raw material ash fusion point), its deadly defect is to stop up the inducement of cinder notch, and the present invention has adopted four countermeasure in engineering:
(1) in vaporizer, do not form the step of depositing slag, and adopt conical surface slope, make ash be difficult for remaining in the vaporizer;
(2) near cinder notch, form gas velocity faster, make coal gas more carry dust, the separate and subside of reduction slag;
(3) near cinder notch configuration down, stop up by reduction as far as possible for water ring, and water ring has two rounds, and direction is different, makes lime-ash sneak into water coolant early, does not adhere to wall;
(4) the high pressure gas jet pipe is set, in case when the resistance of cinder notch increases, can be by blowing the high pressure gas mediation.
The airflow bed gasification furnace of solid-state ash discharge of the present invention comprises:
Cylindrical tube;
Be arranged on the vaporizer and the scrubbing-cooling chamber that is arranged on the cylindrical tube bottom on cylindrical tube top;
Said vaporizer comprises the technology nozzle box, preheating burner chamber, brick-supporting rack and refractory liner, the technology nozzle box is arranged on the periphery of vaporizer, the technology nozzle mechanically is installed in the technology nozzle box, preheating burner chamber is arranged on the vaporizer top, the preheating burner is vertically set in the preheating burner chamber, refractory liner is arranged on the inwall of cylindrical tube, place, technology nozzle box is straight tube, below the straight tube is up big and down small frustum, the above semisphere dome of straight tube for upwards throwing, brick-supporting rack is arranged on the vaporizer bottom, is used to support refractory liner, and the vaporizer bottom is coal gas and lime-ash outlet; Said technology nozzle adopts various ways, as being that raw material adopts the applicant in Chinese patent 95111750.5 and 97235458.1 structures that proposed with slurry attitude carbon compound, as being that raw material adopts the applicant in Chinese patent 200420114032.6 and 200510025050.6 structures that proposed with dry powder attitude carbon compound, relevant technician can select as required;
Said scrubbing-cooling chamber comprises water ring, scrubbing-cooling tube, foam-breaking strip, high pressure gas nozzle and cooling ring pipe;
Said water ring is arranged on the top of scrubbing-cooling chamber, is connected with washing entrance of cooling water on the cylindrical tube, and water ring is provided with along the last hole and the following hole in ring week; Said scrubbing-cooling tube is fixed on the below of water ring by brick-supporting rack, and foam-breaking strip is arranged in the cavity between scrubbing-cooling tube and the cylindrical tube, and the main effect of foam-breaking strip is abolished air pocket and strengthened washing effect; The cooling ring pipe is arranged on the below of brick-supporting rack, the top of scrubbing-cooling tube, is connected with water jet on being arranged on cylindrical tube, and the cooling ring pipe is provided with perforate along circumference; The high pressure gas nozzle is arranged on scrubbing-cooling tube middle part, is connected with high pressure gas import on the cylindrical tube by pipeline; Syngas outlet is arranged on the cylindrical tube on scrubbing-cooling tube top, and the bottom of cylindrical tube is the pulp water outlet.
It is feedstock production coal gas that the airflow bed gasification furnace of solid-state ash discharge of the present invention can be used for containing grey compound with carbon containing, with particle diameter is that the slurry attitude of＜200 μ m or the carbon compound (for example coal) of dry powder attitude are transported to the technology nozzle, the carbon compound of slurry attitude is carried with high-pressure pump, and the carbon compound of dry powder attitude is carried as nitrogen with carrier gas; Gasifying medium and/or process steam also enter the technology nozzle simultaneously to be mixed, with the flow velocity of 90～140 meter per seconds, ejection technology nozzle is coal gas with entering the vaporizer gasification after carbon compound atomizing or the disperse, when containing grey compound for the charging of slurry attitude, without steam as carbon containing; When coal gas carried dust and enters the refractory liner of truncated conelike, gas velocity increased, and the gas speed of the coal gas when going out coal gas and lime-ash and exporting is 0.5～10m/s.
Gasification temperature is 1100～1400 ℃, and vapor pressure is 1.0～10.0MPa;
Said gasifying medium is selected the empty oxygen that divides for use, and the volumetric concentration of its oxygen is＞85%;
The ratio that gasifying medium and carbon containing contain grey compound is (oxygen coal ratio): 400～750Nm
3Gasifying medium/1000kg carbon containing contains grey compound;
When adopting the charging of dry powder attitude, the ratio that process steam and carbon containing contain grey compound is (steam coal ratio): 0～500kg process steam/1000kg carbon containing contains grey compound; The ratio of carrier gas and carbon compound is (solid-gas ratio): 100～600kg carbon containing contains grey compound/m
3Carrier gas;
The front and back pressure reduction of coal gas and lime-ash outlet is 0～0.1MPa;
The temperature of carrying dust is that 1100～1400 ℃ coal gas passes water ring then and enters scrubbing-cooling chamber, temperature is that 165～300 ℃ water coolant sprays from the last hole of water ring and following hole, coal gas is cooled in scrubbing-cooling chamber, and to be cooled to temperature be 175～310 ℃ for water cooling washing, and the water coolant that is vaporized in the coal gas after the washing and the cooling washing process enters lower procedure from syngas outlet; Most of dust ash is under the effect of foam-breaking strip, and the separated liquid phase that enters enters upstream device from the pulp water outlet then.This process is being identical as the contriver described in the patent ZL.01112880.1.
When the front and back pressure reduction of coal gas and lime-ash outlet surpasses 0.04MPa, then feed high pressure gas, blow dust stratification off, said high pressure gas is selected from nitrogen or coal gas, and pressure is 5.0～12.0MPa;
Further, the brick-supporting rack temperature surpasses 260～350 ℃, then water coolant is fed water jet, then sprays from the cooling ring pipe, and brick-supporting rack is lowered the temperature.
Adopt device of the present invention to prepare coal gas, the carbon compound that can select the high ash content of high ash melting point is a raw material, and for example the coal of 1400～1700 ℃ of ash fusion points can carry out solid-state ash discharge.The advantage of this gasification installation is that the raw material suitability is wide, gasification installation can be stablized long-term operation, efficiency of carbon conversion and effective pneumatolytic divide high, reduced investment, ((coal of sulfur-bearing＞4%wt) and day handle an extensive gasification production technique more than 1000 tons has great industrial application meaning to contain ash＞15%wt), high-sulfur to be particularly suitable for handling high ash melting point (＞1400 ℃), high ash content.
Description of drawings
The airflow bed gasification furnace of a kind of dry ash extraction of Fig. 1.
D-D is to synoptic diagram among Fig. 2 Fig. 1.
Fig. 3 water ring synoptic diagram.
Embodiment
Referring to Fig. 1 and Fig. 2, the airflow bed gasification furnace of solid-state ash discharge of the present invention comprises:
Cylindrical tube 1;
Be arranged on the vaporizer 5 and the scrubbing-cooling chamber 11 that is arranged on cylindrical tube 1 bottom on cylindrical tube 1 top;
Said vaporizer 5 comprises technology nozzle box 21, preheating burner chamber 4, brick-supporting rack 6 and refractory liner 3, technology nozzle box 21 is arranged on vaporizer 5 all round, preferably be provided with 3～6, evenly distributed, the technology nozzle mechanically is installed in the technology nozzle box 21, preheating burner chamber 4 is arranged on vaporizer 5 tops, the preheating burner is vertically set in the preheating burner chamber 4, its axis axis best and vaporizer 5 coincides, refractory liner 3 is arranged on the inwall of vaporizer 5, the epimere of technology nozzle box 21 and hypomere are straight tube, below the straight tube is frustum, see that the A among Fig. 1 lights to the bottom of vaporizer 5, the angle β between itself and frustum and the sea line is 75～89 °, and top is preferably the semisphere dome of upwards throwing; The vaporizer bottom is coal gas and lime-ash outlet 17;
Said scrubbing-cooling chamber 11 comprises water ring 7, scrubbing-cooling tube 8, foam-breaking strip 9, high pressure gas nozzle 15 and cooling ring pipe 18;
Said water ring 7 is arranged on the top of scrubbing-cooling chamber 11, as seen from Figure 3, said water ring 7 is connected with washing entrance of cooling water 10 on the cylindrical tube 1, water ring 7 is provided with along the last hole 71 and the following hole 72 in ring week, the medullary ray in last hole 71 and the angle between the vertical line are 40～50 °, and the medullary ray in following hole 72 and the angle between the vertical line are 18～22 °;
Said scrubbing-cooling tube 8 is fixed on the below of water ring 7 by brick-supporting rack 6, and foam-breaking strip 9 is arranged in the cavity between scrubbing-cooling tube 8 and the cylindrical tube 1, and the main effect of foam-breaking strip 9 is to abolish air pocket to strengthen washing effect.
High pressure gas nozzle 15 is arranged on scrubbing-cooling tube 8 middle parts, is connected with high pressure gas import 14 on the cylindrical tube 1 by pipeline;
Syngas outlet 12 is arranged on the cylindrical tube 1 on scrubbing-cooling tube 8 tops, and the bottom of cylindrical tube 1 is pulp water outlet 16.
Embodiment 1
Handle the multi-nozzle powder coal gasification furnace of 1200 (butts) ton coal one day, adopt nitrogen to make the fine coal delivery medium, vapor pressure is 4.0MPa, and gasification temperature is 1350 ℃, and vaporized chemical is oxygen and water vapor, and the oxygen total burn-off is 25800Nm
3/ h, the steam total burn-off is 12500kg/h, goes out vaporizer total gas flow rate 100466Nm
3/ h.Efficiency of carbon conversion＞98%, effectively gas (CO+H
2) composition＞90%.
The front and back pressure reduction of coal gas and lime-ash outlet is＜0.04MPa;
Carrier gas is a nitrogen, and the ratio of carrier gas and carbon compound is (solid-gas ratio): the 400kg carbon containing contains grey compound/m
3Carrier gas;
The temperature of carrying dust is that 1350 ℃ coal gas passes water ring and enters scrubbing-cooling chamber, temperature sprays from the last hole of water ring and following hole for～218 ℃ water coolant, coal gas is cooled in scrubbing-cooling chamber, and to be cooled to temperature be 220 ℃ for water cooling washing, and the water coolant that is vaporized in the coal gas after the washing and the cooling washing process enters lower procedure from syngas outlet; The separated liquid phase that enters of most of dust ash enters upstream device from the pulp water outlet then.
Device structure such as Fig. 1～Fig. 3, significant parameter is as follows:
Vaporizer housing interior diameter is Φ 3400mm, vaporizer straight section reaction zone interior diameter D=Φ 2200mm, top, nozzle box straight section length 1.6D, the hypomere straight section length 0.5D of nozzle box, vaporizer frustum segment length 4D, cinder notch diameter 0.5D under the vaporizer.
Be provided with 4 technology nozzles, the technology that all adopts Chinese patent 200420114032.6 to propose.
The frustum of refractory liner 3 and the angle β between the sea line are 86.42 °, the semisphere dome of top for upwards throwing.
Coal analysis
| Ultimate analysis (wt%, butt) | |
| C | 70.78 |
| H | 2.36 |
| N | 0.86 |
| S | 4.5 |
| O | 1.50 |
| Ash | 20 |
| Ash fusion point ℃ | 1450 |
Go out vapourizing furnace scrubbing-cooling chamber gaseous constituent (vol%, butt)
| H 2 | 26.80 |
| CO | 63.29 |
| CO 2 | 2.04 |
| H 2S | 1.42 |
| COS | 0.15 |
| CH 4 | 0.14 |
| N 2 | 6.14 |
Claims (5)
1. the airflow bed gasification furnace of a solid-state ash discharge, comprise: cylindrical tube (1), be arranged on the vaporizer (5) on cylindrical tube (1) top and be arranged on the scrubbing-cooling chamber (11) of cylindrical tube (1) bottom, said vaporizer (5) comprises technology nozzle box (21), preheating burner chamber (4), brick-supporting rack (6) and refractory liner (3), technology nozzle box (21) is arranged on vaporizer (5) all round, preferably be provided with 3～6, evenly distributed, the technology nozzle mechanically is installed in the technology nozzle box (21), preheating burner chamber (4) is arranged on vaporizer (5) top, the preheating burner is vertically set in the preheating burner chamber (4), its axis axis best and vaporizer (5) coincides, refractory liner (3) is arranged on the inwall of vaporizer (5), and the vaporizer bottom is coal gas and lime-ash outlet (17);
It is characterized in that: refractory liner (3) is straight tube at the epimere and the hypomere of technology nozzle box (21), is frustum below the straight tube;
Said scrubbing-cooling chamber (11) comprises water ring (7), scrubbing-cooling tube (8), foam-breaking strip (9), high pressure gas nozzle (15) and cooling ring pipe (18);
Said water ring (7) is arranged on the top of scrubbing-cooling chamber (11), and water ring (7) is connected with washing entrance of cooling water (10) on the cylindrical tube (1), and water ring (7) is provided with along the ring last hole (71) and the following hole (72) in week;
Said scrubbing-cooling tube (8) is fixed on the below of water ring (7) by brick-supporting rack (6), and foam-breaking strip (9) is arranged in the cavity between scrubbing-cooling tube (8) and the cylindrical tube (1),
Cooling ring pipe (18) is arranged on the below of brick-supporting rack (6), the top of scrubbing-cooling tube (8), is connected with water jet (13) on being arranged on cylindrical tube (1), and cooling ring pipe (18) is provided with aperture along circumference;
High pressure gas nozzle (15) is arranged on scrubbing-cooling tube (8) middle part, is connected with high pressure gas import (14) on the cylindrical tube (1) by pipeline.
2. the airflow bed gasification furnace of solid-state ash discharge according to claim 1 is characterized in that, the frustum of refractory liner (3) and the angle β between the sea line are 75～89 °.
3. the airflow bed gasification furnace of solid-state ash discharge according to claim 2 is characterized in that, the top of refractory liner (3) is preferably the semisphere dome of upwards throwing.
4. the airflow bed gasification furnace of solid-state ash discharge according to claim 1 is characterized in that, the medullary ray of last hole (71) and the angle between the vertical line are 40～50 °, and the medullary ray in following hole (72) and the angle between the vertical line are 18～22 °.
5. the application of the airflow bed gasification furnace of solid-state ash discharge according to claim 1 is characterized in that, being used for containing grey compound with carbon containing is feedstock production coal gas.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610026335 CN100535087C (en) | 2006-05-08 | 2006-05-08 | Fluidized bed gasification furnace with solid-state aih discharge and its indnstrial application |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200610026335 CN100535087C (en) | 2006-05-08 | 2006-05-08 | Fluidized bed gasification furnace with solid-state aih discharge and its indnstrial application |
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| CN100535087C CN100535087C (en) | 2009-09-02 |
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Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101709228A (en) * | 2009-11-26 | 2010-05-19 | 中节环(北京)能源技术有限公司 | Biomass three-section type entrained flow bed gasification technology with function of waste heat utilization |
| CN101775313A (en) * | 2010-03-06 | 2010-07-14 | 太原理工大学 | Entrained flow gasifier |
| CN1994865B (en) * | 2006-12-12 | 2011-05-18 | 华东理工大学 | Gasification device for two-stage gasification coupled with heat recovery and washing and its uses |
| CN101003358B (en) * | 2006-12-12 | 2011-05-18 | 华东理工大学 | Multi nozzle gasification furnace feeding in hydrocarbon-including plasma or powder state |
| CN101486928B (en) * | 2009-02-18 | 2012-11-07 | 刘宏建 | Temperature control method for fixed bed gasification furnace oxidation zone and gasification furnace |
| CN102994160A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Entrained-flow bed gasifier for solid-phase deslagging |
| CZ304134B6 (en) * | 2012-04-20 | 2013-11-13 | Millenium Technologies A.S. | Apparatus for gasification of various kinds of feed material |
| CN104583377A (en) * | 2012-07-09 | 2015-04-29 | 南方公司 | Gasification of high ash, high ash fusion temperature bituminous coals |
| CN106545831A (en) * | 2017-01-24 | 2017-03-29 | 北京金泰瑞和工程科技有限公司 | Waste heat boiler heat exchanger and fixed bed pressured gasification system |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
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2006
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| CN102994160A (en) * | 2012-10-11 | 2013-03-27 | 田原宇 | Entrained-flow bed gasifier for solid-phase deslagging |
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| CN106545831A (en) * | 2017-01-24 | 2017-03-29 | 北京金泰瑞和工程科技有限公司 | Waste heat boiler heat exchanger and fixed bed pressured gasification system |
| CN109054901A (en) * | 2018-08-01 | 2018-12-21 | 万华化学集团股份有限公司 | A kind of down-flow fluidized bed using ECT-fluidized bed tandem gasification process and device |
| CN109054901B (en) * | 2018-08-01 | 2020-09-08 | 万华化学集团股份有限公司 | Descending bed-fluidized bed series type gasification method and device |
| CN112480967A (en) * | 2020-10-21 | 2021-03-12 | 齐祖彬 | Slag discharging device of fluidized bed garbage gasification furnace |
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