CN106753569A - Low pressure dry powder coal gasifying process - Google Patents
Low pressure dry powder coal gasifying process Download PDFInfo
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- CN106753569A CN106753569A CN201611027610.6A CN201611027610A CN106753569A CN 106753569 A CN106753569 A CN 106753569A CN 201611027610 A CN201611027610 A CN 201611027610A CN 106753569 A CN106753569 A CN 106753569A
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- liquid
- synthesis gas
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- 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
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- 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
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- 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
- C10J2300/0953—Gasifying agents
- C10J2300/0959—Oxygen
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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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- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses a kind of low pressure dry powder coal gasifying process, including fine coal feeding gasification furnace gasification is obtained into synthesis gas, the synthesis gas sending into after washed in scrubbing tower synthesis gas by scrubbing tower top discharge feeding subsequent handling after gasification furnace hypomere water Quench, through in the perpendicular nozzle of top of gasification furnace and the lateral nozzle penetrating gasification furnace of the multiple of epimere side wall, simultaneously moment is ignited the mixture of the fine coal and oxygen respectively, in crossing state, fine coal gasifies generation synthesis gas the flame of formation at high temperature；The synthesis gas through air inlet enter scrubbing tower in right-angle elbow pipe in, the water smoke sprayed with obstruction shower nozzle in right-angle elbow pipe exit is sufficiently mixed and lowers the temperature, the water not being atomized then flows into scrubbing tower hypomere along the drainpipe of right-angle elbow pipe bottom, and the synthesis gas after washing is discharged by scrubbing tower top.Present invention process is simple, gasification efficiency is high, equipment investment and operating cost are low, security reliability is good, energy-saving, be particularly well-suited to low-pressure air current art dry coal powder gasification technology.
Description
Technical field
The present invention relates to coal gasification field, specifically a kind of low pressure dry powder coal gasifying process.
Background technology
At present fixed bed gasification technology, combustion are mainly used by raw material of coal by the gasification technology of gasification production fuel gas
Expect the specification of gas：Fuel atmospheric pressure≤0.5MPaG；Calorific value≤2800kcal/Nm3.Fixed bed gasification technology due to energy consumption it is higher-
Show as efficiency of carbon con version about 93%, and discharge of wastewater index is unsatisfactory for environmental protection requirement-show as content of organics in waste water
Up to 2000mg/L, and will gradually be eliminated.
In now more advanced second generation gasification technology, most representational is the water-coal-slurry pressurization gas of GE companies of the U.S.
Change technology, the GSP gasification technologies of Siemens, the SCGP dry coal powder pressure gasifying technologies of Dutch Shell Co. Ltd.These
Technology applies the operating mode in vapor pressure ＞ 4.0MPa, gasification, slagging-off, washing and usage on black water operation to be applied to high pressure substantially
Operating mode.For above-mentioned industry to the pressure demand of fuel gas and clean coal combustion gas the need for, using vapor pressure is relatively low, environmental protection
The good low pressure gas fluidized bed dry coal powder gasification technology of index is a solution.
But for the low-pressure air current art dry coal powder gasification technology that vapor pressure is only 0.3~2.5MPag, exist again
Problems with：1, after fine coal enters gasification furnace with conveying gas blowout, because gasification furnace pressure is relatively low, cause efficiency of carbon con version and gasification strong
Degree is reduced, so as to cause gas production to reduce.To improve efficiency of carbon con version, it is necessary to increase the volume of vaporizer in gasification furnace, to increase
The residence time of coal dust, it is high that this results in the production of gasification furnace, maintenance cost, preparation cost and the increased problem of difficulty；2, be
Fully synthesis gas is washed, it is necessary to be made synthesis gas be sufficiently mixed with cleaning solution, the past generally sets text outside scrubbing tower
Device makes synthesis gas mix with cleaning solution in mound, and synthesis gas local to venturi undergauge section can bring serious abrasion even worn out, be
Raising safety in operation, it will usually sleeve is added outside venturi, causes to install and safeguards inconvenience；3, due to system pressure drop
Low, the Heisui River temperature for causing shock chamber and scrubbing tower discharge is only to be spent 100 more, and this partial heat is difficult to be reclaimed using flash distillation, leads
Causing thermal loss, energy consumption increases, and is unfavorable for energy-saving.
The content of the invention
The invention aims to solve above-mentioned technical problem, there is provided a kind of process is simple, gasification efficiency are high, equipment is thrown
Money is with operating cost is low, security reliability is good, energy-saving, be particularly well-suited to the low pressure of low pressure gas fluidized bed dry coal powder gasification technology
Dry powder coal gasifying process.
Technical scheme includes for fine coal feeding gasification furnace gasification obtaining synthesis gas, and vapor pressure is 0.3~2.5MPag, institute
State synthesis gas sent into after gasification furnace hypomere water Quench washed in scrubbing tower after synthesis gas by scrubbing tower top discharge feeding
The mixture of subsequent handling, the fine coal and oxygen is lateral through the perpendicular nozzle of top of gasification furnace and the multiple of epimere side wall respectively
Nozzle is sprayed into gasification furnace and moment is ignited, and, in the state that crosses, fine coal gasifies generation synthesis gas at high temperature for the flame of formation；
The synthesis gas through air inlet enter scrubbing tower in right-angle elbow pipe in, right-angle elbow pipe exit with obstruction shower nozzle spray water
Mist is sufficiently mixed and lowers the temperature, and the water not being atomized then flows into scrubbing tower hypomere, the conjunction after washing along the drainpipe of right-angle elbow pipe bottom
Discharged by scrubbing tower top into gas.
The lateral nozzle has upward inclination angle, makes the joint of the flame in the top of lateral nozzle.
The upward tilt angles of the lateral nozzle are 5 °~35 °.
Annular space width between the obstruction shower nozzle and right-angle elbow pipe tube wall is 50mm~250mm.
The Heisui River feeding surge tank of the wash tower bottoms carries out preliminary sedimentation, then the filtering carried out through liquid filter
Treatment, is finally re-fed into stripper stripping.
Liquid after being stripped in the stripper carries out separation of solid and liquid into hydrocyclone, and top overflowing liquid is through recycle-water
Storage tank sends into scrubbing tower as cleaning solution, bottom containing solid-liquid through being carried out twice through first-class heat exchanger, secondary heat exchanger successively
Horizontal screw machine separation of solid and liquid is re-fed into after sending into the decompression of pressure-reducing cushioning tank after heat exchange recovery heat energy.
The liquid of the horizontal screw machine discharge is through circulating water storage tank feeding first-class heat exchanger and from hydrocyclone containing solid
Liquid heat exchange reclaims heat energy, and then loopback scrubbing tower is used as cleaning solution.
The surge tank and liquid filter bottom are also fed into hydrocyclone containing solid-liquid.
It is described gasification furnace bottom discharge Quench slag through continuous deslagging device be depressured after enter traveling one through dragveyer again
Step slag-liquid separation, the liquid feeding pressure-reducing cushioning tank isolated.
For problem present in background technology, inventor makes following improvement：(1), in gasification furnace, by past fine coal
Top spray is changed to by top-jet-type with the mixture of oxygen and side spray is combined, by increased multiple lateral nozzles, make the flame of ejection
Not only there is downwardly direction, also make a plurality of flame-shaped into the state of crossing, further make lateral nozzles inclined upwards, make flame
Joint be higher than lateral nozzle, so as to increased residence time of the coal dust in vaporizer, improve the efficiency of carbon con version of coal dust, solution
Certainly because low pressure gasifying brings the problem that coal dust distribution density is low, the residence time is short, therefore without increase gasification body of heater, reduce
It is equipment investment and operating cost, easy to maintain.(2) the venturi device between gasification furnace and scrubbing tower is eliminated, in scrubbing tower
Right-angle elbow pipe is set, the synthesis gas in gasification furnace is introduced in scrubbing tower by right-angle elbow pipe, due to the exit of right-angle elbow pipe
Obstruction head is set, is on the one hand sprayed and is atomized into droplet by blocking shower nozzle, mixed with synthesis gas, be conducive to synthesis gas
Washing, on the other hand, gas flow rate annular space very high is formed between obstruction head and the exit of right-angle elbow pipe, after mixing
Gas by obstruction shower nozzle around annular space continue up, increase afterwards because circulation area first reduces, flow velocity first becomes big
Reduce again afterwards, contact of the synthesis gas with droplet is more abundant, can strengthen the mixed effect of synthesis gas and droplet, effectively replaces
For venturi device, because this part-structure is located in tower, if there is abrasion, also occur over just in tower, will not be to system safety
Property is brought and is had a strong impact on, it is easy to safeguard.(3) it is relatively low for Heisui River temperature, it is unsuitable for the problem that heat energy is reclaimed in flash distillation, inventor is right
Separation of solid and liquid is first carried out to the Heisui River from stripper by hydrocyclone afterwards, the overflow liquid that top overflow goes out can be direct
Scrubbing tower is back to, the partially liq is lowered the temperature without step-down, direct loopback, with existing multistage flash evaporation and flashed vapour heating system
The method of circulation technology buck is compared, and circulating cooling water is on the one hand greatly reduced, and on the other hand, makes this acid Heisui River
Low-pressure low-temperature heat energy is effectively reclaimed, and step-down is small, energy-saving, environmentally friendly.(4) continuous deslagging device is employed, is dropped
Low device framework is highly, further energy-saving.
Further, the outflow of cyclonic unit bottom still keeps relevant temperature and pressure containing solid-liquid, can first through one-level
Heat exchanger reclaims heat energy, then is further cooled down through secondary heat exchanger, then sends into horizontal screw machine after being down to normal pressure through pressure-reducing cushioning tank and consolidate
Liquid is separated.
Further, it is used to reclaim the liquid that the heat transferring medium of heat energy is discharged from the horizontal screw machine in first-class heat exchanger,
Liquid after the liquid heat exchange also loopback scrubbing tower, only introduces recirculated cooling water, absolutely in secondary heat exchanger in whole technique
Most acid Heisui River is recycled utilization, greatly reduces the internal circulating load of recirculated cooling water, energy-saving.
Further, the upward tilt angles of the lateral nozzle are preferably 5 °~35 °, cross conference or too small can all make top
Putting the flame produced with side nozzle cannot cross well, so as to be unable to reach the purpose of enhancing mixing.；The obstruction shower nozzle
It is 50mm~250mm with the annular space width between right-angle elbow pipe tube wall., soaked with washings and washing effect with reaching reinforcing synthesis gas
The purpose of fruit, width is excessive, and gas flow rate change substantially, cannot not strengthen in expanding rear wetting effect..Width is too small, passage
Resistance drop is excessive, then can influence the economy of equipment.
Beneficial effect；
(1) low pressure gas fluidized bed dried coal powder gasification process of the invention is applied under 0.3-2.5MPa, gasification, deslagging and Heisui River
The design for the treatment of process is applied to this low pressure operating mode.About 1300 DEG C~1600 DEG C of gasification temperature, tar, phenol that coal gasification is produced
Decomposed Deng organic matter, larger molecular organicses have been free of in waste water, other content of organics are with bed technology than reducing
90%.The gasification, and combustion pattern sprayed into by improved fine coal improves carbon brick rate, higher than bed technology by 5%.
(2) usage on black water technology can save 35% circulating cooling water, effectively reclaim heat energy, reducing energy consumption；Continuously
Deslagging technique makes gasification frame reduction about 8m, and the height of conveying is needed so as to reduce system process circulation buck, saves energy consumption.
(3) present invention process is simple, equipment investment and operating cost is low, security reliability is good, energy-saving, particularly suitable
In low-pressure air current art dry coal powder gasification bed technique.
Brief description of the drawings
Fig. 1 is present invention process flow chart.
Fig. 2 is the scheme of installation of right-angle elbow pipe.
Fig. 3 is the arrangement schematic diagram of lateral nozzle.
Fig. 4 be lateral nozzle section under arrange schematic diagram.
Wherein, 1- gasification furnaces, 2- continuous deslagging devices, 3- scrubbing towers water circulating pump, 4- scrubbing towers, 4.1- right-angle elbow pipes,
4.2- annular spaces, 4.3- drainpipes, 4.4- obstructions shower nozzle, 5- dragveyers, 6- surge tanks, 7- liquid filters, 8- strippers, 9- water
Power cyclone, 10- reuses water storage tank, 11- first-class heat exchangers, 12- secondary heat exchangers, 13- pressure-reducing cushionings tank, 14- horizontal screw machines,
15- circulations water storage tank, 16- water circulating pumps, 17- dragveyers water pump, 18- reuses water pump, 19- perpendicular nozzles, the lateral nozzles of 20-.
Specific embodiment
Explanation is further explained to the present invention below in conjunction with the accompanying drawings：
System embodiment：
Referring to Fig. 1, the connection scrubbing tower 4 of gasification furnace 1, the top of the gasification furnace 1 is provided with nozzle sets, and the nozzle sets are by gas
The lateral nozzles 20 of multiple that the perpendicular nozzle 19 and epimere side wall at the top of change stove 1 are arranged circumferentially are (referring to Fig. 3 and Fig. 4, this reality
Apply in example as three) composition, the lateral nozzle 20 has upward inclination angle.The upward tilt angles a of the lateral nozzle is
5 °~35 °.；Working off one's feeling vent one's spleen for the gasification furnace 1 is connected with the air inlet of scrubbing tower 4, the circulating water outlet of the hypomere of the scrubbing tower 4
Scrubbed tower water circulating pump 3 is connected with the circulating water intake of gasification furnace 1.Referring to Fig. 2, be provided with inside the stage casing of the scrubbing tower 4 with
The right-angle elbow pipe 4.1 of air inlet connection, the bottom of the right-angle elbow pipe 4.1 is additionally provided with drainpipe 4.3 vertically downward, the right angle
The exit of bend pipe 4.1 is provided between obstruction shower nozzle 4.4, the tube wall for blocking shower nozzle 4.4 and right-angle elbow pipe 4.1 has annular space
4.2, the annular space width between the obstruction shower nozzle 4.4 and right-angle elbow pipe tube wall is 50mm~250mm；The gasification furnace 1 and washing
The outlet of the bottom Heisui River of tower 4 is sequentially connected surge tank 6, liquid filter 7 and stripper 8.The liquid outlet of the bottom of the stripper 8
Connection hydrocyclone 9, the overfall at the top of the hydrocyclone 9 is through reuse water pot 10, the connection scrubbing tower of reuse water pump 18
4, the leakage fluid dram of bottom is connected through first-class heat exchanger 11, secondary heat exchanger 12, pressure-reducing cushioning tank 13 and horizontal screw machine 14 successively.It is described
The liquid outlet of horizontal screw machine 14 connects 11 and connects scrubbing tower 4 through circulating water storage tank 15, water circulating pump 16, first-class heat exchanger.The buffering
Tank 6, the leakage fluid dram of the bottom of liquid filter 7 are also connected with aqueous vapor movable flow device 9.On the other hand the slag of the bottom of the gasification furnace 1 goes out
Mouth is connected through continuous deslagging device 2 with dragveyer 5 successively, and the leakage fluid dram of the dragveyer 5 is also slow with decompression through dragging for pulp water pump 17
Tank 13 is rushed to connect.
Process example：
Referring to Fig. 1-Fig. 3,
Respectively by the perpendicular nozzle 19 () and side wall at the top of gasification furnace 1 after the coal dust of Geldart-D particle and oxidation mixing
(three) penetrating gasification furnaces of lateral nozzle 20, carry out violent chemical reaction and produce the flame of the synthesis gas of high temperature, formation to be in
Cross state, and at 1300~1600 DEG C, vapor pressure is 0.3~2.5MPag to temperature, and synthesis gas is in the bottom of gasification furnace 1 by water
Chilling process is lowered the temperature and removes substantial amounts of lime-ash, and the bottom of gasification furnace 1 produces substantial amounts of Quench slag, and Quench slag is through continuous deslagging device
2 enter dragveyer 5, and the solid slag that dragveyer is pulled out is discharged into out-of-bounds, and liquid is through the feeding pressure-reducing cushioning of dragveyer water pump 17 tank 13；
Synthesis gas in gasification furnace 1 after cooling enters the further cooling dedusting of scrubbing tower 4, and synthesis gas enters by air inlet
Right-angle elbow pipe 4.1, is moved upwards by right-angle elbow pipe 4.1, and by blocking during shower nozzle 4.4, washings spray from obstruction shower nozzle 4.4
And droplet is atomized into, and being mixed with synthesis gas, mixed gas continues by the annular space 4.2 around obstruction shower nozzle 4.4
Motion, increases afterwards because circulation area first reduces upwards, and flow velocity first becomes big rear and reduces, and contact of the synthesis gas with droplet is more
Fully, the mixed effect of synthesis gas and droplet can be strengthened.The water that fraction is not atomized is then by through the bottom of right-angle elbow pipe 4.1
The tunnel of drainpipe 4.3 enter the bottom of scrubbing tower 4.Synthesis gas successively passes upward through the tower tray layer of scrubbing tower 4 and fills out after leaving bend pipe
The bed of material contacts washing with process water, and dustiness is further reduced in making synthesis gas, and dustiness is less than 1mg/Nm3, the conjunction after washing
Into gas (also known as raw gas) gasification battery limit (BL) is discharged eventually through the syngas outlet at top.A part of Heisui River of the bottom of scrubbing tower 4
The bottom of gasification furnace 1 then is returned to by scrubbing tower water circulating pump 3, is used as chilled water.
(temperature is 110~200 DEG C, and pressure is 0.3 in the Heisui River discharged from the Heisui River of the bottom of scrubbing tower 4 and gasification furnace bottom
~2.5MPag, the solid particle containing solid content less than 2.8wt%,
The CO of 100~2000ppm2, SO2, H2The sour gas such as S) preliminary sedimentation is carried out into surge tank 6 together, then pass through
The filtration treatment that liquid filter 7 is carried out, preliminary sedimentation, the purpose of filtering are to prevent solid particle from being caused in follow-up equipment
Block.Filtrate (solid content be less than 1.6wt%) after filtering finally enters stripper 8 and strips that (stripping fluid is steam or inertia
Gas), the CO dissolved in removing Heisui River2, SO2, H2The sour gas such as S, stripper 8 produce sour gas by top discharge into
Enter postprocessing working procedures, such as shift conversion step or thermo-power station.Liquid after the stripping of stripping tower bottom 4 and from surge tank and filter body mistake
Filter 7 bottom sends into hydrocyclone 9 containing solid-liquid together, and separation of solid and liquid, water are further realized by hydraulic cyclone effect
The top overflowing liquid of power cyclone 9 (temperature be 110~200 DEG C, pressure be 0.2~2.4MPag, content of acid gas be 20ppm with
Under, solid content is down to below 0.1wt%) into storing standby in reuse water storage tank 10, most it is recycled to through recycle-water pump 18 afterwards and is washed
Tower 4 is washed as cleaning solution.The bottom of hydrocyclone 9 carries out cooling treatment containing solid-liquid by two-stage heat exchanger, one-level heat exchange
Device 11 is exchanged heat using circulation technology buck, can use recirculated cooling water conduct with recovery section heat, secondary heat exchanger 12
Cooling medium, is cooled to less than 50 DEG C and is depressurized into pressure-reducing cushioning tank 13 afterwards in liquid, and subsequently entering horizontal screw machine 14 carries out slag liquid
Separate, it is standby that liquid after separation enters circulation water pot 15, wet ash discharge battery limit (BL), circulate clarified solution (the i.e. circulation industrial of water pot 15
Skill buck) reuse of loopback scrubbing tower 4 again after water circulating pump 16 carries out indirect heat exchange into first-class heat exchanger 11, it is possible to reduce
The loss of heat, improves the utilization ratio of heat.
Claims (9)
1. a kind of low pressure dry powder coal gasifying process, including fine coal feeding gasification furnace gasification is obtained into synthesis gas, vapor pressure is 0.3
~2.5MPag, the synthesis gas sending into after washed in scrubbing tower synthesis gas by scrubbing tower after gasification furnace hypomere water Quench
Top discharge feeding subsequent handling, it is characterised in that the mixture of the fine coal and oxygen is respectively through the vertical of top of gasification furnace
The lateral nozzle of multiple of nozzle and epimere side wall is sprayed into gasification furnace and moment is ignited, and the flame of formation is in cross state, powder
Coal gasifies generation synthesis gas at high temperature；The synthesis gas through air inlet enter scrubbing tower in right-angle elbow pipe in, in quarter bend
The water smoke that pipe exit sprays with obstruction shower nozzle is sufficiently mixed and lowers the temperature, and the water not being atomized is then along the drainpipe of right-angle elbow pipe bottom
Scrubbing tower hypomere is flowed into, the synthesis gas after washing is discharged by scrubbing tower top.
2. low pressure dry powder coal gasifying process as claimed in claim 1, it is characterised in that the lateral nozzle has and upward inclines
Angle, makes the joint of the flame in the top of lateral nozzle.
3. low pressure dry powder gasification system as claimed in claim 2, it is characterised in that the upward inclination angle angle of the lateral nozzle
Spend is 5 °~35 °.
4. low pressure dry powder coal gasifying process as claimed in claim 1, it is characterised in that the obstruction shower nozzle and right-angle elbow pipe pipe
Annular space width between wall is 50mm~250mm.
5. the low pressure dry powder coal gasifying process as described in claim any one of 1-4, it is characterised in that the wash tower bottoms
Heisui River feeding surge tank carries out preliminary sedimentation, then the filtration treatment carried out through liquid filter, is finally re-fed into stripper vapour
Carry.
6. low pressure dry powder coal gasifying process as claimed in claim 5, it is characterised in that the liquid after being stripped in the stripper
Separation of solid and liquid is carried out into hydrocyclone, top overflowing liquid sends into scrubbing tower as cleaning solution through reuse water storage tank, bottom
Pressure-reducing cushioning tank is sent into containing solid-liquid after being exchanged heat twice through first-class heat exchanger, secondary heat exchanger reclaim heat energy successively to depressurize
After be re-fed into horizontal screw machine separation of solid and liquid.
7. the low pressure dry powder coal gasifying process described in claim 6, it is characterised in that the liquid of the horizontal screw machine discharge is through circulation
Water storage tank sends into first-class heat exchanger and reclaims heat energy, then loopback scrubbing tower conduct with from hydrocyclone heat exchange containing solid-liquid
Cleaning solution.
8. low pressure dry powder coal gasifying process as claimed in claims 6 or 7, it is characterised in that the surge tank and liquid are filtered
Device bottom is also fed into hydrocyclone containing solid-liquid.
9. low pressure dry powder coal gasifying process as claimed in claims 6 or 7, it is characterised in that the gasification furnace bottom row
The Quench slag for going out carries out further slag-liquid separation through dragveyer again after being depressured through continuous deslagging device, and the liquid feeding isolated subtracts
Pressure surge tank.
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| CN107418634A (en) * | 2017-09-15 | 2017-12-01 | 中科清能燃气技术（北京）有限公司 | A kind of circulation fluidized bed coal gasifying Multi-stage cooling dust collecting process and device |
| CN108795502A (en) * | 2018-08-21 | 2018-11-13 | 北京清创晋华科技有限公司 | A kind of dry coal powder airflow bed gasification system of low pressure and method |
| CN109082305A (en) * | 2018-08-28 | 2018-12-25 | 昆山优利德能源技术有限公司 | The integration heating raw material coal water slurry gasification system and technique of heat exchange without phase-change |
| CN109097107A (en) * | 2018-08-28 | 2018-12-28 | 昆山优利德能源技术有限公司 | The coal water slurry gasification system and technique of high efficient heat exchanging applied to air flow bed |
| CN109135832A (en) * | 2018-09-25 | 2019-01-04 | 深圳瑞科天启科技有限公司 | A kind of water-coal-slurry gasification method and device recycling carbon black water waste heat |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107418634A (en) * | 2017-09-15 | 2017-12-01 | 中科清能燃气技术（北京）有限公司 | A kind of circulation fluidized bed coal gasifying Multi-stage cooling dust collecting process and device |
| CN107418634B (en) * | 2017-09-15 | 2023-05-16 | 中科清能燃气技术（北京）有限公司 | Multistage cooling and dedusting process and device for circulating fluidized bed coal gasification |
| CN108795502A (en) * | 2018-08-21 | 2018-11-13 | 北京清创晋华科技有限公司 | A kind of dry coal powder airflow bed gasification system of low pressure and method |
| CN109082305A (en) * | 2018-08-28 | 2018-12-25 | 昆山优利德能源技术有限公司 | The integration heating raw material coal water slurry gasification system and technique of heat exchange without phase-change |
| CN109097107A (en) * | 2018-08-28 | 2018-12-28 | 昆山优利德能源技术有限公司 | The coal water slurry gasification system and technique of high efficient heat exchanging applied to air flow bed |
| CN109135832A (en) * | 2018-09-25 | 2019-01-04 | 深圳瑞科天启科技有限公司 | A kind of water-coal-slurry gasification method and device recycling carbon black water waste heat |
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