CN104987889A - Second-segment entrained flow bed gasification method - Google Patents
Second-segment entrained flow bed gasification method Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 82
- 238000000034 method Methods 0.000 title claims abstract description 32
- 239000003245 coal Substances 0.000 claims abstract description 40
- 239000000446 fuel Substances 0.000 claims abstract description 25
- 238000006243 chemical reaction Methods 0.000 claims abstract description 20
- 239000002893 slag Substances 0.000 claims abstract description 12
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 10
- 239000006200 vaporizer Substances 0.000 claims description 45
- 239000007789 gas Substances 0.000 claims description 36
- 239000002245 particle Substances 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 19
- 238000002485 combustion reaction Methods 0.000 claims description 19
- 239000001301 oxygen Substances 0.000 claims description 19
- 229910052760 oxygen Inorganic materials 0.000 claims description 19
- 238000012546 transfer Methods 0.000 claims description 18
- 239000002817 coal dust Substances 0.000 claims description 15
- 239000003034 coal gas Substances 0.000 claims description 9
- 239000007921 spray Substances 0.000 claims description 9
- 238000001816 cooling Methods 0.000 claims description 7
- 239000000203 mixture Substances 0.000 claims description 7
- 239000013589 supplement Substances 0.000 claims description 6
- 239000000428 dust Substances 0.000 claims description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 3
- 239000002028 Biomass Substances 0.000 claims description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 2
- 235000011089 carbon dioxide Nutrition 0.000 claims description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 2
- 230000002708 enhancing effect Effects 0.000 claims description 2
- 150000002430 hydrocarbons Chemical class 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 229910052757 nitrogen Inorganic materials 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 abstract description 7
- 238000005516 engineering process Methods 0.000 abstract description 4
- 239000010881 fly ash Substances 0.000 abstract description 3
- 239000002699 waste material Substances 0.000 abstract description 3
- 239000003795 chemical substances by application Substances 0.000 abstract description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 2
- 230000002035 prolonged effect Effects 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 11
- 239000000126 substance Substances 0.000 description 10
- 238000002156 mixing Methods 0.000 description 9
- 239000000567 combustion gas Substances 0.000 description 5
- 239000000843 powder Substances 0.000 description 3
- 206010020843 Hyperthermia Diseases 0.000 description 2
- 239000002956 ash Substances 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 230000036031 hyperthermia Effects 0.000 description 2
- 239000004615 ingredient Substances 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 239000004480 active ingredient Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000002802 bituminous coal Substances 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000003628 erosive effect Effects 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000007774 longterm Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002844 melting Methods 0.000 description 1
- 230000008018 melting Effects 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000001590 oxidative effect Effects 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000005855 radiation Effects 0.000 description 1
- 230000036632 reaction speed Effects 0.000 description 1
- 230000003014 reinforcing effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005728 strengthening Methods 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
Abstract
The invention discloses a second-segment entrained flow bed gasification method. In order to widely popularize an entrained flow bed gasification technology, a gasification reaction method which is long in service life, high in carton conversion rate and uniform in gasification reaction intensity needs to be developed. In the first segment, part of gasification fuel in a pre-gasification chamber is gasified to generate high-temperature raw gas, and in the second segment, a gasification agent continues to be supplemented in a main gasification chamber so that the high-temperature raw gas jetted from the pre-gasification chamber and remaining gasification fuel can be completely gasified. The service life of a furnace liner is prolonged, the carbon conversion rate can be over 99.5%, and fly ash components in gas can be reduced by 40-70%; besides, fuel waste caused when pulverized coal falls in a slag pond through a slag discharge opening is reduced, and the method is particularly suitable for occasions where pulverized coal is used for manufacturing industrial gas.
Description
Technical field
The present invention relates to gasification field, specifically a kind of two-section type entrained flow gasification method.
Background technology
Development of industry in China be unable to do without coal, and current groundwork is solution Coal Clean, utilizes efficiently, with the discharge of decreasing pollution thing, improves the utilization ratio of fuel.In the industry using coal gasification as the most effectual way of cleaning coal utilization, it is one of China's energy strategy important development direction.
Current nearly all dry coal powder airflow bed gasification furnace all adopts directly to throwing in coal dust and vaporized chemical (oxygen, water vapour) in vapourizing furnace, and the main kinetic energy of vaporized chemical jet that relies on realizes mixing mass transfer effect in vapourizing furnace between vaporized chemical with coal dust, and this gasification process easily causes following problem:
One, near process burner ejiction opening, on the one hand because oxygen concentration is quite high, fugitive constituent is overflowed rapidly by the coal dust in addition owing to injecting burner hearth, under the Involving velocity of jet, oxidizing reaction often along with high strength near burner, temperature is very high, causes the furnace lining of burner near zone to be easy to, by erosion, scaling loss, therefore directly cause vapourizing furnace blowing out.
Two, do not form uniform mass transfer intensity in vapourizing furnace, burner near zone mass transfer intensity is large, and the region mass transfer intensity away from burner is minimum, finally affects gasification efficiency; Because mixing mass transfer intensity in vapourizing furnace is mainly caused by vaporized chemical jet, nature is very large in jet exit near zone mass transfer intensity, and temperature levels is higher, and pulverized coal particle has just started to carry out gasification reaction, activity is comparatively large, and therefore the gasification reaction speed in this region is also very fast; Then in the region away from jet exit, in stove, the intensity of mixing mass transfer weakens gradually, and temperature of reaction also reduces, and the reactive behavior of the semicoke particle in this region is minimum, makes these semicoke particles can not get being gasified totally, have impact on the efficiency of gasification of coal.
In sum, entrained flow bed gasification technology be made extensively to be promoted, need to develop one and possess long service life, efficiency of carbon conversion height and the uniform gasification reaction method of gasification response intensity.
Summary of the invention
The present invention is directed to the deficiency of above-mentioned existing entrained flow bed gasification technology, a kind of two-section type entrained flow gasification method is provided, it first generates high temperature rough gas in pre-vaporized room vaporising fuel partial gasification at first paragraph, and second segment continues to supplement high temperature rough gas that vaporized chemical makes pre-vaporized room inject and remains vaporising fuel and is gasified totally in main vaporizer.
For this reason, the present invention solves above-mentioned technical problem by the following technical programs: a kind of two-section type entrained flow gasification method, it comprises the steps:
Step 1), spray in pre-vaporized room by 30 ~ 80% of whole vaporising fuels and gasification amount of oxygen, in pre-vaporized indoor, the vaporising fuel of 20 ~ 85% is gasified and generate high temperature rough gas, then high temperature rough gas and the semicoke particle completely that do not gasify spray into main vaporizer from exit, pre-vaporized room, mass percent shared by the height temperature rough gas of exit, pre-vaporized room is 25 ~ 98%, and pre-vaporized room temperature out controls between 800 ~ 1400 DEG C;
Step 2), supplement remaining gasification oxygen by the technique nozzle be arranged on main vaporizer, high temperature rough gas and and the semicoke particle and being gasified totally in main vaporizer with the gasification oxygen of secondary supplement completely that do not gasify.Namely in main vaporizer, remaining vaporized chemical (gasify 20 ~ 70% of the total consumption of oxygen needed for whole vaporising fuel) is sprayed into by technique nozzle (i.e. vaporized chemical nozzle).
The airflow bed gasification furnace of two-section type gasification possesses higher carbon conversion efficiency.Active ingredient in the indoor coal particles of pre-vaporized obtains and gasifies rapidly, at least complete the gasification reaction of 30 ~ 90%, relative difficult carries out main vaporizer with the semicoke particle of gasification along with coal gas jet, the semicoke particle of small particle size in coal gas, continuing, having acted on of powerful swirling eddy is gasified rapidly, larger, the semicoke particle do not gasified and ash content simultaneously rapidly catch by the slag film of melting on the wall of main vaporizer, sufficient gasification reaction is carried out under the disturbance of wall air-flow, most fuel ash defines slag and wall along main vaporizer falls into slag bath Quench, contained carbon residue is almost nil, enter flying dust residual carbon content entrained in the air-flow in slag bath on a small quantity very low, the slag particles that slag bath is discharged is clean clean.In addition, because efficiency of carbon conversion reaches more than 99.5%, in coal gas, contained flying dust is also little, greatly reduces follow-up load of dust remove.
Described oxidation can adopt oxygen enrichment or air to replace.
Further, described pre-vaporized room is one or more, and the outlet of pre-vaporized room is connected with main vaporizer, the method of enhancing mixed mass transfer utilizing the jet of exit, pre-vaporized room height temperature rough gas to form the circle of contact or liquidate in main vaporizer, makes the conversion zone forming good mass-transfer heat transfer in winner's vaporizer; Coal gasification burner is equipped with in room to pre-vaporized.
Because pre-vaporized room volume is little, pre-vaporized room can be designed as demountable parts, separates with main vaporizer; Pre-vaporized room is relative to main vaporizer, and working conditions rather harsh, such structure design has taken into full account the accessibility of maintenance of the equipment: when pre-vaporized room is damaged, and the pre-vaporized chamber component that can at once more renew, resumes production at once.
Because the raw gas volumetric flow rate of pre-vaporized room outlet is large, therefore raw gas jet rigidity is large, jet is easy to the conversion zone forming good mass-transfer intensity in main vaporizer, plays very important effect to solid-state semicoke particle gasification remaining in the high temperature rough gas of strengthening.
The vaporized chemical (gasify 30 ~ 80% of the total consumption of oxygen needed for whole vaporising fuel) of whole vaporising fuels and part enters pre-vaporized room by starting ignition burner and process burner, due to the oxygen that the oxygen entered is not all needed for gasification, therefore pre-vaporized room temp is not high, and pre-vaporized room temperature out controls between 800 ~ 1400 DEG C.
Further, described coal gasification burner comprises main burner and is arranged at least one coal nozzle on main burner outer wall,
The head of one flame detecting pipe is placed in the central position in described main burner, and the skin of flame detecting pipe is provided with blast tube, and the head of this blast tube is provided with gas jet; The skin of described blast tube is provided with combustion air passage, and the head of this combustion air passage is provided with cyclone structure, and described gas jet and cyclone structure are all placed in main burner;
The space formed between described flame detecting tube head to main burner head is settling chamber, and the length of this settling chamber is 0.2 ~ 3:1 with the ratio of main burner internal diameter;
Be provided with burning torch in described combustion wind passage, the crater of this burning torch is positioned at settling chamber, and the afterbody of flame detecting pipe is provided with flame detecting device;
During coal gasification burner work, logical cooling air in described flame detecting pipe.
During coal gasification burner work, combustion air is after the cyclone structure of combustion air passage head, with the combustion gas mixing ejected from gas jet, settling chamber produce rotate flow field carry out primary combustion, then with eddy flow shape toward jet flames in the burner hearth of main burner outside; When after the temperature reaching regulation in burner hearth, the coal dust ejected from coal nozzle mixes with from prechamber injection flame out, and ignite coal dust, takes fire in burner hearth; After coal powder ignition in burner hearth is stable, close gas supply, settling chamber cutoff, mix with from coal nozzle coal dust out in main burner outlet from settling chamber combustion air out, in burner hearth high temperature reflux flue gas igniting under, in burner hearth, realize stable burning or gasification.Described combustion air is one or several mixture of air, oxygen enrichment, pure oxygen.
Further, described main burner is cylindrical, and its outlet is reducing, effectively ensures that the flame sprayed in burner hearth is eddy flow shape; Described coal nozzle is arranged on main burner exit, burns, and do not burn in settling chamber after making the coal dust that ejects from coal nozzle and mixing from prechamber injection flame out in burner hearth; The outer wall of described main burner connects at least one water-cooling channel of lowering the temperature for main burner, main burner is protected.
Further, described main vaporizer is one, is also provided with slag-drip opening and gas exit in main vaporizer.
Further, described coal gas comprises the component of following mass percent: carbon monoxide 5 ~ 80%, hydrogen 5 ~ 50%, methane 0 ~ 10%, hydrocarbon compound 0 ~ 5%, nitrogen 2 ~ 70%, carbonic acid gas 3 ~ 20% and water vapor 2 ~ 22%.
The mixture that described high temperature rough gas is made up of the coal gas of pure gaseous state, do not gasify solid-state semicoke particle, solid-state flying dust and molten slag completely.
Described vaporising fuel is one or more the mixture in coal dust, coke powder, biomass fuel.
In the gasification zone of described first paragraph, its effect is that first the vaporized chemical of utilization part gasifies to gasifying section the easiest in vaporising fuel, the raw gas volumetric flow rate produced is large, and jet possesses larger rigidity, ready for creating good mixing mass transfer effect in second segment vaporizer; Amount of oxygen in addition owing to entering this region is less, reduces the temperature of localized high temperature regions near burner, plays the effect of protection furnace lining.
After vaporising fuel and partial gasification agent enter pre-vaporized room, in vaporising fuel, the easiest gasifying section is gasified in pre-vaporized room, general bituminous coal just can complete the vaporization rate of nearly more than 70% within the time in a short second, therefore pre-vaporized room is not high to the mixing mass transfer requirement of strength in burner hearth, and therefore in structure design, pre-vaporized indoor are not easy the high-temperature area producing local; In addition because pre-vaporized room does not spray into the oxygen all needed for gasification, therefore pre-vaporized room is easy to be designed to the burner hearth that does not have localized hyperthermia, very well helps, pre-vaporized room can be worked steadily in the long term to protection furnace lining.
In the gasification zone of described second segment; its effect carries out fully gasifying thoroughly to the semicoke particle do not gasified in pre-vaporized room; because remaining semicoke seed activity is lower; require that burner hearth inner transmission matter effect will be got well; therefore main vaporizer space is comparatively large, to the gasification reaction time that remaining semicoke particle is longer.
The flow velocity of the high temperature rough gas jet in exit, pre-vaporized room is 5 ~ 50m/s.
Step 2) in, from exit, pre-vaporized room spray into air-flow main vaporizer along main vaporizer surrounding rotate and under, spiral along main vaporizer central position again after arriving bottom and up flow, discharge from the outlet at main vaporizer top.Thoroughly gasified by the semicoke particle do not gasified, in main vaporizer, formation defines a uniform conversion zone from top to bottom.
The high speed utilizing pre-vaporized room to export, the jet of large discharge, rigidity is large, is easy to be formed rotation very strong in main vaporizer or all kinds ofly entrainments flow field, reinforcing mass transfer effect.In main vaporizer, mixing mass transfer intensity and temperature levels evenly, can give full play to the effect in gasification reaction space, Reaction time shorten like this, improve the efficiency of gasification of coal.
The beneficial effect that the present invention has is: furnace lining is 3 ~ 5 times of traditional gasification stove work-ing life, efficiency of carbon conversion can arrive more than 99.5%, in coal gas, flyash ingredient can reduce 40 ~ 70%, and reduce coal dust and fall into waste of fuel caused by slag bath by slag-drip opening, be very suitable for the occasion utilizing pulverized coal preparation industrial combustion gas.Coal gasification burner integrates vaporized state measuring ability in ignition trigger, coal dust gasification and burner hearth, and intelligence degree is high, and effectively ensure that vapourizing furnace is normal, steady operation, structure is simple simultaneously, easy to operate.
Accompanying drawing explanation
Fig. 1 is the present invention's equipment schematic diagram used.
Fig. 2 is process flow diagram of the present invention.
Fig. 3 is the structural representation of coal gasification burner of the present invention.
Fig. 4 is the schematic cross-section at coal nozzle place of the present invention.
Embodiment
Below in conjunction with specification drawings and specific embodiments, to describe technical scheme of the present invention in detail.
Two-section type entrained flow gasification method of the present invention carries out in the two-section type airflow bed gasification furnace shown in Fig. 1, and pre-vaporized room is multiple, pre-vaporized room is equipped with coal gasification burner 4.Main vaporizer is one, is provided with technique nozzle 3 in main vaporizer, and the outlet of multiple pre-vaporized room 1 is connected with main vaporizer 2 and uniform along main vaporizer 2.
Process flow sheet of the present invention as shown in Figure 2, during work, treat that main vaporizer is elevated to specified temperature after the igniting of starting ignition burner, spray in pre-vaporized room 1 by 30 ~ 80% of whole fuel and gasification amount of oxygen, vaporising fuel gasification in pre-vaporized indoor 20 ~ 85% generates high temperature rough gas, high temperature rough gas and the semicoke particle completely that do not gasify spray into main vaporizer 2 from exit, pre-vaporized room 1, mass percent shared by this high temperature rough gas of exit, pre-vaporized room is 25 ~ 98%, and pre-vaporized room temperature out controls between 800 ~ 1400 DEG C.
Step 2): supplement remaining gasification amount of oxygen (namely accounting for 20 ~ 70% of gasification oxygen total amount) by the technique nozzle 3 be arranged on main vaporizer 2, the vaporized chemical of high temperature rough gas and do not gasify semicoke particle and secondary supplement is completely gasified totally in main vaporizer 2.
According to test result, adopt gasification process of the present invention, furnace lining is 4.5 times of traditional gasification stove work-ing life, efficiency of carbon conversion can arrive 99.8%, in coal gas, flyash ingredient can reduce 53%, and reduce coal dust and fall into waste of fuel 32% caused by slag bath by slag-drip opening, and pre-vaporized room can be changed separately, is very suitable for the occasion utilizing pulverized coal preparation industrial combustion gas.
Coal gasification burner as shown in Figure 3-4, is made up of main burner 11 and multiple coal nozzles 12 of being arranged on main burner exit.
The described cylindrical structure of main burner 11, the outlet of main burner is reducing, and the head of flame detecting pipe 15 is placed in the central position in described main burner, and the skin of flame detecting pipe 15 is provided with blast tube 16, and the head of this blast tube 16 is provided with gas jet.The skin of described blast tube 16 is provided with combustion air passage 17, and the head of this combustion air passage 17 is provided with cyclone structure 6, and described gas jet and cyclone structure 6 are all placed in main burner 11.The swirl vane 13 that described cyclone structure 6 is distributed between the outer side wall of blast tube 16 and the inner side-wall of combustion air passage 17 by multiple circumference forms.
The space formed between flame detecting pipe 15 head to main burner 11 head is settling chamber 7 (i.e. pre-vaporized room), and settling chamber 7 length L is 0.2 ~ 3:1 with the ratio of main burner 11 internal diameter D.
The head axes of coal nozzle 12 and the angle α of main burner 11 axis are 10 ~ 90 ゜, and the head axes of coal nozzle 12 and the angle β of main burner 11 outlet medullary ray are 0 ~ 60 ゜.
The firelock 8 that sets up an office in combustion air passage 17 ignites combustion gas, and the crater of this burning torch 8 is positioned at settling chamber 7.The outer wall of main burner 11 is provided with water-cooling channel 5, carries out cooling protection to main burner 11.
The afterbody of flame detecting pipe 15 is provided with flame detecting device 14, is connected with cooling air in flame detecting pipe 15 always, avoids hyperthermia radiation pyrolytic damage flame detecting device.
During coal gasification burner work, combustion air is after the cyclone structure 6 of combustion air passage 17 head, with the combustion gas mixing ejected from gas jet, settling chamber 7 produce rotate flow field carry out primary combustion, then with eddy flow shape toward jet flames in the burner hearth of main burner 11 outside; When after the temperature reaching regulation in burner hearth, the coal dust ejected from coal nozzle 12 mixes with the flame ejected from settling chamber 7, and ignite coal dust, takes fire in burner hearth.After coal powder ignition in burner hearth is relatively stable, close gas supply, settling chamber 7 cutoff, to export at main burner 11 from settling chamber 7 combustion air out and mix with from coal nozzle 12 coal dust out, in burner hearth high temperature reflux flue gas igniting under, in burner hearth, realize stable burning or gasification.
The above is only preferred embodiment of the present invention, not does any pro forma restriction to technical scheme of the present invention.Every above embodiment is done according to technical scheme essence of the present invention any simple modification, equivalent variations and modification, all fall within the scope of protection of the present invention.
Claims (10)
1. a two-section type entrained flow gasification method, it comprises the steps:
Step 1), spray in pre-vaporized room (1) by 30 ~ 80% of whole vaporising fuels and gasification amount of oxygen, in pre-vaporized indoor, the vaporising fuel of 20 ~ 85% is gasified and generate high temperature rough gas, then high temperature rough gas and the semicoke particle completely that do not gasify spray into main vaporizer (2) from pre-vaporized room (1) exit, mass percent shared by the height temperature rough gas of exit, pre-vaporized room is 25 ~ 98%, and pre-vaporized room temperature out controls between 800 ~ 1400 DEG C;
Step 2), remaining gasification oxygen is supplemented, high temperature rough gas and the semicoke particle and being gasified totally in main vaporizer (2) with the gasification oxygen of secondary supplement completely that do not gasify by being arranged on technique nozzle (3) on main vaporizer (2).
2. two-section type entrained flow gasification method according to claim 1, it is characterized in that, step 1) in, described pre-vaporized room is one or more, and the outlet of pre-vaporized room is connected with main vaporizer, the method of enhancing mixed mass transfer utilizing the jet of exit, pre-vaporized room height temperature rough gas to form the circle of contact or liquidate in main vaporizer, makes the conversion zone forming good mass-transfer heat transfer in winner's vaporizer; Coal gasification burner (4) pre-vaporized room is equipped with.
3. two-section type entrained flow gasification method according to claim 2, is characterized in that, described coal gasification burner (4) comprises main burner (11) and is arranged at least one coal nozzle (12) on main burner outer wall,
The head of one flame detecting pipe (15) is placed in the central position in described main burner, and the skin of flame detecting pipe (15) is provided with blast tube (16), and the head of this blast tube (16) is provided with gas jet; The skin of described blast tube (16) is provided with combustion air passage (17), the head of this combustion air passage (17) is provided with cyclone structure (6), and described gas jet and cyclone structure (6) are all placed in main burner (11);
The space formed between described flame detecting pipe (15) head to main burner (11) head is settling chamber (7), and the length of this settling chamber (7) and the ratio of main burner (11) internal diameter are 0.2 ~ 3:1;
Burning torch (8) is provided with in described combustion wind passage (16), the crater of this burning torch (8) is positioned at settling chamber (7), and the afterbody of flame detecting pipe (15) is provided with flame detecting device (14);
During coal gasification burner work, logical cooling air in described flame detecting pipe (15).
4. two-section type airflow bed gasification furnace according to claim 3, is characterized in that, described main burner (11) is cylindrical, and its outlet is reducing; Described coal nozzle (12) is arranged on main burner (11) exit; The outer wall of described main burner (11) connects at least one water-cooling channel of lowering the temperature for main burner (5).
5. two-section type entrained flow gasification method according to claim 1, is characterized in that, step 2) in, described main vaporizer is one, is also provided with slag-drip opening and gas exit in main vaporizer.
6. the two-section type entrained flow gasification method according to any one of claim 1-4, it is characterized in that, described coal gas comprises the component of following mass percent: carbon monoxide 5 ~ 80%, hydrogen 5 ~ 50%, methane 0 ~ 10%, hydrocarbon compound 0 ~ 5%, nitrogen 2 ~ 70%, carbonic acid gas 3 ~ 20% and water vapor 2 ~ 22%.
7. the two-section type entrained flow gasification method according to any one of claim 1-4, is characterized in that, the mixture that described high temperature rough gas is made up of the coal gas of pure gaseous state, do not gasify solid-state semicoke particle, solid-state flying dust and molten slag completely.
8. the two-section type entrained flow gasification method according to any one of claim 1-4, is characterized in that, described vaporising fuel is one or more the mixture in coal dust, coke powder, biomass fuel.
9. the two-section type entrained flow gasification method according to any one of claim 1-4, is characterized in that, the flow velocity of the high temperature rough gas jet in pre-vaporized room (1) exit is 5 ~ 50m/s.
10. the two-section type entrained flow gasification method according to any one of claim 1-4, it is characterized in that, step 2) in, from pre-vaporized room (1) exit spray into air-flow main vaporizer (2) along main vaporizer (2) surrounding rotate and under, spiral along main vaporizer central position again after arriving bottom and up flow, discharge from the outlet at main vaporizer (2) top.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108410509A (en) * | 2018-05-14 | 2018-08-17 | 上海谊快能源技术有限公司 | The coke powder and coal gas environment-protection production method to be gasified based on coal powder pure oxygen half |
| CN109126642A (en) * | 2016-04-15 | 2019-01-04 | 四川省雷波明信化工有限公司 | A kind of combustion method for fluidized bed |
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| CN109126642A (en) * | 2016-04-15 | 2019-01-04 | 四川省雷波明信化工有限公司 | A kind of combustion method for fluidized bed |
| CN109126642B (en) * | 2016-04-15 | 2021-09-21 | 雷波明信实业发展有限公司 | Combustion method for fluidized bed |
| CN108410509A (en) * | 2018-05-14 | 2018-08-17 | 上海谊快能源技术有限公司 | The coke powder and coal gas environment-protection production method to be gasified based on coal powder pure oxygen half |
| CN108410509B (en) * | 2018-05-14 | 2024-01-23 | 浙江大学 | Coke powder and coal gas environment-friendly production method based on pulverized coal pure oxygen semi-gasification |
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