CN103320174B - Chinese medicine residue gasification system based on dual-circuit circulating fluidized bed and process - Google Patents
Chinese medicine residue gasification system based on dual-circuit circulating fluidized bed and process Download PDFInfo
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- 238000002309 gasification Methods 0.000 title claims abstract description 81
- 239000003814 drug Substances 0.000 title claims abstract description 40
- 238000000034 method Methods 0.000 title claims abstract description 17
- 230000008569 process Effects 0.000 title claims abstract description 13
- 239000012530 fluid Substances 0.000 claims description 66
- 239000007789 gas Substances 0.000 claims description 47
- 239000002893 slag Substances 0.000 claims description 37
- 239000002994 raw material Substances 0.000 claims description 26
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 22
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 16
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 15
- 239000003546 flue gas Substances 0.000 claims description 15
- 239000007921 spray Substances 0.000 claims description 13
- 238000003860 storage Methods 0.000 claims description 13
- 239000000126 substance Substances 0.000 claims description 12
- 238000005070 sampling Methods 0.000 claims description 11
- 238000012805 post-processing Methods 0.000 claims description 9
- 238000012360 testing method Methods 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 7
- 238000012545 processing Methods 0.000 claims description 5
- 239000006004 Quartz sand Substances 0.000 claims description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 4
- 239000002245 particle Substances 0.000 claims description 4
- 239000003517 fume Substances 0.000 claims description 3
- 239000000567 combustion gas Substances 0.000 description 34
- 238000006243 chemical reaction Methods 0.000 description 29
- 239000002737 fuel gas Substances 0.000 description 26
- 239000011269 tar Substances 0.000 description 21
- 230000008859 change Effects 0.000 description 9
- 239000011280 coal tar Substances 0.000 description 7
- 230000001590 oxidative effect Effects 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 239000002956 ash Substances 0.000 description 5
- 239000011285 coke tar Substances 0.000 description 5
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000000463 material Substances 0.000 description 5
- 239000010881 fly ash Substances 0.000 description 4
- 239000005457 ice water Substances 0.000 description 4
- 238000004519 manufacturing process Methods 0.000 description 4
- 239000002028 Biomass Substances 0.000 description 3
- 230000005540 biological transmission Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 230000003247 decreasing effect Effects 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 239000002075 main ingredient Substances 0.000 description 3
- 238000006722 reduction reaction Methods 0.000 description 3
- 240000003248 Zanthoxylum nitidum Species 0.000 description 2
- 229910052799 carbon Inorganic materials 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000002708 enhancing effect Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 230000004044 response Effects 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 150000001413 amino acids Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010504 bond cleavage reaction Methods 0.000 description 1
- 229920002678 cellulose Polymers 0.000 description 1
- 239000001913 cellulose Substances 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000014759 maintenance of location Effects 0.000 description 1
- 239000002398 materia medica Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 230000007017 scission Effects 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 229930195735 unsaturated hydrocarbon Natural products 0.000 description 1
- 238000005303 weighing Methods 0.000 description 1
Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
Abstract
The invention discloses a Chinese medicine residue gasification system based on a dual-circuit circulating fluidized bed and a process. The system comprises a circulating fluidized bed boiler. The top of the circulating fluidized bed boiler is connected with the bottom of the circulating fluidized bed boiler through a primary returning unit; the top of the primary returning unit is connected with the bottom of the primary returning unit through a secondary returning unit; the top of the secondary returning unit is successively connected with a vapor generator and an air preheater; the vapor generator and the air preheater are both connected with the air inlet end of the circulating fluidized bed boiler; the air inlet end of the circulating fluidized bed boiler and the air inlet end of the air preheater are both connected with an air blower; the air preheater is connected with a post-treatment unit; and a primary returning valve and a secondary returning valve are respectively arranged between the primary returning unit and the circulating fluidized bed boiler and between the secondary returning unit and the primary returning unit.
Description
Technical field
The present invention relates to a kind of Chinese medicine slag gasification system, be specifically related to a kind of Chinese medicine slag gasification system and technique based on double-loop circulating fluidized bed.
Background technology
Chinese medicine slag is the resistates after medicinal material decocts, and contains large amount of organic matter.China is maximum in the world Chinese medicine producing country, and the Chinese medicine slag that produces every year nearly 1,200 ten thousand tons needs to process, have generation large, discharge concentrated feature.Chinese medicine slag initial aqueous rate is more than 70%, perishable rotten, and current domestic Chinese medicine slag major part does landfill and processing is stacked in fixed position, has not only caused the huge wasting of resources, and can produce serious environmental pollution, and health of human body has been formed to potential threat.Therefore the Chinese medicine slag that, how reasonable processing and utilizing is resource and source of pollution has become an important topic in Chinese materia medica, environment and chemical science field.
Due to Chinese medicine slag, contain the organic substances such as rich in protein, Mierocrystalline cellulose and amino acid, in recent years, gasification temperature and the temperature rise rate impact on Shinyleaf Pricklyash Root dregs of a decoction pyrolytic gasification process that had scholar's research, obtains the ideal conditions of Shinyleaf Pricklyash Root dregs of a decoction gasification.Also utilize respectively fluidized-bed and fixed bed to carry out gasification test to QIJU DIHUANG WAN, LIUWEI DIHUANG WAN, the XIANGSHA YANGWEI WAN dregs of a decoction, obtained the optimum excess air ratio of its gasification, verified that three kinds of dregs of a decoction all have good pyrolytic gasification characteristic.But in existing technology, in the ash content of raw material after circulating fluidized bed gasification, still have certain remaining carbon.
Summary of the invention
The object of the invention is for overcoming above-mentioned the deficiencies in the prior art, a kind of Chinese medicine slag gasification system and technique based on double-loop circulating fluidized bed is provided.The present invention be take circulating fluidized bed as basis, add two-stage material-returning device, form double-loop circulating fluidized bed, improved temperature in stove, promote coke tar cracking, reduced remaining carbon, thereby improved gasification efficiency, improve raw material energy transformation ratio, thereby provide technical foundation for Chinese medicine slag class industry biomass harmless and recycling.
For achieving the above object, the present invention adopts following technical proposals:
Chinese medicine slag gasification system based on double-loop circulating fluidized bed, comprise circular fluid bed, its top is connected to the bottom of circular fluid bed through one-level returning charge unit, the top of one-level returning charge unit is connected to the bottom of one-level returning charge unit through secondary returning charge unit, the top of secondary returning charge unit is connected with air preheater with steam evaporator successively, described steam evaporator and air preheater are all connected to the inlet end of circular fluid bed, the inlet end of described circular fluid bed and the inlet end of air preheater are all connected to gas blower, described air preheater is connected with post-processing unit, wherein, between described one-level returning charge unit and circular fluid bed, between secondary returning charge unit and one-level returning charge unit, be respectively equipped with one-level returning charge valve and secondary returning charge valve.
Described post-processing unit comprises spray column, Venturi scrubber, induced draft fan and the gas storage holder connecting successively, and described spray column is connected with air preheater.
Between described air preheater and spray column, be provided with sampling and testing point, between induced draft fan and gas storage holder, be provided with gas meter.
Between described secondary returning charge unit and steam evaporator, be provided with ash handling equipment.
Described ash handling equipment is fly-ash separator.
The feed end of described circular fluid bed adopts screw feeding device.
In described circular fluid bed, be provided with successively several temperature points from bottom to top.
The burning process of above-mentioned Chinese medicine slag gasification system, concrete grammar is as follows:
1) Chinese medicine slag enters the gasification of CFBB Hot solution and produces flue gas, one-level returning charge valve is opened, secondary returning charge valve cuts out, and a part is returned to circular fluid bed with the flue gas of carbon residue through one-level returning charge unit, and with the new raw material mixing gasifying that enters circular fluid bed;
2) part enters secondary returning charge unit with the flue gas of carbon residue, and secondary returning charge valve is opened, and the flue gas with carbon residue in secondary returning charge unit returns to circular fluid bed through one-level returning charge unit, and with the new raw material mixing gasifying that enters circular fluid bed;
3) remaining partial fume enters post-processing unit through steam evaporator and air preheater successively through ash handling equipment and carries out aftertreatment, and steam evaporator and air preheater are processed the bottom that enters circular fluid bed after the air mixed of the air that obtains and gas blower;
4) flue gas after air preheater is processed enters gas storage holder storage after spray column and Venturi scrubber processing.
Described circular fluid bed adopts the quartz sand of particle diameter 0.3～0.8mm as fluidizing medium, the gas mixture of 200 ℃ of air or 200 ℃ of air and 150 ℃ of water vapour of take is vaporized chemical, the inlet amount of Chinese medicine slag is 190～330kg/h, wherein, air equivalent than the span of ER is: 0.2≤ER≤0.34, ER is the important control parameter of gasifying process, refers to the oxygen amount (m consuming in gasification
3/ kg) with the needed theoretical oxygen amount (m of sample introduction raw material perfect combustion
3/ kg) ratio; In described gas mixture, the span of water vapour proportioning S/B is: 0≤S/B≤0.8, S/B is the ratio that in gasification, water vapour is supplied with quality (kg/h) and Chinese medicine slag charging quality (kg/h).
Preferably, the inlet amount of Chinese medicine slag is 210kg/h.
Preferably, when secondary returning charge unit is closed, 0.24≤ER≤0.30; When secondary returning charge unit is opened, 0.26≤ER≤0.30.
Preferably, the span of water vapour proportioning S/B is: 0.2≤S/B≤0.5.
Principle of work of the present invention:
When secondary returning charge cell operation, the part carbon residue of complete reaction is not back in circular fluid bed and the new raw material participation gasification reaction that is mixed, it is mainly the thermopositive reaction that oxidizing fire occurs, thereby improved the temperature in circular fluid bed, on the other hand, between the old raw material of high temperature and new raw material, there is heat transmission, reduced the energy that new raw material is drawn from gasification reaction; Thereby the tar content in reduction combustion gas; Material gasification efficiency and combustion heat value have been improved.
The invention has the beneficial effects as follows, the present invention utilizes double-loop circulating fluidized bed that Chinese medicine slag pyrolytic gasification is obtained to the high-grade biomass clean combustion gas of high heating value, improve reaction in furnace temperature, effectively reduced the tar content in combustion gas, improved material gasification efficiency and combustion heat value.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Fig. 2 is combustion gas and tar sampling unit;
Fig. 3 is the impact of ER on Gas Components, when 3a is secondary returning charge unit closure, when 3b is the unlatching of secondary returning charge unit;
Fig. 4 is the influence curve of ER to fuel gases calorific value and gasification efficiency;
Fig. 5 is the influence curve of ER to temperature in circular fluid bed and the coal-tar middle oil mass concentration of combustion gas;
Fig. 6 is the influence curve of S/B to Gas Components and calorific value;
Fig. 7 is the variation of the S/B impact on temperature in circular fluid bed and quality of coke tar concentration;
Wherein 1. gas blowers, 2. screw feeding device, 3. circular fluid bed, 4. one-level returning charge unit, 5. secondary returning charge unit, 6. secondary returning charge valve, 7. fly-ash separator, 8. steam evaporator, 9. air preheater, 10. sampling and testing point, 11. spray columns, 12. Venturi scrubbers, 13. induced draft fans, 14. gas meters, 15. gas storage holders, 16. surge flasks, 17. ice-water bath tar trapping bottles, 18. cartridge filters, 19. under meters, 20. vacuum pumps, 21. gas drying bottles, 22. chromatographic instruments; T1～T4 is temperature point.
Embodiment
Below in conjunction with drawings and Examples, the present invention will be further elaborated, should be noted that following explanation is only in order to explain the present invention, does not limit its content.
Embodiment 1:
As shown in Figure 1, the present invention is a kind of Chinese medicine slag gasification system based on double-loop circulating fluidized bed, it comprises circular fluid bed 3, its top is connected to the bottom of circular fluid bed 3 through one-level returning charge unit 4, the top of one-level returning charge unit 4 is connected to the bottom of one-level returning charge unit 4 through secondary returning charge unit 5, the top of secondary returning charge unit 5 is connected with air preheater 9 with steam evaporator 8 successively, steam evaporator 8 and air preheater 9 are all connected to the inlet end of circular fluid bed 3, the inlet end of the inlet end of circular fluid bed 3 and air preheater 9 is all connected to gas blower 1, air preheater 9 is connected with post-processing unit, wherein, between one-level returning charge unit 4 and circular fluid bed 3, between secondary returning charge unit 5 and one-level returning charge unit 4, be respectively equipped with one-level returning charge valve and secondary returning charge valve 6.
Post-processing unit comprises spray column 11, Venturi scrubber 12, induced draft fan 13 and the gas storage holder 15 connecting successively, and spray column 11 is connected with air preheater 9.
Between air preheater 9 and spray column 11, be provided with sampling and testing point 10, between induced draft fan 13 and gas storage holder 15, be provided with gas meter 14.
Between secondary returning charge unit 5 and steam evaporator 8, be provided with fly-ash separator 7.
The feed end of circular fluid bed 3 adopts screw feeding device 2.
In circular fluid bed 3, be provided with successively 4 temperature points, i.e. T1～T4 in Fig. 1 from bottom to top.
The burning process of above-mentioned Chinese medicine slag gasification system, concrete grammar is as follows:
1) Chinese medicine slag enters circular fluid bed 3 pyrolytic gasifications and produces flue gas, one-level returning charge valve is opened, secondary returning charge valve 6 cuts out, and a part is returned to circular fluid bed 3 with the flue gas of carbon residue through one-level returning charge unit 4, and with the new raw material mixing gasifying that enters circular fluid bed 3;
2) part enters secondary returning charge unit 5 with the flue gas of carbon residue, secondary returning charge valve 6 is opened, flue gas with carbon residue in secondary returning charge unit 5 returns to circular fluid bed 3 through one-level returning charge unit 4, and with the new raw material mixing gasifying that enters circular fluid bed 3;
3) remaining partial fume enters post-processing unit through steam evaporator 8 and air preheater 9 successively through fly-ash separator 7 and carries out aftertreatment, and steam evaporator 8 and air preheater 9 are processed the bottom that enters circular fluid bed 3 after the air mixed of the air that obtain and gas blower 1;
4) flue gas after air preheater 9 is processed enters gas storage holder 15 storages after spray column 11 and Venturi scrubber 12 processing.
Circular fluid bed 3 adopts the quartz sand of particle diameter 0.5mm as fluidizing medium, and the 200 ℃ of air of take are vaporized chemical, and the inlet amount of Chinese medicine slag is 210kg/h.
Air equivalent than the span of ER is: 0.2≤ER≤0.34, ER is the important control parameter of gasifying process, refers to the oxygen amount (m consuming in gasification
3/ kg) with the needed theoretical oxygen amount (m of sample introduction raw material perfect combustion
3/ kg) ratio.
Regulate air equivalent ER, after waiting system is stable, at sampling and testing point 10, sample, and test the coal-tar middle oil content of combustion gas and Gas Components.Sampling is to realize by the combustion gas shown in Fig. 2 and tar sampling unit, it comprises surge flask 16, surge flask 16 is by being communicated with several ice-water bath tar trapping bottles 17 successively communicating pipe, the ice-water bath tar trapping bottle 17 of most end is successively by cartridge filter 18, under meter 19, vacuum pump 20, be communicated to gas drying bottle 21, gas drying bottle 21 is connected with chromatographic instrument 22.Combustion gas passes into surge flask 16 by A, through ice-water bath tar trapping bottle 17, absorbs after tar and dry filter, connects the main ingredient that Micro GC Agilent-3000 gas chromatograph 22 detects combustion gas sample at gas outlet B place.For reducing testing error, under identical operating mode, every 15min sampling once, sample 3 groups, get its mean value as test-results.
Utilize that the volatilization sampling of RE52A Rotary Evaporators obtains containing tar organic solution, by FA2004A analytical balance, weigh remaining tar sample quality, by the quality of coke tar content in the combustion gas of formula (1) Units of Account volume
λ=m/q （1）
In formula, λ is tar and combustion gas quality volume ratio, mg/m
3; M is contained quality of coke tar in combustion gas sample, mg; Q is sampling combustion gas volume, m
3.
To the combustion gas main component (CH recording under different operating modes
4, C
nh
m, CO, H
2, CO
2), by formula (2), calculate the Lower heat value of combustion gas
In formula, Q
vfor low calorific gas value, kJ/m
3;
represent respectively unsaturated hydrocarbons, CO, CH in combustion gas sample
4and H
2volume fraction, %.
Gasification efficiency refers to the ratio of the biomass material gasification total heat of generating gas and the total heat of gasified raw material, is the important indicator of weighing gasification, can calculate by formula (3)
In formula, η is gasification efficiency, %; V
mfor the gas production rate of the unit mass dregs of a decoction, m3/kg; Q
vfor the Lower heat value of gasification burning, kJ/m
3; H is the Lower heat value of Chinese medicine slag raw material, kJ/kg.
Under 5 unlatchings of secondary returning charge unit and closed two states, changing air output makes ER increase to gradually 0.34 from 0.2, investigate the impact of ER on temperature in gasification burning component, calorific value, gasification efficiency, Reaktionsofen and the coal-tar middle oil content of combustion gas, and contrast the changing conditions that the gasification of front and back is opened in secondary returning charge unit 5.
Before and after secondary returning charge unit 5 is opened, ER on the impact of Gas Components as shown in Figure 3.By Fig. 3 a, can be found out, under secondary returning charge unit 5 closure states, air equivalent increases to than ER at 0.22 o'clock by 0.2, the CH in combustion gas
4and H
2content all raises to some extent, then along with the increase of ER, declines gradually; From Fig. 3 b, after secondary returning charge unit 5 is opened, CH
4and H
2content all presents the trend of monotone decreasing along with the increase of ER.This is because at ER hour, air supply quantity not sufficient, has caused the pyrolytic gasification of raw material insufficient, after secondary returning charge valve 6 is opened, carbon residue in ash content returns to circular fluid bed 3 by secondary returning charge unit 5 and participate in reaction together with new raw material, at ER, hour just produces more CH
4and H
2.In addition, before and after secondary returning charge unit 5 is opened, other main ingredients in combustion gas are basically identical with the variation tendency of ER: along with the increase of ER, in gasification system, oxygen feed rate increases, oxidizing fire increased response, and in combustion gas, CO content constantly reduces, and CO
2content increases gradually, C
nh
mcontent does not have considerable change.
In combustion gas in comparison diagram 3 before and after 5 unlatchings of secondary returning charge unit, each component volume fraction can be found out, under identical ER condition, and the volume fraction of this component when the Gas Components volume fraction behind unlatching secondary returning charge unit 5 is greater than secondary returning charge unit 5 closure.
Fuel gases calorific value change curve in Fig. 4 can be found out, secondary returning charge unit 5 open before and after fuel gases calorific values along with the increase of ER is all the variation tendency of first increases and then decreases, but the fuel gases calorific value of secondary returning charge unit 5 opened conditions fuel gases calorific value during all apparently higher than closure state, this is because fuel gases calorific value depends on the content of combustion gas inflammable gas component, inflammable gas component concentration is higher, and fuel gases calorific value is higher.
Gasification efficiency change curve in Fig. 4 can find out, under identical ER condition, the gasification efficiency after secondary returning charge unit 5 is opened is higher, and the gasification efficiency effect of haveing a certain upgrade of the 5 pairs of systems in secondary returning charge unit is described; When ER hour, vaporized chemical feed rate is little, gasification reaction is incomplete, fuel gases calorific value is higher, but because gas production rate is little, has caused gasification efficiency on the low side; Along with the increase of ER, gas production rate increases, and the dual function of fuel gases calorific value and gas production rate causes gasification efficiency to present the trend of first increases and then decreases.
When secondary returning charge unit 5 is closed, the gasification efficiency of ER when 0.24～0.30 scope can reach 71～74%, fuel gases calorific value is at 5100kJ/m
3above, wherein gasification efficiency is up to 74%, and now ER is 0.26, fuel gases calorific value is 5600kJ/m
3; When secondary returning charge unit is opened, gasification efficiency can reach 76～78%, and corresponding ER scope is 0.26～0.30, fuel gases calorific value 5400kJ/m
3eR when above, gasification efficiency is got maximum 78% is 0.28, fuel gases calorific value is 5600kJ/m
3.Therefore, under secondary returning charge unit 5 opening and closing two states, fuel gases calorific value when gasification efficiency is all got maximum is identical, but the gasification efficiency of opened condition during than closure state improved 4%.
4 temperature values that the interior temperature point T1～T4 of circular fluid bed 3 monitors, get its mean value as the temperature of circular fluid bed 3.Under different ER conditions, the change curve of the temperature in circular fluid bed 3 and the coal-tar middle oil mass content of combustion gas as shown in Figure 5, can find out, increase along with ER, oxygen feed rate increases, promote the interior oxidizing fire reaction of circular fluid bed 3, discharged amount of heat, thus the temperature in the burner hearth of raising circular fluid bed 3; The rising of circular fluid bed 3 temperature, is conducive to the scission reaction of tar, and then reduces the coal-tar middle oil content of combustion gas.
In comparison diagram 5,5 keyings, two kinds of operating modes in secondary returning charge unit can be found, under identical ER condition, 5 unlatchings of secondary returning charge unit are higher than the interior temperature of circular fluid bed 3 under closed operating mode, tar content is low, this be because, when 5 work of secondary returning charge unit, the part carbon residue of complete reaction is not back to circular fluid bed 3 and the new raw material participation gasification reaction that is mixed, and heat transmission occurs between the old raw material of high temperature and new raw material, has reduced the energy that new raw material is drawn from gasification reaction; On the other hand, the carbon residue being back in circular fluid bed 3 is mainly the thermopositive reaction that oxidizing fire occurs, thereby has improved the temperature in circular fluid bed 3, reduces the tar content in combustion gas; And along with the increase of ER and the enhancing of oxidizing reaction, the difference trend that the interior temperature of front and back circular fluid bed and tar content are opened in secondary returning charge unit 5 increases.
Embodiment 2:
Circular fluid bed 3 adopts the quartz sand of particle diameter 0.3mm as fluidizing medium, the gas mixture of 200 ℃ of air and 150 ℃ of water vapour of take is vaporized chemical, the inlet amount of Chinese medicine slag is 210kg/h, wherein, in described gas mixture, the span of water vapour proportioning S/B is: 0≤S/B≤0.8, S/B is the ratio that in gasification, water vapour is supplied with quality (kg/h) and Chinese medicine slag charging quality (kg/h).
The rest part of system and technique is with embodiment 1, and it will not go into details.
Change after water vapour proportioning S/B, adopt the mode identical with embodiment 1 to sample.
In embodiment 1, secondary returning charge unit 5 is opened with the test-results of closed pair gasification result impact known, the content of inflammable gas component and the cracking of tar in gasification burning during secondary returning charge unit 5 opened condition, have been improved to a certain extent, improved fuel gases calorific value and gasification efficiency, gasification result is better.Therefore, in test gasification result being affected in water vapour proportioning, keep secondary returning charge unit in opened condition, the inlet amount of Chinese medicine slag is 210kg/h, adopting 200 ℃ of warm airs and 150 ℃ of water vapour is vaporized chemical, fixedly ER value is 0.28, studies the gasification property of Chinese medicine slag under different water vapour conditions of mixture ratios.
Fuel gases calorific value and main ingredient with the Changing Pattern of S/B as shown in Figure 6, along with the increase of S/B, CO in combustion gas
2concentration content raise gradually, CO content declines gradually; Along with the interpolation of vaporized chemical water vapour, CH
4and C
nh
mcontent all slightly raise, but after S/B is greater than 0.4, CH
4content slightly declines, and C
nh
mcontent kept stable; When S/B changes between 0～0.5, H
2content increases fast, when S/B is greater than 0.5, and H
2there is slow decreasing trend in content.
Chinese medicine slag pyrolytic gasification process comprises pyrolytic reaction, oxidizing reaction, reduction reaction and gas reformation reaction etc.Add after water vapour, the principal reaction in vapourizing furnace is as follows:
C+O
2=CO
2 △H=-393.5kJ/mol (4)
H
2O+C=CO+H
2 △H=+131.4kJ/mol (5)
2H
2O+C=CO
2+2H
2 △H=+90kJ/mol (6)
H
2O+CO=CO
2+H
2 △H=-43.6kJ/mol (7)
C+2H
2=CH
4 △H=-74.9kJ/mol (8)
CH
4+H
2O=3H
2+CO △H=+206.1kJ/mol (9)
In gasification, the reaction that water vapour participates in mainly contains (5), (6), (7), and the increase of S/B raises water vapour content in circular fluid bed, has promoted the carrying out of reaction (5)～(7); And in the reaction participating at water vapour, reaction (7) dominate
[15], consume CO, increase CO
2and H
2.H
2the carrying out of the increase meeting intensified response (8) of content, produces more CH
4, but along with the increase of S/B can cause reacting the enhancing of (9), consume CH
4, so combined reaction (8), (9), the CH in combustion gas
4content is between 0～0.2, to have outside small size rising, not occur considerable change at S/B.
As shown in Figure 6, change there is a comparatively desirable interval with S/B in fuel gases calorific value, and when S/B reaches preferable states 0.2～0.5 time, now, in combustion gas, the content of inflammable gas component is higher, and fuel gases calorific value can reach 6000～6200kJ/m
3.
Figure 7 shows that tar content in the interior medial temperature of circular fluid bed 3 and combustion gas is with the change curve of S/B, can find out, water vapour proportioning increases, circular fluid bed 3 interior reaction temperatures reduce, tar content raises, but S/B is when 0.2～0.5 preferable states, data (see figure 5) when contrasting pure air and being vaporized chemical, tar content does not obviously raise.
It is vaporized chemical that embodiment 1 be take 200 ℃ of warm airs, along with air equivalent is than the increase of ER, the gasification property that secondary returning charge unit 5 is opened in the circular fluid bed 3 of front and back has all presented similar variation tendency: the temperature in circular fluid bed 3 raises gradually, the coal-tar middle oil content of fuel gases calorific value and combustion gas reduces gradually, gasification efficiency first increases and then decreases, and under identical ER condition during secondary returning charge unit 5 opened condition fuel gases calorific value and gasification efficiency all higher than closure state;
When secondary returning charge unit 5 is closed, comparatively ideal ER is 0.24～0.30, fuel gases calorific value 5100～5800kJ/m
3, gasification efficiency is about 71～74%, and wherein gasification efficiency is up to 74%, and now ER is 0.26, fuel gases calorific value is 5600kJ/m
3; When secondary returning charge unit 5 is opened, comparatively ideal ER span is 0.26～0.30, and fuel gases calorific value is at 5400～5900kJ/m
3, gasification efficiency is 76～78%, ER when wherein gasification efficiency is up to 78% is 0.28, fuel gases calorific value is 5600kJ/m
3.Under secondary returning charge unit 5 opened conditions, increase fluidized-bed interior reaction temperature and coke tar cracking, improved capacity usage ratio and the gasification efficiency of circulating fluidized bed.
It is vaporized chemical that embodiment 2 be take 200 ℃ of warm airs and 150 ℃ of water vapour, and makes secondary returning charge unit 5 in opened condition, and fixedly ER is 0.28, along with the increase of water vapour proportioning S/B, and CO in combustion gas
2content raises gradually, and CO content declines gradually, CH
4with C
nh
mthere is no considerable change; S/B is between 0～0.5 time, H
2content increases fast, when S/B is greater than 0.5, and H
2content slow decreasing; The interior temperature of circular fluid bed 3 reduces gradually, and the coal-tar middle oil content of combustion gas raises, and fuel gases calorific value first increases afterwards and reduces, and when S/B is 0.4, fuel gases calorific value reaches maximum value 6200kJ/m
3.
Principle of work of the present invention:
When 5 work of secondary returning charge unit, the part carbon residue of complete reaction is not back in circular fluid bed 3 and the new raw material participation gasification reaction that is mixed, it is mainly the thermopositive reaction that oxidizing fire occurs, thereby improved the temperature in circular fluid bed, on the other hand, between the old raw material of high temperature and new raw material, there is heat transmission, reduced the energy that new raw material is drawn from gasification reaction; Thereby the tar content in reduction combustion gas; Material gasification efficiency and combustion heat value have been improved.
Although above-mentioned, by reference to the accompanying drawings the specific embodiment of the present invention is described; but be not limiting the scope of the invention; on the basis of technical scheme of the present invention, those skilled in the art do not need to pay various modifications that creative work can make or distortion still in protection scope of the present invention.
Claims (10)
1. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed, it is characterized in that, comprise circular fluid bed, its top is connected to the bottom of circular fluid bed through one-level returning charge unit, the top of one-level returning charge unit is connected to the bottom of one-level returning charge unit through secondary returning charge unit, the top of secondary returning charge unit is connected with air preheater with steam evaporator successively, described steam evaporator and air preheater are all connected to the inlet end of circular fluid bed, the inlet end of described circular fluid bed and the inlet end of air preheater are all connected to gas blower, described air preheater is connected with post-processing unit, wherein, between described one-level returning charge unit and circular fluid bed, between secondary returning charge unit and one-level returning charge unit, be respectively equipped with one-level returning charge valve and secondary returning charge valve.
2. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed according to claim 1, it is characterized in that, described post-processing unit comprises spray column, Venturi scrubber, induced draft fan and the gas storage holder connecting successively, and described spray column is connected with air preheater.
3. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed according to claim 2, is characterized in that, is provided with sampling and testing point between described air preheater and spray column, between induced draft fan and gas storage holder, is provided with gas meter.
4. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed according to claim 1, is characterized in that, between described secondary returning charge unit and steam evaporator, is provided with ash handling equipment.
5. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed according to claim 1, is characterized in that, the feed end of described circular fluid bed adopts screw feeding device.
6. the Chinese medicine slag gasification system based on double-loop circulating fluidized bed according to claim 1, is characterized in that, is provided with successively several temperature points in described circular fluid bed from bottom to top.
7. according to the burning process of the Chinese medicine slag gasification system based on double-loop circulating fluidized bed described in claim 2 or 3, it is characterized in that, concrete grammar is as follows:
1) Chinese medicine slag enters the gasification of CFBB Hot solution and produces flue gas, one-level returning charge valve is opened, secondary returning charge valve cuts out, and a part is returned to circular fluid bed with the flue gas of carbon residue through one-level returning charge unit, and with the new raw material mixing gasifying that enters circular fluid bed;
2) part enters secondary returning charge unit with the flue gas of carbon residue, and secondary returning charge valve is opened, and the flue gas with carbon residue in secondary returning charge unit returns to circular fluid bed through one-level returning charge unit, and with the new raw material mixing gasifying that enters circular fluid bed;
3) remaining partial fume enters post-processing unit through steam evaporator and air preheater successively through ash handling equipment and carries out aftertreatment, and steam evaporator and air preheater are processed the bottom that enters circular fluid bed after the air mixed of the air that obtains and gas blower;
4) flue gas after air preheater is processed enters gas storage holder storage after spray column and Venturi scrubber processing.
8. burning process according to claim 7, it is characterized in that, described circular fluid bed adopts the quartz sand of particle diameter 0.3～0.8mm as fluidizing medium, the gas mixture of 200 ℃ of air or 200 ℃ of air and 150 ℃ of water vapour of take is vaporized chemical, the inlet amount of Chinese medicine slag is 190～330kg/h, wherein, air equivalent than the span of ER is: 0.2≤ER≤0.34; In described gas mixture, the span of water vapour proportioning S/B is: 0≤S/B≤0.8.
9. burning process according to claim 8, is characterized in that, when secondary returning charge unit is closed, and 0.24≤ER≤0.30; When secondary returning charge unit is opened, 0.26≤ER≤0.30.
10. burning process according to claim 8, is characterized in that, the span of water vapour proportioning S/B is: 0.2≤S/B≤0.5.
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| CN201873648U (en) * | 2010-11-20 | 2011-06-22 | 山东百川同创能源有限公司 | Drying, pyrolysis and gasification system for high-moisture-content traditional Chinese medicine residue |
| CN203440324U (en) * | 2013-07-12 | 2014-02-19 | 山东百川同创能源有限公司 | Chinese medicinal residue gasifying system based on double-loop circulating fluidized bed |
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| CN201873648U (en) * | 2010-11-20 | 2011-06-22 | 山东百川同创能源有限公司 | Drying, pyrolysis and gasification system for high-moisture-content traditional Chinese medicine residue |
| CN203440324U (en) * | 2013-07-12 | 2014-02-19 | 山东百川同创能源有限公司 | Chinese medicinal residue gasifying system based on double-loop circulating fluidized bed |
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