CN103555371A - Method for improving gasification efficiency of slurry feed gasification device - Google Patents
Method for improving gasification efficiency of slurry feed gasification device Download PDFInfo
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- CN103555371A CN103555371A CN201310573590.2A CN201310573590A CN103555371A CN 103555371 A CN103555371 A CN 103555371A CN 201310573590 A CN201310573590 A CN 201310573590A CN 103555371 A CN103555371 A CN 103555371A
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Abstract
The invention discloses a method for improving gasification efficiency of a slurry feed gasification device. A slurry carbon material and an oxidant entering inside a gasification furnace are preheated in a wet feed gasification technology by using low-grade energy; the temperature of the raw material in the gasification furnace is improved, so that the gasification efficiency of the slurry feed gasification device is improved. By adopting the technology, the raw material in the gasification furnace is preheated by using by-produced low-grade energy rich in low-pressure vapor from a water-gas shift unit and the like, and indirectly converted into high-grade chemical energy. Thus, the raw material consumption of the gasification system is effectively reduced; the efficiency of a cooled coal gas is improved, so that the gasification efficiency of the slurry feed gasification device is improved.
Description
Technical field
The present invention relates to a kind of heat recovery method, be specifically related to a kind of method of carrying out preheating to entering vapourizing furnace slurry state carbon raw material and oxygenant in wet feeding gasification technology.
Technical background
Water gas shift reaction is shown below:
Be an important chemical reaction, be generally used for adjustments of gas component, carry out Partial Transformation or convert completely, make the gas composition after conversion meet Chemical Manufacture, can also purify unstripped gas, be conducive to realize CO simultaneously
2catch and seal up for safekeeping.
Water gas shift reaction is thermopositive reaction, and hydrosphere transformation unit discharges a large amount of heats, and existing hydrosphere transformation system thermal reclaims the main modes such as by-product low pressure steam, preheating de-salted water of leaning on and reclaims.Because transformation system be take a large amount of low-grade low-pressure steam of by-product as main, low-grade steam energy utilization ratio is low, is not utilized effectively now in full scale plant.The way of recycling that goes out airflow bed gasification furnace high-temperature synthesis gas heat has two kinds, adopts waste heat boiler and chilling process.For chilling process, the heat that goes out airflow bed gasification furnace high-temperature synthesis gas is saturated in synthetic gas with the form of water vapor, in synthetic gas, water vapor/synthetic gas volume is than high, make the water vapor in synthetic gas a large amount of more than needed concerning converter unit, a large amount of low-grade remaining heats that reclaim by by-product water vapor at transformation system.How to reclaim efficiently low-grade steam energy is the emphasis problem of research of technique always.
Vapourizing furnace is the unit equipment of a highly energy-consuming, and industrial entrained flow gasification feeding manner mainly contains two kinds, wet feeding and dry feed.The cold gas efficiency of wet method gasification technology is lower than dry method cold gas efficiency, reason be water in charging slurry heating, evaporate, be superheated to gasification temperature and need consumption of calorie, oxygen heats up, be superheated to gasification temperature also needs consumption of calorie, cause gasification system oxygen consumption, coal consumption to increase, effectively gas (CO+H
2) component concentration reduction, invalid gaseous fraction CO
2content increases, and the chemical energy that the chemical energy that makes feed stock for blast furnace is finally retained in synthetic gas after by gasification reaction reduces.
After slurry temperature raises, the pedesis aggravation of particle, obtains material dispersion more even; After slurry heats up, volume increases, and Intermolecular Forces weakens, and slurry reduced viscosity is conducive to the conveying of slurry.The surface tension of high temperature slurry reduces, and atomization improves, and has increased the contact surface of slurry and vaporized chemical, promotes that gasification reaction carries out completely.The mobility of the rear slurry of slurry temperature rising improves and makes to prepare the slurry of greater concn, improves the efficiency of gasification system.Because slurry preheating temperature is lower, the probability that generates by product in warm is lower.
Therefore, in order to make up wet feeding gasification unit high energy consumption, inefficient shortcoming, and realize and effectively utilize the low-grade energy in follow-up system, the present invention proposes a kind of method of utilizing low-grade energy to improve slurry state feeding gas gasifying device gasification efficiency.
Summary of the invention
In view of above problem, the invention provides a kind of method of carrying out preheating to entering vapourizing furnace slurry state carbon raw material and oxygenant in wet feeding gasification technology, the heat recuperation that hydrosphere transformation unit is discharged is delivered to vapourizing furnace imported raw material (comprising slurry state carbon raw material and oxygenant), the heat of realizing slurry state carbon raw material gasification unit and hydrosphere transformation unit is integrated, the temperature that improves vapourizing furnace imported raw material, reaches and effectively utilizes hydrosphere transformation unit tow taste heat.Concrete technical scheme is as follows:
A method that improves slurry state feeding gas gasifying device gasification efficiency, comprises the steps:
Steam (S2) from hydrosphere transformation unit waste heat boiler (1) is divided into two strands, one steam (S3) enters the slurry state feed heater (2) with the heat exchange of carbonaceous slurry state raw material (S5), and another strand of steam (S7) enters the oxidant heater (3) with oxygenant (S9) heat exchange; The nozzle that the carbonaceous slurry state raw material (S6) of pulp state feed heater (2) and oxidant heater (3) and oxygenant (S10) are directly sent to vapourizing furnace;
Wherein:
Carbonaceous slurry state raw material (S5) is sent to slurry state feed heater (2) through high pressure shurry pump (5) from carbonaceous slurry state raw material storage tank (4);
Oxygenant (S9) is directly from the hyperbaric oxygen agent of air separation facility (6);
The tube side of slurry state feed heater (2) is walked carbonaceous slurry state raw material (S5), shell side is walked steam (S3).
For the vapourizing furnace that contains the charging of multichannel slurry state raw material, can slurry state feed heater (2) be set separately every road carbonaceous slurry state raw material (S5), also can multichannel (being more than or equal to 2) slurry state raw material charging parallel connection enter a slurry state feed heater (2).For avoiding deposition and the uneven distribution of carbonaceous slurry state raw material (S5) in slurry state feed heater (2), each road tube side of preferably starching state feed heater (2) all arranges a high pressure shurry pump (5).For an outlet that has high pressure shurry pump (5) the ，Mei road carbonaceous slurry state raw material (S5) of multichannel (being more than or equal to 2) slurry state material outlet corresponding to high pressure shurry pump (5).
The tube side of described slurry state feed heater (2) is shell and tube, U-shaped tubular type, coil tube type or helix tube type.
Go out the carbonaceous slurry state raw material (S5) of high pressure shurry pump (5) and be between 0.1～12MPa from the pressure of the oxygenant (S9) of air separation facility (6).
Pressure from the steam (S2) of hydrosphere transformation unit waste heat boiler (1) is between 0.1～12MPa.By steam (S3), to carbonaceous slurry state raw material (S5), heat, in order to make not generate gas or do not produce bubble in carbonaceous slurry state raw material (S5), the temperature after carbonaceous slurry state raw material (S5) is heated should be starched water saturation temperature under the pressure of state raw material (S5) place lower than carbonaceous.
Carbonaceous in described carbonaceous slurry state raw material (S5) is a kind of in coal, refinery coke, biomass, pitch, residual oil, bio-oil or mixture that they are several; Oxygenant (S9) is a kind of in oxygen, air, oxygen-rich air, water vapor, carbonic acid gas or mixture that they are several.
Optionally preheating carbonaceous of described steam (S2) slurry state raw material (S5), oxygenant (S9) or to both equal preheatings, select according to concrete production technique.
Described steam (S2) can, from hydrosphere transformation unit, also can, from the steam of other system, also can replace steam with other thermal source, as various fuel.
This technique is high-grade chemical energy by the low-grade energy indirect reformer of low-pressure steam, effectively reduces the raw material consumption of gasification system, has improved cold gas efficiency, and then improves the gasification efficiency of slurry state feeding gas gasifying device.
Accompanying drawing explanation
Fig. 1 is the integrated schematic diagram of heat of starching state carbon raw material gasification unit and hydrosphere transformation unit in embodiment;
Fig. 2 is embodiment Zhong Mei road slurry state raw material independence heat exchange schematic diagram;
Fig. 3 is multichannel slurry state raw material parallel heat exchanging schematic diagram in embodiment.
Nomenclature
1 steam waste heat boiler; 2 slurry state feed heater; 3 oxidant heaters;
4 carbonaceous slurry state raw material storage tanks; 5 high pressure shurry pumps; 6 air separation facilitys;
S1 oiler feed; S2 steam; S3 steam; S4 phlegma;
S5 carbonaceous slurry state raw material; Carbonaceous slurry state raw material after S6 heating; S7 steam;
S8 phlegma; S9 oxygenant; Oxygenant after S10 heating; S11 phlegma.
Embodiment
Be below embodiments of the invention, provided detailed embodiment and concrete operating process, its object is only being understood content of the present invention better.Therefore protection scope of the present invention is not subject to the restriction of illustrated embodiment.
Referring to Fig. 1, the integrated core content of the heat of slurry state carbon raw material gasification unit and hydrosphere transformation unit is by utilizing the charging (comprise and starch state carbon raw material and oxygenant) of tow taste heat preheating gasification feed unit, by low-grade energy indirect reformer, be high-grade chemical energy, improve the gasification efficiency of slurry state feeding gas gasifying device.
Steam S2 is divided into two strands, and wherein one steam S3 enters the slurry state feed heater 2 with carbonaceous slurry state raw material S5 heat exchange, and another gang of steam S7 enters the oxidant heater 3 with oxygenant S9 heat exchange.The nozzle that the carbonaceous slurry state raw material S6 of pulp state feed heater 2 and oxidant heater 3 and oxygenant S10 are directly sent to vapourizing furnace.
Carbonaceous slurry state raw material S5 is sent to slurry state feed heater 2 through high pressure shurry pump 5 from carbonaceous slurry state raw material storage tank 4.Oxygenant S9 is the direct hyperbaric oxygen agent from air separation facility 6.
Referring to Fig. 2 and Fig. 3, the tube side of slurry state feed heater 2 is walked carbonaceous slurry state raw material S5, shell side is walked steam S3.For the vapourizing furnace that contains the charging of multichannel slurry state raw material, can slurry state feed heater 2 be set separately every road carbonaceous slurry state raw material S5, also can multichannel (being more than or equal to 2 tunnels) slurry state raw material charging parallel connection enter a slurry state feed heater 2.For an outlet that has the high pressure shurry pump 5 ，Mei road carbonaceous slurry state raw material S5 of multichannel (being more than or equal to 2 tunnels) slurry state material outlet corresponding to high pressure shurry pump 5.
The present invention is not limited to the combination form of the slurry state feed heater 2 shown in Fig. 2 and Fig. 3, and other combination form is also in the scope of protection of the invention.
Embodiment 1
To take the gasification technology of the wet feeding that coal water slurry is raw material, produce synthetic gas, synthetic gas and then can be used for the application such as synthesis of chemicals, hydrogen manufacturing, IGCC.Table 1 is the character of feed coal.Vapourizing furnace, based on multi-nozzle opposed COAL-WATER SLURRY TECHNOLOGY, adopts the multiple-nozzle contraposition type coal water slurry gasification stove that has 4 opposed burners, and vapor pressure is 4.0MPa, and gasification temperature is 1300 ℃, and vapourizing furnace adopts lining of fire brick.Effective gas (the CO+H of separate unit vapourizing furnace
2) output is 134375Nm
3/ h.
The character of table 1 feed coal
In the present embodiment, high pressure shurry pump 5 is provided with two, and every high pressure shurry pump 5 has two outlets, respectively the coal slurry pipeline of a pair of opposed two burners of corresponding vapourizing furnace.Employing feeds coal slurry and the oxygen preheat of vapourizing furnace from the low-pressure steam of hydrosphere transformation unit 0.5～1.0MPa, the temperature after preheating is 150 ℃.Every road coal slurry arranges a slurry state feed heater 2, and the tube side of slurry state feed heater 2 is walked coal slurry, shell side is walked steam.Tube side adopts coil pipe pattern.Table 2 is main gasification condition and the technic index of preheating with two kinds of situations of not preheating.
Table 2 gasification condition and technic index
As can be seen from Table 2, when the temperature of vapourizing furnace import coal water slurry and oxygen is all preheating to 150 ℃, the ratio coal consumption of gasification installation, than oxygen consumption, reduced respectively 2.8%, 6.4%, cold gas efficiency has improved 2.1 percentage points, and the gasifying process performance after heat is integrated is better than original gasifying process performance.
Claims (7)
1. a method that improves slurry state feeding gas gasifying device gasification efficiency, is characterized in that, comprises the steps:
Steam (S2) from hydrosphere transformation unit waste heat boiler (1) is divided into two strands, one steam (S3) enters the slurry state feed heater (2) with the heat exchange of carbonaceous slurry state raw material (S5), and another strand of steam (S7) enters the oxidant heater (3) with oxygenant (S9) heat exchange; The nozzle that the carbonaceous slurry state raw material (S6) of pulp state feed heater (2) and oxidant heater (3) and oxygenant (S10) are directly sent to vapourizing furnace;
Wherein:
Carbonaceous slurry state raw material (S5) is sent to slurry state feed heater (2) through high pressure shurry pump (5) from carbonaceous slurry state raw material storage tank (4);
Oxygenant (S9) is directly from the hyperbaric oxygen agent of air separation facility (6);
The tube side of slurry state feed heater (2) is walked carbonaceous slurry state raw material (S5), shell side is walked steam (S3).
2. method according to claim 1, is characterized in that, the tube side of described slurry state feed heater (2) is shell and tube, U-shaped tubular type, coil tube type or helix tube type.
3. method according to claim 1, is characterized in that, goes out the carbonaceous slurry state raw material (S5) of high pressure shurry pump (5) and is between 0.1～12MPa from the pressure of the oxygenant (S9) of air separation facility (6).
4. method according to claim 1, is characterized in that, from the pressure of the steam (S2) of hydrosphere transformation unit waste heat boiler (1), is between 0.1～12MPa.
5. method according to claim 1, is characterized in that, the carbonaceous in described carbonaceous slurry state raw material (S5) is a kind of in coal, refinery coke, biomass, pitch, residual oil, bio-oil or mixture that they are several; Oxygenant (S9) is a kind of in oxygen, air, oxygen-rich air, water vapor, carbonic acid gas or mixture that they are several.
6. method according to claim 1, is characterized in that, optionally preheating carbonaceous of described steam (S2) slurry state raw material (S5), oxygenant (S9) or to both equal preheatings.
7. method according to claim 1, is characterized in that, the temperature after carbonaceous slurry state raw material (S5) is heated is lower than water saturation temperature under the pressure of carbonaceous slurry state raw material (S5) place.
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107541294A (en) * | 2016-06-28 | 2018-01-05 | 通用电气神华气化技术有限公司 | Hydrocarbon gasification system and internal heat integrate Application way |
| CN109722312A (en) * | 2019-02-27 | 2019-05-07 | 中煤陕西榆林能源化工有限公司 | A kind of method of low energy consumption coal water slurry gasification system and heating water-coal-slurry |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107541294A (en) * | 2016-06-28 | 2018-01-05 | 通用电气神华气化技术有限公司 | Hydrocarbon gasification system and internal heat integrate Application way |
| CN109722312A (en) * | 2019-02-27 | 2019-05-07 | 中煤陕西榆林能源化工有限公司 | A kind of method of low energy consumption coal water slurry gasification system and heating water-coal-slurry |
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