CN101161792B - Heat recovering technique for synthetic gas production process by coal gasification - Google Patents
Heat recovering technique for synthetic gas production process by coal gasification Download PDFInfo
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Abstract
The invention discloses a heat recovery technological method for making synthetic gas during coal gasification, including the following steps: the high-temperature synthetic gas and the scoria are generated inside the vaporizer of a coal gasification furnace; chill water is sprayed into the outlet of the furnace through a primary chiller to chill the synthetic gas and the scoria below ash fusion point T1; the chilled synthetic gas and scoria are fed into a first steam generator, a steam superheater and a second steam generator for reclaiming the afterheat of the synthetic gas; moreover, part fine clinker is removed through a dust separator and residual fine clinker is removed inside a secondary chiller after further heat recovery through a boiler feeding preheater; meanwhile, the synthetic gas is humidified and then is fed into a next process unit. The invention increases the unitization value of recycled heat energy and prevents scoria from solidifies on the tube wall of the first steam generator, thereby further reducing energy consumption of equipment.
Description
Technical field
The present invention relates to a kind of coal gasification technical process, be specifically related to a kind of gasification preparing synthetic gas heat recovering technique.
Background technology
Coal is the world saving the widest fossil energy of distribution at most, under the background of soaring oil prices, the rate of exchange advantage of coal resources is obvious day by day, and world's coal workable reserves and the exploitation time limit obviously greater than oil and natural gas, this provides good development environment for the Coal Chemical Industry industry.The cleaning of coal and efficient utilization are the great technical tasks in the current energy and environment protection field, also are one of gordian techniquies of Chinese national economy sustainable development.
Recent two decades comes, and external a lot of companies have carried out development and research in order to improve coal-burning power plant's thermo-efficiency to the integrated coal gasification combined cycle technology, have promoted the development of Coal Gasification Technology.Present technology comparative maturity, technic index advanced person, the more representative dry coal powder gasification technology that Dutch shell (Shell) company is arranged (ZL88102581, ZL02829258.8, ZL200480010079.0) of achievement and the coal water slurry coal gasifying process (ZL94106474.3, ZL94117093.4, ZL98807310.2) of U.S. GE (former Texaco (Texaco)) company in the world.In the full scale plant that has built up, the heat recovery method of high-temperature synthesis gas has two kinds of common flow processs, and a kind of is to be the pot destroying process of representative with the Shell dry coal dust gasification furnace, and another kind is to be the chilling process of representative with the GE coal slurry gasifier.So-called pot destroying process is meant and utilizes heat exchanging apparatus (being waste heat boiler) directly to reclaim high-temperature synthesis gas sensible heat, and produces the technical process of high temperature and high pressure steam.Chilling process be meant high-temperature synthesis gas at first water Quench to lower temperature then utilize heat exchanging apparatus to reclaim the latent heat of synthetic gas after the Quench again, the steam of lesser temps, pressure takes place, this kind steam to utilize scope to be not so good as the steam of High Temperature High Pressure extensive, utility value is also relatively low.
Shell is disclosed a kind of coal gasifying process in patent US4859213, slag falls under gravity into the slag bath jar of vaporizer below, high-temperature synthesis gas is being carried dust secretly and is being risen to quench zone, about the cold synthetic gas cold shock to 900 that is recycled in the vapourizing furnace exit ℃, enter syngas cooler then and further reclaim heat, according to the purposes difference of synthetic gas, the synthetic gas temperature is cooled to about 250-400 ℃.Syngas cooler adopts the waterpipe type waste heat boiler, is used for production high pressure steam, middle pressure steam or superheated vapour.Synthetic gas goes out syngas cooler behind dry method dust, and a part enters quench zone after compressing through recycle gas compressor, is used for the high-temperature synthesis gas of Quench vapourizing furnace outlet, and remaining synthetic gas is delivered to lower procedure.The coal gasifying process of Shell exists cold gas efficiency low, and facility investment increases, and the compressor power consumption is big, the synthetic gas that the is used for Quench shortcomings such as dedusting that need circulate.
GE discloses a kind of coal water slurry coal gasifying process in ZL94117093.4, its synthetic gas heat recuperation has two kinds of forms, i.e. the direct vapourizing furnace of Quench mode or the vapourizing furnace of radiant cooler is housed.In direct chilling-type vapourizing furnace, high-temperature synthesis gas is the water spray in the shock chamber, and by Quench to 130～260 ℃, the sensible heat with synthetic gas in washing directly changes into steam.Thisly high temperature heat source is changed into low-grade low temperature heat energy using, is extremely irrational in the utilization of heat energy, and the utility value of heat recuperation is not high yet.GE is in U.S. Pat 4436530, and US4377132 discloses two kinds of vapourizing furnaces that radiant cooler is housed, and its radiant cooler adopts water wall structure and waterpipe type structure respectively.High-temperature synthesis gas is earlier through behind the decline passway radiation heat transfer of radiant cooler, the temperature of synthetic gas dropped in 250-600 ℃ the scope water Quench slagging-off again.In this heat recuperation mode, the fused lime-ash can reduce the heat transfer efficiency of radiant cooler easily on the water wall surface or the water wall surface adhesion when serious.
Summary of the invention
At the technological deficiency that exists in the existing procedure, the objective of the invention is: the heat recovering technique that a kind of synthetic gas production process by coal gasification is provided, this process program combines the advantage of chilling process and pot destroying process, change the low-grade low temperature heat energy of recovery in the existing technology into recovery high-grade high temperature heat, improve the use value of heat energy.
The technical solution adopted for the present invention to solve the technical problems is as follows:
A kind of heat recovering technique of synthetic gas production process by coal gasification, this method comprises the processing step of following order:
(1) with coal dust or coal water slurry in oxygenant enters the vaporizer 5 of coal gasifier 1, partial oxidation reaction takes place in vaporizer 5, generate high-temperature synthesis gas;
(2) temperature of coming out from vaporizer 5 is 1200-1500 ℃ of one-tenth gas and a slag that closes, and after process one-level chiller 7 carries out Quench, is cooled to the ash fusion point T of feed coal
1Below;
(3) high-temperature synthesis gas after step (2) Quench, enter the tube side of first vapour generator 8, with the pressure from drum 14 of its shell side be that the water of 4.0～16MPa carries out heat exchange, aquagenic steam water interface returns drum 14 again, and the synthetic gas of tube side is cooled to 650-1000 ℃ in the exit of first vapour generator;
(4) synthetic gas and the lime-ash that exports from first vapour generator 8, lower space in the shock chamber is carried out gravity separation, lime-ash is deposited in the bottom of shock chamber, drain into afterwards in the lock slag ladle 16, and synthetic gas makes progress at the shell and the passage baffling between the vapourizing furnace shock chamber refractory liner 3 of first vapour generator 8, go out coal gasifier through coal gasifier outlet 15, then, be sent to vapor superheater 9, synthetic gas carries out heat exchange with saturation steam from drum 14 in vapor superheater 9, saturation steam is superheated to 330-590 ℃, send the steam user to use, and synthetic gas is cooled to 500-900 ℃;
(5) enter second vapour generator 10 through step (4) refrigerative synthetic gas, with pressure from drum 14 be that the water of 4.0～16MPa carries out heat exchange, aquagenic steam water interface returns drum 14 again, synthetic gas is cooled to 300-600 ℃;
(6) enter dust separator 11 through step (5) refrigerative synthetic gas, the thin lime-ash in the synthetic gas is further separated in dust separator 11, send the lime-ash processing unit to handle after slag-drip opening is discharged;
(7) synthetic gas after step (6) dedusting enters feedwater preheater 12, carry out heat exchange with oiler feed from unit for treating water, be further cooled to 250～400 ℃, and oiler feed is preheated to 110～330 ℃, the oiler feed after the preheating is sent in the drum 14;
(8) enter secondary chiller 13 through the cooled synthetic gas of step (7), synthetic gas is in secondary chiller 13, by spraying into chilled water, thin lime-ash in the synthetic gas is further removed, contained thin cindery pulp water and send the pulp water processing unit to handle, simultaneously, the chilled water that sprays into is partly vaporized, add in the synthetic gas, make that the content of water vapor reaches capacity in the synthetic gas, the synthetic gas temperature of coming out from secondary chiller 13 is 200～250 ℃ and is sent to the subsequent technique unit;
Equipment related in the present technique method mainly comprises: coal gasifier 1, downtake 2, shock chamber's refractory liner 3, shock chamber 4, vaporizer 5, one-level chiller 7, first vapour generator 8, vapor superheater 9, second vapour generator 10, dust separator 11, feedwater preheater 12, secondary chiller 13, drum 14 and lock slag ladle 16.Wherein:
The first vapor generation vapour 8, vapor superheater 9, second vapour generator 10 and feedwater preheater 12 can be common tube and shell heat exchanger, synthesize and make tube side leave with rage, and other medium is walked shell side.The technician of the industry knows this equipment very much;
Dust separator 11 is a dry method cyclonic separator, thin lime-ash in the synthetic gas is separated, discharged in the bottom of cyclonic separator, synthetic gas comes out from the top of cyclonic separator, realize that gas separates with solid, this equipment also is one of chemical industry common equipment.
Coal gasifier 1 is meant the equipment of method preparing synthetic gas such as adopting coal water slurry or fine coal, and it generally includes: vaporizer 5, shock chamber 4, shock chamber 4 comprise shock chamber's refractory liner 3, one-level chiller 7 and downtake 2.Coal is in vaporizer 5, and the generation synthetic gas gasifies under the oxygenant existence condition; One-level chiller 7 is a multi-nozzle atomising unit, chilled water can be sprayed in the synthesis gas stream with vaporific, evenly apace synthetic gas is cooled off, and cooled synthetic gas enters the first coupled vapour generator 8 downwards along downtake 2; Shock chamber's refractory liner 3 is high temperature resistant non-metal heat-insulating material, in order to the metal shell of protection vapourizing furnace.
The inventive method has adopted two-stage Quench (one-level chiller 7 and secondary chiller 13) method and useless pot (first vapour generator 8, vapor superheater 9 and second vapour generator 10) flow process process combined flow process.Described two-stage Quench method is synthetic gas carries out Quench through one-level chiller 7 and secondary chiller 13 a method; Described pot destroying process is the flow process that synthetic gas enters first vapour generator 8, vapor superheater 9 and second vapour generator 10.At first adopt the one-level chiller temperature of high-temperature synthesis gas to be cooled to the ash fusion point T of coal
1Below.The first vapour generator 8 tube sides top-down motion of high-temperature synthesis gas in shock chamber 4, first vapour generator 8 adopts the fire-tube type vapour generator to carry out heat recuperation.
The design and the principle of technical solution of the present invention are: with coal raw material (comprising fine coal or coal water slurry) and oxygenant (oxygen, air, water vapour etc.) enter coal gasifier 1 together, partial oxidation reaction takes place in vaporizer 5, generate crude synthesis gas, the heat that reaction discharges makes lime-ash be in molten state, synthetic gas is being carried the fused lime-ash secretly downwards by vaporizer 5, in exporting the one-level chiller 7 at 6 places, vaporizer is recycled the water coolant Quench, slag is frozen into lime-ash, synthetic gas and lime-ash enter the tube side that is arranged on first vapour generator 8 of coaxial position under the vaporizer, carry out heat exchange with the oiler feed from drum 14 of shell side, synthetic gas that is cooled and lime-ash in the shock chamber 4 lower space carry out gravity separation, lime-ash is deposited in the bottom of shock chamber, drain into afterwards in the lock slag ladle, and make progress at the shell and the passage baffling between the vapourizing furnace shock chamber refractory liner 3 of first vapour generator 8 from the synthetic gas that first vapour generator 8 comes out, go out coal gasifier through coal gasifier outlet 15, then, be sent to vapor superheater 9, and the lime-ash solid particles sediment in the shock chamber 4 bottom, and drain into lock slag ladle 16.
Synthesis gas is in vapor superheater 9, carry out heat exchange with saturation steam from drum 14, saturation steam is superheated to 330-590 ℃, send the steam user to use, and synthetic gas is cooled to 500-900 ℃, after entering second vapour generator, 10 heat-shifts then, enter dust separator 11, remove the most of thin lime-ash that carries in the synthetic gas, enter oiler feed interchanger 12 again, further reclaim heat after, enter secondary chiller 13 again, water enters the subsequent technique unit after the synthetic gas thorough washing is removed residual thin lime-ash.
The higher-grade heat of the synthetic gas that reclaims by first vapour generator 8, vapor superheater 9 and second vapour generator 10 is used for producing the ultra-high voltage superheated vapour, further uses for follow up device.
Oiler feed is sent into drum 14 after feedwater preheater 12 preheatings.The saturation water that is come out by drum 14 enters first vapour generator 8 and second vapour generator 10 respectively, the steam water interface that produces after the heat exchange returns drum and carries out carbonated drink separation, saturation steam is delivered to vapor superheater 9, exports after being superheated to assigned temperature, uses for the steam user.
The extra high pressure steam of by-product can be incorporated steam pipe system output in present method, also can be used to driving steam turbine and drives other rotating machinerys or generating.
Processing method of the present invention has been drawn the advantage of existing chilling process and pot destroying process, and the two is combined, change the low-grade low temperature heat energy of recovery in the existing technology into recovery high-grade high temperature heat, improve the use value of heat energy, have significant advantage:
(1) the present invention with less water Quench pyritous synthetic gas and slag, makes slag be in ash fusion point T at outlet 6 places of vaporizer 5
1Below, avoided slag on the tube wall of follow-up vapour generator, to bond, stablize the heat transfer efficiency between synthetic gas and vapour generator.
(2) the present invention's sensible heat that will go out the high-temperature synthesis gas of vaporizer directly reclaims and is converted into the steam of High Temperature High Pressure, has improved the utility value of the synthetic gas sensible heat that reclaims, and has enlarged the range of application that reclaims heat energy, has reduced the energy consumption of device effectively.
(3) the present invention adopts the dry method dust separating device that the thin lime-ash that synthetic gas carries is separated, and has reduced the consumption of chilled water and washing water in the heat recovering process, has reduced the treatment capacity and the quantity discharged in device Heisui River, helps energy-conserving and environment-protective.
Description of drawings
Fig. 1 is the heat recovery technique schema of coal gasification course of the present invention
Fig. 2 is the process flow diagram of Fig. 1
Among the figure, 1. coal gasifier 2. downtakes 3. refractory liners 4. shock chambers 5. vaporizers, 6. vaporizers export 7. one-level chillers, 8. first vapour generators, 9. vapor superheaters, 10. second vapour generators, 11. dust separators, 12. feedwater preheaters, 13. secondary chillers, 14. drums, 15. coal gasifiers outlet, 16. lock slag ladles
Embodiment
The present invention is further described below in conjunction with drawings and Examples.
Vapourizing furnace with 35 tons/hour of coal treatment capacities is an example, with reference to Fig. 1, is provided with vaporizer 5 and shock chamber 4 in the coal gasifier 1 of this device; Transition linkage section in vaporizer and shock chamber is provided with one-level chiller 7, and one-level chiller 7 is made up of 20 atomizing nozzles.The synthetic gas pressure that vaporizer 5 produces is 6.5MPa, temperature is 1250～1350 ℃, enter one-level chiller 7 from the outlet 6 of vaporizer, one-level chiller 7 with chilled water with in the vaporific logistics that evenly sprays into synthetic gas, can make synthetic gas evenly, promptly be cooled like this, thereby can avoid the slag caking, the pressure of the synthetic gas after the Quench is 6.5MPa, temperature is 1050～1150 ℃, synthetic gas after the Quench and lime-ash are downward along downtake 2, enter first vapour generator 8 that is connected with downtake 2; The first vapour generator 8 tube sides top-down motion of high-temperature synthesis gas in shock chamber 4, first vapour generator 8 adopts the fire-tube type vapour generator to carry out heat recuperation.
First vapour generator 8 is located at the bottom of coal gasifier, coaxial position place under vaporizer 5, it is actual to be a tube and shell heat exchanger, form by the heat transfer tube and the shell that gather, there is tube sheet at two ends, synthesize and make tube side leave with rage, and saturated feedwater is walked shell side, after the synthetic gas in the pipe and the saturation water of shell side carried out heat exchange, synthetic gas was cooled to 850～900 ℃; 4 inwall is provided with heatproof insulating refractory lining 3 in the shock chamber, and this heatproof insulating refractory lining 3 adds the composite structure of water wall for refractory materials or refractory materials; The synthetic gas and the cindery mixture that come out from first vapour generator 8, in the cavity of its underpart, the part lime-ash is deposited to the bottom of shock chamber 4, and enter the lock slag ladle 16, synthetic gas then through the passage baffling that forms between the shell of first vapour generator 8 and the shock chamber's refractory liner 3 upwards, be provided with coal gasifier outlet 15 in middle and upper part, coal gasifier shock chamber, synthetic gas from then on mouth goes out coal gasifier.
Synthetic gas from coal gasifier outlet 15 enters vapor superheater 9 by pipe connection, and the pressure that drum 14 is produced is that the saturation steam of 13.5MPa is superheated to 510～540 ℃, and this steam can be sent to the steam user and use; It is 6.5MPa that synthetic gas is cooled to pressure, and temperature is 600～650 ℃, enters second vapour generator 10 then, and continuing pressure takes place is the saturation steam of 13.5MPa, and simultaneously, it is 6.45MPa that synthetic gas is further cooled to pressure, and temperature is 450 ℃; Then, synthetic gas enters dust separator 11, this dust separator is actual to be the dry method cyclonic separator, thin lime-ash in the synthetic gas is separated, discharge bottom at separator, send the lime-ash processing unit to handle, synthetic gas is then drawn from the top of separator, deliver to feedwater preheater 12 with pipeline, oiler feed is preheating to about 250 ℃, drum 14 is sent in oiler feed after the preheating, and it is 6.40MPa that the while synthetic gas is cooled to pressure, and temperature is 350 ℃, enter secondary chiller 13 then, in this equipment, by spraying into chilled water the fine dust in the synthetic gas is further washed, the slag-water slurry that the washing back forms (is called: Heisui River) discharge in its underpart, send the pulp water processing unit to handle, washing cooled synthetic gas pressure is 6.40MPa, and temperature is 245 ℃, and cooled synthetic gas is sent to the subsequent technique unit.Above-mentioned process flow diagram as shown in Figure 2.
The output and the parameter of by-product superelevation steam see Table 1 in the present embodiment.
Detailed description in conjunction with Fig. 1 and embodiment can be understood purpose of the present invention and feature better, but not as restriction foundation of the present invention.
Claims (5)
1. the heat recovering technique of a synthetic gas production process by coal gasification, it is characterized in that: this method comprises the processing step of following order:
(1) with coal dust or coal water slurry in oxygenant enters the vaporizer (5) of coal gasifier (1), partial oxidation reaction takes place in vaporizer (5), generate high-temperature synthesis gas;
(2) temperature of coming out from vaporizer (5) is 1200-1500 ℃ synthetic gas and a slag, after process one-level chiller (7) carries out Quench, is cooled to the ash fusion point T of feed coal
1Below;
(3) high-temperature synthesis gas after step (2) Quench, enter the tube side of first vapour generator (8), with the pressure from drum (14) of its shell side be that the water of 4.0～16MPa carries out heat exchange, aquagenic steam water interface returns drum (14) again, and the synthetic gas of tube side is cooled to 650-1000 ℃ in the exit of first vapour generator;
(4) synthetic gas and the lime-ash that exports from first vapour generator (8), lower space in the shock chamber is carried out gravity separation, lime-ash is deposited in the bottom of shock chamber, drain into afterwards in the lock slag ladle (16), and synthetic gas makes progress at the shell and the passage baffling between the vapourizing furnace shock chamber refractory liner (3) of first vapour generator (8), go out coal gasifier through coal gasifier outlet (15), be sent to vapor superheater (9) then, synthetic gas is in vapor superheater (9), carry out heat exchange with saturation steam from drum (14), saturation steam is superheated to 330-590 ℃, send the steam user to use, and synthetic gas is cooled to 500-900 ℃;
(5) enter second vapour generator (10) through step (4) refrigerative synthetic gas, with pressure from drum (14) be that the water of 4.0～16MPa carries out heat exchange, aquagenic steam water interface returns drum (14) again, synthetic gas is cooled to 300-600 ℃;
(6) enter dust separator (11) through step (5) refrigerative synthetic gas, the thin lime-ash in the synthetic gas is further separated in dust separator (11), send the lime-ash processing unit to handle after slag-drip opening is discharged;
(7) synthetic gas after step (6) dedusting enters feedwater preheater (12), carry out heat exchange with oiler feed from unit for treating water, be further cooled to 250～400 ℃, and oiler feed is preheated to 110～330 ℃, the oiler feed after the preheating is sent in the drum (14);
(8) enter secondary chiller (13) through the cooled synthetic gas of step (7), synthetic gas is in secondary chiller (13), by spraying into chilled water, thin lime-ash in the synthetic gas is further removed, contained thin cindery pulp water and send the pulp water processing unit to handle, simultaneously, the chilled water that sprays into is partly vaporized, add in the synthetic gas, make that the content of water vapor reaches capacity in the synthetic gas, the synthetic gas temperature of coming out from secondary chiller (13) is 200～250 ℃ and is sent to the subsequent technique unit;
Described drum (14) be used for separating step (3) from first vapour generator (8) and the step (5) from the steam water interface of second vapour generator (10), and be used for the oiler feed of receiving step (7) from feedwater preheater (12), in addition, drum (14) is used for step (3) provides oiler feed to second vapour generator (10) in first vapour generator (8) and step (5), also being used for step (4) provides saturation steam to vapor superheater (9).
2. the heat recovering technique of synthetic gas production process by coal gasification according to claim 1 is characterized in that: adopt two-stage Quench method and pot destroying process process combined flow process; Described two-stage Quench method is synthetic gas carries out Quench through one-level chiller (7) and secondary chiller (13) a method; Described pot destroying process is the flow process that synthetic gas enters first vapour generator (8), vapor superheater (9) and second vapour generator (10).
3. the heat recovering technique of synthetic gas production process by coal gasification according to claim 1 is characterized in that: at first adopt the one-level chiller temperature of high-temperature synthesis gas to be cooled to the ash fusion point T of coal
1Below.
4. the heat recovering technique of synthetic gas production process by coal gasification according to claim 1, it is characterized in that: first vapour generator (8) the tube side top-down motion of high-temperature synthesis gas in shock chamber (4), first vapour generator (8) adopt the fire-tube type vapour generator to carry out heat recuperation.
5. the heat recovering technique of synthetic gas production process by coal gasification according to claim 1, it is characterized in that: the synthetic gas that comes out from first vapour generator (8), shell and the passage baffling between shock chamber's refractory liner (3) at first vapour generator make progress, and go out coal gasifier from coal gasifier outlet (15), and the lime-ash solid particles sediment in the shock chamber bottom of (4), and drain into lock slag ladle (16).
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104017606A (en) * | 2014-06-24 | 2014-09-03 | 中国神华能源股份有限公司 | Coal water slurry gasification process system |
| CN104017606B (en) * | 2014-06-24 | 2016-04-20 | 中国神华能源股份有限公司 | Coal-water slurry gasification system |
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| CN101161792A (en) | 2008-04-16 |
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