CN109181782A - A kind of air cooling of mating coal water slurry gasification and water cooling isothermal conversion process - Google Patents
A kind of air cooling of mating coal water slurry gasification and water cooling isothermal conversion process Download PDFInfo
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- CN109181782A CN109181782A CN201811160904.5A CN201811160904A CN109181782A CN 109181782 A CN109181782 A CN 109181782A CN 201811160904 A CN201811160904 A CN 201811160904A CN 109181782 A CN109181782 A CN 109181782A
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- heat exchanger
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/74—Construction of shells or jackets
- C10J3/76—Water jackets; Steam boiler-jackets
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
Abstract
The present invention relates to a kind of air cooling of mating coal water slurry gasification and water cooling isothermal conversion process, including water-cooled reactor, two groups of heat exchanger tubes are equipped in the water-cooled reactor, crude synthesis gas removes liquid, heat exchange, it is divided into two strands after detoxification, it respectively enters air cooling reactor and water-cooled reactor carries out linear transformation, transformed one-stage transfor-mation gas cocurrent, enter adiabatic reactor after heat exchange and carries out quadratic transformation, monitor the CO concentration in two-dimensional transform gas, when CO concentration is less than 0.4v%, two groups of heat exchanger tubes work at the same time, when CO concentration is greater than 0.4v%, close one group of heat exchanger tube, to guarantee the requirement of catalyst activity temperature in water-cooled reactor, constant steam pipe network and yield simultaneously.
Description
Technical field
The present invention relates to carbon monodixe conversion technical fields, refer specifically to a kind of air cooling of mating coal water slurry gasification and water cooling
Isothermal conversion process.
Background technique
Based on the current resources situation of the few oily lack of gas of the more coals in China, quickly sent out by the chemical industry of raw material of coal in recent years
Exhibition, coal are obtained with H by high-temperature gasification2It is production C1 chemical industry and its derivative produce with CO crude synthesis gas as main component
The Suitable base of product.Water coal slurry pressurized gasification technology is due to conveying continuous-stable, carbon conversion with coal wide adaptation range, coal slurry
Rate is high, pressurized gasification is saved the features such as gas downstream compression energy consumption and equipment investment are few and is widely applied.Using water-coal-slurry
The crude synthesis gas of gasification process production, main component CO, CO2And H2, subsequent to be respectively provided with CO converting means, effect is handle
Excessively high CO is transformed into CO in crude synthesis gas2, while generating H2, to adjust CO and H in crude synthesis gas2Content, meet downstream dress
Set the requirement to hydrogen-carbon ratio in synthesis gas.
Conversion process, that is, CO and vapor generate H under the effect of the catalyst2And CO2Process, which is applied to earliest
Ammonia synthesizing industry, it is subsequent to be applied to numerous industries such as hydrogen manufacturing, synthesizing methanol, synthetic oil, natural gas from coal successively.CO transformation is anti-
It should be strong exothermal reaction, different according to the heat-removing way to reaction heat, CO conversion process is divided into insulation conversion process and isothermal becomes
Change technique.
Isothermal is converted by the way that heat exchange equipment is arranged in change furnace, generally using liquid water as heat transfer medium, steam after heat absorption
Steam is turned to, reaction heat can be quickly absorbed, reaction bed temperature is maintained to stablize, and then realizes the stabilization of converting means
Operation.Compare con-ventional insulation converter technique, and isothermal conversion process is with process is short, equipment is few, investment is low, capacity usage ratio
Height is easy to the features such as enlargement, receive more and more attention.
The fluctuation that CO converts just latter stage reaction temperature in isothermal transformation can be transmitted in reaction bed for moving the heat exchange of heat
Pipe, and then cause the fluctuation of institute's producing steam temperature and pressure in heat exchanger tube, enlargement and polyphyly especially as CO converting means
Columnization, the quantity of steam that richness produces is also more and more, but isothermal shift-converter can not solve the fluctuation and correlation of steam pressure always
Increase problem is invested in equipment and pipeline engineering.The isothermal conversion process developed in recent years, exists in water-cooled reactor by-product
It presses steam pressure unstable, especially in latter stage operating condition, as catalyst activity reduces, the temperature shift reactions temperature such as need to improve
Degree, to maintain conversion reaction conversion ratio, then the middle pressure steam pressure of water-cooled reactor by-product generates big ups and downs, drastically influences
The stable operation of the steam pipe network of the even full factory of device.
" the shunting-type isothermal sulfur-tolerant conversion as disclosed in the Chinese invention patent application application No. is 200910056342.4
Technique and its equipment ", the isothermal sulfur-tolerant conversion is in latter stage operating condition, with the promotion for entering water-cooled reactor synthesis gas temperature, water
Cold reactor by-product middle pressure steam pressure by it is normal when 6.5MPaG soar to about 10.0MPaG or more, serious confining device
Stable operation, the big ups and downs of steam pressure also increase the investment of the equipment such as drum and pipeline；The technique will be from gasification process
The crude synthesis gas come is sent directly into the first change furnace, carries out first time transformation to high concentration CO using adiabatic reactor, easily goes out
Overtemperatute in existing heat insulation furnace, causes the catalyst inactivation in adiabatic reactor fast, and replacement frequently, increases operating cost；Together
When in order to inhibit to be insulated change furnace overtemperature, insulation change furnace enters saliva/dry gas molar ratio and is up to 2.0 in the technique, excessively high water
Gas ratio will cause catalyst devulcanization, shorten the service life of transformation catalyst.
Summary of the invention
The technical problem to be solved by the present invention is to the statuses for the prior art to provide a kind of significant decrease water cooling reaction
Device by-product middle pressure steam pressure oscillation, while reducing air cooling and the water cooling isothermal transformation work of the mating coal water slurry gasification of plant investment
Skill.
The technical scheme of the invention to solve the technical problem is: the air cooling of the mating coal water slurry gasification and water cooling
Isothermal conversion process, including water-cooled reactor, more heat exchanger tubes are equipped in the water-cooled reactor, and the entrance of the heat exchanger tube is logical
The boiler water out of boiler water pipeline connection drum is crossed, the outlet of each heat exchanger tube connects the vapour by Steam Recovery pipeline
The steam inlet of packet；It is characterized by:
The heat exchanger tube includes the second heat exchanger tube of more first heat exchanger tubes and Duo Gen, and each first set of heat exchange tubes is at first
Group heat exchanger tube；Each second set of heat exchange tubes is at second group of heat exchanger tube；The sum of the area of lumenal cross-section of each first heat exchanger tube
The 15~60% of the sum of the area of cross section for each second heat exchange tube cavity；
Accordingly, the boiler water pipeline has two；
The entrance of each first heat exchanger tube connects the first boiler water pipeline, the entrance connection of each second heat exchanger tube the
Two boiler water pipelines；The first boiler water pipeline is equipped with valve；
The crude synthesis gas of 230~250 DEG C of temperature, 6.0~6.5MPaG of pressure from coal water slurry gasifying device, CO butt
Content 40~50%, aqueous vapor molar ratio are 1.3~1.5, after isolating liquid phase, are exchanged heat to 250 DEG C~290 DEG C, after imurity-removal
It is divided into two strands；Wherein first strand of crude synthesis gas accounts for 20~50v% of crude synthesis gas total amount；
First strand of crude synthesis gas enters air cooling reactor and carries out linear transformation reaction, the reaction temperature of control air cooling reactor
It is 330 DEG C~380 DEG C, CO contents on dry basis is 2%~6% in the one-stage transfor-mation gas of outlet cold reactor；
Second strand of crude synthesis gas enters water-cooled reactor and carries out linear transformation reaction, and the boiler water in drum enters the simultaneously
One group of heat exchanger tube and second group of heat exchanger tube exchange heat with catalyst bed, and the temperature of generation is that 252~300 DEG C of pressure are 4.0
Saturated vapor is pressed to return to drum in~8.7MPaG；
It controls the middle pressure saturated vapor flow of by-product in water-cooled reactor and enters the raw synthesis gas stream in water-cooled reactor
The ratio (molar ratio) of amount is 1:6~1:10；The reaction temperature of water-cooled reactor is 290 DEG C~330 DEG C；Water-cooled reactor out
CO contents on dry basis is 1%~4% in one-stage transfor-mation gas；
The one-stage transfor-mation gas of the one-stage transfor-mation gas of outlet cold reactor and out water cooling conversion gas converges, heat exchange to 230 DEG C~
It is sent into insulation change furnace after 280 DEG C and carries out quadratic transformation reaction；The conversion gas temperature for being insulated change furnace out is 240 DEG C~290
DEG C, CO contents on dry basis sends to downstream process after recycling heat less than 0.4%；
CO contents on dry basis in the quadratic transformation gas of insulation change furnace (8) out is monitored, when secondary transformation changes
When CO contents on dry basis in gas is greater than 0.4v%, the valve on the first boiler water pipeline, first group of heat exchanger tube are closed
It does not work, only second group of heat exchanger tube work；Pressure in the drum is 4.0~8.7MPaG, temperature is 250~300 DEG C
Boiler water enters second group of heat exchanger tube from the second boiler water pipeline, and the temperature generated after heat exchange is that 250~300 DEG C of pressure are 4.0
Saturated vapor is pressed to return to drum in~8.7MPaG.
Preferably, the one-stage transfor-mation gas of the air cooling converter is introduced into and is cooled to 270 DEG C through middle pressure steam generator out
It after~310 DEG C, then mixes with the one-stage transfor-mation gas of the water-cooled reactor out, is cooled to 260 DEG C~310 with crude synthesis gas heat exchange
DEG C, it enters back into 1# low-pressure steam generator and further recycles heat, the insulation is entered after being cooled to 230 DEG C~280 DEG C and is converted
Furnace.Program energy conservation and consumption reduction effects are good.
Preferably, the two-dimensional transform gas of the insulation converter sequentially enters low-pressure steam superheater out and 2# low pressure is steamed
Vapour generator recycles heat, send downstream process to handle after being cooled to 200 DEG C~220 DEG C；
Low-pressure boiler water from battery limit (BL) generates 0.5 through 1# low-pressure steam generator and the heating of 2# low-pressure steam generator
The low-pressure saturated steam of~1.5MPaG sends out battery limit (BL) after overheating into the low-pressure steam superheater.
Preferably, the middle pressure steam flow of medium pressure steam generator by-product and entrance medium pressure steam generator
The ratio (molar ratio) of one-stage transfor-mation throughput is 1:8~1:12.
In above-mentioned each scheme, preferably each first heat exchanger tube uniform cloth in the catalyst bed of the water-cooled reactor
It sets, each second heat exchanger tube is evenly arranged in the catalyst bed of the water-cooled reactor.
It is preferred that the second heat exchanger tube described in being at least evenly equipped with three around the first heat exchanger tube described in every；Every first
Heat exchanger tube and each second heat exchanger tube being arranged in around first heat exchanger tube constitute heat exchanger tube pair.
Second heat exchanger tube described in being equipped with 3~6 around every first heat exchanger tube.
Further, each second heat exchanger tube of each heat exchanger tube centering is evenly arranged on the center of first heat exchanger tube
For on the same circumference in the center of circle.
Adjacent heat exchange tubes second heat exchanger tube described in common sparing between.The structure makes the distribution of the second heat exchanger tube more
Uniformly, heat transfer effect is more preferable, avoids the local run aways of catalyst bed.
Preferably, the steam collection pipe road includes the first steam collection pipe road being arranged in parallel and the second steam collection pipe
Road；
The outlet of each first heat exchanger tube connects first steam collection pipe road, the outlet of each second heat exchanger tube
Connect the second steam collection pipe road.When the structure can effectively avoid first group of heat exchanger tube from not working, steam suppresses the heat exchange in shut-down
In pipe.
Compared with prior art, the present invention has an advantage that
1, shift process introduces air cooling reactor, on the one hand can reduce water-cooled reactor load, while having reached overheat again
By-product middle pressure steam purpose；By parallel connection air cooling reactor, water-cooled reactor, water-cooled reactor specification can effectively reduce, favorably
In device enlargement.
2, medium-pressure boiler water supply is sent into water-cooled reactor by two strands of independent concetrated pipes and is passed through in conversion reaction latter stage
Control valve on pipeline closes the boiler feedwater of a wherein concetrated pipe, to reduce effective heat-exchanging tube bundle number in water-cooled reactor
Amount, can significantly reduce the pressure oscillation of by-product middle pressure steam, maintain the stable operation of device.
3, since water-cooled reactor byproduct steam pressure oscillation is small, the equipment design pressure such as drum is minimized, and is facilitated
Reduce equipment investment.
4, the crude synthesis gas of high concentration CO gas is first sent into air cooling reactor, water-cooled reactor, it is anti-to give full play to water cooling
Answer device will not overtemperature process characteristic, it is ensured that there is not overtemperatute, catalyst long service life, operation in entire shift process
Expense is low, and converter unit is stable；
5, in by-product, low-pressure steam carrying device after steam superheater overheats, is conducive to byproduct steam and externally conveys.
Detailed description of the invention
Fig. 1 is the process flow diagram of the embodiment of the present invention.
Fig. 2 is the longitudinal sectional view of the embodiment of the present invention.
Fig. 3 is the transverse sectional view of the embodiment of the present invention.
Fig. 4 is the partial enlarged view of part A in Fig. 3.
Fig. 5 is the process flow diagram of comparative example.
Specific embodiment
The present invention will be described in further detail below with reference to the embodiments of the drawings.
As shown in Figures 1 to 4, water-cooled reactor used in the present embodiment includes:
Furnace body 1 ', is conventional structure, including upper cover 11, lower head 12 and be connected to upper cover 11 and lower head 12 it
Between cylinder 13.
Catalyst frame 2 ' is used for loading catalyst, is arranged in cylinder 13；Multiple stomatas are evenly equipped on its side wall (in figure
It is not shown).Catalyst frame 2 ' can according to need select it is in the prior art any one, the present embodiment is radial reactor,
Crude synthesis gas is converted from the catalyst bed that each stomata enters in catalyst frame.
The medium position in 2 cavity of catalyst frame is arranged in, for collecting synthesis gas, the upper end in synthesis gas collecting pipe 3 '
Mouth closing, lower port connect synthesis gas collecting pipe 33, and linear transformation gas is sent out furnace body 1 ' by synthesis gas pipeline 33.
Heat exchanger tube is threaded through in the catalyst bed between catalyst frame 2 ' and synthesis gas collecting pipe 3 ', including by more
First set of heat exchange tubes of the first heat exchanger tube 41 composition and the second set of heat exchange tubes being made of more second heat exchanger tubes 42.
For convenient for difference, each first heat exchanger tube is indicated in Fig. 4 with filled circles, and each second heat exchanger tube is indicated with open circles.
Wherein, it is evenly arranged in cavity of each first heat exchanger tube 41 between catalyst frame and synthesis gas collecting pipe；Second
Heat exchanger tube 42 is evenly arranged around the first heat exchanger tube around the first heat exchanger tube 41；Around every first heat exchanger tube 41 at least
It is evenly equipped with three second heat exchanger tubes 42；Arrange the second heat exchanger tube of the six roots of sensation 42 in the present embodiment around every heat exchanger tube 41, six
It is the center of circle on same circumference L that the second heat exchanger tube of root 42, which is arranged in using the first corresponding heat exchanger tube,.
Each first heat exchanger tube 41 forms heat exchanger tube pair in surrounding each second heat exchanger tube 42 with setting；Adjacent heat exchange tubes pair
Between the second heat exchanger tube of common sparing 42, i.e. circumference L arranged crosswise where each second heat exchanger tube of adjacent heat exchange tubes centering.
The quantity of each pair of the second heat exchanger tube of heat exchanger tube centering can also be according to the specifications design of unit scale and reactor
Other quantity, for example, it may be three, four, five or more.
The sum of area of lumenal cross-section of each first heat exchanger tube 41 is the face of the cross section of each second heat exchanger tube, 42 inner cavity
The 15~60% of the sum of product, the present embodiment 35%.The bore of first heat exchanger tube can be equal with the bore of the second heat exchanger tube,
It can not wait, it is equal in the present embodiment, it both is controlled by the quantity and the quantity of the second heat exchanger tube that control the first heat exchanger tube
Cross-sectional area, i.e. heat exchange area corresponding to the first set of heat exchange tubes and the second set of heat exchange tubes.
The entrance of each first heat exchanger tube 41 connects the first boiler water pipeline 91, the first boiler water tube by the first distributor 43
Road 91 is equipped with control valve 95；The entrance of each second heat exchanger tube 42 connects the second boiler water pipeline 92 by the second distributor 44.
First boiler water pipeline 91 and the second boiler water pipeline 92 are gone out by the boiler water that boiler water conveyance conduit 96 connects drum 11
Mouthful；Boiler water conveyance conduit 96 is equipped with water pump 10.
The outlet of each first heat exchanger tube 41 by the first steam collection pipe 45 connect the first jet chimney 93, each described second
The outlet of heat exchanger tube 42 connects the second jet chimney 94 by the second steam collection pipe 46.First jet chimney 93 and the second steam
Pipeline 94 connects the steam inlet of drum 11 by steam conveying pipe 97.
Crude synthesis gas entrance is arranged at the top of furnace body 1 '.
Crude synthesis gas from 242 DEG C of coal water slurry gasifying device temperature, pressure 6.3MPaG, aqueous vapor molar ratio are 1.42, are sent
Enter gas-liquid separator 1, isolates the liquid phase being condensed out since pipeline is lost, that sends out at the top of gas-liquid separator 1 is thick
Synthesis gas enters input and output material heat exchanger 2 and one-stage transfor-mation gas exchanges heat, and after being heated to 250 DEG C~290 DEG C, is sent into detoxification slot 3, removing
The impurity such as the dust in crude synthesis gas.
The crude synthesis gas sent out from detoxification slot 3 is divided into two strands, wherein first strand of crude synthesis gas accounts for the 20 of crude synthesis gas total amount
~50%, it is sent into air cooling reactor 5 and carries out conversion reaction, reaction heat is for pressing saturated vapor in overheating.
The temperature of control air cooling reactor 5 is 330 DEG C~380 DEG C, CO butt in the one-stage transfor-mation gas of outlet cold reactor 5
Content is 2%~6%, after middle pressure steam generator 6 is cooled to 290 DEG C~340 DEG C, imports water-cooled reactor 4 is sent out one
In grade conversion gas.
It controls by-product middle pressure steam flow in middle pressure steam generator and enters the one-stage transfor-mation in middle pressure steam generator
The ratio (molar ratio) of throughput is 1:9~1:11.
Second strand of crude synthesis gas is sent into water-cooled reactor 4 and carries out conversion reaction, and the temperature of control water-cooled reactor 4 is 290
DEG C~310 DEG C.
Medium-pressure boiler water in drum 11 respectively enters each from the first boiler water pipeline 91 and the second boiler water pipeline 92
It in one heat exchanger tube and each second heat exchanger tube, exchanges heat with heat caused by conversion reaction in water-cooled reactor, generates pressure
The middle pressure saturated vapor for being 282 DEG C for 6.5MPaG, temperature returns to drum from the first jet chimney 93 and the second jet chimney 94
11.To remove heat caused by conversion reaction, the constant of water-cooled reactor interior reaction temperature is maintained.
The middle pressure saturated vapor generated returns to drum 11 and carries out gas-liquid separation, the middle pressure saturated vapor temperature come out from drum 11
About 288 DEG C of degree, after the middle pressure saturated vapor sent out with middle pressure steam generator 6 converges, heat, mistake are taken into air cooling reactor 5
Heat is to 350 DEG C or so rear carrying device battery limit (BL)s.
Control by-product middle pressure steam flow and the ratio into the crude synthesis gas flow in water-cooled reactor in water-cooled reactor
Example (molar ratio) is 1:7~1:9.
CO contents on dry basis is about 1%~4% in the one-stage transfor-mation gas of water-cooled reactor 4 out, with middle pressure steam generator 6 out
One-stage transfor-mation gas converge after, into input and output material heat exchanger 2 and crude synthesis gas heat exchange be cooled to 260 DEG C~310 DEG C, enter back into 1#
Low-pressure steam generator 7 and low-pressure boiler water exchange heat, and further recycle heat, and insulation is sent into after being cooled to 230 DEG C~280 DEG C
Change furnace 8 carries out quadratic transformation reaction.
The two-dimensional transform temperature degree for being insulated change furnace 8 out is 240 DEG C~290 DEG C, and CO contents on dry basis enters less than 0.4%
Low-pressure steam superheater 9 and low-pressure steam exchange heat, after being cooled to 235 DEG C~285 DEG C, into 2# low-pressure steam generator 10 with it is low
Boiler water heat exchange is pressed, continues to recycle heat, send downstream process to handle after being cooled to 200 DEG C~220 DEG C.
130 DEG C of pressure of medium-pressure boiler coolant-temperature gage from battery limit (BL) are about 10MPaG, are divided into two strands, one is sent into drum 11,
One send to middle pressure steam generator 6, presses saturated vapor in by-product 6.5MPaG, sends out boundary after overheating into air cooling reactor 5
Area.
Low-pressure boiler water from battery limit (BL) is through 1# low-pressure steam generator 7 and the production of 2# low-pressure steam generator 10 1.0
The low-pressure saturated steam of MPaG, and battery limit (BL) is sent out after the overheat of low-pressure steam superheater 9.
In device operational process, it is dry that the CO being insulated in the two-dimensional transform gas of change furnace 8 is gone out using on-line period analysis detection
Base content.When the CO contents on dry basis in the ventilation of secondary transformation is greater than 0.4v%, show catalyst activity reduction, to keep reaction
Reaction temperature need to be gradually increased in constant conversion ratio, maintain catalyst activity, the present embodiment is by closing the first boiler water pipeline
On valve stop the work of the first set of heat exchange tubes, only second group of heat exchanger tube work.
The node for closing the first set of heat exchange tubes can also be judged according to the activity decay phase of catalyst, when catalyst makes
When reaching the decline phase with the time, the control valve for the boiler feed pipe road that the first set of heat exchange tubes is connected can be closed.Existing skill
Common catalyst is cobaltmolybdate catalyst in art, and the activity decay phase is 3 years, can close first after device is run 3 years and change
The control valve for the boiler feed pipe road that heat pipe heat is connected.
After first set of heat exchange tubes is closed, compared to two groups set of heat exchange tubes are worked at the same time, and heat exchange area reduces 20%, passes through
Heat exchange area is reduced, conversion reaction latter stage is reduced, influence of the promotion of reaction temperature to isothermal transformation byproduct steam pressure is protected
The stable operation of steam pipe network and device is demonstrate,proved.
Therefore, in the application during the entire process of device is run, the yield of conversion gas is constant, by-product middle pressure steam
Pressure oscillation it is small or do not fluctuate, device is stable.
Comparative example
As shown in figure 5, this comparative example and embodiment process flow are essentially identical, water cooling used in comparative example is reacted
Device is conventional non-adjustable isothermal shift-converter, is specifically included:
Crude synthesis gas from 242 DEG C of coal water slurry gasifying device temperature, pressure 6.3MPaG, (water rubs water-gas ratio than dry gas
That ratio) it is about 1.42, it is sent into gas-liquid separator 1, the liquid phase being condensed out since pipeline is lost is isolated, from gas-liquid separation
The crude synthesis gas sent out at the top of device 1 is sent into detoxification slot 3 after input and output material heat exchanger 2 is heated to 250 DEG C~290 DEG C, removes thick close
At impurity such as dust in gas.
The crude synthesis gas sent out from detoxification slot 3 is divided into two strands, and first strand accounts for about the 20~50% of crude synthesis gas total amount, is sent into
The reactor 5 that is gas-cooled carries out conversion reaction, and reaction heat is for pressing saturated vapor in overheating；
The temperature of control air cooling reactor 5 is 330 DEG C~380 DEG C, CO butt in the one-stage transfor-mation gas of outlet cold reactor 5
Content is about 2%~6%, and after middle pressure steam generator 6 is cooled to 290 DEG C~340 DEG C, remittance is sent out by water-cooled reactor 4
One-stage transfor-mation gas in；
It controls by-product middle pressure steam flow in middle pressure steam generator and enters the one-stage transfor-mation in middle pressure steam generator
The ratio (molar ratio) of throughput is 1:9~1:11.
Second strand of crude synthesis gas is sent into water-cooled reactor 4 and carries out conversion reaction, and generated heat produces 6.5MPaG for rich
Middle pressure saturated vapor, is specifically configured to, and the medium-pressure boiler water supply in drum 11 is sent after being pressurizeed by boiler cycle pump 12 to water
In cold reactor 4, for removing heat caused by conversion reaction, to maintain the reaction temperature substantially constant of water-cooled reactor.
The middle pressure saturated vapor generated returns to drum 11 and carries out gas-liquid separation, and the middle pressure saturated-steam temperature come out from drum 11 is about
281 DEG C, after the middle pressure saturated vapor sent out with middle pressure steam generator 6 converges, the reactor 5 that is gas-cooled is superheated to 350 DEG C or so
Carrying device battery limit (BL) afterwards.
Control by-product middle pressure steam flow and the ratio into the crude synthesis gas flow in water-cooled reactor in water-cooled reactor
Example (molar ratio) is 1:7~1:9.
The temperature for controlling water-cooled reactor 4 is 290 DEG C~310 DEG C, out CO butt in the one-stage transfor-mation gas of water-cooled reactor 4
Content is about 1%~4%, after converging with the one-stage transfor-mation gas from air cooling reactor 5, is sent into effluent exchanger 2 and thick synthesis
Gas heat exchange is cooled to 260 DEG C~310 DEG C, then further recycles heat through 1# low-pressure steam generator 7, is cooled to 230 DEG C~280
It is sent into insulation change furnace 8 after DEG C and continues conversion reaction；
The conversion gas temperature for being insulated change furnace 8 out is 240 DEG C~290 DEG C, and CO contents on dry basis is steamed less than 0.4% through low pressure
After vapour superheater 9 is cooled to 235 DEG C~285 DEG C, send 2# low-pressure steam generator 10 continue recycle heat, be cooled to 200 DEG C~
Downstream process is sent to handle after 220 DEG C.
130 DEG C of pressure of medium-pressure boiler coolant-temperature gage from battery limit (BL) are about 10MPaG, are divided into two strands, one is sent into drum 11,
One send to middle pressure steam generator 6, presses saturated vapor in by-product 6.5MPaG, and battery limit (BL) is sent out after overheating.
Low-pressure boiler water from battery limit (BL) is through 2# low-pressure steam generator 7 and the production of 2# low-pressure steam generator 10 1.0
The low-pressure saturated steam of MPaG, and battery limit (BL) is sent out after the overheat of low-pressure steam superheater 9.
In conversion reaction latter stage operating condition, with the reduction of catalyst activity, reaction temperature need to be improved to maintain constant conversion
Rate, water-cooled reactor interior reaction temperature are promoted to about 325 DEG C, and water-cooled reactor byproduct steam pressure is gradually increased to 10.0MPaG
More than, steam pressure fluctuation acutely, is unfavorable for the stable operation of steam pipe network and device, simultaneously because byproduct steam pressure wave
It is dynamic, cause the equipment such as drum and circuit design pressure in this comparative example to greatly improve, increases equipment and pipeline investment.
By taking the synthetic ammonia installation using coal water slurry gasification gas making as an example, into effective gas (H2+CO) of isothermal converting means
About 85000Nm3/ h, to the air cooling of mating coal water slurry gasification and the progress of water cooling isothermal conversion process major parameter under this benchmark
Comparison is shown in Table 1.
Table 1
As can be seen from Table 1, the synthetic ammonia installation of coal water slurry gasification gas making, the used air cooling of the present embodiment and water cooling etc.
Warm conversion process, water-cooled reactor by-product middle pressure steam pressure oscillation are substantially reduced, and are conducive to the long-term of steam pipe network and device
Stable operation, while drum and circuit design pressure are remarkably decreased in embodiment, equipment and pipeline investment reduce about 1,600,000 yuan.
Claims (10)
1. a kind of air cooling of mating coal water slurry gasification and water cooling isothermal conversion process, including water-cooled reactor (4), the water cooling are anti-
It answers and is equipped with more heat exchanger tubes in device (4), the entrance of the heat exchanger tube is gone out by the boiler water of boiler water pipeline connection drum (11)
Mouthful, the outlet of each heat exchanger tube connects the steam inlet of the drum (11) by Steam Recovery pipeline；It is characterized by:
The heat exchanger tube includes more first heat exchanger tubes (41) and more second heat exchanger tubes (42), each first heat exchanger tube (41)
Form first group of heat exchanger tube；Each second heat exchanger tube (42) forms second group of heat exchanger tube；The inner cavity of each first heat exchanger tube (41)
The sum of area of cross section is the 15~60% of the sum of area of cross section of each second heat exchanger tube (42) inner cavity；
Accordingly, the boiler water pipeline has two；
The entrance of each first heat exchanger tube connects the first boiler water pipeline (91), the entrance connection of each second heat exchanger tube the
Two boiler water pipelines (92)；The first boiler water pipeline (91) is equipped with valve；
The crude synthesis gas of 230~250 DEG C of temperature, 6.0~6.5MPaG of pressure from coal water slurry gasifying device, CO contents on dry basis
40~50%, aqueous vapor molar ratio is 1.3~1.5, after isolating liquid phase, exchanges heat to 250 DEG C~290 DEG C, is divided into after imurity-removal
Two strands；Wherein first strand of crude synthesis gas accounts for 20~50v% of crude synthesis gas total amount；
First strand of crude synthesis gas enters air cooling reactor (5) and carries out linear transformation reaction, the reaction temperature of control air cooling reactor
It is 330 DEG C~380 DEG C, CO contents on dry basis is 2%~6% in the one-stage transfor-mation gas of outlet cold reactor；
Second strand of crude synthesis gas enters water-cooled reactor (4) and carries out linear transformation reaction, the boiler water in drum (11) simultaneously into
Enter first group of heat exchanger tube and second group of heat exchanger tube exchanges heat with catalyst bed, the temperature of generation is 252~300 DEG C, pressure
To press saturated vapor to return to drum (11) in 4.0~8.7MPaG；
Control the middle pressure saturated vapor flow of by-product and the crude synthesis gas flow in entrance water-cooled reactor in water-cooled reactor
Ratio (molar ratio) is 1:6~1:10；The reaction temperature of water-cooled reactor is 290 DEG C~330 DEG C；The level-one of water-cooled reactor out
CO contents on dry basis is 1%~4% in conversion gas；
The one-stage transfor-mation gas of the one-stage transfor-mation gas of outlet cold reactor and out water cooling conversion gas converges, and exchanges heat to 230 DEG C~280 DEG C
It is sent into insulation change furnace (8) afterwards and carries out quadratic transformation reaction；
The conversion gas temperature for being insulated change furnace out is 240 DEG C~290 DEG C, and CO contents on dry basis is sent to after recycling heat less than 0.4%
Downstream process；
CO contents on dry basis in the quadratic transformation gas of insulation change furnace (8) out is monitored, when in the ventilation of secondary transformation
CO contents on dry basis when being greater than 0.4v%, close the valve on the first boiler water pipeline (91), first group of heat exchanger tube
It does not work, only second group of heat exchanger tube work；Pressure in the drum (11) is 4.0~8.7MPaG, temperature is 250~300 DEG C
Boiler water from the second boiler water pipeline enter second group of heat exchanger tube, the temperature generated after heat exchange is that 250~300 DEG C of pressure are
Saturated vapor is pressed to return to drum (11) in 4.0~8.7MPaG.
2. the air cooling of mating coal water slurry gasification according to claim 1 and water cooling isothermal conversion process, it is characterised in that go out
The one-stage transfor-mation gas of air cooling converter (2) is introduced into after middle pressure steam generator is cooled to 270 DEG C~310 DEG C, then with
The one-stage transfor-mation gas mixing of the water-cooled reactor out is cooled to 260 DEG C~310 DEG C with crude synthesis gas heat exchange, it is low to enter back into 1#
Pressure steam generator (7) further recycles heat, and the insulation change furnace is entered after being cooled to 230 DEG C~280 DEG C.
3. the air cooling of mating coal water slurry gasification according to claim 1 and water cooling isothermal conversion process, it is characterised in that go out
The two-dimensional transform gas of insulation converter (8) sequentially enters low-pressure steam superheater (9) and 2# low-pressure steam generator (10)
Heat is recycled, send downstream process to handle after being cooled to 200 DEG C~220 DEG C；
Low-pressure boiler water from battery limit (BL) is generated through 1# low-pressure steam generator (7) and 2# low-pressure steam generator (10) heating
The low-pressure saturated steam of 0.5~1.5MPaG sends out battery limit (BL) after overheating into the low-pressure steam superheater (9).
4. the air cooling of mating coal water slurry gasification according to claim 3 and water cooling isothermal conversion process, it is characterised in that institute
It states the middle pressure steam flow of middle pressure steam generator (6) by-product and enters the one-stage transfor-mation gas of medium pressure steam generator (6)
The ratio (molar ratio) of flow is 1:8~1:12.
5. according to claim 1 to the air cooling of mating coal water slurry gasification described in 4 any claims and water cooling isothermal transformation work
Skill, it is characterised in that each first heat exchanger tube is evenly arranged in the catalyst bed of the water-cooled reactor (4), each described
Second heat exchanger tube is evenly arranged in the catalyst bed of the water-cooled reactor (4).
6. the air cooling of mating coal water slurry gasification according to claim 5 and water cooling isothermal conversion process, it is characterised in that every
Second heat exchanger tube described in being at least evenly equipped with three around first heat exchanger tube described in root；Every first heat exchanger tube be arranged in
Each second heat exchanger tube around first heat exchanger tube constitutes heat exchanger tube pair.
7. the air cooling of mating coal water slurry gasification according to claim 6 and water cooling isothermal conversion process, it is characterised in that every
Second heat exchanger tube described in being equipped with 3~6 around first heat exchanger tube described in root.
8. the air cooling of mating coal water slurry gasification according to claim 7 and water cooling isothermal conversion process, it is characterised in that each
Each second heat exchanger tube of heat exchanger tube centering is evenly arranged on using the center of first heat exchanger tube as the same circumference in the center of circle
On.
9. the air cooling of mating coal water slurry gasification according to claim 8 and water cooling isothermal conversion process, it is characterised in that phase
Adjacent heat exchanger tube second heat exchanger tube described in common sparing between.
10. the air cooling of mating coal water slurry gasification according to claim 9 and water cooling isothermal conversion process, it is characterised in that institute
Stating steam collection pipe road includes the first steam collection pipe road (93) and the second steam collection pipe road (94) being arranged in parallel；
The outlet of each first heat exchanger tube connects first steam collection pipe road (93), the outlet of each second heat exchanger tube
Connect the second steam collection pipe road (94).
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