CN109054908A - A kind of isothermal conversion process of mating coal gasification - Google Patents
A kind of isothermal conversion process of mating coal gasification Download PDFInfo
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- CN109054908A CN109054908A CN201811160885.6A CN201811160885A CN109054908A CN 109054908 A CN109054908 A CN 109054908A CN 201811160885 A CN201811160885 A CN 201811160885A CN 109054908 A CN109054908 A CN 109054908A
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- heat exchanger
- exchanger tube
- isothermal
- change furnace
- heat
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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
- C10J3/82—Gas withdrawal means
-
- 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
- C10J3/46—Gasification of granular or pulverulent flues in suspension
-
- 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
- C10J2300/093—Coal
-
- 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
- C10J2300/16—Integration of gasification processes with another plant or parts within the plant
- C10J2300/1603—Integration of gasification processes with another plant or parts within the plant with gas treatment
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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
Abstract
The present invention relates to a kind of isothermal conversion process of mating coal gasification, including isothermal change furnace, it is characterised in that: two groups of heat exchanger tubes are equipped in isothermal change furnace；Crude synthesis gas isolates heat exchange, imurity-removal after liquid phase, is sent into the isothermal change furnace and carries out linear transformation reaction；The catalyst bed that medium-pressure boiler water enters in two groups of heat exchanger tubes and isothermal change furnace in drum exchanges heat, and generates steam, and the one-stage transfor-mation pneumatic transmission of isothermal change furnace enters to be insulated change furnace progress quadratic transformation reaction out, obtains quadratic transformation gas；CO contents on dry basis in the quadratic transformation gas of the insulation change furnace out is monitored, when the CO contents on dry basis in the ventilation of secondary transformation is greater than 1.2v%, close one group of heat exchanger tube, another group of heat exchanger tube work, to guarantee the Active pharmaceutical and constant yield of catalyst in the case where not changing steam pipe network.
Description
Technical field
The present invention relates to carbon monodixe conversion technical fields, refer specifically to a kind of isothermal transformation work of mating coal gasification
Skill.
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 gasification have obtained extensively since its coal adapts to the features such as wide, energy utilization rate is high and equipment unit gas deliverability is high
Using.Coal is obtained with H by high-temperature gasification2It is production C1 chemical industry and its derivative with CO crude synthesis gas as main component
The Suitable base of product.The crude synthesis gas produced using fine coal gasification process, main component CO, CO2 and H2, subsequent equal
CO converting means is set, and effect is that CO excessively high in crude synthesis gas is transformed into CO2, while generating H2, to adjust in crude synthesis gas
CO and H2Content, meet requirement of the downstream unit 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 conversion reaction
It is strong exothermal reaction, different according to the heat-removing way to reaction heat, CO conversion process is divided into insulation conversion process and isothermal transformation
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 isothermal change furnace by-product
It presses steam pressure unstable, especially in last stage reaction operating condition, as catalyst activity reduces, the temperature shift reactions such as need to improve
Temperature, to maintain conversion reaction conversion ratio, then the middle pressure steam pressure of isothermal change furnace by-product generates big ups and downs, seriously affects
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 last stage reaction operating condition, with mentioning into isothermal change furnace synthesis gas temperature
Rise, isothermal change furnace by-product middle pressure steam pressure is rapidly increased to about 6.5MPaG or more from 4.0MPaG, serious confining device it is steady
Fixed operation, and increase the equipment such as drum and pipeline investment；The crude synthesis gas come from gasification process is sent directly into the by the technique
One change furnace carries out first time transformation to high concentration CO using adiabatic reactor, overtemperatute in heat insulation furnace easily occurs, cause
Catalyst inactivation in adiabatic reactor is fast, and replacement frequently, increases operating cost；Surpass simultaneously in order to inhibit to be insulated change furnace
Temperature, insulation change furnace enters saliva/dry gas molar ratio and is up to 2.0 in the technique, and 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 isothermal transformation
Furnace by-product middle pressure steam pressure oscillation, while reducing the isothermal transformation work of the mating coal gasification of plant investment and operating cost
Skill.
The technical scheme of the invention to solve the technical problem is: the isothermal of the mating coal gasification converts work
Skill, including isothermal change furnace, more heat exchanger tubes are equipped in the isothermal change furnace, and the entrance of the heat exchanger tube passes through boiler water tube
Road connects the boiler water out of drum, and the outlet of each heat exchanger tube is entered by the steam that Steam Recovery pipeline connects the drum
Mouthful；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 15~35% 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；
Temperature from gasifying powder coal device is 190~210 DEG C, pressure is 3.6~4.0MPaG, and CO contents on dry basis is
Heat exchange is to 245 DEG C~255 DEG C after the crude synthesis gas of 55v%~75v% isolates liquid phase, and removes the impurity in crude synthesis gas,
It is sent into the isothermal change furnace and carries out linear transformation reaction；
Control isothermal change furnace by-product middle pressure steam flow and enter isothermal change furnace crude synthesis gas flow ratio (mole
Than) it is 1:3~1:4；
The medium-pressure boiler water that 4.0~5.5MPaG, temperature in the drum are 250~270 DEG C is from the first boiler water pipeline
It respectively enters in each first heat exchanger tube and each second heat exchanger tube, and becomes in isothermal change furnace with the second boiler water pipeline
Change heat caused by reaction to exchange heat, generate steam, from steam collection pipe road return the drum carry out gas-liquid separation from
Send out at the top of drum pressure be 4.0~5.5MPaG, the middle pressure saturated vapor that temperature is 250~270 DEG C；The isothermal is controlled to become
The temperature changed in furnace is 275 DEG C~315 DEG C；
CO contents on dry basis is 4%~12% in the one-stage transfor-mation gas of isothermal change furnace out；
One-stage transfor-mation gas exchanges heat to after 220 DEG C~235 DEG C, fills into middle pressure steam and medium-pressure boiler water supply, is adjusted to temperature
215 DEG C~225 DEG C, water/dry gas molar ratio be 0.4~0.6 after, be sent into insulation change furnace carry out quadratic transformation reaction；
The quadratic transformation temperature degree for being insulated change furnace out is 250 DEG C~290 DEG C, CO contents on dry basis is less than 1.2%, recycling heat
It is sent after amount to downstream；
CO contents on dry basis in the quadratic transformation gas of the insulation change furnace out is monitored, when in the ventilation of secondary transformation
CO contents on dry basis when being greater than 1.2v%, close the valve on the first boiler water pipeline, first group of heat exchanger tube not work
Make, only second group of heat exchanger tube work；The boiler water that 4.0~5.5MPaG, temperature in the drum are 250~270 DEG C is from second
Boiler water pipeline enter second group of heat exchanger tube, obtained after heat exchange pressure be 4.0~5.5MPaG, temperature be 250~270 DEG C saturation
Steam returns to the drum from steam collection pipe road.
Preferably, out the linear transformation gas of the isothermal change furnace be introduced into low-pressure steam superheater be cooled to 240 DEG C~
It 280 DEG C, then exchanges heat with the crude synthesis gas to sending to the insulation change furnace after 220 DEG C~235 DEG C.
It is preferred that the quadratic transformation gas for going out the insulation change furnace enters low-pressure steam generator and is cooled to 195 DEG C~205 DEG C
After send downstream process to handle.
As an improvement, the middle pressure steam of the drum can be all added into the linear transformation gas out；
In above-mentioned each scheme, preferably each first heat exchanger tube uniform cloth in the catalyst bed of the isothermal change furnace
It sets, each second heat exchanger tube is evenly arranged in the catalyst bed of the isothermal change furnace.
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, medium-pressure boiler water supply is sent into isothermal change furnace by two groups of independent heat exchanger tubes, in catalyst latter stage operating condition,
The wherein boiler feedwater of concetrated pipe all the way is closed by the control valve on pipeline, to reduce effective heat-exchanging tube bundle in isothermal change furnace
Quantity can significantly reduce the pressure oscillation of by-product middle pressure steam, be conducive to the stable operation of device.
2, since isothermal change furnace byproduct steam pressure oscillation is small, the equipment design pressure such as drum is minimized, equipment and
Pipeline investment is minimized.
3, the crude synthesis gas of high concentration CO gas is first fed into isothermal change furnace to convert, gives full play to isothermal transformation
Furnace is not in the process characteristic of overtemperature, it is ensured that overtemperatute, catalyst long service life, behaviour does not occur in entire shift process
It is low to make expense, converter unit is stable；
4, by the reasonably optimizing to shift process, the produced middle pressure steam of shift conversion step is completely used for itself conversion reaction,
Middle pressure steam superheater is eliminated, equipment investment is reduced.
5, by-product low-pressure steam carrying device after low-pressure steam superheater overheat, is conducive to low-pressure 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 isothermal change furnace in the embodiment of the present invention.
Fig. 3 is the transverse sectional view of Fig. 2.
Fig. 4 is the partial enlarged view of part A in Fig. 2.
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, isothermal change furnace used in the present embodiment includes:
Furnace body 1 ' is conventional structure, including upper cover 11, lower head 12 and is connected between upper cover 11 and lower head 12
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 15~35% of the sum of product, the present embodiment 25%.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 connect the boiler water out of drum 9 by boiler water conveyance conduit 96；
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 9 by steam conveying pipe 97.
Crude synthesis gas entrance is arranged at the top of furnace body 1 '.
Crude synthesis gas from 201 DEG C of gasifying powder coal device temperature, pressure 3.8MPaG, CO contents on dry basis 60%~75%,
It is sent into gas-liquid separator 1, the condensate liquid generated due to the thermal loss in pipe conveying procedure is isolated, from gas-liquid separator
The crude synthesis gas that 1 top is sent out is sent into detoxification slot 3 after input and output material heat exchanger 2 is heated to 245 DEG C~255 DEG C, removes thick synthesis
After the impurity such as the dust in gas, isothermal change furnace 4 is sent into from top.
Crude synthesis gas carries out conversion reaction in isothermal change furnace 4；Controlling the temperature in the isothermal change furnace is 275 DEG C
~295 DEG C.
Medium-pressure boiler water in drum 9 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 isothermal change furnace, generates pressure
The middle pressure saturated vapor for being 252 DEG C for 4.0MPaG, temperature returns to drum from the first jet chimney 93 and the second jet chimney 94
9.To remove heat caused by conversion reaction, the constant of isothermal change furnace interior reaction temperature is maintained.
The middle pressure saturated vapor generated returns to drum 9 and carries out gas-liquid separation, and it is full that 252 DEG C of middle pressure is sent out at the top of drum 9
And steam, pressure saturated vapor is fully incorporated in linear transformation gas for being humidified in this.
Out in the linear transformation gas of isothermal change furnace CO contents on dry basis be 6%~10%, into low-pressure steam superheater 5 with
Low-pressure steam heat exchange from low-pressure steam generator 8, recycles heat, is cooled to 240 DEG C~280 DEG C, exchange heat into input and output material
Device 2 and crude synthesis gas exchange heat, and continue to recycle heat, are cooled to 220 DEG C~235 DEG C；With from drum 9 middle pressure saturated vapor and
From the medium-pressure boiler water supply that temperature out-of-bounds is 130 DEG C, pressure is 4.0MPaG in static mixer 6 after mixing, obtain
To the linear transformation gas that temperature is 215 DEG C~225 DEG C, water/dry gas molar ratio is 0.4~0.6, it is sent into insulation change furnace 7 and carries out
Quadratic transformation reaction.
The quadratic transformation temperature degree for being insulated change furnace 7 out is 250 DEG C~290 DEG C, and CO contents on dry basis enters less than 1.2%
Low-pressure steam generator 8 recycles heat, exchanges heat with low-pressure boiler water, send downstream process to handle after being cooled to 195 DEG C~205 DEG C.
The medium-pressure boiler water that temperature is about 130 DEG C, pressure is 4.0~6.0MPaG is supplemented to drum 9；Control isothermal transformation
The ratio (molar ratio) of the total flow of furnace by-product middle pressure steam and the crude synthesis gas total flow entered in isothermal change furnace be 1:3~
1:4。
Low-pressure boiler water from battery limit (BL) generates the low-pressure saturated steam of 0.5~1.2MPaG through low-pressure steam generator 8,
Battery limit (BL) is sent out after the overheat of low-pressure steam superheater 5.
In device operational process, it is dry that the CO being insulated in the quadratic transformation gas of change furnace 7 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 1.2v%, show that catalyst activity has reduced, to keep anti-
Constant conversion ratio is answered, reaction temperature need to be gradually increased, catalyst activity is maintained, can close what the first set of heat exchange tubes was connected
The control valve of boiler feed pipe road.
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.
The control valve on the first boiler water pipeline is closed, first group of heat exchanger tube does not work, only second group of heat exchanger tube work.
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, isothermal change furnace used in comparative example
For conventional non-adjustable isothermal change furnace, specifically include:
Crude synthesis gas from 201 DEG C of gasifying powder coal device temperature, pressure 3.8MPaG, CO contents on dry basis 60%~75%,
It is sent into gas-liquid separator 1, the condensate liquid generated due to the thermal loss in pipe conveying procedure is isolated, from gas-liquid separator
The crude synthesis gas that 1 top is sent out is sent into detoxification slot 3 after input and output material heat exchanger 2 is heated to 245 DEG C~255 DEG C, removes thick synthesis
After the impurity such as the dust in gas, it is sent into isothermal change furnace 4；
Crude synthesis gas carries out conversion reaction in isothermal change furnace 4, and the heat of generation produces pressure 4.0MPaG, temperature for rich
Degree is to press saturated vapor in 252 DEG C, is specifically configured to, the medium-pressure boiler water supply in drum 9 is pressurizeed by boiler cycle pump 10
Enter isothermal change furnace afterwards, for removing heat caused by conversion reaction, maintains the reaction temperature of isothermal change furnace substantially permanent
It is fixed.
The middle pressure saturated vapor generated returns to drum 9 and carries out gas-liquid separation, the middle pressure saturated vapor sent out at the top of drum 9
One-stage transfor-mation gas is all sent into for being humidified.
The reaction temperature for controlling isothermal transformation is 280 DEG C, and CO contents on dry basis is about in the one-stage transfor-mation gas of isothermal change furnace 4 out
It is 4%~12%, is cooled to 240 DEG C~280 DEG C through low-pressure steam superheater 5, is sent into input and output material heat exchanger 2 and continues recycling heat
Amount, be cooled to 220 DEG C~235 DEG C, by fill into isothermal convert by-product middle pressure steam and medium-pressure boiler water supply to one-stage transfor-mation
Gas is finely adjusted, and the temperature of control one-stage transfor-mation gas is 215 DEG C~225 DEG C, after water/dry gas molar ratio is 0.4~0.6, is sent into
It is insulated change furnace 7 and continues conversion reaction.
The conversion gas temperature for being insulated change furnace 7 out is 250 DEG C~290 DEG C, and CO contents on dry basis is steamed less than 1.2% through low pressure
Vapour generator 8 recycles heat, send downstream process to handle after being cooled to 195 DEG C~205 DEG C.
Medium-pressure boiler coolant-temperature gage from battery limit (BL) is about 130 DEG C, pressure is 4.0~8.0MPaG, most of to be sent into drum 9,
It is produced through isothermal change furnace 4 and presses saturated vapor in 4.0MPaG, rest part is for adjusting one-stage transfor-mation air water vapour when temperature.
Low-pressure boiler water from battery limit (BL) generates the low-pressure saturated steam of 1.0MPaG through low-pressure steam generator 8, through low pressure
Steam superheater 5 sends out battery limit (BL) after overheating.
In conversion reaction latter stage operating condition, with the reduction of catalyst activity, reaction temperature need to be improved to maintain constant conversion
Rate, isothermal change furnace interior reaction temperature are promoted to about 310 DEG C, isothermal change furnace byproduct steam pressure be gradually increased to 6.7MPaG with
On, steam pressure fluctuation acutely, is unfavorable for the stable operation of steam pipe network and device, simultaneously because byproduct steam pressure oscillation,
Cause the equipment such as drum and circuit design pressure in this comparative example to greatly improve, increases equipment and pipeline investment.
By using coal gasification gas making synthetic ammonia installation for, into isothermal converting means effective gas (H2+CO) about
For 85000Nm3/ h compares the isothermal converter technique major parameter of mating coal gasification under this benchmark and is shown in Table 1.
Table 1 (whether the supplement in PLSCONFM table 1 is correct)
As can be seen from Table 1, for the synthetic ammonia installation of coal gasification gas making, the used isothermal of the present embodiment converts skill
Art, isothermal change furnace by-product middle pressure steam pressure oscillation are substantially reduced, and are conducive to the operation steady in a long-term of steam pipe network and device,
Drum and circuit design pressure are remarkably decreased in embodiment simultaneously, and equipment and pipeline investment reduce about 1,200,000 yuan.
Claims (10)
1. a kind of isothermal conversion process of mating coal gasification, including isothermal change furnace (4), set in the isothermal change furnace (4)
There are more heat exchanger tubes, boiler water out of the entrance of the heat exchanger tube by boiler water pipeline connection drum (9), each heat exchange
The outlet of pipe connects the steam inlet of the drum (9) by Steam Recovery pipeline；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 changed at first group
Heat pipe；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 41 is
The 15~35% of the sum of the 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；
Temperature from gasifying powder coal device is 190~210 DEG C, pressure is 3.6~4.0MPaG, CO contents on dry basis be 55v%~
Heat exchange is to 245 DEG C~255 DEG C after the crude synthesis gas of 75v% isolates liquid phase, and removes the impurity in crude synthesis gas, described in feeding
Isothermal change furnace carries out linear transformation reaction；
The medium-pressure boiler water that 4.0~5.5MPaG, temperature in the drum (9) are 250~270 DEG C is from the first boiler water pipeline
(91) it respectively enters in each first heat exchanger tube and each second heat exchanger tube with the second boiler water pipeline (92), becomes with isothermal
It changes heat caused by conversion reaction in furnace to exchange heat, generation pressure is 4.0~5.5MPaG, temperature is 250~270 DEG C
Saturated vapor returns to the drum (9) from steam collection pipe road；Controlling the temperature in the isothermal change furnace is 275 DEG C~315
℃；
Controlling out CO contents on dry basis in the one-stage transfor-mation gas of isothermal change furnace is 4%~12%；
One-stage transfor-mation gas exchanges heat to after 220 DEG C~235 DEG C, fills into middle pressure steam and medium-pressure boiler water supply, is adjusted to 215 DEG C of temperature
~225 DEG C, water/dry gas molar ratio be 0.4~0.6 after, be sent into insulation change furnace 7 carry out quadratic transformation reaction；
The quadratic transformation temperature degree for being insulated change furnace 7 out is 250 DEG C~290 DEG C, CO contents on dry basis is less than 1.2%, recycles heat
After send to downstream；
CO contents on dry basis in the quadratic transformation gas of insulation change furnace (7) out is monitored, when in the ventilation of secondary transformation
CO contents on dry basis when being greater than 1.2v%, 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；The boiler that 4.0~5.5MPaG, temperature in the drum (9) are 250~270 DEG C
Water enters second group of heat exchanger tube from the second boiler water pipeline, obtained after heat exchange pressure be 4.0~5.5MPaG, temperature be 250~
270 DEG C of saturated vapors return to the drum (9) from the second jet chimney (94).
2. the isothermal conversion process of mating coal gasification according to claim 1, it is characterised in that go out the isothermal transformation
The linear transformation gas of furnace is introduced into low-pressure steam superheater (5) and is cooled to 240 DEG C~280 DEG C, then changes with the crude synthesis gas
Heat is to sending to the insulation change furnace (7) after 220 DEG C~235 DEG C.
3. the isothermal conversion process of mating coal gasification according to claim 1, it is characterised in that go out the insulation transformation
The quadratic transformation gas of furnace (7), which enters after low-pressure steam generator (8) is cooled to 195 DEG C~205 DEG C, send downstream process to handle.
4. the isothermal conversion process of mating coal gasification according to claim 1, it is characterised in that go out the drum (9)
Middle pressure steam is all added into the linear transformation gas.
5. according to claim 1 to the isothermal conversion process of mating coal gasification described in 4 any claims, it is characterised in that
Each first heat exchanger tube is evenly arranged in the catalyst bed of the isothermal change furnace (4), and each second heat exchanger tube exists
It is evenly arranged in the catalyst bed of the isothermal change furnace (4).
6. the isothermal conversion process of mating coal gasification according to claim 5, it is characterised in that first described in every
Second heat exchanger tube described in being at least evenly equipped with three around heat exchanger tube；Every first heat exchanger tube and it is arranged in first heat exchanger tube
Each second heat exchanger tube of surrounding constitutes heat exchanger tube pair.
7. the isothermal conversion process of mating coal gasification according to claim 6, it is characterised in that every described first is changed
Second heat exchanger tube described in being equipped with 3~6 around heat pipe.
8. the isothermal conversion process of mating coal gasification according to claim 7, it is characterised in that each heat exchanger tube pair
In each second heat exchanger tube be evenly arranged on using the center of first heat exchanger tube as on the same circumference in the center of circle.
9. the isothermal conversion process of mating coal gasification according to claim 8, it is characterised in that adjacent heat exchange tubes are to it
Between the second heat exchanger tube described in common sparing.
10. the isothermal conversion process of mating coal gasification according to claim 9, it is characterised in that the 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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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110898769A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace |
| CN110921620A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation parallel adiabatic transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103435006A (en) * | 2013-08-20 | 2013-12-11 | 湖南安淳高新技术有限公司 | High-CO high-conversion-rate isothermal shift reactor |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| CN207102558U (en) * | 2017-07-11 | 2018-03-16 | 德艾柯工程技术（上海）有限公司 | A kind of modularization temperature control reactor |
| WO2018107110A1 (en) * | 2016-12-09 | 2018-06-14 | Velocys Technologies Limited | Process for operating a highly productive tubular reactor |
| CN108325476A (en) * | 2018-02-08 | 2018-07-27 | 湖南安淳高新技术有限公司 | A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
| CN207774800U (en) * | 2017-11-07 | 2018-08-28 | 刘金成 | A kind of carbon monoxide isothermal converting means of by-product superheated steam |
-
2018
- 2018-09-30 CN CN201811160885.6A patent/CN109054908B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103435006A (en) * | 2013-08-20 | 2013-12-11 | 湖南安淳高新技术有限公司 | High-CO high-conversion-rate isothermal shift reactor |
| CN105457563A (en) * | 2014-09-09 | 2016-04-06 | 航天长征化学工程股份有限公司 | Isothermal shift reactor with built-in tube bundle |
| WO2018107110A1 (en) * | 2016-12-09 | 2018-06-14 | Velocys Technologies Limited | Process for operating a highly productive tubular reactor |
| CN207102558U (en) * | 2017-07-11 | 2018-03-16 | 德艾柯工程技术（上海）有限公司 | A kind of modularization temperature control reactor |
| CN207774800U (en) * | 2017-11-07 | 2018-08-28 | 刘金成 | A kind of carbon monoxide isothermal converting means of by-product superheated steam |
| CN108325476A (en) * | 2018-02-08 | 2018-07-27 | 湖南安淳高新技术有限公司 | A kind of suspension type U-shaped vapour pipe isothermal reactor and reaction method |
| CN108404821A (en) * | 2018-05-22 | 2018-08-17 | 中石化宁波工程有限公司 | A kind of energy-saving and high efficient radial direction methanol reactor |
Non-Patent Citations (1)
| Title |
|---|
| 王庆新: "《等温变换技术在几种煤气化变换装置中的应用》", 《氮肥技术》 * |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110898769A (en) * | 2019-10-24 | 2020-03-24 | 中石化宁波工程有限公司 | Poly-generation isothermal transformation process matched with pulverized coal gasification process and isothermal transformation furnace |
| CN110921620A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation parallel adiabatic transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
| CN110921620B (en) * | 2019-10-24 | 2023-04-04 | 中石化宁波工程有限公司 | Isothermal transformation parallel adiabatic transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
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