CN109319734A - A kind of CO conversion process of mating methanol-fueled CLC - Google Patents
A kind of CO conversion process of mating methanol-fueled CLC Download PDFInfo
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- C01B3/02—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen
- C01B3/06—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents
- C01B3/12—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide
- C01B3/16—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of inorganic compounds containing electro-positively bound hydrogen, e.g. water, acids, bases, ammonia, with inorganic reducing agents by reaction of water vapour with carbon monoxide using catalysts
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- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
- F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
- F28D7/163—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation with conduit assemblies having a particular shape, e.g. square or annular; with assemblies of conduits having different geometrical features; with multiple groups of conduits connected in series or parallel and arranged inside common casing
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- C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
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Abstract
The present invention relates to a kind of CO conversion process of mating methanol-fueled CLC, it is characterized by comprising following step: raw gas initially enters low-pressure steam generator cooling and liquid separation adjusts water-gas ratio, raw gas after liquid separation is divided into two strands, one about 45%~55% conduct non-shifting gas, residue successively enters the air cooling change furnace of parallel connection after share split again after temperature raising, detoxification as second strand and isothermal change furnace carries out isothermal transformation respectively, and recycle heat, it is used as synthesis gas after mixing later with first strand of non-shifting gas, controls H in synthesis gas2It controls with the molar ratio of CO 2.1~2.3.Saturated vapor and low-pressure superheated steam are pressed in by-product of the present invention, the change furnace that is gas-cooled is using conversion gas as refrigerant；It is converted using multiple share split, process is short, and change furnace size is small, no overtemperature risk, and used isothermal change furnace heat exchange area is adjustable, and by-product middle pressure steam pressure oscillation is small, and system operation is more stable.
Description
Technical field
The present invention relates to carbon monodixe conversion technical fields, refer specifically to a kind of CO conversion process of mating methanol-fueled CLC.
Background technique
Since 21st century, China is rapidly developed by the chemical industry of raw material of coal, is introduced from Holland
Shell fine coal gasification process starts, and derivative develops the autonomous technique of various kinds of coal gasization, and CO is dry in the unstripped gas that such technique is produced
Base content is generally higher, up to 60% or more, for being filled using the production of gasification process producing synthesis gas and downstream C1 chemical products
It sets, need to generally be removed the CO in unstripped gas by conversion reaction, which consumes water vapour and H2 is made, while CO is become again
Readily removed CO2.Downstream product includes hydrogen manufacturing, synthesizes ammonia, methanol processed, synthetic oil, natural gas from coal etc., and different downstreams
Product is different to the CO content requirement in synthesis gas, and corresponding conversion reaction depth and technique are also different.
Carbon monodixe conversion is a kind of strongly exothermic reversible reaction under the action of catalyst, according to the shifting heat side to reaction heat
Formula is different, and CO conversion process is divided into insulation conversion process and isothermal conversion process.
Country's high concentration CO transformation at present is more to be mainly arranged stream by the way of " thermal energy recycles between multistage insulation reaction+section "
Journey, the technique there are easy overtemperature, long flow path, easy equipment are more, investment is big, energy consumption is high, system pressure drop is big, catalyst life is short etc. asks
Topic.
The isothermal conversion process developed in recent years is that heat transfer is situated between with liquid water by the way that heat exchange equipment is arranged in change furnace
Matter, steam turns to steam after heat absorption, can quickly absorb reaction heat, and reaction bed temperature is maintained to stablize, and then realizes
The stable operation of converting means.Compare con-ventional insulation converter technique, and isothermal conversion process is with process is short, equipment is few, investment
It is low, capacity usage ratio is high, is easy to the features such as enlargement, receive more and more attention in recent years.
But converting as isothermal converts string insulation for current domestic-developed, becomes since the CO gas of high concentration passes through insulation first
Furnace is changed, so still asking that the insulation change furnace overtemperature that solves to occur when high concentration CO insulation transformation, catalyst inactivation are not fast etc.
Topic, cannot achieve the long-period stable operation of high concentration CO converting means.For another example double isothermals convert tandem process, and conversion gas is all
For full tolerance by all change furnaces, equipment size is big, and cost is high, manufactures transport difficult, in addition, existing isothermal transformation both at home and abroad
Furnace is each equipped with drum by-product middle pressure steam, but due to reducing in conversion reaction middle and later periods catalyst activity, mentions to change furnace
When temperature operation, it is necessary to improve byproduct steam pressure, to guarantee that the heat of isothermal change furnace removes, steam pressure fluctuation reaches
2.5MPaG or more causes to impact to the steam pipe network of device, operation not good for system stability, and need to correspondingly increase middle pressure steam
Design of pipe networks pressure, increases pipeline investment.
" a kind of high concentration CO unstripped gas as disclosed in the Chinese invention patent application application No. is 201410439881.7
Isothermal conversion process ", the process which is converted using one section of heat insulation furnace and one section of isothermal, firstly, the first change furnace is adopted
With insulation change furnace, furnace wall will bear the conversion gas of high temperature and pressure, cause equipment wall thickness big, and equipment investment is high；And first becomes
Change furnace catalyst and be chronically under higher temperature and run, running environment is harsh, and catalyst life is shorter, replacement frequently, operating cost
With height；Meanwhile first change furnace use heat insulation furnace, temperature control it is more difficult, be easy to appear overtemperatute, to shift conversion step safety
Operation adversely affects, and there are security risks.In addition, the two changes isothermal change furnace by-product 4.0MPa steam is only urged in transformation
Agent can be maintained using initial stage, use mid-term and later period in transformation catalyst, after change furnace temperature raising operation, steam needs pressure-raising extremely
6.5MPa can meet constant-temperature oven move heat demand, the first reactor entrance water-gas ratio required by this patent and at a temperature of and produce
Under steam pressure, in the middle and later periods that transformation catalyst uses, progress that conversion reaction can not be stable.
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 CO of mating methanol-fueled CLC
Conversion process, can effectively solve con-ventional insulation change furnace overtemperature, isothermal change furnace in the catalyst later period temperature raising operation after middle pressure
The big variable area isothermal conversion process of vapour system pressure oscillation.
The technical scheme of the invention to solve the technical problem is: the CO conversion process of the mating methanol-fueled CLC,
Including isothermal change furnace, more heat exchanger tubes are equipped in the isothermal change furnace, the entrance of the heat exchanger tube passes through boiler water pipeline
The boiler water out of drum is connected, 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 include by more first set of heat exchange tubes at the first set of heat exchange tubes and the second set of heat exchange tubes of Duo Gen at
To second group of heat exchanger tube；The sum of area of lumenal cross-section of each first heat exchanger tube is the cross section of each second heat exchange tube cavity
The 15~60% of the sum of area；
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；First boiler water pipeline and the connection of the second boiler water pipeline
The boiler water out of drum；
230 DEG C~260 DEG C of temperature that upstream coal gasification process is sent, pressure 5.6MPaG~6.6MPaG, CO contents on dry basis
The raw gas temperature of 40v%~50v% is reduced to 210 DEG C~230 DEG C, is divided into two strands after isolating liquid phase；Account for raw gas total amount
First strand of raw gas of 45v%~55v% directly send downstream as non-shifting gas, and second strand of remaining 45v%~55v% is thick
Coal gas enter air cooling change furnace as take thermal medium heating lift temperature to 250 DEG C~265 DEG C, water/dry gas molar ratio be 0.6~0.8
Afterwards, into after detoxification slot detoxification, second strand of raw gas after detoxification is again broken down into two branches；
The first branch for accounting for second gang of raw gas total amount 10v%~20v% enters air cooling change furnace and carries out conversion reaction, out
The conversion gas temperature of air cooling change furnace is 280 DEG C~295 DEG C, CO contents on dry basis 3.5v%~5v%, water/dry gas molar ratio are
0.2~0.3；
The second branch for accounting for second gang of raw gas total amount 80v%~90v%, which enters, carries out isothermal transformation in isothermal change furnace,
Controlling the import and export temperature rise of isothermal change furnace is 30 DEG C；The conversion gas temperature of isothermal change furnace is 280 DEG C~295 DEG C, CO butt out
Content is 3.5v%~5v%, water/dry gas molar ratio is 0.2~0.3；Boiler water in drum, which is used as, to be taken thermal medium while entering
First group of heat exchanger tube and second group of heat exchanger tube exchange heat with the reaction heat of isothermal change furnace catalyst bed, and generation 4.0~
5.5MPaG, the middle pressure saturated vapor that temperature is 250~270 DEG C return to drum；
In device operational process, on-line monitoring isothermal converts outlet of still conversion gas CO butt volume content, when isothermal converts
When outlet of still conversion gas CO contents on dry basis is greater than 5v%, second strand of raw gas is exchanged heat to sending after 265 DEG C~280 DEG C to isothermal and is become
Furnace and air cooling change furnace are changed, and closes the valve on the first boiler water pipeline, first group of heat exchanger tube does not work in isothermal change furnace,
Boiler water in drum only enters second group of heat exchanger tube, and the reaction heat of boiler water and catalyst bed in second group of heat exchanger tube changes
Heat generates the middle pressure saturated vapor that pressure is 4.0~5.5MPaG, temperature is 250~270 DEG C and returns to the drum；Isothermal transformation
The temperature of outlet of still conversion gas is 295~310 DEG C, CO contents on dry basis is 3.5v%~5v%, water/dry gas molar ratio be 0.2~
0.3；The conversion gas temperature of air cooling change furnace is 295 DEG C~310 DEG C, CO contents on dry basis 3.5v%~5v%, water/dry gas mole out
Than being 0.2~0.3；
Heat is recycled after the conversion gas reflux that conversion gas and air cooling reactor that isothermal change furnace comes out come out, heat exchange is extremely
210 DEG C~230 DEG C, converge with first strand of raw gas, as synthesis pneumatic transmission downstream methanol synthesis procedure, controls the H in synthesis gas2
It controls with the molar ratio of CO 2.1~2.3.
Preferably, the raw gas from upstream coal gasification process is introduced into 1# low-pressure steam generator and low-pressure boiler
Water heat exchange recycling heat, by-product 1.5MPaG low-pressure saturated steam, low-pressure saturated steam enter low-pressure steam superheater and isothermal out
The conversion gas heat exchange of change furnace and air cooling change furnace, send pipe network after being superheated to 240 DEG C~260 DEG C；
The conversion gas heat exchange of isothermal change furnace and air cooling change furnace is cooled to 230 DEG C~260 DEG C out, into 2# low-pressure steam
Generator exchanges heat with low-pressure boiler water, and by-product 1.5MPaG low-pressure saturated steam, the low-pressure saturated steam is steamed with from 1# low pressure
Enter low-pressure steam superheater after the low-pressure saturated steam cocurrent of vapour generator；Conversion gas exchanges heat to 210 DEG C~230 DEG C and first
Stock raw gas converges.
Variable area isothermal change furnace used in above-mentioned technique can be used it is in the prior art any one.Preferably
Ground avoids local run aways for the uniformity for being further ensured that catalyst bed cooling, in above-mentioned each scheme, the isothermal transformation
Furnace may include furnace body and setting in the intracorporal catalyst frame of the furnace, and the middle part of the catalyst frame is collected equipped with synthesis gas
Pipe, the upper port closing of synthesis gas collecting pipe, lower port are conversion gas outlet；
Radial direction radial arrangement of each first heat exchanger tube along catalyst bed；Each second heat exchanger tube edge
The radial arrangement of the radial direction of the furnace body.
Further, each heat exchanger tube is in circumferential direction multiple same centered on the axis of the catalyst frame
It is evenly arranged on heart circumference.
To guarantee after closing first group of heat exchanger tube, the uniformity of catalyst bed cooling, on each concentric circles contour
It is disposed with second heat exchanger tube.
As the further improvement of above-mentioned each scheme, each second heat exchanger tube is divided to two in catalyst frame in the radial direction
A region arrangement, wherein first area is close to the gas-collecting pipe, and second area is close to the outer peripheral edge of the catalyst frame；And
And first heat exchanger tube and second heat exchanger tube are successively alternately arranged in the circumferential.
Preferably, the spacing m on same contour between adjacent heat exchange tubes is controlled on 30~150mm, same radioactive ray
Spacing n between adjacent heat exchange tubes is controlled in 30~150mm；
Also, the absolute value of m-n is 0~50mm.
It is preferred that m is 30~150mm, n is 30~50mm.
The present invention is provided with two groups of heat exchanger tubes in isothermal change furnace, and each group heat exchanger tube can be independently supplied boiler water, be used for
The heat exchange area in isothermal change furnace is controlled, adjusts heat exchange area when conversion reaction middle and later periods catalyst activity reduces, thus
By-product middle pressure steam ductwork pressure fluctuation is avoided, and maintains the constant of conversion ratio.
Alternatively, the isothermal change furnace in above-mentioned each scheme includes furnace body and is arranged in the intracorporal catalyst frame of the furnace, institute
The middle part for stating catalyst frame is equipped with synthesis gas collecting pipe, and the upper port of synthesis gas collecting pipe is closed, and lower port is conversion gas outlet；
Each first heat exchanger tube is evenly arranged on catalyst bed, and each second heat exchanger tube is on catalyst bed
It is evenly arranged.
Preferably, the quantity of first heat exchanger tube is equal with the quantity of second heat exchanger tube；Each first heat exchange
Pipe is respectively wound around on corresponding each second heat exchanger tube；Two the first heat exchanger tubes mutually wound and the second heat exchanger tube are formed
Heat exchanger tube pair, each heat exchanger tube are evenly arranged on catalyst bed.
Compared with existing insulation and isothermal shift process, of the invention is a little:
1, using variable area isothermal change furnace, operation is more flexible, especially drops in conversion reaction middle and later periods catalyst activity
Low, after carrying out temperature raising, by-product middle pressure steam pressure oscillation is small, is conducive to system stable operation.
2, shift process is short, and resistance is small, and the work done during compression of system, reduces energy consumption after saving；
3, using non-shifting gas line share split stream, final synthesis gas components can be effectively adjusted, increase converting means control hand
Section reduces the raw gas tolerance for participating in transformation, reduces loaded catalyst and operating cost.
4, the change furnace that will be gas-cooled is in parallel with variable area isothermal change furnace, can effectively reduce change furnace size, reduction is set
Manufacture and transport difficulty are set, equipment investment is saved；
5, isothermal change furnace low operation temperature, the overtemperature for avoiding high concentration CO from converting, catalyst running environment milder make
It is long with the service life, shift conversion step long-period stable operation easy to accomplish；
6, variable area isothermal shift-converter provided by the present invention, overcomes the prejudice of the prior art, isothermal is converted
Reactor design can be according to reaction each stage by the design of multiple groups heat exchanger tube at the isothermal shift-converter of variable area
The Active pharmaceutical of catalyst changes cooling amount, to meet the requirement of each stage catalyst active temperature, maintains yield constant, together
When avoid in the prior art reaction the later period need to increase drum and heat exchange overpressure led come the method for improving reaction temperature
The increase of heat exchange thickness of pipe wall, wall thickness of boiler barrel increase and the supporting pipelines and equipment of cause need the problems such as changing, and reduce equipment throwing
Money avoids the difficult problem of front and back phase control.
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 1；
Fig. 3 is the transverse sectional view of isothermal change furnace in the embodiment of the present invention 1；
Fig. 4 is the partial enlarged view of part A in Fig. 3；
Fig. 5 is the partial enlarged view of part B in Fig. 3；
Fig. 6 is the transverse sectional view of isothermal change furnace in the embodiment of the present invention 2；
Fig. 7 is the partial enlarged view of C portion in Fig. 6；
Fig. 8 is the winding arrangement schematic diagram of the first heat exchanger tube and the second heat exchanger tube in the embodiment of the present invention 2；
Fig. 9 is the attachment structure schematic diagram in the embodiment of the present invention 2 between first heat exchanger tube and the second heat exchanger tube.
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 5, isothermal change furnace used in the present embodiment includes:
Furnace body 10 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 20 is used for loading catalyst, is arranged in cylinder 13.It is existing that catalyst frame 20 can according to need selection
There is any one in technology, the present embodiment is radial reactor, and unstripped gas enters catalyst from the side wall of catalyst frame 20
In frame.
Synthesis gas collecting pipe 30 sends out furnace body 10 by synthesis gas pipeline 33 for collecting synthesis gas, and by synthesis gas, if
The medium position in 20 cavity of catalyst frame is set, is successively detachably connected by multistage cylinder 31, each cylinder in the present embodiment
Pass through flanged joint between body 31；Multiple foot of ladders 32 are in axial direction successively equipped at intervals on the inner sidewall of cylinder 31.End cap can
For dismantling connection in the upper port of synthesis gas collecting pipe 30, the lower port of synthesis gas collecting pipe 30 connects synthesis gas pipeline 33.
Heat exchanger tube is arranged in the catalyst bed between catalyst frame 20 and synthesis gas collecting pipe 30, 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, in Fig. 3, into Fig. 5, each first heat exchanger tube indicates that with filled circles, each second heat exchanger tube is with open circles
It indicates.
Each first heat exchanger tube 41 and each second heat exchanger tube 42 in the present embodiment pass through the respective edge in part of catalyst bed
The radial arrangement of the radial direction of catalyst frame 2, radiation line position where each second heat exchanger tube 42 on corresponding position
Radioactive ray where each first heat exchanger tube 41 successively interlaced arrangement.
Each heat exchanger tube is simultaneously also in circumferential direction in multiple concentric circumferences centered on the axis of the catalyst frame
It is evenly arranged on line.
In view of reacting the uniformity of later period cooling, in entire catalyst bed in the radial direction by interior in the present embodiment
And it is outer be divided into four regions, wherein being only disposed with the second heat exchanger tube 42, the secondth area close to the first area of synthesis gas collecting pipe
The first heat exchanger tube and the second heat exchanger tube are simutaneously arranged in domain, and the first heat exchanger tube and the friendship of the second heat exchanger tube on same contour
For arrangement, it is only disposed with the second heat exchanger tube in third region, has been simutaneously arranged first in the fourth region of catalyst frame and has changed
Heat pipe 41 and the second heat exchanger tube 42, the arrangement principle phase of the arrangement principle and second area of the first heat exchanger tube and the second heat exchanger tube
Together.
In the present embodiment, in circumferential direction, the circumferential spacing between adjacent first heat exchanger tube is controlled 30 each heat exchanger tube
Between~100mm；After the second heat exchanger tube 42 is added, the spacing m between adjacent heat exchange tubes is controlled between 30~50mm.Same diameter
On line direction, the spacing n between adjacent heat exchange tubes is in 30~50mm, and the absolute value of m-n controls between 0~30mm.
Spacing between each heat exchanger tube can also select other sizes, m according to caliber and the kinetics equation of catalyst
It is preferred that 30~150mm, n preferably 30~50mm.
Also, the sum of cross-sectional area of inner cavity of each first heat exchanger tube 41 is the transversal of the inner cavity of each second heat exchanger tube 42
The 30% of the sum of face area.The ratio can be calculated according to the kinetics equation of used catalyst, be controlled 15~60%.
In this way, each second heat exchanger tube is still able to the heat in catalyst bed is equal after the first heat exchanger tube 41 deactivates
It is even to withdraw.Also, when the first heat exchanger tube enables, since the edge that each first heat exchanger tube is largely proximate to catalyst frame is set
It sets, and is arranged between the radioactive ray of the second adjacent heat exchanger tube, therefore run early period in the higher device of catalyst activity, the
The arrangement of one heat exchanger tube has filled up the problem that spacing is larger between the second heat exchanger tube on the adjacent radioactive ray in outside, so that catalysis
It being capable of uniform cooling under agent activity higher state.
Each radial arrangement of heat exchanger tube, also facilitates catalyst discharging.When maintenance, to the catalyst block of product knot, tool
Catalyst block can be broken into pieces to facilitate from being inserted into gap between adjacent radioactive ray；The filling of catalyst, dress are also facilitated simultaneously
When filling out catalyst, it is only necessary to simply catalyst is poured into catalyst frame from top, catalyst granules i.e. can along each heat exchanger tube it
Between gap fall, will not in catalyst dropping process and because these gaps are unblocked from top to bottom hinders
It is blocked, can equably be covered with the inner cavity of entire catalyst frame.
Water inlet line, for connecting drum and each heat exchanger tube, including the first boiler water pipeline 51 and the second boiler water pipeline
52, the first boiler water pipeline 51 is equipped with valve 55, and the first boiler water pipeline 51 connects the first bobbin carriage 53, the second boiler water pipeline
52 the second bobbin carriages 54 of connection, the entrance of each first heat exchanger tube connect the first bobbin carriage 53, the entrance connection second of each second heat exchanger tube
Bobbin carriage 54.For convenient for absorbing swelling stress, the present embodiment is provided on the first boiler water pipeline and the second boiler water pipeline
Expansion joint.
Jet chimney includes the first steam connection tube 56 and the second steam connection tube 57 for connecting drum 5, to absorb expansion
Stress is provided with expansion joint on the first steam connection tube 56 and the second steam connection tube 57；First steam connection tube 56 connects
The first steam collection pipe 58 is connect, the second steam connection tube 57 connects the second steam collection pipe 59, and the outlet of each first heat exchanger tube connects
The first steam collection pipe 57 is connect, the outlet of each second heat exchanger tube connects the second steam collection pipe 58.
Send 242 DEG C of temperature of upstream coal gasification apparatus, the saturated mode rough coal of pressure 6.3MPaG, CO contents on dry basis 44%
Gas recycles heat through 1# low-pressure steam generator 8, and after by-product 1.5MPaG saturation low-pressure steam, raw gas temperature is reduced to 220
DEG C, subsequently into the lime set after the charging separation cooling of liquid separation tank 1 and water-gas ratio is adjusted, the raw gas for isolating liquid phase is divided into two
Stock, one about 50% raw gas directly send downstream as non-shifting gas, and the raw gas of another stock about 50% passes through air cooling transformation
The heating of furnace 3 lifts temperature to 250 DEG C, and water/dry gas molar ratio is 0.7, subsequently into detoxification slot 2, effectively adsorbs and filter raw gas
In impurity and the poisonous substance such as tar, dust and arsenic, guard catalyst or hydrolytic reagent extend it and use the longevity from the damage of poisonous substance
Life guarantees the long-term operation of isothermal change furnace.
Preferably, the 1# low-pressure steam generator 8 can be arranged raw gas in tube side and bypass for adjusting raw gas temperature,
Further adjust water-gas ratio.
Raw gas after detoxification is again broken down into two strands, respectively enters air cooling change furnace 3 and isothermal change furnace 4, the air cooling
Change furnace and isothermal change furnace are parallel connection.
First strand 12% of raw gas enters air cooling change furnace 3 and is converted, and the reaction heat of air cooling change furnace 3 is for preheating
The conversion gas temperature of raw gas, the change furnace that is gas-cooled out is 280 DEG C, and air cooling transformation outlet of still CO butt volume content is about 4%,
Water/dry gas molar ratio is 0.22.
Isothermal transformation is carried out in second strand 88% of rough coal pneumatic transmission isothermal change furnace 4, the temperature rise of control isothermal change furnace 4 is
30℃；The conversion gas temperature of isothermal change furnace is 280 DEG C out, and it is about 4% that isothermal, which converts outlet of still CO butt volume content, water/
Dry gas molar ratio is 0.22.
CO contents on dry basis in device operational process, in on-line monitoring isothermal transformation outlet of still conversion gas.
With the operation of device, catalyst activity is reduced, when CO butt volume content is greater than 5v%, to remain constant
Conversion ratio need to promote the operation temperature of isothermal change furnace, specifically: the valve on the first boiler water pipeline is closed, stops first
Group heat exchanger tube 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 while work
Make, heat exchange area reduces 30%, by reducing heat exchange area, reaction bed temperature is made to maintain active temperature range.
The node for closing first group of heat exchanger tube can also be judged according to the decay of activity period of catalyst, in catalyst
Activity closes first group of heat exchanger tube when reaching half-life period.Such as the common catalyst of the prior art is cobaltmolybdate catalyst, activity
Half-life period is 3 years, can close the control valve 55 on the first boiler water pipeline when device runs 3 years full.
After closing first group of heat exchanger tube, the boiler water in drum 5 only enters second group of heat exchanger tube, in second group of heat exchanger tube
The reaction heat of boiler water and catalyst bed heat exchange, generate pressure be 4.0~5.5MPaG, the middle pressure that temperature is 250~270 DEG C
Saturated vapor returns to the drum；
In device operational process, on-line monitoring isothermal converts outlet of still conversion gas CO butt volume content, when isothermal converts
Outlet of still conversion gas CO butt volume content is greater than 5%, and isothermal change furnace entrance conversion gas, which is sent after lifting temperature to 280 DEG C to isothermal, to be become
Furnace is changed, and closes the valve on the first boiler water pipeline, first group of heat exchanger tube does not work, and the boiler water in drum only enters second
The reaction heat of group heat exchanger tube, boiler water and catalyst bed in second group of heat exchanger tube exchanges heat, generate pressure be 4.0~
5.5MPaG, the middle pressure saturated vapor that temperature is 250~270 DEG C return to the drum；The temperature of isothermal transformation outlet of still conversion gas
It is 310 DEG C, CO butt volume content is 4%, and water/dry gas molar ratio is 0.22.
The conversion gas come out from isothermal change furnace 4 enters low-pressure steam after mixing with the conversion gas that air cooling reactor 3 comes out
Superheater 7, conversion gas are cooled to 244 DEG C, and subsequently into 2# low-pressure steam generator 10, by-product 1.5MPaG is saturated low-pressure steam,
Conversion gas temperature is reduced to 220 DEG C, and the conversion gas after cooling converges with the non-shifting gas, final to close as synthesis pneumatic transmission downstream
It controls at the molar ratio of H2 and CO in gas 2.2, send downstream methanol synthesis procedure.
After 2# low-pressure steam generator 10 is mixed with the 1.5MPaG of 8 by-product of 1# low-pressure steam generator saturation low-pressure steam
Into low-pressure steam superheater 7, it is transformed after gas is superheated to 250 DEG C and send pipe network.
Embodiment 2
As shown in Figures 6 to 9, in the present embodiment, the first heat exchanger tube 41 and the second heat exchanger tube 42 correspond arrangement.This reality
It applies in example and the second heat exchanger tube 42 is spirally wound on the first heat exchanger tube 41, as shown in figure 9, being connected between the two by pipe clamp 43
Together.
Each first heat exchanger tube 41 and corresponding second heat exchanger tube 42 can also be uprightly arranged, corresponding two first heat exchange
It is positioned between pipe and the second heat exchanger tube by connector；Alternatively, can also be that the first heat exchanger tube is spirally wound on the second heat exchanger tube
On；Alternatively, being also possible to corresponding two first heat exchanger tubes and the second heat exchanger tube is spirally wound together into.
The internal diameter of first heat exchanger tube 41 is 1/5th of the internal diameter of the second heat exchanger tube 42；The cross of each first heat exchange tube cavity
The sum of sectional area is the 20% of the cross-sectional area sum of each second heat exchange tube cavity；The first heat exchanger tube and the second heat exchange after winding
Tubular heat exchanger tube in a pair, it is each to exchange concentric circles circumferential direction arrangement of the heat pipe along catalyst frame, and between adjacent circumferential line
Interval it is identical, the spacing on same contour between adjacent heat exchange tubes pair is identical, to achieve the purpose that uniform heat extraction, avoids part
The generation of temperature runaway phenomenon.
Remaining content is same as Example 1.
Comparative example
By taking the synthesizing methanol device using coal gasification gas making as an example, into effective gas (H2+CO) of isothermal converting means
About 85000Nm3/ h, all operating conditions are that the present invention is consistent, and change furnace used by difference is only that is common isothermal
Change furnace, and the present invention uses completely new variable area isothermal change furnace, only carries out with regard to change furnace and boiler system major parameter
Comparison is shown in Table 1.
Table 1
As can be seen from Table 1, for the methanol synthesizer of coal gasification gas making, the used variable area of the present embodiment etc.
Warm converter technique, isothermal change furnace by-product middle pressure steam pressure oscillation are substantially reduced, the design pressure of drum, boiler water pipe network and
Middle pressure steam design of pipe networks pressure, change furnace design pressure have biggish reduction, reduce equipment design thickness, equipment investment
It being substantially reduced, equipment and pipeline direct investment can reduce about 1,200,000 yuan, meanwhile, the steam pipe network pressure relative to comparative example exists
Fluctuation in a wide range of, institute's producing steam ductwork pressure of the present invention is more stable, is conducive to device operation and steam pipe network and device
Operation steady in a long-term.
Claims (10)
1. a kind of CO conversion process of mating methanol-fueled CLC, including isothermal change furnace, more are equipped in the isothermal change furnace and is changed
Heat pipe, the entrance of the heat exchanger tube connect the boiler water out of drum by boiler water pipeline, and the outlet of each heat exchanger tube is logical
Cross the steam inlet that Steam Recovery pipeline connects the drum；It is characterized by:
The heat exchanger tube include by more first set of heat exchange tubes at the first set of heat exchange tubes and the second set of heat exchange tubes of Duo Gen pairs of
Two groups of heat exchanger tubes；The sum of area of lumenal cross-section of each first heat exchanger tube is the area of the cross section of each second heat exchange tube cavity
The sum of 15~60%；
The entrance of each first heat exchanger tube connects the first boiler water pipeline, and the entrance of each second heat exchanger tube connects second pot
Furnace water pipe road；The first boiler water pipeline is equipped with valve；First boiler water pipeline and the second boiler water pipeline connect drum
Boiler water out；
230 DEG C~260 DEG C of temperature that upstream coal gasification process is sent, pressure 5.6MPaG~6.6MPaG, CO contents on dry basis 40v%
The raw gas temperature of~50v% is reduced to 210 DEG C~230 DEG C, is divided into two strands after isolating liquid phase；Account for raw gas total amount 45v%
First strand of raw gas of~55v% directly send downstream, second strand of raw gas of remaining 45v%~55v% as non-shifting gas
Into air cooling change furnace as take thermal medium heating lift temperature to 250 DEG C~265 DEG C, water/dry gas molar ratio be 0.6~0.8 after, into
After entering detoxification slot detoxification, second strand of raw gas after detoxification is again broken down into two branches；
The first branch for accounting for second gang of raw gas total amount 10v%~20v% enters air cooling change furnace and carries out conversion reaction, is gas-cooled out
The conversion gas temperature of change furnace is 280 DEG C~295 DEG C, CO contents on dry basis 3.5v%~5v%, water/dry gas molar ratio be 0.2~
0.3；
The second branch for accounting for second gang of raw gas total amount 80v%~90v%, which enters, carries out isothermal transformation in isothermal change furnace, control
Isothermal change furnace import and export temperature rise is 30 DEG C；The conversion gas temperature of isothermal change furnace is 280 DEG C~295 DEG C, CO contents on dry basis out
It is 0.2~0.3 for 3.5v%~5v%, water/dry gas molar ratio；Boiler water in drum, which is used as, to be taken thermal medium while entering first
Group heat exchanger tube and second group of heat exchanger tube exchange heat with the reaction heat of isothermal change furnace catalyst bed, generate 4.0~5.5MPaG, temperature
Degree returns to drum for 250~270 DEG C of middle pressure saturated vapor；
In device operational process, on-line monitoring isothermal converts outlet of still conversion gas CO butt volume content, when isothermal change furnace goes out
When mouthful conversion gas CO contents on dry basis is greater than 5v%, second strand of raw gas is exchanged heat to sending to isothermal change furnace after 265 DEG C~280 DEG C
With air cooling change furnace, and the valve on the first boiler water pipeline is closed, first group of heat exchanger tube does not work in isothermal change furnace, drum
Interior boiler water only enters second group of heat exchanger tube, the reaction heat heat exchange of boiler water and catalyst bed in second group of heat exchanger tube,
It generates the middle pressure saturated vapor that pressure is 4.0~5.5MPaG, temperature is 250~270 DEG C and returns to the drum；Isothermal change furnace
The temperature of outlet conversion gas is 295~310 DEG C, CO contents on dry basis is 3.5v%~5v%, water/dry gas molar ratio be 0.2~
0.3；The conversion gas temperature of air cooling change furnace is 295 DEG C~310 DEG C, CO contents on dry basis 3.5v%~5v%, water/dry gas mole out
Than being 0.2~0.3；
Heat, heat exchange to 210 are recycled after the conversion gas reflux that conversion gas and air cooling reactor that isothermal change furnace comes out come out
DEG C~230 DEG C, converge with first strand of raw gas, as synthesis pneumatic transmission downstream methanol synthesis procedure, controls the H in synthesis gas2With
The molar ratio of CO is controlled 2.1~2.3.
2. the CO conversion process of mating methanol-fueled CLC according to claim 1, it is characterised in that described to come from upstream coal gas
The raw gas of chemical industry sequence is introduced into 1# low-pressure steam generator and low-pressure boiler water heat exchange recycling heat, by-product 1.5MPaG low pressure
Saturated vapor, low-pressure saturated steam enters low-pressure steam superheater and the conversion gas of isothermal change furnace out and the change furnace that is gas-cooled changes
Heat send pipe network after being superheated to 240 DEG C~260 DEG C；
The conversion gas heat exchange of isothermal change furnace and air cooling change furnace is cooled to 230 DEG C~260 DEG C out, occurs into 2# low-pressure steam
Device exchanges heat with low-pressure boiler water, and by-product 1.5MPaG low-pressure saturated steam, the low-pressure saturated steam is sent out with from 1# low-pressure steam
Enter low-pressure steam superheater after the low-pressure saturated steam cocurrent of raw device；Conversion gas exchanges heat to 210 DEG C~230 DEG C thick with first strand
Coal gas converges.
3. the CO conversion process of mating methanol-fueled CLC according to claim 1 or 2, it is characterised in that the isothermal change furnace
Including furnace body and setting in the intracorporal catalyst frame of the furnace, the middle part of the catalyst frame is equipped with synthesis gas collecting pipe, synthesis
The upper port of gas collecting pipe is closed, and lower port is conversion gas outlet；
Radial direction radial arrangement of each first heat exchanger tube along catalyst bed；Each second heat exchanger tube is described in
The radial arrangement of the radial direction of furnace body.
4. the CO conversion process of mating methanol-fueled CLC according to claim 3, it is characterised in that each heat exchanger tube is in week
It is evenly arranged on multiple concentric circles contours centered on the axis of the catalyst frame on direction.
5. the CO conversion process of mating methanol-fueled CLC according to claim 4, it is characterised in that each concentric circles contour
On be arranged with second heat exchanger tube.
6. the CO conversion process of mating methanol-fueled CLC according to claim 5, it is characterised in that and each second heat exchange
Pipe is divided to two regions to arrange that wherein first area is close to the gas-collecting pipe, the secondth area in the radial direction catalyst frame
Domain is close to the outer peripheral edge of the catalyst frame；And first heat exchanger tube and second heat exchanger tube successively replace in the circumferential
Arrangement.
7. the CO conversion process of mating methanol-fueled CLC according to claim 6, it is characterised in that adjacent on same contour to change
Spacing m between heat pipe control the spacing n control on 30~150mm, same radioactive ray between adjacent heat exchange tubes 30~
150mm；
Also, the absolute value of m-n is 0~50mm.
8. the CO conversion process of mating methanol-fueled CLC according to claim 7, it is characterised in that m is 30~150mm, and n is
30~50mm.
9. the CO conversion process of mating methanol-fueled CLC according to claim 1 or 2, it is characterised in that the isothermal change furnace
Including furnace body and setting in the intracorporal catalyst frame of the furnace, the middle part of the catalyst frame is equipped with synthesis gas collecting pipe, synthesis
The upper port of gas collecting pipe is closed, and lower port is conversion gas outlet；
Each first heat exchanger tube is evenly arranged on catalyst bed, and each second heat exchanger tube is uniform on catalyst bed
Arrangement.
10. the CO conversion process of mating methanol-fueled CLC according to claim 9, it is characterised in that first heat exchanger tube
Quantity is equal with the quantity of second heat exchanger tube；Each first heat exchanger tube is respectively wound around corresponding each second heat exchange
Guan Shang；Two the first heat exchanger tubes mutually wound and the second heat exchanger tube form heat exchanger tube pair, and each heat exchanger tube is in catalyst bed
On be evenly arranged.
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110787737A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN110790227A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Isothermal transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110803681A (en) * | 2019-10-24 | 2020-02-18 | 中石化宁波工程有限公司 | Gas-cooled conversion series isothermal conversion hydrogen production process matched with coal water slurry gasification and isothermal conversion furnace |
| CN110925722A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation process and isothermal transformation furnace matched with coal chemical device |
| CN110921617A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation parallel air-cooled transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
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Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020122965A1 (en) * | 1999-11-08 | 2002-09-05 | Yu Paul Taichiang | Down-sized water-gas-shift reactor |
| CN101704513A (en) * | 2009-08-13 | 2010-05-12 | 上海国际化建工程咨询公司 | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof |
| US20160200572A1 (en) * | 2013-08-20 | 2016-07-14 | Hunan Anchun Advanced Technology Co., Ltd | Isothermal conversion reactor with high co and high conversion rate, and process therefor |
-
2018
- 2018-09-30 CN CN201811160903.0A patent/CN109319734B/en active Active
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20020122965A1 (en) * | 1999-11-08 | 2002-09-05 | Yu Paul Taichiang | Down-sized water-gas-shift reactor |
| CN101704513A (en) * | 2009-08-13 | 2010-05-12 | 上海国际化建工程咨询公司 | Shunting-type isothermal sulfur-tolerant conversion process and equipment thereof |
| US20160200572A1 (en) * | 2013-08-20 | 2016-07-14 | Hunan Anchun Advanced Technology Co., Ltd | Isothermal conversion reactor with high co and high conversion rate, and process therefor |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110787737A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Isothermal shift reactor |
| CN110790227A (en) * | 2019-10-24 | 2020-02-14 | 中石化宁波工程有限公司 | Isothermal transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110803681A (en) * | 2019-10-24 | 2020-02-18 | 中石化宁波工程有限公司 | Gas-cooled conversion series isothermal conversion hydrogen production process matched with coal water slurry gasification and isothermal conversion furnace |
| CN110925722A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation process and isothermal transformation furnace matched with coal chemical device |
| CN110921617A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Isothermal transformation parallel air-cooled transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
| CN110921618A (en) * | 2019-10-24 | 2020-03-27 | 中石化宁波工程有限公司 | Air-cooled transformation series isothermal transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
| CN110803681B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Gas-cooled transformation series isothermal transformation hydrogen production process matched with coal water slurry gasification and isothermal transformation furnace |
| CN110921617B (en) * | 2019-10-24 | 2023-03-14 | 中石化宁波工程有限公司 | Isothermal transformation parallel air-cooled transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
| CN110790227B (en) * | 2019-10-24 | 2023-03-24 | 中石化宁波工程有限公司 | Isothermal transformation hydrogen production method and isothermal transformation furnace matched with coal water slurry gasification device |
| CN110921618B (en) * | 2019-10-24 | 2023-04-07 | 中石化宁波工程有限公司 | Air-cooled transformation series isothermal transformation synthesis gas preparation process matched with pulverized coal gasification and isothermal transformation furnace |
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