CN101955153B - Process for converting high-concentration CO-tolerant sulfur - Google Patents
Process for converting high-concentration CO-tolerant sulfur Download PDFInfo
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- CN101955153B CN101955153B CN2010102958888A CN201010295888A CN101955153B CN 101955153 B CN101955153 B CN 101955153B CN 2010102958888 A CN2010102958888 A CN 2010102958888A CN 201010295888 A CN201010295888 A CN 201010295888A CN 101955153 B CN101955153 B CN 101955153B
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- 238000000034 method Methods 0.000 title claims abstract description 147
- 230000008569 process Effects 0.000 title claims abstract description 134
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 title claims abstract description 32
- 229910052717 sulfur Inorganic materials 0.000 title claims abstract description 32
- 239000011593 sulfur Substances 0.000 title claims abstract description 32
- 239000007789 gas Substances 0.000 claims abstract description 113
- 238000006243 chemical reaction Methods 0.000 claims abstract description 62
- 239000002994 raw material Substances 0.000 claims abstract description 31
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 8
- 230000009466 transformation Effects 0.000 claims description 21
- 230000008859 change Effects 0.000 claims description 20
- 239000003054 catalyst Substances 0.000 claims description 13
- 239000012535 impurity Substances 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 230000002939 deleterious effect Effects 0.000 claims description 5
- 230000000694 effects Effects 0.000 claims description 5
- 238000010521 absorption reaction Methods 0.000 claims description 4
- 238000002156 mixing Methods 0.000 claims description 4
- 238000000746 purification Methods 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 239000002918 waste heat Substances 0.000 claims description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 3
- 229910052739 hydrogen Inorganic materials 0.000 abstract description 3
- 239000001257 hydrogen Substances 0.000 abstract description 3
- 239000000203 mixture Substances 0.000 description 19
- 238000005516 engineering process Methods 0.000 description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 9
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 9
- 239000003034 coal gas Substances 0.000 description 9
- 238000002309 gasification Methods 0.000 description 8
- 239000000047 product Substances 0.000 description 7
- 239000007795 chemical reaction product Substances 0.000 description 6
- 229910002091 carbon monoxide Inorganic materials 0.000 description 4
- 239000003245 coal Substances 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 238000011068 loading method Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 230000003245 working effect Effects 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000001066 destructive effect Effects 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229910001385 heavy metal Inorganic materials 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 230000002045 lasting effect Effects 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000004148 unit process Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
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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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
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- Industrial Gases (AREA)
- Hydrogen, Water And Hydrids (AREA)
Abstract
The invention discloses a process for converting high-concentration CO-tolerant sulfur, which belongs to production of hydrogen-containing mixed gases. The process is characterized in that: a, at least one pre-converting reactor and at least one main converting reactor are adopted; b, a raw material process gas at least accounts for 15 to 40 percent of the total volume and is introduced into the pre-converting reactor in a to perform a pre-converting reaction first, then the pre-converted process gas is mixed with a raw material process gas which is not introduced into the pre-converting reactor, and the mixed gas is introduced into the main converting reactor to perform a converting reaction continuously; and c, the process condition of the pre-converting reactor is that: the water/gas volume ratio is 0.8 to 3.0, the dry gas space velocity is 1,000 to 10,000 m<3>/h, and the intake temperature is 220 to 320 DEG C. The process for converting the high-concentration C0-tolerant sulfur has low steam consumption, saves equipment investment, can effectively prevent overhigh temperature of a converting reactor bed layer, and makes the heat generated by the converting reaction in the converting reactors fully utilized.
Description
Technical field
The present invention is a kind of high concentration CO sulfur-resisting transformation system and process method.Belong to the production of oxo-synthesis gas, hydrogeneous gas mixture, particularly employing sulfur-resistant transformation catalyst is with the process method of water vapour and high-concentration carbon monoxide reacted oxo-synthesis gas, hydrogeneous gas mixture.
Background technology
In the technology coal gas that gasification produced, mainly contain CO, CO
2, H
2, H
2O also contains little amount of N
2, CH
4, H
2S, COS, Ar etc.The derived product that with coal gas is raw material is to the H in the raw material coal gas
2The requirement of/CO ratio is different.Be raw material when preparing product such as methyl alcohol, dme, alkene, acetic acid through oxo process with coal gas, generally only need the CO in the part coal gas be transformed to H
2:
The technology coal gas of not participating in transformationreation through shift reaction product and part mixes, and regulates the CO content in the virgin gas.When the product needed hydrogen of downstream, like synthetic ammonia, DCL/Direct coal liquefaction etc., generally need 2～4 shift-converters, CO is reacted completely as far as possible, produce hydrogen as much as possible.
Coal gasifying process is different, and the technology coal gas that is produced is formed different.Be that the butt of CO is formed and (do not comprised water in the coal gas that produced of the coal water slurry gasification technology of representative with the Texaco; Be roughly 40-50mol% down together); The processing condition of first shift-converter, WGR (mol ratio of other component beyond dewatering in water vapor and the process gas, down together) is 1.0～1.4 usually; 220～280 ℃ of inlet temperature of reaction, pressure 3.0～8.0MPa.Reactor outlet CO butt forms 4～10%, 420～460 ℃ of reactor outlet temperature.
Be that the butt of CO is formed and is roughly 60～75% in the process gas that fine coal gasification process was produced of representative with Shell, GSP, space flight stove etc.CO is up to getting into shift-converter more than 60%; Under the same transformationreation condition; The general meeting of the temperature of reaction of reaction bed bottom is near 500 ℃, even above 530 ℃, so just the material to reactor drum has proposed special requirement; Increase the cost of reactor drum, also increased the insecurity of device operation.In addition, because CO is dense, the top reaction impellent of beds is very big, and the catalyst particle internal temperature is higher than gas flow temperature far away, is prone to cause catalyst deactivation.
The main path that solves the high concentration CO transformation problem at present has three.The high WGR of a kind of employing reduces bed temperature, can reduce to the temperature of bed bottom below 460 ℃ as bringing up to WGR about 1.8; But there is the big problem of consumption quantity of steam.Another kind method is before main transformer changes reactor drum, to increase a pre-reactor; All introduce pre-reactor to gasifying process gas; The CO butt is formed reduces to about 40%-50%; Get into main transformer again and change reactor drum, the problem of existence is that preparatory shift reaction product need be lowered the temperature and could be got into main reactor, otherwise main reactor still can overtemperature; Because all gas is through preparatory shift-converter, heat interchanging area needs enough big.Also having a kind of method is that first shift-converter adopts very low WGR (as 0.2～0.4), through the consumption limited reactions degree of water, thus the control bed temperature; But there is the danger that methanation reaction takes place down in low WGR, and methanation reaction is a strong exothermal reaction, in case methanation reaction takes place, reactor bed will " temperature runaway ", causes sintering of catalyst, even reactor drum is damaged; The WGR of main is most of gasifying process gas itself just is higher than 0.2-0.4, adopts low WGR technology to exist material repeatedly to cool off processes such as intensification, and energy consumption is high, facility investment is big.
More than it seems, in the prior art, for the raw material technology coal gas of high-concentration carbon monoxide; Get into transformation system; The increase of the shift-converter load that causes and the transformation catalyst problems of excessive heat that is caused, disclosed technical scheme, also exist following not enough: 1. high WGR reduces bed temperature; Steam consumption is big, and energy consumption increases; 2. shift reaction product need be provided with the big interchanger of heat interchanging area in advance, has increased facility investment; 3. there is the danger that methanation reaction takes place in low WGR limited reactions heat release, and causes the sintering of catalyst fault, even causes reactor drum destructive serious consequence.
Summary of the invention
Technical problem to be solved by this invention provides and a kind ofly need not excessively improve the aqueous vapor ratio, and steam consumption is low; The pre-reactor interchanger need not be set, practice thrift facility investment; Avoid taking place the danger of methanation reaction; Can prevent effectively that the shift-converter bed temperature is too high, and the heat that shift-converter inner conversion reaction is produced the high concentration CO sulfur-resisting transformation system and the process method of being fully used.
The object of the invention can reach through following measure:
High concentration CO sulfur resistant conversion process of the present invention is characterized in that:
A. comprise at least that a preparatory shift-converter and a main transformer change reactor drum;
B. the raw material process gas has 15～40% of TV at least; At first getting into described in a in advance, shift-converter carries out preparatory transformationreation;, get into main transformer again and change reactor drum with after the raw material process gas that does not get into preparatory umformer is mixed through the process gas after the preparatory conversion, proceed transformationreation;
C. the preparatory processing condition of shift-converter:
Water/gas volume ratio 0.8～3.0
Dry gas air speed m
3/ h 1000～10000
Temperature in ℃ 220～320.
Because getting into main transformer changes in the process gas of reactor drum the butt of CO and forms and be lower than 50%; Main transformer changes reactor drum can be at general technology condition (dry gas air speed 2000～4000h-1; WGR 0.8～1.4) operation down, therefore, even shift-converter is operated under higher WGR in advance; The water vapour add-on that the entering main transformer changes reactor drum also can reduce, so total water steam add-on does not increase.
Because the tolerance that gets into preparatory shift-converter only accounts for the sub-fraction of gasifying process tolerance, has reduced reactor volume,, also can reduce the cost of reactor drum even adopt the reactor drum of higher material requirement.
Device breaks down when upstream and downstream, and the ratio that duty ratio gets into preparatory shift-converter when low tolerance accounts for the total tolerance of raw material process gas can be higher than 15-40%, does not even change the requirement that reactor drum just can reach the CO transformation efficiency through main transformer.
The object of the invention can also reach through following measure:
High concentration CO sulfur resistant conversion process of the present invention is characterized in that preparatory shift-converter is divided into upper and lower two sections described in a., and at the initial stage of putting into production, catalyst activity is high, and process gas is only through preparatory shift-converter hypomere; Production run is used preparatory shift-converter epimere series connection to the middle and later periods again.
High concentration CO sulfur resistant conversion process of the present invention; It is characterized in that 15～40% of the process gas of raw material described in b TV; At first getting into described in a in advance, shift-converter carries out preparatory transformationreation; Process gas after preparatory conversion and the raw material process gas that does not get into preparatory umformer get into main transformer again and change reactor drum after in pipeline, perhaps mixing in the mixing tank, proceed transformationreation.
High concentration CO sulfur resistant conversion process of the present invention; It is characterized in that 15～40% of the process gas of raw material described in b TV; Get at first described in a in advance that shift-converter carries out preparatory transformationreation, process gas after conversion in advance and the raw material process gas that do not get into preparatory umformer after regulating, are changed the reactor inlet pipeline at main transformer and are converged respectively; Get into main transformer together and change reactor drum, proceed transformationreation.
High concentration CO sulfur resistant conversion process of the present invention; It is characterized in that 15～40% of the process gas of raw material described in b TV, get at first described in a in advance that shift-converter carries out preparatory transformationreation, process gas after conversion in advance and the raw material process gas that does not get into preparatory umformer; Changing the reactor inlet pipeline at main transformer converges; And after adding suitable quantity of water adjusting WGR, get into main transformer together and change reactor drum, proceed transformationreation.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that main transformer described in a changes the reactor drum use of connecting with common shift-converter more than.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that described in the c processing condition of shift-converter in advance:
Water/gas volume ratio 1.0～1.6
Dry gas air speed m
3/ h 3000～10000
Temperature in 220～280.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that described in the c processing condition of shift-converter in advance:
Water/gas volume ratio 1.0～1.3
Dry gas air speed m
3/ h 4000～6000
Temperature in ℃ 220～280.
Be preparatory shift-converter when under the higher space velocity condition, operating, a preferred scheme.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that described in the c processing condition of shift-converter in advance:
Water/gas volume ratio 1.4～3.0
Dry gas air speed m
3/ h 1000～4000
Temperature in ℃ 240～280.
Preferably operation under higher WGR of shift-converter in advance like WGR 1.4～3.0, thereby is controlled at below 460～480 ℃ the temperature of bed bottom.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that described in the c processing condition of shift-converter in advance:
Water/gas volume ratio 1.6～2.5
Dry gas air speed m
3/ h 1000～4000
Temperature in 240～280.
Be the preferably operation under higher WGR of preparatory shift-converter, a preferred scheme.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that main transformer described in a changes the processing condition of reactor drum:
Water/gas volume ratio 0.8～1.6
Temperature in ℃ 240～280
Dry gas air speed m
3/ h 1000～5000.
High concentration CO sulfur resistant conversion process of the present invention; It is characterized in that said raw material process gas gets into before the preparatory shift-converter; At first the product with main reactor carries out heat exchange; Then, through purification the ash content remove wherein and other to the deleterious impurity of catalyzer after, get into high concentration CO sulfur-resisting transformation system again.
The process gas that gasification produces is at first carried out heat exchange with the product of main reactor; Temperature of charge is brought up to suitable with the temperature in of preparatory shift-converter; Get into cleaner then and remove ash content in the gasifying process gas, heavy metal etc., get into high concentration CO sulfur-resisting transformation system again the deleterious impurity of catalyzer.All is favourable for the lasting high reactivity that keeps catalyzer with the work-ing life of improving catalyzer.As shown in Figure 3.
High concentration CO sulfur resistant conversion process of the present invention; It is characterized in that said raw material process gas gets into before the preparatory shift-converter; At first the product with pre-reactor carries out heat exchange; Then, through purification the ash content remove wherein and other to the deleterious impurity of catalyzer after, get into high concentration CO sulfur-resisting transformation system again.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that process gas adopts one of following heat exchange process:
1.. main transformer changes reactor outlet process gas and the raw material process gas heat exchange that gets into preparatory shift-converter, will change the raw material process gas that reaction heat that reactor drum produces is passed to the entering system at main transformer;
2.. the process gas that gets into high concentration CO sulfur-resisting transformation system is at first carried out heat exchange, the reaction heat that absorption technique gas produces at preparatory shift-converter with preparatory shift-converter outlet process gas;
3.. the process gas that gets into high concentration CO sulfur-resisting transformation system is at first carried out heat exchange, the reaction heat that absorption technique gas produces at common shift-converter with common shift-converter outlet process gas;
4.. adopt waste heat boiler to utilize each shift-converter reaction liberated heat to produce steam, reduce material temperature simultaneously.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that preparatory shift-converter, main transformer change in the reactor drum, and the catalyzer that is adopted is one or both different catalyst.
High concentration CO sulfur resistant conversion process of the present invention is characterized in that preparatory shift-converter, main transformer change in the reactor drum, and the catalyzer that is adopted is sulfur-resistant transformation catalyst.
High concentration CO sulfur resistant conversion process of the present invention; Principle technical process when being specially adapted to downstream unit and being oxo process device (like methyl alcohol, dme, alkene, acetic acid production device); When downstream are the oxo process device, adopt the part process gas to regulate the CO content that gets in the lower procedure gas usually through mixing with gasifying process gas after the transformationreation.Shown in accompanying drawing 2.
High concentration CO sulfur-resisting transformation system of the present invention and process method, comparing prior art has following positively effect:
1. provide a kind of and need not excessively improve the aqueous vapor ratio, steam consumption is low; The pre-reactor interchanger need not be set, practice thrift facility investment; Avoid taking place the danger of methanation reaction; Can prevent effectively that the shift-converter bed temperature is too high, and the heat that shift-converter inner conversion reaction is produced the high concentration CO sulfur-resisting transformation system and the process method of being fully used.
2. few part of gasifying process gas (accounting for below 40% of gasifying process gas) gets into a preparatory shift-converter, under higher WGR, carries out transformationreation, prevents that effectively reactor batch temperature from crossing high a series of problem.
3. the high-temperature reaction product of shift-converter directly mixes or adds the laggard shift-converter of becoming owner of of suitable quantity of water adjusting WGR with the lower gasifying process gas of the temperature that does not get into preparatory shift-converter in advance; Need not adopt heat-exchange equipment, and make full use of the heat that pre-reactor inner conversion reaction is produced.
4. facility investment is low, requires flexibility strong to different process; Flexible and convenient operation has improved the throughput of equipment.
5. improve catalyst activity, prolonged catalyzer work-ing life, increased the life cycle of changing device.
6. save energy is protected environment.
Description of drawings
Accompanying drawing 1 is high concentration CO sulfur-resisting transformation system of the present invention and process method process flow diagram
Accompanying drawing 2 is downstream unit process flow diagrams when being oxo process device (like methyl alcohol, dme, alkene, acetic acid production device)
Accompanying drawing 3 is that the process gas that gasification produces is getting into the shift-converter process flow sheet synoptic diagram of process purifying treatment before
1. the process gas that gasification produces in the accompanying drawing 1 is divided into, 5. two bursts of logistics; 2. 1. the logistics that wherein accounts for raw material process gas 15～40% mix formed logistics with water vapour and 3. get into preparatory shift-converter; 5. 4. its reaction product mixed with remaining process gas and can directly be got into main transformer and change reactor drum; Also can 6. mix, get into main transformer again and change reactor drum with water vapour or liquid water.
Embodiment
The present invention below will combine embodiment further to detail:
Embodiment 1
Certain device adopts the Shell gasifying process, and the dry gas amount that produces process gas is 120000Nm3/h, requires to form≤1.6% through the butt of CO after the transformationreation.Adopt operational condition, the import and export composition of each reactor drum of technical process shown in the accompanying drawing 1 to see table 1.
Table 1, embodiment 1 each material condition
Embodiment 2
The dry gas amount of process gas that certain gasification installation produces is 39000kmol/h, and WGR is 1.25, require to form≤8.0% through the butt of CO after the transformationreation, with do not mix through all the other process gas of transformationreation after be used for oxo process.Technical process shown in the accompanying drawing 3 of employing the present invention design; WGR from gasification unit is 1.25 gasifying process gas; Be introduced into ash in the cleaner removing process gas impurity that grades after heating up with the heat exchange of main reactor product, be divided into two strands then, wherein account for need conversion dry gas amount be 1/3 one 2. 5. mix the back and get into preparatory shift-converter with water vapour; 3. 6. high-temperature reaction product mix with the gasifying process gas that does not advance preparatory shift-converter; Add an amount of liquid water more 8., play the effect of regulating temperature in and WGR simultaneously, 9. mixture flow gets into main reactor and carries out transformationreation.Composition, the condition of each burst logistics are seen table 2, and the operational condition of reactor drum is seen table 3.
Composition, the condition of table 2 embodiment 2 each logistics
The operational condition of table 3 embodiment 2 each reactor drum
| Processing condition | Pre-reactor | Main reactor |
| Inlet flow rate (butt, NM 3/h) | 129671 | 469427 |
| The inlet WGR, mol/mol | 1.81 | 1.11 |
| Temperature in, ℃ | 268 | 293 |
| Temperature out, ℃ | 472 | 442 |
| The catalyzer loading amount, m 3 | 33 | 124 |
| The dry gas air speed, h -1 | 3930 | 3785 |
| Advance preparatory exsiccation tolerance/dry gas total amount | 1/3 | / |
It is thus clear that, except two reactor drums wanting required for the present invention, only needing an interchanger, flow process is simple, has solved the problem of the easy overtemperature of high concentration CO conversion simultaneously.
The amount of gasifying process gas, composition and identical with embodiment 2 to requirement, technical process through the butt composition of CO after the transformationreation etc.Different with embodiment 2 is to get into the technology tolerance of preparatory shift-converter for needing 15% of conversion process tolerance.Composition, the condition of each burst logistics are seen table 4, and the operational condition of reactor drum is seen table 5.
Composition, the condition of table 4 embodiment 3 each burst logistics
The operational condition of table 5 embodiment 3 reactor drums
| Processing condition | Pre-reactor | Main reactor |
| Inlet flow rate (butt, NM 3/h) | 58352 | 424888 |
| The inlet WGR, mol/mol | 2.09 | 1.30 |
| Temperature in, ℃ | 272 | 236 |
| Temperature out, ℃ | 469 | 438 |
| The catalyzer loading amount, m 3 | 26 | 146 |
| The dry gas air speed, h -1 | 2250 | 2910 |
| Advance preparatory exsiccation tolerance/dry gas total amount | 0.15 | / |
The amount of gasifying process gas, composition and identical with embodiment 2 to requirement, technical process through the butt composition of CO after the transformationreation etc.Different with embodiment 2 is to get into the technology tolerance of preparatory shift-converter for needing 40% of conversion process tolerance.Composition, the condition of each burst logistics are seen table 6, and the operational condition of reactor drum is seen table 7.
Composition, the condition of table 6 embodiment 4 each burst logistics
The operational condition of table 7 embodiment 4 reactor drums
| Processing condition | Pre-reactor | Main reactor |
| Inlet flow rate (butt, NM 3/h) | 155606 | 485358 |
| The inlet WGR, mol/mol | 1.82 | 1.12 |
| Temperature in, ℃ | 272 | 284 |
| Temperature out, ℃ | 486 | 412 |
| The catalyzer loading amount, m 3 | 90 | 110 |
| The dry gas air speed, h -1 | 1730 | 4410 |
| Advance preparatory exsiccation tolerance/dry gas total amount | 0.40 | / |
Claims (8)
1. high concentration CO sulfur resistant conversion process is characterized in that:
A. comprise at least that a preparatory shift-converter and a main transformer change reactor drum; Said preparatory shift-converter is divided into upper and lower two sections, and at the initial stage of putting into production, catalyst activity is high, and process gas is only through preparatory shift-converter hypomere; Production run is used preparatory shift-converter epimere series connection to the middle and later periods again;
B. the raw material process gas has 15～40% of TV at least; At first getting into described in a in advance, shift-converter carries out preparatory transformationreation;, get into main transformer again and change reactor drum with after the raw material process gas that does not get into preparatory umformer is mixed through the process gas after the preparatory conversion, proceed transformationreation;
C. the preparatory processing condition of shift-converter:
Water/gas volume ratio 1.4～3.0
Dry gas air speed m
3/ h 1000～4000
Temperature in ℃ 240～280;
D. process gas adopts one of following heat exchange process:
1.. main transformer changes reactor outlet process gas and the raw material process gas heat exchange that gets into preparatory shift-converter, will change the raw material process gas that reaction heat that reactor drum produces is passed to the entering system at main transformer;
2.. the process gas that gets into high concentration CO sulfur-resisting transformation system is at first carried out heat exchange, the reaction heat that absorption technique gas produces at preparatory shift-converter with preparatory shift-converter outlet process gas;
3.. the process gas that gets into high concentration CO sulfur-resisting transformation system is at first carried out heat exchange, the reaction heat that absorption technique gas produces at common shift-converter with common shift-converter outlet process gas;
4.. adopt waste heat boiler to utilize each shift-converter reaction liberated heat to produce steam, reduce material temperature simultaneously.
2. according to the high concentration CO sulfur resistant conversion process of claim 1; It is characterized in that 15～40% of the process gas of raw material described in b TV, get at first described in a in advance that shift-converter carries out preparatory transformationreation, after the process gas after conversion in advance and the raw material process gas that does not get into preparatory umformer are perhaps mixed in the mixing tank in pipeline; Get into main transformer again and change reactor drum; Proceed transformationreation, perhaps the process gas after preparatory conversion and the raw material process gas that does not get into preparatory umformer after regulating, are changed the reactor inlet pipeline at main transformer and are converged respectively; Get into main transformer together and change reactor drum, proceed transformationreation.
3. according to the high concentration CO sulfur resistant conversion process of claim 1; It is characterized in that 15～40% of the process gas of raw material described in b TV, get at first described in a in advance that shift-converter carries out preparatory transformationreation, process gas after conversion in advance and the raw material process gas that does not get into preparatory umformer; Changing the reactor inlet pipeline at main transformer converges; And after adding suitable quantity of water adjusting WGR, get into main transformer together and change reactor drum, proceed transformationreation.
4. according to the high concentration CO sulfur resistant conversion process of claim 1, it is characterized in that main transformer described in a changes the reactor drum use of connecting with common shift-converter more than.
5. according to the high concentration CO sulfur resistant conversion process of claim 1; It is characterized in that said raw material process gas gets into before the preparatory shift-converter; At first the product with main reactor carries out heat exchange; Then, through purification the ash content remove wherein and other to the deleterious impurity of catalyzer after, get into high concentration CO sulfur-resisting transformation system again.
6. according to the high concentration CO sulfur resistant conversion process of claim 1; It is characterized in that said raw material process gas gets into before the preparatory shift-converter; At first the product with pre-reactor carries out heat exchange; Then, through purification the ash content remove wherein and other to the deleterious impurity of catalyzer after, get into high concentration CO sulfur-resisting transformation system again.
7. according to the high concentration CO sulfur resistant conversion process of claim 1, it is characterized in that preparatory shift-converter, main transformer change in the reactor drum, the catalyzer that is adopted is one or both different catalyst.
8. according to the high concentration CO sulfur resistant conversion process of claim 1, it is characterized in that preparatory shift-converter, main transformer change in the reactor drum, the catalyzer that is adopted is sulfur-resistant transformation catalyst.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010102958888A CN101955153B (en) | 2010-09-28 | 2010-09-28 | Process for converting high-concentration CO-tolerant sulfur |
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|---|---|---|---|
| CN2010102958888A CN101955153B (en) | 2010-09-28 | 2010-09-28 | Process for converting high-concentration CO-tolerant sulfur |
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| Publication Number | Publication Date |
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| CN101955153A CN101955153A (en) | 2011-01-26 |
| CN101955153B true CN101955153B (en) | 2012-09-05 |
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| GB201119957D0 (en) | 2011-11-18 | 2012-01-04 | Johnson Matthey Plc | Process |
| GB201119960D0 (en) * | 2011-11-18 | 2012-01-04 | Johnson Matthey Plc | Process |
| CN103508416B (en) * | 2012-06-27 | 2015-05-20 | 中国石油化工股份有限公司 | CO (Carbonic Oxide) sulfur-tolerant shift catalytic reaction process |
| CN102784669B (en) * | 2012-08-17 | 2014-04-09 | 中国石油化工集团公司 | Individual activating process for catalysts in converting furnaces of CO (carbon oxide) sulfur-resistant converting device |
| CN103449364B (en) * | 2012-11-12 | 2015-09-30 | 山东齐鲁科力化工研究院有限公司 | A kind of process for converting high-concentration CO-tolerant sulfur and device making full use of reaction heat |
| CN104152187B (en) * | 2014-08-06 | 2016-02-17 | 中石化宁波工程有限公司 | A kind of can the CO conversion process in extending catalyst work-ing life |
| CN107176591A (en) * | 2017-06-26 | 2017-09-19 | 北京清创晋华科技有限公司 | A kind of transformation system and method without gas preheater |
| CN110894061B (en) * | 2018-09-12 | 2021-11-05 | 中国石化工程建设有限公司 | Sulfur-tolerant shift method and device for multi-stage adjustment of water-gas ratio |
| CN112195041B (en) * | 2020-10-23 | 2021-07-06 | 中国石油化工股份有限公司 | Coal water slurry purification pre-transformation furnace |
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| CN1830756A (en) * | 2006-03-16 | 2006-09-13 | 五环科技股份有限公司 | Secondary transformation technological method of high concentration carbon monooxide |
| CN101157442A (en) * | 2007-04-27 | 2008-04-09 | 中国石化集团宁波工程有限公司 | Waste heat reclaiming process for CO transformation |
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| CN1830756A (en) * | 2006-03-16 | 2006-09-13 | 五环科技股份有限公司 | Secondary transformation technological method of high concentration carbon monooxide |
| CN101157442A (en) * | 2007-04-27 | 2008-04-09 | 中国石化集团宁波工程有限公司 | Waste heat reclaiming process for CO transformation |
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