CN104591084B - The method and system that a kind of carbon monoxide either shallow converts - Google Patents
The method and system that a kind of carbon monoxide either shallow converts Download PDFInfo
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- CN104591084B CN104591084B CN201410837337.8A CN201410837337A CN104591084B CN 104591084 B CN104591084 B CN 104591084B CN 201410837337 A CN201410837337 A CN 201410837337A CN 104591084 B CN104591084 B CN 104591084B
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Abstract
The invention discloses the method and system that a kind of carbon monoxide either shallow converts, water gas is introduced preposition waste heat boiler, absorb sensible heat and latent heat, reduce the WGR in water gas；Separating condensed water, process condensate water goes to island of gasifying；Water gas is heated；Water gas is carried out detoxification reaction；Water Sproading reaction heat is used in water gas enters water shifting heat change furnace after detoxification；Deaerated water is used to reclaim the sensible heat in conversion gas and latent heat；Desalted water continues to reclaim the sensible heat in previous step conversion gas and latent heat, separating technology condensed water；Ammonia in demineralized water washing changer；Low-pressure steam is used to be flashed off by the gas in process condensate water；Tail gas goes torch burning, process condensate water to go to island of gasifying.Guarantee not use under recirculated cooling water premise, conversion gas outlet temperature≤40 DEG C；The present invention's is practical, can meet all unstripped gas conversion process, both may be used for grassroot project, it is also possible to for old plant modification.
Description
Technical field
The present invention relates to the technology of a kind of unstripped gas CO conversion, the side that a kind of carbon monoxide either shallow converts
Method and system.
Background technology
The unstripped gas CO that has in Coal Chemical Industry, gas chemical industry, coal bed gas chemical industry, biogas chemical industry needs to change, especially
It is the high aqueous vapor that the pressurization coal continuous gasification furnaces such as coal gasification, coal water slurry gasification, GSP, multiinjector, shell (shell) produce
The high CO of ratio, needs at catalyst (catalyst type has Fe-series catalyst, cobalt-molybdenum series catalyst, copper-zinc system catalyst) existence condition
Under, possess suitable temperature and pressure, make CO and H2O generates CO2And H2Reach CO and be converted into H2Purpose, its reaction equation
For:
Existing change furnace is adiabatic reaction, arranges indirect heat exchange equipment to reclaim conversion gas after taking reactor
Sensible heat and latent heat；The rank reclaiming heat is more, and special low grade heat energy is more；
One section of adiabatic change furnace loaded catalyst difficulty determines: limited by activity coefficient (TF): TF is an experience
Value, needs the data after reality application to go to check.When selecting " one section of adiabatic change furnace " catalyst amount, if TF choosing is big, urge
Agent consumption is the fewest, and " one section of adiabatic change furnace " conversion ratio does not just reach requirement, brings load increase, system to postorder change furnace
Between energy recovery and design load, deviation is the biggest；If TF is little, " one section of adiabatic change furnace " catalyst amount is the most, and " one section absolutely
Thermal conversion stove " occur as soon as overtemperature (probably occurring that phenomenon burnt by catalyst), bring therewith is that methanation side reaction increases,
And bring the biggest potential safety hazard to system operation；
Coal liquifaction, ammonia from coal, olefin hydrocarbon making by coal, coal system (ring) alkane, natural gas from coal, coal-ethylene glycol, coal formic acid
Still use the operation energy consumption height of " conversion+non-shifting " etc. the converting means of large-scale coal chemical engineering equipment, sewage discharge is many, cool down water
The defects such as consumption is big, operation easier is big；
Conversion series is many, and it is the most that low-temp methanol washes series, and operation easier is big, construction investment is big to cause low-temp methanol to wash
Defect；
Conversion low grade heat energy is many, overall operation cannot thermal balance, a large amount of heat energy need to consume a lot of cooling water cooling and arrive
Less than 40 DEG C, cause low-grade heat to reclaim, cool down the defect that water consumption is high
The most existing adiabatic change furnace technique there is also following defect: equipment is many, process route length, construction investment big, be
System resistance point big, dew point corrosion is many, operation energy consumption is high, catalyst is short for service life.
Summary of the invention
It is an object of the invention to overcome the deficiencies in the prior art, it is provided that a kind of carbon monoxide either shallow convert method and
System, it is achieved efficient absorption and the heat recovery to water gas.
The present invention is achieved by the following technical solutions, the method that the present invention a kind of carbon monoxide either shallow converts, including
Following steps:
(1) water gas is introduced preposition waste heat boiler, absorb sensible heat and latent heat, reduce the WGR in water gas；
(2) separating condensed water, process condensate water goes to island of gasifying；
(3) water gas is heated；
(4) water gas is carried out detoxification reaction；
(5) after detoxification, part CO is converted into H in entering water shifting heat change furnace by water gas2, CO, part organic sulfur conversion is
Inorganic sulfur, by-product 2.0～10.0MPa saturated vapor, use Water Sproading reaction heat；
(6) sensible heat in the conversion gas of deaerated water recycling step (3) and latent heat are used；
(7) desalted water continues to reclaim the sensible heat in previous step conversion gas and latent heat, and demineralized water heats >=104 DEG C, conversion gas
≤40℃；
(8) separating technology condensed water；
(9) ammonia in demineralized water washing changer；
(10) low-pressure steam is used to be flashed off by the gas in process condensate water；
(11) tail gas goes torch burning, process condensate water to go to island of gasifying.
In described step (1), by-product 0.3～1.6MPa saturated vapor, original 0.7～1.6 WGR V in water gasH20/
VButt coal gasIt is down to 0.2～0.6.
Before described water gas carries out detoxification reaction, temperature >=TWater gas dew point temperature+30℃。
The system that a kind of carbon monoxide either shallow converts, including two-way, wherein a road includes the preposition waste heat boiler being sequentially connected with
Stove, gas-liquid separator, gas-gas heat exchanger, deaerated water heater, desalted water heater, cooler and Ammonic washing tower, also include detoxification
Groove and water shifting heat change furnace, gas-gas heat exchanger, detoxification groove and water shifting heat change furnace be sequentially connected, and the air-flow of water shifting heat change furnace goes out
Mouth is back to gas-gas heat exchanger；Another road includes hybrid heater, flash column, water cooler and flashed vapour separator, Ammonic washing tower, mixed
Closing heater and flash column to be sequentially connected, the air stream outlet of flash column returns to hybrid heater, another of hybrid heater
Outlet, water cooler and flashed vapour separator are sequentially connected with.
Before water gas enters transformation system, the sensible heat in preposition waste heat boiler recycle-water coal gas and latent heat, by-product are set
0.3～1.6MPa saturated vapor, makes original 0.7～1.6 WGR (V in water gasH20/VButt coal gas) it is down to 0.2～0.6, effectively
Reducing the invalid material into transformation system, whole system heat recovery moves forward, it is ensured that conversion gas cooling water consumption is " zero "；
The upper strata of described detoxification groove arranges adsorbent, and a small amount of cobalt-molybdenum series catalyst, unstripped gas load in the lower floor of detoxification groove
Middle part CO and H2O reaction is converted into H2And CO2, water gas temperature rises to 190～280 DEG C, and detoxification groove is two alternately to be made
With.
Described water gas drops to less than 40 DEG C by deaerated water heater and desalted water heater conversion gas temperature.
Described cooler is water-cooled cooler, vapotron or air cooler.
Cleaning mixture and condensed fluid are entered flash column after flashed vapour heat exchange by described hybrid heater, complete in flash column
Flash distillation, flash off gas through heater, water cooler cooling after, flashed vapour separator separate after send to torch, condensed fluid
Being transported to gasification process recycle, the liquid of flash column bottom delivers to island recycling of gasifying.
Described water shifting heat change furnace is full radial structure, filling cobalt-molybdenum series catalyst bed, cobalt molybdenum in water shifting heat change furnace
Shifting hot-water line unit is set in series catalysts bed.
The present invention has the advantage that the present invention arranged one before water gas does not enters whole system compared to existing technology
Sensible heat in platform preposition waste heat boiler recycle-water coal gas and latent heat, by-product 0.3～1.6MPa saturated vapor, make in water gas original
0.7～1.6 WGR (VH20/VButt coal gas) it is down to 0.2～0.6, effectively reduce the invalid material into transformation system；Detoxification groove designs
It is two, is used alternatingly, not only the poisonous substance in absorption water gas, simultaneously to when driving every time, urged by the internal filling of detoxification groove
The catalytic action of agent makes saturation water in water gas be changed into superheated steam, causes follow-up due to saturated vapor when stopping to drive
" dew point corrosion " of equipment, it is ensured that change furnace catalyst service life >=8 year；Bury inside the beds of water shifting heat change furnace
There are the heat exchanger tube of water shifting heat, water shifting heat change furnace reaction heat and detoxification groove reaction heat all by being embedded in the catalysis of water shifting heat change furnace
Agent bed inner water tube removes, and by-product 2.0～10.0MPa saturated vapor, owing to the reaction heat of water shifting heat change furnace is internal
Water pipe is removed in time, and change furnace outlet temperature is easy to control, and catalyst can fill more；The furnace temperature of water shifting heat change furnace beds
Regulated by change furnace byproduct steam pressure, it is ensured that regulation aspect is flexible, easy to control；When also ensuring that driving simultaneously, take to
The natural water circulation system of water shifting heat change furnace adds steam, change furnace temperature rise is got up rapidly, to shorten the driving time；Water moves
Natural Circulation is taked in thermal conversion stove water route, and when stopping suddenly, the CO of change furnace internal residual part continues reaction, and water route remains on
Keep circulation, and beds internal heat is removed, it is ensured that the furnace temperature at unexpected dead ship condition change furnace also will not be too high；
Recycle-water moves thermal conversion outlet of still conversion gas sensible heat and latent heat uses deaerated water and desalted water to reclaim, it is ensured that do not use circulating cooling
Under water premise, conversion gas outlet temperature≤40 DEG C；The present invention's is practical, can meet all unstripped gas conversion process, both
May be used for grassroot project, it is also possible to for old plant modification.
Accompanying drawing explanation
Fig. 1 is the structural representation of the present invention；
Fig. 2 is the process flow diagram of the present invention；
Fig. 3 is the structural representation of water shifting heat change furnace.
Detailed description of the invention
Elaborating embodiments of the invention below, the present embodiment is carried out under premised on technical solution of the present invention
Implement, give detailed embodiment and concrete operating process, but protection scope of the present invention is not limited to following enforcement
Example.
Embodiment 1
As depicted in figs. 1 and 2, the system that a kind of carbon monoxide either shallow converts, including two-way, wherein a road includes connecting successively
The preposition waste heat boiler 1 that connects, gas-liquid separator 2, gas-gas heat exchanger 3, deaerated water heater 7, desalted water heater 8, cooler 9
With Ammonic washing tower 11, also include that detoxification groove 4 and water shifting heat change furnace 5, gas-gas heat exchanger 3, detoxification groove 4 and water shifting heat change furnace 5 depend on
Secondary connected, the air stream outlet of water shifting heat change furnace 5 is back to gas-gas heat exchanger 3；Another road includes hybrid heater 10, flash column
12, water cooler 13 and flashed vapour separator 15, Ammonic washing tower 11, hybrid heater 10 and flash column 12 be sequentially connected, flash column 12
Air stream outlet return to hybrid heater 10, another outlet, water cooler 13 and flashed vapour separator of hybrid heater 10
15 are sequentially connected with.Also set up drum 6 for collecting heat simultaneously, flash liquid delivery pump 14 is set for carrying flash liquid, arranges
Condensed fluid delivery pump 16 is for transport of condensate.
In Fig. 1, A is low-pressure steam, and B is mesohigh steam, and C is tedge, and D is down-comer, and E is filling pipe, and F is deoxygenation
Water sends pipe outside, and G is that desalted water sends pipe, H washing pipe outside, and I is conversion trachea, and J is rough coal trachea, and K is low pressure water inlet pipe, and L is
Condensate line, M is high-pressure intake pipe, N desalted water upper hose, and O is to live steam pipe, P flash distillation trachea.
The present embodiment comprises the following steps:
(1) water gas is introduced preposition waste heat boiler 1, absorb sensible heat and latent heat, reduce the WGR in water gas；
(2) separating condensed water, process condensate water goes to island of gasifying；
(3) water gas is heated；
(4) water gas is carried out detoxification reaction；
(5) after detoxification, part CO is converted into H in entering water shifting heat change furnace 5 by water gas2, CO, part organic sulfur conversion
For inorganic sulfur, by-product 2.0～10.0MPa saturated vapor, use Water Sproading reaction heat；Guarantee beds not overtemperature, Wu Jia
Alkanisation side reaction；
(6) sensible heat in the conversion gas of deaerated water recycling step (3) and latent heat are used；
(7) desalted water continues to reclaim the sensible heat in previous step conversion gas and latent heat, and demineralized water heats >=104 DEG C, conversion gas
≤40℃；
(8) separating technology condensed water；
(9) ammonia in demineralized water washing changer；
(10) low-pressure steam is used to be flashed off by the gas in process condensate water；
(11) tail gas goes torch burning, process condensate water to go to island of gasifying.
Filling magnesia-alumina spinel structure detoxifying agent hereinafter referred to as detoxifying agent+pre-change catalyzer of cobalt molybdenum system in detoxification groove 4；Water coal
Gas sensible heat in preposition waste heat boiler 1 recycle-water coal gas and latent heat, by-product 0.3～1.6MPa saturated vapor, make in water gas
Original 0.7～1.6 WGR (VH20/VButt coal gas) it is down to 0.2～0.6, in water gas, a large amount of water are liquid phase by gas phase conversion, effectively
Reduce the invalid material into transformation system；In gas-liquid separator 2, by machinery means by water gas at preposition waste heat boiler 1
Dust and the harmful substance carried secretly in the water condensed out and condensed water separate, and high-temperature condensation water are directly sent to gas simultaneously
Change island；Water gas in gas-gas heat exchanger 3 by exporting high temperature shift gas heat exchange with water shifting heat change furnace 5, it is ensured that enter detoxification groove 4
Water gas temperature >=TWater gas dew point temperature+ 30 DEG C, protection detoxifying agent and cobaltmolybdate catalyst；The heavy metal oxidation contained in water gas
Thing, dust and other to catalyst harmful substance by detoxification groove 4 upper strata sorbent；The cobalt that the filling of detoxification groove 4 lower floor is a small amount of
Molybdenum series catalyst is by part CO in unstripped gas and H2O reaction is converted into H2And CO2(CO+H2O→H2+CO2+QHeat release), water gas temperature
Rising to 190～280 DEG C, detoxification groove 4 is used alternatingly for A, B two, it is ensured that the catalyst of water shifting heat change furnace 5 is transported steadily in the long term
OK.
Water gas only completes part CO in one-level water shifting heat change furnace 5 and is converted into H2、CO2(CO+H2O→H2+CO2+
QHeat release), organic sulfur conversion be inorganic sulfur, reaction heat be embedded in beds move water in heat pipe bundle absorb by-product produce 0.5～
The saturated vapor of 10.0MPa, water route is Natural Circulation, flashes off 2.0～10.0MPa steam and send outside in drum 6, and product converts
H in gas2Arbitrarily regulate in/CO=1.0～5.0, organic transformation rate ＞ 98%；
Just can be accomplished by deaerated water heater 7 and the sensible heat of desalted water heater 8 two-stage recovery conversion gas and latent heat
Conversion gas temperature drops to less than 40 DEG C, it is not necessary to arrange water recirculator 9 again；The deoxygenation soft water of heating supplies drum 6 and sends outside
Other operation uses, and desalted water is heated to 104 DEG C by room temperature and is directly sent to system for deoxidizing by heat power；
The cooler 9 of the present embodiment is vapotron, and cooler 9 device drives to use, without putting into time properly functioning
Running, conversion gas can take a shorter way, it is achieved cools down water consumption when converting properly functioning for " zero "；
Gas completes washing, purifying at Ammonic washing tower 11, and after purification, gas removes subsequent processing.Cleaning mixture and condensed fluid are through overmulling
Close heater 10 and enter flash column 12 after flashed vapour heat exchange, in flash column 12, complete flash distillation, flash off gas through overmulling
After closing heater 10, water cooler 13 cooling, sending to torch after flashed vapour separator 15 separates, condensed fluid carries through flash liquid
Pump 14 is transported to gasification process and recycles, and flash column 12 lower liquid delivers to, through subcooling condensate delivery pump 16, the island recovery profit that gasifies
With, it is achieved transformation system sewage discharge is " zero "；
As it is shown on figure 3, water shifting heat change furnace 5 is the transformation task that one-level just completes CO；Water shifting heat change furnace 5 be overall diameter to
Structure, arranges the shifting hot-water line unit being easy to lifting in cobalt-molybdenum series catalyst bed；Remove the water of water shifting heat change furnace 5 reaction heat
For Natural Circulation, and parse saturated vapor in drum 6；
Water shifting heat change furnace 5 includes pressure-bearing shell 51 and the catalyst frame 52 being arranged in pressure-bearing shell 51 and moves heat pipe bundle
53；Described shifting heat pipe bundle 53 includes water inlet pipe 531, outlet pipe 532, water inlet distributor box 533, aqueduct 534, caecum pipe 535, ring
Pipe 536, exit branch 537 and header tank 538；Water inlet pipe 531 connects water inlet distributor box 533, water inlet distributor box 533 and aqueduct
534 connect, and described caecum pipe 535 includes the supervisor 5351 being positioned at center and multiple auxiliary pipe arranged along supervisor 5351 surrounding
5352, the open top of described supervisor 5351, bottom lock, the two ends of auxiliary pipe 5352 are respectively communicated with top and the end of supervisor 5351
Portion, aqueduct 534 enters from the top of supervisor 5351 and is set in supervisor 5351, the top connection endless tube 536 of supervisor 5351,
Endless tube 536 is by exit branch 537 connected set water tank 538, and header tank 538 is connected with outlet pipe 532, and caecum pipe 535 is arranged at
In catalyst frame 52.
Pressure-bearing shell 51 includes upper cover 511, low head 512, cylinder 513, supports seat 514；Described upper cover 511 and cylinder
Body 513 is connected by flange 5111, and low head 512 and cylinder 513 are one-body molded, and the inwall of cylinder 513 is fixedly installed for propping up
Support catalyst frame 52 and the support seat 514 of shifting heat pipe bundle 53, described upper cover 511 is respectively arranged to connect water inlet pipe 531
Water inlet 516, for connecting the outlet 517 of outlet pipe 532 and for the air inlet 515 of air inlet, on described low head 512
It is respectively provided with the self-unloading mouth 518 of catalyst discharging and for the gas outlet 519 given vent to anger.
Catalyst frame 52 includes sealing plate 521, support beam 522, gas distributor 523, gas collecting jar with ground-on cover plate 524；Described sealing plate
521 tops being arranged at gas distributor 523 form frame structure, the bottom of gas distributor 523 and low head 512 and seal even
Connecing, water inlet pipe 531 and outlet pipe 532 are each passed through sealing plate 521 and are connected to water inlet 516 and outlet 517, the gas collection of correspondence
Cylinder 524 is supporting along the central authorities being radially arranged in gas distributor 523 of gas distributor 523, the top braces of gas collecting jar with ground-on cover plate 524
On beam 522, the connection gas outlet, bottom 519 of gas collecting jar with ground-on cover plate 524, support beam 522 supports gas collecting jar with ground-on cover plate 524, endless tube 536 and gas respectively
Distributor 523, the two supports of support beam 522 is supporting on seat, gas distributor 523 and cylinder 513 gap shape radially
Becoming gas distributing chamber, caecum pipe 535 is positioned at gas distributor 523, loading catalyst in gas distributor 523.
Gas distributor 523 and gas collecting jar with ground-on cover plate 524 is radially even offers multiple passage.The bottom of gas distributor 523
Seal disc 526 and black box 527 are set, between bottom and the low head 512 of gas distributor 523 by seal disc 526 even
Connecing, described black box 527 is arranged between the bottom of seal disc 526 and gas distributor 523.Figure hollow core arrow is current
Direction, filled arrows is airflow direction.
Normal driving uses steam supply thermal source.Driving steam heating water moves the natural cycle system of thermal conversion stove 5, passes through
Beds is preheated by the circulation of water, and catalyst also reaches light-off temperature, it is not necessary to additionally arrange electric heater supply thermal source；
The present embodiment is that certain Chemical Group designs with powdered coal pressuring gasified 1,000,000 tons of methanol/annual transform device, refers specifically to
Mark is as shown in table 1.Table understands investment estimate at least halve.
The technique of table 1 embodiment 1 contrasts catalog with con-ventional insulation conversion process main technique index
| Technical parameter | The technique of the present embodiment | Traditional handicraft (two-stage nitration is adiabatic) |
| 2.5～4.0MPaG saturated vapors | 91t/h | 90t/h |
| 0.5～0.8MpaG saturated vapor | 110t/h | 50t/h |
| Synthesizing methanol deaerated water | 151t/h (180 degree) | 151t/h (150 degree) |
| Heat 25 degree of desalted waters | 356t/h | 291t/h |
| Consume recirculated cooling water | No-cooling-water consumes | 5700t/h |
| SR | 0.05MPA | 0.4MPA |
| The total number of units of equipment (containing auxiliary equipment) | 16 | 26 |
| Unstripped gas is through number of devices | 9 | 12 |
| The heat transmission equipment of dew point corrosion | 3 | 8 |
| System maximum temperature point | 280 degree | 420 degree |
| Band by-pass regulation equipment | 1 | 4 |
| Investment estimate | “0.5” | “1” |
Embodiment 2
The present embodiment is certain Chemical Group design 900,000 tons of methanol/annual transform device with water coal slurry pressure gasification, other
Embodiment is same as in Example 1.Specific targets are as shown in table 2.Table understands investment estimate at least halve.
The technique of table 2 embodiment 2 contrasts catalog with con-ventional insulation conversion process main technique index
Claims (9)
1. the system that a carbon monoxide either shallow converts, it is characterised in that include two-way, before wherein a road includes being sequentially connected with
Put waste heat boiler (1), gas-liquid separator (2), gas-gas heat exchanger (3), deaerated water heater (7), desalted water heater (8), cold
But device (9) and Ammonic washing tower (11), also includes detoxification groove (4) and water shifting heat change furnace (5), gas-gas heat exchanger (3), detoxification groove (4)
Being sequentially connected with water shifting heat change furnace (5), the air stream outlet of described water shifting heat change furnace (5) is back to gas-gas heat exchanger (3)；Separately
One tunnel includes hybrid heater (10), flash column (12), water cooler (13) and flashed vapour separator (15), described Ammonic washing tower
(11), hybrid heater (10) and flash column (12) be sequentially connected, the air stream outlet of described flash column (12) returns to mixing and adds
Hot device (10), another outlet, water cooler (13) and the flashed vapour separator (15) of described hybrid heater (10) are sequentially connected with.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described detoxification groove (4)
Upper strata adsorbent is set, the cobalt-molybdenum series catalyst that the filling of the lower floor of detoxification groove (4) is a small amount of, part CO and H in unstripped gas2O is anti-
H should be converted into2And CO2, water gas temperature rises to 190～280 DEG C, and detoxification groove (4) is two and is used alternatingly.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described water gas passes through
Deaerated water heater (7) and desalted water heater (8) conversion gas temperature drop to less than 40 DEG C.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described cooler (9)
For water-cooled cooler, vapotron or air cooler.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described hybrid heater
(10) cleaning mixture and condensed fluid are entered flash column (12) after flashed vapour heat exchange, in flash column (12), complete flash distillation, flash distillation
Out gas is after heater, water cooler (13) cooling, sends to torch, condensed fluid quilt after flashed vapour separator (15) separates
Being transported to gasification process recycle, the liquid of flash column (12) bottom delivers to island recycling of gasifying.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described water shifting heat converts
Stove (5) is full radial structure, and in water shifting heat change furnace (5), filling cobalt-molybdenum series catalyst bed, sets in cobalt-molybdenum series catalyst bed
Put shifting hot-water line unit.
The system that a kind of carbon monoxide either shallow the most according to claim 1 converts, it is characterised in that described system carries out one
The method that carbonoxide either shallow converts comprises the following steps:
(1) water gas is introduced preposition waste heat boiler (1), absorb sensible heat and latent heat, reduce the WGR in water gas；
(2) separating condensed water, process condensate water goes to island of gasifying；
(3) water gas is heated；
(4) water gas is carried out detoxification reaction；
(5) after detoxification, part CO is converted into H in entering water shifting heat change furnace (5) by water gas2, CO, part organic sulfur conversion is nothing
Machine sulfur, by-product 2.0～10.0MPa saturated vapor, use Water Sproading reaction heat；
(6) sensible heat in the conversion gas of deaerated water recycling step (3) and latent heat are used；
(7) desalted water continues to reclaim the sensible heat in previous step conversion gas and latent heat, and demineralized water heats >=104 DEG C, conversion gas≤40
℃；
(8) separating technology condensed water；
(9) ammonia in demineralized water washing changer；
(10) low-pressure steam is used to be flashed off by the gas in process condensate water；
(11) tail gas goes torch burning, process condensate water to go to island of gasifying.
The system that a kind of carbon monoxide either shallow the most according to claim 7 converts, it is characterised in that in described step (1),
By-product 0.3～1.6MPa saturated vapor, original 0.7～1.6 WGR V in water gasH20/VButt coal gasIt is down to 0.2～0.6.
The system that a kind of carbon monoxide either shallow the most according to claim 7 converts, it is characterised in that described water gas is carried out
Before detoxification reaction, temperature >=TWater gas dew point temperature+30℃。
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| US5464606A (en) * | 1994-05-27 | 1995-11-07 | Ballard Power Systems Inc. | Two-stage water gas shift conversion method |
| CN202337769U (en) * | 2011-10-31 | 2012-07-18 | 神华集团有限责任公司 | Partially methanated water gas shift system |
| CN102701149B (en) * | 2012-06-07 | 2014-05-28 | 王揽月 | Water heat-transfer shift process for by-product high-grade steam energy-saving deep conversion |
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| CN104176705B (en) * | 2014-08-08 | 2016-05-25 | 山东齐鲁科力化工研究院有限公司 | A kind of sulfur resistant conversion process of producing synthesis gas |
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