CN105565269A - Device and method for making shifted gas for synthesis of ammonia synthesis poly-generation methanol - Google Patents

Device and method for making shifted gas for synthesis of ammonia synthesis poly-generation methanol Download PDF

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CN105565269A
CN105565269A CN201610087494.0A CN201610087494A CN105565269A CN 105565269 A CN105565269 A CN 105565269A CN 201610087494 A CN201610087494 A CN 201610087494A CN 105565269 A CN105565269 A CN 105565269A
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gas
washing tower
threeway
methanol
outlet
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CN105565269B (en
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刘伟
杨国洞
王洪营
吴培
张泽海
渠会丽
许世方
崔玉彪
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Jiangxi Xinlianxin Chemical Industry Co ltd
Xinjiang Xinlianxin Energy Chemical Co ltd
Henan Xinlianxin Chemicals Group Co Ltd
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Henan Xinlianxin Fertilizer Co Ltd
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • 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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/02—Processes for making hydrogen or synthesis gas
    • C01B2203/0283—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step
    • C01B2203/0288—Processes for making hydrogen or synthesis gas containing a CO-shift step, i.e. a water gas shift step containing two CO-shift steps
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/061—Methanol production
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/06—Integration with other chemical processes
    • C01B2203/068—Ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/16—Controlling the process
    • C01B2203/1642—Controlling the product
    • C01B2203/1671—Controlling the composition of the product

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  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Industrial Gases (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

The invention belongs to a device and method for making shifted gas for synthesis of ammonia synthesis poly-generation methanol. The device comprises a mechanical part and a control part. The mechanical part comprises a gasification washing tower, an outlet of the gasification washing tower is connected with an inlet of a second heat and condensate recycling unit through a pipe, the pipe between the outlet of the gasification washing tower and the second heat and condensate recycling unit is sequentially provided with a fifth tee joint, a first self-regulating valve, a first tee joint and a second tee joint, an outlet of the second heat and condensate recycling unit is connected with an inlet in the middle of a second ammonia-washing tower, and a gas phase outlet in the top of the second ammonia-washing tower is connected with an inlet in the lower portion of a shifted gas washing tower for synthesis of methanol through a pipe; the control part comprises a first online analysis and calculation display instrument, a second online analysis and calculation display instrument, a second self-regulating valve and a third self-regulating valve. The device and method have the advantages that matching efficiency and accuracy are high, a great number of regulating means are adopted, a great amount of high-quality steam is generated, and meanwhile the content of COS in the methanol removing and washing shifted gas is lowered.

Description

The device for making of ammonia synthesis Poly-generation methanol-fueled CLC conversion gas and preparation method
Technical field
The invention belongs to Coal Chemical Industry production technical field, be specifically related to a kind of device for making and preparation method of ammonia synthesis Poly-generation methanol-fueled CLC conversion gas.
Background technology
The multi-joint device looking into methyl alcohol of current synthetic ammonia, when conversion section produces methanol-fueled CLC conversion gas, after generally adopting a certain amount of raw gas and the second shift converter, gas and vapor permeation is prepared and is met (H 2-CO 2)/(CO+CO 2the conversion gas of)=2.05 ~ 2.1.But this situation, because the second shift converter gas CO content is out low, required rough coal tolerance is just many, raw gas like this through the first shift converter will correspondingly reduce, the also corresponding minimizing of first shift converter high-temperature gas out, finally cause utilizing high-temperature gas change thermogenetic in press through hot steam amount and reduce.When the preferential electricity price of current national cancellation fertilizer industry, product high-quality steam is totally unfavorable to enterprise's reduction production cost less.Simultaneously because rough coal tolerance is more, the COS of this part gas owing to carrying without shift converter, the COS bringing methanol wash column into is just many, causes methanol wash column CO 2in gas product, COS exceeds standard, and it is passive to cause to urea production.
Summary of the invention
The object of the invention is to overcome defect of the prior art and provide one provide proportioning efficiency and precision high, produce middle pressure steam amount more, the device for making of the ammonia synthesis Poly-generation methanol-fueled CLC conversion gas simultaneously going methanol wash column conversion gas COS low and preparation method.
The object of the present invention is achieved like this: comprise mechanical part and control section, a, mechanical part comprises gasification water wash column, the outlet of gasification water wash column is connected with the second heat and the import of phlegma recovery unit by pipeline, the outlet of gasification water wash column and the pipeline between the second heat and phlegma recovery unit are provided with the 5th threeway successively, first self-adjusting valve, first threeway and the second threeway, second heat and the outlet of phlegma recovery unit are connected with the second Ammonic washing tower centre inlet, second Ammonic washing tower top gas phase outlet is connected with methanol-fueled CLC conversion gas washing tower lower inlet by pipeline, methanol-fueled CLC conversion gas washing tower top gaseous phase outlet is connected with methanol synthesizer, described 5th threeway the 3rd end is connected with gas-liquid separator, the outlet of gas-liquid separator bottom liquid phases is connected with the import of gasification water wash column by lime set pump, the outlet of gas-liquid separator top gas phase is connected with the import of feed preheater tube side, the outlet of feed preheater tube side is successively by the first shift converter, 3rd threeway, middle pressure steam superheater tube side, feed preheater shell side, middle pressure steam producer tube side, second shift converter, 4th threeway, first heat and phlegma recovery unit are connected with the import of the first Ammonic washing tower bottom, first Ammonic washing tower top gas phase outlet is connected with ammonia synthesis conversion gas washing tower lower inlet, ammonia synthesis conversion gas washing tower top gaseous phase outlet is connected with ammonia synthesizer by liquid nitrogen washing device, de-salted water pipeline is connected with middle pressure steam pipe network with middle pressure steam producer shell side, middle pressure steam superheater shell side by pipeline successively, 3rd end of described 3rd threeway is connected with the 3rd end of the first threeway by pipeline, and the 3rd end of the 4th threeway is connected with the 3rd end of the second threeway by pipeline, described second Ammonic washing tower bottom liquid phases outlet is connected with aftertreatment device respectively with the first Ammonic washing tower bottom liquid phases outlet, in the middle part of described second Ammonic washing tower, fluid inlet and fluid inlet in the middle part of the first Ammonic washing tower seal waterpipe be connected with gasifications respectively, the bottom liquid phases outlet of described ammonia synthesis conversion gas washing tower is connected with rich methanol liquid regenerating unit respectively with the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower, the middle part fluid inlet of described ammonia synthesis conversion gas washing tower is connected with poor methanol liquid pipeline respectively with the middle part fluid inlet of methanol-fueled CLC conversion gas washing tower, b, control section comprise the first on-line analysis be arranged between the first threeway and the second threeway on pipeline calculate display instrument, be arranged on pipeline that the second Ammonic washing tower top gas phase outlet and pipeline second on-line analysis between methanol-fueled CLC conversion gas washing tower lower inlet calculate between display instrument, the 3rd end of the 3rd threeway and the 3rd end of the first threeway on the second self-adjusting valve, the 3rd end of the 4th threeway installed be connected with the 3rd end of the second threeway between pipeline on the 3rd self-adjusting valve that arranges, described first on-line analysis calculates display instrument and is connected with the input terminus of controller respectively with the second on-line analysis calculating display instrument, and the output terminal of controller is connected with the second self-adjusting valve, the 3rd self-adjusting valve respectively.
Preferably, described second shift converter is adiabatic shift converter or controlledly moves one of thermal conversion stove.
Preferably, to comprise at least one cover interchanger respectively in series with at least a set of gas-liquid separator for described first heat and phlegma recovery unit and the second heat and phlegma recovery unit.
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator through the 3rd end of the 5th threeway, and another part is connected with the second heat and phlegma recovery unit with the second threeway through the 5th threeway, the first self-adjusting valve, the first threeway; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column by the outlet of gas-liquid separator bottom liquid phases, lime set pump and the import of gasification water wash column; Gas phase enters in the first shift converter by the outlet of gas-liquid separator top gas phase and feed preheater tube side; Described raw gas carries out the volume fraction of carbon monoxide after transformationreation in the first shift converter: 4.0 ~ 7.0%; Described raw gas in feed preheater tube side by heat exchange to 270 ~ 310 DEG C; Described raw gas, in the first shift converter, transformationreation occurs becomes conversion gas, and described conversion gas temperature is: 440 ~ 455 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway the saturation steam being 3.5 ~ 4.0Mpa with the pressure of coming in middle pressure steam producer shell side in middle pressure steam superheater tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 400 ~ 430 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater shell side enters in middle pressure steam pipe network;
Four, the conversion gas that temperature described in step 3 is reduced to 400 ~ 430 DEG C enters the raw gas entering feed preheater tube side in feed preheater shell side and step 2 and carries out heat exchange, and described conversion gas temperature is reduced to 370 ~ 400 DEG C;
Five, enter the second shift converter after the conversion gas that the temperature in step 4 is reduced to 370 ~ 400 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer shell side in middle pressure steam producer tube side and de-salted water pipeline and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer tube side enters in middle pressure steam superheater shell side; Described enter the second shift converter carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 0.4 ~ 1.7%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit becomes the gas that temperature is 20 ~ 40 DEG C after phlegma, and temperature is that the gas of 20 ~ 40 DEG C enters in the first Ammonic washing tower;
Seven, temperature described in step 6 is seal the normal temperature of waterpipe with gasification after the gas of 20 ~ 40 DEG C enters the first Ammonic washing tower, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in ammonia synthesis conversion gas washing tower, and contact with the poor methanol liquid entered in poor methanol liquid pipeline in ammonia synthesis conversion gas washing tower is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower enters into aftertreatment device by the first Ammonic washing tower bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device by ammonia synthesis conversion gas washing tower top gaseous phase outlet, and liquid nitrogen washing device removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower inner bottom part enters in rich methanol liquid regenerating unit by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower;
Nine, mixed gas is become after being mixed with the conversion gas of the 3rd end by the first shift converter, the 3rd threeway the 3rd end, the second self-adjusting valve and the first threeway by the raw gas of the 5th threeway and the first self-adjusting valve described in step one, above-mentioned mixed gas enters the second heat and phlegma recovery unit and reclaims phlegma in heat and gas and become the gas that temperature is 20 ~ 40 DEG C after mixing with the quadratic transformation gas of the 3rd end through the 3rd end of the second shift converter, the 4th threeway, the 3rd self-adjusting valve and the second threeway, temperature is that the gas of 20 ~ 40 DEG C enters in the second Ammonic washing tower;
Ten, temperature described in step 9 is seal the normal temperature of waterpipe with gasification after the gas of 20 ~ 40 DEG C enters the second Ammonic washing tower, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in methanol-fueled CLC conversion gas washing tower, and contact with the poor methanol liquid entered in poor methanol liquid pipeline in methanol-fueled CLC conversion gas washing tower is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower enters into aftertreatment device by the second Ammonic washing tower bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer, as the unstripped gas of methanol by methanol-fueled CLC conversion gas washing tower top gaseous phase outlet; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower inner bottom part enters in rich methanol liquid regenerating unit by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument Real-Time Monitoring first threeway and the second threeway (H in gas 2-CO 2)/(CO+CO 2) value, as this value display < 2.0 or > 2.15, first on-line analysis calculates display instrument by signal feedback to controller, signal transmission is given the second self-adjusting valve by controller, the corresponding increase of second self-adjusting valve aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument Real-Time Monitoring second Ammonic washing tower top gas phase with methanol-fueled CLC conversion gas washing tower lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when the display of this value is not between 2.05 ~ 2.1, the second on-line analysis calculates display instrument by signal feedback to controller, and signal transmission is given the 3rd self-adjusting valve by controller, the corresponding increase of 3rd self-adjusting valve aperture or reduction, until displayed value is 2.05 ~ 2.1.
The present invention is slightly joined first by one raw gas before one conversion gas after arranging the first shift converter and the first shift converter, and then with one conversion gas after the second shift converter and gas mixture before again essence join, ensure methanol-fueled CLC unstripped gas H 2-CO 2/ CO+CO 2=2.05 ~ 2.1, add ratio monitoring and varitrol simultaneously, ensure precision preparation and the efficiency of methanol-fueled CLC unstripped gas.Because thick dosage is large, smart dosage is little, and one section of product high-quality steam amount is many, simultaneously in methanol-fueled CLC unstripped gas, COS content is relatively low, there is proportioning efficiency and precision high, regulating measure is many, produce high-quality steam amount more, reduce the advantage of removing COS content in methanol wash column conversion gas simultaneously.
Accompanying drawing explanation
Fig. 1 is structural representation of the present invention;
Fig. 2 is control section structural representation of the present invention.
Embodiment
In order to there be understanding clearly to technical characteristic of the present invention, object and effect, now contrast accompanying drawing and the specific embodiment of the present invention is described, label identical in the various figures represents identical parts.For making simplified form, only schematically show and invent relevant part in each figure, they do not represent its practical structures as product.
As Fig. 1, shown in 2, the present invention includes mechanical part and control section, a, mechanical part comprises gasification water wash column 1, gasification water wash column 1 is exported and is connected with the second heat and phlegma recovery unit 22 import by pipeline, gasification water wash column 1 exports and pipeline between the second heat and phlegma recovery unit 22 is provided with the 5th threeway 25 successively, first self-adjusting valve 15, first threeway 20 and the second threeway 21, second heat and phlegma recovery unit 22 export and are connected with the second Ammonic washing tower 23 centre inlet, second Ammonic washing tower 23 top gas phase outlet is connected with methanol-fueled CLC conversion gas washing tower 24 lower inlet by pipeline, methanol-fueled CLC conversion gas washing tower 24 top gas phase outlet is connected with methanol synthesizer 34, described 5th threeway 25 the 3rd end is connected with gas-liquid separator 2, the outlet of gas-liquid separator 2 bottom liquid phases is connected with the import of gasification water wash column 1 by lime set pump 28, the outlet of gas-liquid separator 2 top gas phase is connected with the import of feed preheater 3 tube side, the outlet of feed preheater 3 tube side is successively by the first shift converter 4, 3rd threeway 18, middle pressure steam superheater 5 tube side, feed preheater 3 shell side, middle pressure steam producer 6 tube side, second shift converter 7, 4th threeway 19, first heat and phlegma recovery unit 8 are connected with the import of the first Ammonic washing tower 9 bottom, first Ammonic washing tower 9 top gas phase outlet is connected with ammonia synthesis conversion gas washing tower 10 lower inlet, ammonia synthesis conversion gas washing tower 10 top gas phase outlet is connected with ammonia synthesizer 29 by liquid nitrogen washing device 31, de-salted water pipeline 13 is connected with middle pressure steam pipe network 14 with middle pressure steam producer 6 shell side, middle pressure steam superheater 5 shell side by pipeline successively, 3rd end of described 3rd threeway 18 is connected with the 3rd end of the first threeway 20 by pipeline, and the 3rd end of the 4th threeway 19 is connected with the 3rd end of the second threeway 21 by pipeline, described second Ammonic washing tower 23 bottom liquid phases outlet is connected with aftertreatment device 12 respectively with the first Ammonic washing tower 9 bottom liquid phases outlet, in the middle part of described second Ammonic washing tower 23, fluid inlet and fluid inlet in the middle part of the first Ammonic washing tower 9 seal waterpipe 11 be connected with gasifications respectively, the bottom liquid phases outlet of described ammonia synthesis conversion gas washing tower 10 is connected with rich methanol liquid regenerating unit 33 respectively with the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24, the middle part fluid inlet of described ammonia synthesis conversion gas washing tower 10 is connected with poor methanol liquid pipeline 32 respectively with the middle part fluid inlet of methanol-fueled CLC conversion gas washing tower 24, b, control section comprises the first on-line analysis be arranged between the first threeway 20 and the second threeway 21 on pipeline and calculates display instrument 27, be arranged on pipeline second on-line analysis between the second Ammonic washing tower 23 top gas phase outlet and methanol-fueled CLC conversion gas washing tower 24 lower inlet and calculate display instrument 26, the second self-adjusting valve 16 that pipeline between 3rd end of the 3rd threeway 18 and the 3rd end of the first threeway 20 is installed, the 3rd self-adjusting valve 17 that pipeline between 3rd end of the 4th threeway 19 is connected with the 3rd end of the second threeway 21 is arranged, described first on-line analysis calculates display instrument 27 and is connected with the input terminus of controller 30 respectively with the second on-line analysis calculating display instrument 26, and the output terminal of controller 30 is connected with the second self-adjusting valve 16, the 3rd self-adjusting valve 17 respectively.
Described second shift converter 7 is for adiabatic shift converter or controlledly move one of thermal conversion stove.
Described first heat and phlegma recovery unit 8 and the second heat and phlegma recovery unit 22 in series by least one cover interchanger and at least a set of gas-liquid separator respectively.
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 4.0 ~ 7.0%; Described raw gas in feed preheater 3 tube side by heat exchange to 270 ~ 310 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 440 ~ 455 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 3.5 ~ 4.0Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 400 ~ 430 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 400 ~ 430 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 370 ~ 400 DEG C;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 370 ~ 400 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 0.4 ~ 1.7%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 20 ~ 40 DEG C after phlegma, temperature is that the gas of 20 ~ 40 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 20 ~ 40 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 20 ~ 40 DEG C, temperature is that the gas of 20 ~ 40 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 20 ~ 40 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, as this value display < 2.0 or > 2.15, first on-line analysis calculates display instrument 27 by signal feedback to controller 30, signal transmission is given the second self-adjusting valve 16 by controller 30, the second corresponding increase of self-adjusting valve 16 aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when the display of this value is not between 2.05 ~ 2.1, the second on-line analysis calculates display instrument 26 by signal feedback to controller 30, and signal transmission is given the 3rd self-adjusting valve 17 by controller 30, the 3rd corresponding increase of self-adjusting valve 17 aperture or reduction, until displayed value is 2.05 ~ 2.1.
First heat described in the present invention and phlegma recovery unit 8 and the second heat and phlegma recovery unit 22 in series by least one cover interchanger and at least a set of gas-liquid separator respectively.First heat and phlegma recovery unit 8 and the second heat and phlegma recovery unit 22 its objective is and to reclaim in conversion gas phlegma in heat and gas, make the gas temperature discharged be 20 ~ 40 DEG C.
In order to more detailed explanation the present invention, now the present invention is further elaborated in conjunction with the embodiments.Specific embodiment is as follows:
Embodiment one
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 4.0%; Described raw gas in feed preheater 3 tube side by heat exchange to 270 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 440 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 3.5Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 400 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 400 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 370;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 370 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 0.4%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 20 DEG C after phlegma, temperature is that the gas of 20 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 20 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 20 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 20 DEG C, temperature is that the gas of 20 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 20 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 20 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, when this value shows 1.8, first on-line analysis calculate display instrument 27 by signal feedback to controller 30, controller 30 by signal transmission give the second self-adjusting valve 16, the second corresponding increase of self-adjusting valve 16 aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as 2.0, second on-line analysis calculate display instrument 26 by signal feedback to controller 30, controller 30 by signal transmission give the 3rd self-adjusting valve the 17, three corresponding increase of self-adjusting valve 17 aperture or reduction, until displayed value is 2.05 ~ 2.1.
Embodiment two
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 7.0%; Described raw gas in feed preheater 3 tube side by heat exchange to 310 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 455 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 4.0Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 430 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 430 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 400 DEG C;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 400 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 1.7%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 40 DEG C after phlegma, temperature is that the gas of 40 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 40 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 40 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 40 DEG C, temperature is that the gas of 40 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 40 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 40 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, when this value shows 2.1, first on-line analysis calculate display instrument 27 by signal feedback to controller 30, controller 30 by signal transmission give the second self-adjusting valve 16, second self-adjusting valve 16 aperture constant;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as 2.3, second on-line analysis calculate display instrument 26 by signal feedback to controller 30, controller 30 by signal transmission give the 3rd self-adjusting valve the 17, three corresponding increase of self-adjusting valve 17 aperture or reduction, until displayed value is 2.05 ~ 2.1.
Embodiment three
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 5.5%; Described raw gas in feed preheater 3 tube side by heat exchange to 290 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 447.5 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 3.25Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 415 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 415 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 385 DEG C;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 385 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 1.05%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 30 DEG C after phlegma, temperature is that the gas of 30 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 30 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 30 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 30 DEG C, temperature is that the gas of 30 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 30 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 30 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as 2.2, first on-line analysis calculate display instrument 27 by signal feedback to controller 30, controller 30 by signal transmission give the second self-adjusting valve 16, the second corresponding increase of self-adjusting valve 16 aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as 2.07, second on-line analysis calculate display instrument 26 by signal feedback to controller 30, controller 30 by signal transmission give the 3rd self-adjusting valve the 17, three self-adjusting valve 17 aperture constant.
Embodiment four
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 5.5%; Described raw gas in feed preheater 3 tube side by heat exchange to 290 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 450 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 3.5Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 420 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 420 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 390 DEG C;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 390 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 1.5%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 25 DEG C after phlegma, temperature is that the gas of 25 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 25 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 25 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, COO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 40 DEG C, temperature is that the gas of 40 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 40 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 40 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, when this value shows 2.3, first on-line analysis calculate display instrument 27 by signal feedback to controller 30, controller 30 by signal transmission give the second self-adjusting valve 16, the second corresponding increase of self-adjusting valve 16 aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as between 2.25, the second on-line analysis calculates display instrument 26 by signal feedback to controller 30, and signal transmission is given the 3rd self-adjusting valve 17 by controller 30, the 3rd corresponding increase of self-adjusting valve 17 aperture or reduction, until displayed value is 2.05 ~ 2.1.
Embodiment five
A preparation method for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises the steps:
One, gasify water wash column 1 be divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator 2 through the 3rd end of the 5th threeway 25, and another part is connected with the second heat and phlegma recovery unit 22 with the second threeway 21 through the 5th threeway 25, first self-adjusting valve 15, first threeway 20; The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator 2 carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column 1 by the outlet of gas-liquid separator 2 bottom liquid phases, lime set pump 28 and the import of gasification water wash column 1; Gas phase enters in the first shift converter 4 by the outlet of gas-liquid separator 2 top gas phase and feed preheater 3 tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter 4: 7.0%; Described raw gas in feed preheater 3 tube side by heat exchange to 310 DEG C; Transformationreation occurs described raw gas in the first shift converter 4 becomes conversion gas, and described conversion gas temperature is: 455 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway 18 saturation steam being 4.0Mpa with the pressure of coming in middle pressure steam producer 6 shell side in middle pressure steam superheater 5 tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 430 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater 5 shell side enters in middle pressure steam pipe network 14;
Four, the conversion gas that temperature described in step 3 is reduced to 430 DEG C enters in feed preheater 3 shell side and step 2 the raw gas entering feed preheater 3 tube side and carries out heat exchange, and described conversion gas temperature is reduced to 400 DEG C;
Five, enter the second shift converter 7 after the conversion gas that the temperature in step 4 is reduced to 400 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer 6 shell side in middle pressure steam producer 6 tube side and de-salted water pipeline 13 and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer 6 tube side enters in middle pressure steam superheater 5 shell side; Described enter the second shift converter 7 carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 1.7%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit 8 becomes the gas that temperature is 40 DEG C after phlegma, temperature is that the gas of 40 DEG C enters in the first Ammonic washing tower 9;
Seven, temperature described in step 6 is the normal temperature sealing waterpipe 11 after the gas of 40 DEG C enters the first Ammonic washing tower 9 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower 9 top gas phase after the gas removal ammonia of 40 DEG C to enter in ammonia synthesis conversion gas washing tower 10, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in ammonia synthesis conversion gas washing tower 10 is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; Phlegma bottom described first Ammonic washing tower 9 enters into aftertreatment device 12 by the first Ammonic washing tower 9 bottom liquid phases outlet;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device 31 by the outlet of ammonia synthesis conversion gas washing tower 10 top gas phase, and liquid nitrogen washing device 31 removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer 29 go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower 10 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower 10;
Nine, pass through the raw gas of the 5th threeway 25 and the first self-adjusting valve 15 described in step one and pass through the first shift converter 4, 3rd threeway 18 the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve 16 and the first threeway 20, above-mentioned mixed gas with through the second shift converter 7, 3rd end of the 4th threeway 19, enter the second heat and phlegma recovery unit 22 after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve 17 and the second threeway 21 to reclaim phlegma in heat and gas and become the gas that temperature is 30 DEG C, temperature is that the gas of 30 DEG C enters in the second Ammonic washing tower 23,
Ten, temperature described in step 9 is the normal temperature sealing waterpipe 11 after the gas of 30 DEG C enters the second Ammonic washing tower 23 with gasification, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower 23 top gas phase after the gas removal ammonia of 30 DEG C to enter in methanol-fueled CLC conversion gas washing tower 24, and contact with the poor methanol liquid entered in poor methanol liquid pipeline 32 in methanol-fueled CLC conversion gas washing tower 24 is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; Phlegma bottom described second Ammonic washing tower 23 enters into aftertreatment device 12 by the second Ammonic washing tower 23 bottom liquid phases outlet;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer 34, as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower 24 top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower 24 inner bottom part enters in rich methanol liquid regenerating unit 33 by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower 24;
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument 27 Real-Time Monitoring first threeway 20 and the second threeway 21 (H in gas 2-CO 2)/(CO+CO 2) value, when this value shows 2.13, first on-line analysis calculate display instrument 27 by signal feedback to controller 30, controller 30 by signal transmission give the second self-adjusting valve 16, second self-adjusting valve 16 aperture constant;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument 26 Real-Time Monitoring second Ammonic washing tower 23 top gas phase with methanol-fueled CLC conversion gas washing tower 24 lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when this value is shown as 2.09, second on-line analysis calculate display instrument 26 by signal feedback to controller 30, controller 30 by signal transmission give the 3rd self-adjusting valve the 17, three self-adjusting valve 17 aperture constant.
A series of detailed description listed is above only illustrating for feasibility embodiment of the present invention; they are also not used to limit the scope of the invention, all do not depart from the skill of the present invention equivalent implementations done of spirit or change all should be included within protection scope of the present invention.It is to be noted in this article, " first ", " second " etc. only for differentiation each other, but not represent they significance level and order etc.

Claims (4)

1. a device for making for ammonia synthesis Poly-generation methanol-fueled CLC conversion gas, comprises mechanical part and control section, it is characterized in that:
A, mechanical part comprises gasification water wash column (1), gasification water wash column (1) outlet is connected with the second heat and phlegma recovery unit (22) import by pipeline, gasification water wash column (1) outlet and the pipeline between the second heat and phlegma recovery unit (22) are provided with the 5th threeway (25) successively, first self-adjusting valve (15), first threeway (20) and the second threeway (21), second heat and phlegma recovery unit (22) outlet are connected with the second Ammonic washing tower (23) centre inlet, the outlet of second Ammonic washing tower (23) top gas phase is connected with methanol-fueled CLC conversion gas washing tower (24) lower inlet by pipeline, methanol-fueled CLC conversion gas washing tower (24) top gas phase outlet is connected with methanol synthesizer (34),
Described 5th threeway (25) the 3rd end is connected with gas-liquid separator (2), the outlet of gas-liquid separator (2) bottom liquid phases is connected with gasification water wash column (1) import by lime set pump (28), the outlet of gas-liquid separator (2) top gas phase is connected with feed preheater (3) tube side import, the outlet of feed preheater (3) tube side is successively by the first shift converter (4), 3rd threeway (18), middle pressure steam superheater (5) tube side, feed preheater (3) shell side, middle pressure steam producer (6) tube side, second shift converter (7), 4th threeway (19), first heat and phlegma recovery unit (8) are connected with the import of the first Ammonic washing tower (9) bottom, the outlet of first Ammonic washing tower (9) top gas phase is connected with ammonia synthesis conversion gas washing tower (10) lower inlet, ammonia synthesis conversion gas washing tower (10) top gas phase outlet is connected with ammonia synthesizer (29) by liquid nitrogen washing device (31), de-salted water pipeline (13) is connected with middle pressure steam pipe network (14) with middle pressure steam producer (6) shell side, middle pressure steam superheater (5) shell side by pipeline successively, 3rd end of described 3rd threeway (18) is connected with the 3rd end of the first threeway (20) by pipeline, and the 3rd end of the 4th threeway (19) is connected with the 3rd end of the second threeway (21) by pipeline, described second Ammonic washing tower (23) bottom liquid phases outlet is connected with aftertreatment device (12) respectively with the outlet of the first Ammonic washing tower (9) bottom liquid phases, described second Ammonic washing tower (23) middle part fluid inlet seals waterpipe (11) with gasification respectively with the first Ammonic washing tower (9) middle part fluid inlet and is connected, the bottom liquid phases outlet of described ammonia synthesis conversion gas washing tower (10) is connected with rich methanol liquid regenerating unit (33) respectively with the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower (24), the middle part fluid inlet of described ammonia synthesis conversion gas washing tower (10) is connected with poor methanol liquid pipeline (32) respectively with the middle part fluid inlet of methanol-fueled CLC conversion gas washing tower (24),
B, control section comprises the first on-line analysis be arranged between the first threeway (20) and the second threeway (21) on pipeline and calculates display instrument (27), be arranged on pipeline second on-line analysis between the outlet of the second Ammonic washing tower (23) top gas phase and methanol-fueled CLC conversion gas washing tower (24) lower inlet and calculate display instrument (26), the second self-adjusting valve (16) that pipeline between 3rd end of the 3rd threeway (18) and the 3rd end of the first threeway (20) is installed, the 3rd self-adjusting valve (17) that pipeline between 3rd end of the 4th threeway (19) is connected with the 3rd end of the second threeway (21) is arranged, described first on-line analysis calculates display instrument (27) and is connected with the input terminus of controller (30) respectively with the second on-line analysis calculating display instrument (26), and the output terminal of controller (30) is connected with the second self-adjusting valve (16), the 3rd self-adjusting valve (17) respectively.
2. the device for making of a kind of ammonia synthesis Poly-generation methanol-fueled CLC conversion gas according to claim 1, is characterized in that: described second shift converter (7) is for adiabatic shift converter or controlledly move one of thermal conversion stove.
3. the device for making of a kind of ammonia synthesis Poly-generation methanol-fueled CLC conversion gas according to claim 1, is characterized in that: it is in series with at least a set of gas-liquid separator that described first heat and phlegma recovery unit (8) and the second heat and phlegma recovery unit (22) comprise at least one cover interchanger respectively.
4. the preparation method of the device for making of a kind of ammonia synthesis Poly-generation methanol-fueled CLC conversion gas as claimed in claim 1, is characterized in that: the method comprises the steps:
What the water wash column (1) that, gasifies came is divided into two portions by vapour-saturated raw gas, a part enters in gas-liquid separator (2) through the 3rd end of the 5th threeway (25), and another part is connected with the second heat and phlegma recovery unit (22) with the second threeway (21) through the 5th threeway (25), the first self-adjusting valve (15), the first threeway (20); The temperature of described raw gas is: 225 ~ 240 DEG C, and pressure is: 5.3 ~ 8.5Mpa, the volume fraction of carbon monoxide: 40 ~ 55%;
Two, after the raw gas entered described in step one in gas-liquid separator (2) carries out gas-liquid separation, the water of liquid phase enters in gasification water wash column (1) by the outlet of gas-liquid separator (2) bottom liquid phases, lime set pump (28) and gasification water wash column (1) import; Gas phase enters in the first shift converter (4) by the outlet of gas-liquid separator (2) top gas phase and feed preheater (3) tube side; The volume fraction of carbon monoxide after described raw gas carries out transformationreation in the first shift converter (4): 4.0 ~ 7.0%; Described raw gas in feed preheater (3) tube side by heat exchange to 270 ~ 310 DEG C; Transformationreation occurs described raw gas in the first shift converter (4) becomes conversion gas, and described conversion gas temperature is: 440 ~ 455 DEG C;
Three, the conversion gas described in step 2 enters by the 3rd threeway (18) saturation steam being 3.5 ~ 4.0Mpa with the pressure of coming in middle pressure steam producer (6) shell side in middle pressure steam superheater (5) tube side and carries out heat exchange, makes the temperature of conversion gas be reduced to 400 ~ 430 DEG C; Becoming superheated vapour by the middle pressure steam after heat exchange in middle pressure steam superheater (5) shell side enters in middle pressure steam pipe network (14);
Four, the conversion gas that temperature described in step 3 is reduced to 400 ~ 430 DEG C enters the raw gas entering feed preheater (3) tube side in feed preheater (3) shell side and step 2 and carries out heat exchange, and described conversion gas temperature is reduced to 370 ~ 400 DEG C;
Five, enter the second shift converter (7) after the conversion gas that the temperature in step 4 is reduced to 370 ~ 400 DEG C carries out heat exchange by the de-salted water entering middle pressure steam producer (6) shell side in middle pressure steam producer (6) tube side and de-salted water pipeline (13) and carry out transformationreation, the steam produced after carrying out heat exchange with middle pressure steam producer (6) tube side enters in middle pressure steam superheater (5) shell side; Described enter the second shift converter (7) carry out transformationreation after quadratic transformation gas gas in the volume fraction of carbon monoxide be: 0.4 ~ 1.7%;
Six, the gas of quadratic transformation described in step 5 reclaims in heat and gas through the first heat and phlegma recovery unit (8) becomes the gas that temperature is 20 ~ 40 DEG C after phlegma, and temperature is that the gas of 20 ~ 40 DEG C enters in the first Ammonic washing tower (9);
Seven, temperature described in step 6 is that the gas of 20 ~ 40 DEG C enters the first Ammonic washing tower (9) and seal the normal temperature of waterpipe (11) with gasification afterwards, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the first Ammonic washing tower (9) top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in ammonia synthesis conversion gas washing tower (10), and contact with the poor methanol liquid entered in poor methanol liquid pipeline (32) in ammonia synthesis conversion gas washing tower (10) is reverse, remove sour gas, become purified gas; CO in described purified gas 2≤ 20ppm, total sulfur < 0.1ppm, CH 3oH≤25ppm; The phlegma of described first Ammonic washing tower (9) bottom enters into aftertreatment device (12) by the outlet of the first Ammonic washing tower (9) bottom liquid phases;
Eight, the purified gas described in step 7 enters liquid nitrogen washing device (31) by the outlet of ammonia synthesis conversion gas washing tower (10) top gas phase, and liquid nitrogen washing device (31) removes the CH in gas further 4, CO 2, CO 3oH, CO, Ar composition, and configure nitrogen hydrogen ratio be 3: 1 synthetic gas deliver to ammonia synthesizer (29) go produce synthetic ammonia; The rich methanol liquid of described ammonia synthesis conversion gas washing tower (10) inner bottom part enters in rich methanol liquid regenerating unit (33) by the bottom liquid phases outlet of ammonia synthesis conversion gas washing tower (10);
Nine, pass through the raw gas of the 5th threeway (25) and the first self-adjusting valve (15) described in step one and pass through the first shift converter (4), 3rd threeway (18) the 3rd end, mixed gas is become after the conversion gas mixing of the 3rd end of the second self-adjusting valve (16) and the first threeway (20), above-mentioned mixed gas with through the second shift converter (7), 3rd end of the 4th threeway (19), enter the second heat and phlegma recovery unit (22) after the quadratic transformation gas mixing of the 3rd end of the 3rd self-adjusting valve (17) and the second threeway (21) to reclaim phlegma in heat and gas and become the gas that temperature is 20 ~ 40 DEG C, temperature is that the gas of 20 ~ 40 DEG C enters in the second Ammonic washing tower (23),
Ten, temperature described in step 9 is that the gas of 20 ~ 40 DEG C enters the second Ammonic washing tower (23) and seal the normal temperature of waterpipe (11) with gasification afterwards, pressure is: after the reverse contact of sealing water of 8.0 ~ 9.0Mpa, temperature is exported by the second Ammonic washing tower (23) top gas phase after the gas removal ammonia of 20 ~ 40 DEG C to enter in methanol-fueled CLC conversion gas washing tower (24), and contact with the poor methanol liquid entered in poor methanol liquid pipeline (32) in methanol-fueled CLC conversion gas washing tower (24) is reverse, remove sour gas, become secondary-cleaned gas; Total sulfur < 0.1ppm, CH in described secondary-cleaned gas 3oH≤25ppm; The phlegma of described second Ammonic washing tower (23) bottom enters into aftertreatment device (12) by the outlet of the second Ammonic washing tower (23) bottom liquid phases;
11, secondary-cleaned gas described in step 10 enters in methanol synthesizer (34), as the unstripped gas of methanol by the outlet of methanol-fueled CLC conversion gas washing tower (24) top gas phase; The rich methanol liquid of described methanol-fueled CLC conversion gas washing tower (24) inner bottom part enters in rich methanol liquid regenerating unit (33) by the bottom liquid phases outlet of methanol-fueled CLC conversion gas washing tower (24);
12, in above-mentioned production process, the first on-line analysis to calculate between display instrument (27) Real-Time Monitoring first threeway (20) and the second threeway (21) (H in gas 2-CO 2)/(CO+CO 2) value, as this value display < 2.0 or > 2.15, first on-line analysis calculates display instrument (27) by signal feedback to controller (30), signal transmission is given the second self-adjusting valve (16) by controller (30), the corresponding increase of second self-adjusting valve (16) aperture or reduction, until displayed value is 2.0 ~ 2.15;
13, in above-mentioned production process, the second on-line analysis to calculate between the outlet of display instrument (26) Real-Time Monitoring second Ammonic washing tower (23) top gas phase with methanol-fueled CLC conversion gas washing tower (24) lower inlet (H in gas 2-CO 2)/(CO+CO 2) value, when the display of this value is not between 2.05 ~ 2.1, second on-line analysis calculates display instrument (26) by signal feedback to controller (30), signal transmission is given the 3rd self-adjusting valve (17) by controller (30), the 3rd corresponding increase of self-adjusting valve (17) aperture or reduction, until displayed value is 2.05 ~ 2.1.
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