US20220170389A2 - Method for operating a chemical plant - Google Patents

Method for operating a chemical plant Download PDF

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US20220170389A2
US20220170389A2 US17/286,418 US201917286418A US2022170389A2 US 20220170389 A2 US20220170389 A2 US 20220170389A2 US 201917286418 A US201917286418 A US 201917286418A US 2022170389 A2 US2022170389 A2 US 2022170389A2
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steam
pressure turbine
turbine stage
synthesis gas
plant
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US20210301685A1 (en
US12078086B2 (en
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Wolff Balthasar
Peter KOSS
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/064—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle in combination with an industrial process, e.g. chemical, metallurgical
    • 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
    • C01B3/025—Preparation or purification of gas mixtures for ammonia synthesis
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01C—AMMONIA; CYANOGEN; COMPOUNDS THEREOF
    • C01C1/00—Ammonia; Compounds thereof
    • C01C1/02—Preparation, purification or separation of ammonia
    • C01C1/04—Preparation of ammonia by synthesis in the gas phase
    • C01C1/0405—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst
    • C01C1/0417—Preparation of ammonia by synthesis in the gas phase from N2 and H2 in presence of a catalyst characterised by the synthesis reactor, e.g. arrangement of catalyst beds and heat exchangers in the reactor
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/15—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively
    • C07C29/151—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases
    • C07C29/152—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the reactor used
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K11/00—Plants characterised by the engines being structurally combined with boilers or condensers
    • F01K11/02—Plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K3/00—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein
    • F01K3/18—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
    • F01K3/188—Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters using heat from a specified chemical reaction
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K7/00—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating
    • F01K7/16—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type
    • F01K7/22—Steam engine plants characterised by the use of specific types of engine; Plants or engines characterised by their use of special steam systems, cycles or processes; Control means specially adapted for such systems, cycles or processes; Use of withdrawn or exhaust steam for feed-water heating the engines being only of turbine type the turbines having inter-stage steam heating
    • 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
    • C01B2203/1614—Controlling the temperature
    • 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
    • C01B2203/1628—Controlling the pressure
    • 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
    • C01B2203/169—Controlling the feed

Definitions

  • the present disclosure relates to a method for operating a chemical plant as well as to a chemical plant.
  • steam turbines are not only used in power plants for power generation, where a single turbine generally generates a very high output, but are also employed, in smaller sizes, in plants of the chemical industry, which regularly produce process steam that may be used in a steam turbine. In such chemical plants, the steam turbine frequently drive mechanical devices directly, without an intermediate power generation step.
  • Catalytic partial oxidation which is also referred to as autothermic reforming, is a preferred manner of producing the synthesis gas in chemical plants.
  • the exiting synthesis gas due to the supply of oxygen to the process, has such a large carbon monoxide partial pressure that a use of the synthesis gas for overheating the steam for the supply to the steam turbine appears not to be feasible in light of the current state of material sciences. For this high carbon monoxide partial pressure would result in a rapid destruction of the overheating device by metal dusting.
  • An object of the inventors was to develop a steam turbine in a chemical plant and a method for operating such a chemical plant in such a way that the steam turbine is able to provide its output for overheating the steam with a smaller consumption of natural gas or other energy carrier.
  • overheating the steam again between the pressure turbine stages (which process of repeated overheating is also referred to as reheating—can not only be carried out in the area of the high pressures, i.e. between the first two pressure turbine stages, but also in the area of lower pressures between the respectively subsequent pressure turbine stages.
  • reheating process of repeated overheating
  • internal process heat of the chemical plant may then be used for overheating, so that the fired heating device is not required at least for this overheating process.
  • FIG. 1 shows a schematic illustration of an embodiment of a chemical plant.
  • a method serves for operating a chemical plant illustrated in FIG. 1 .
  • the chemical plant has a steam turbine 1 with a shaft 2 and with a first pressure turbine stage 3 and a second pressure turbine stage 4 .
  • the first pressure turbine stage 3 and the second pressure turbine stage 4 are each disposed on the shaft 2 and connected in series in terms of the steam process.
  • the connection in series of the first pressure turbine stage 3 and the second pressure turbine stage 4 in terms of the steam process means that turbine steam flowing through the steam turbine 1 for driving the shaft 2 first flows through the first pressure turbine stage 3 and only then through the second pressure turbine stage 4 .
  • this turbine steam may in principle pass through any number of further pressure turbine stages of the steam turbine 1 or be supplied to another process.
  • the steam turbine 1 has an electrical maximum output of at least 30 MW, and in some embodiments an electrical maximum output of between 50 MW and 200 MW.
  • Steam 5 for driving the steam turbine 1 is obtained from a reactor plant 6 , which reactor plant 6 produces a hydrogen-containing substance 7 from a carbon-containing energy-carrier flow 8 , and wherein the steam 5 is heated in an overheating step prior to being supplied to the second pressure turbine stage 4 .
  • the chemical plant includes the reactor plant 6 .
  • the overheating step may basically have an arbitrary duration and cause the steam 5 to be heated to a basically arbitrary temperature.
  • the steam 5 is heated to a temperature above the saturation temperature. The latter is the saturation temperature at the pressure that the steam 5 has in the overheating step. Heating may also take place in a basically arbitrary manner and fed by a basically arbitrary energy source.
  • the steam 5 is already heated when it is being obtained from the reactor plant 6 , and thus prior to being supplied to the steam turbine 1 —e.g., prior to being supplied to the first pressure turbine stage 3 .
  • the steam 5 is heated to a temperature above the saturation temperature of the steam 5 prior to being supplied to the steam turbine 1 —e.g., prior to being supplied to the first pressure turbine stage 3 . Therefore, the heating prior to the supply to the second pressure turbine stage 4 , at which point in time the steam 5 has already been supplied to the steam turbine 1 , is a re-heating.
  • the steam turbine 1 has a third pressure turbine stage 9 disposed on the shaft 2 , which third pressure turbine stage 9 is connected between the first pressure turbine stage 3 and the second pressure turbine stage 4 in terms of the steam process.
  • the turbine steam may in principle pass through any number of further pressure turbine stages or be supplied to another process, in each case between the first pressure turbine stage 3 and the third pressure turbine stage 9 , and between the third pressure turbine stage 9 and the second pressure turbine stage 4 .
  • the steam 5 passes through the overheating step after exiting the third pressure turbine stage 9 .
  • the steam 5 is heated in the overheating step prior to being supplied to the second pressure turbine stage 4 .
  • the chemical plant includes the steam turbine 1 , which in turn comprises the shaft 2 , the first pressure turbine stage 3 and the second pressure turbine stage 4 , wherein the first pressure turbine stage 3 and the second pressure turbine stage 4 are each disposed on the shaft 2 and connected in series in terms of the steam process.
  • the chemical plant further includes the reactor plant 6 for producing the hydrogen-containing substance 7 from the carbon-containing energy-carrier flow 8 , wherein steam 5 for driving the steam turbine 1 is obtained from the reactor plant 6 .
  • the chemical plant also includes a heating assembly 6 a for heating the steam 5 prior to it being supplied to the second pressure turbine stage 4 .
  • this heating assembly 6 a may be any device or group of devices of the chemical plant, which may optionally also be included in the reactor plant 6 .
  • the steam turbine 1 has a third pressure turbine stage 9 , which is disposed on the shaft 2 and which is connected between the first pressure turbine stage 3 and the second pressure turbine stage 4 in terms of the steam process.
  • the heating assembly 6 a further heats the steam 5 subsequent to it exiting the third pressure turbine stage 9 .
  • a heating process takes place between the third pressure turbine stage 9 and the second pressure turbine stage 4 .
  • the steam 5 has a temperature of at least 450° C. prior to being supplied to the steam turbine 1 —e.g., prior to being supplied to the first pressure turbine stage 3 .
  • the steam 5 is overheated.
  • the steam 5 may have a temperature of between 450° C. and 600° C. prior to being supplied to the steam turbine 1 —e.g., prior to being supplied to the first pressure turbine stage 3 .
  • the steam 5 is heated in the overheating step to at least the temperature of the steam 5 prior to being supplied to the steam turbine 1 —e.g., prior to being supplied to the first pressure turbine stage 3 .
  • the steam 5 is heated in the overheating step to a temperature of at least 450° C., and particularly to a temperature of between 450° C. and 650° C.
  • the heating assembly 6 a heats the steam 5 to a temperature of at least 450° C., and in some such embodiments to a temperature of between 450° C. and 650° C.
  • the steam 5 has a pressure of between 1 bar and 20 bars when it is supplied to the second pressure turbine stage 4 . In some such embodiments, the steam 5 may have a pressure of between 2 bars and 8 bars when it is supplied to the second pressure turbine stage 4 .
  • the first pressure turbine stage 3 may also be referred to as a high-pressure turbine stage
  • the third pressure turbine stage 9 connected downstream of the first pressure turbine stage 3 may be referred to as a medium-pressure turbine stage
  • the second pressure turbine stage 4 may be referred to as a low-pressure turbine stage.
  • the steam 5 may, for instance, have a pressure of between 80 bars and 300 bars, e.g., between 100 bars and 200 bars, prior to flowing through the first pressure turbine stage 3 .
  • the steam 5 after flowing through the first pressure turbine stage 3 and prior to flowing through the third pressure turbine stage 9 , has a pressure of between 30 bars and 100 bars, and finally a pressure of between 0.01 and 0.1 bars after flowing through the second pressure turbine stage 4 .
  • the steam overheated, upstream of the first pressure turbine stage 3 and upstream of the second pressure turbine stage 4 , to a temperature of in this case more than 500° C. still has a temperature of, for example, between 15° C. and 40° C., or between 20° C. and 30° C., when exiting the second pressure turbine stage 4 .
  • the steam has a temperature of at least 280° C. or of substantially 280° C. when exiting the first pressure turbine stage 3 .
  • the hydrogen-containing substance 7 may be any such substance.
  • the hydrogen-containing substance 7 may be hydrogen.
  • the hydrogen-containing substance 7 may also be synthesis gas including carbon oxides and hydrogen.
  • the hydrogen-containing substance 7 may also be a hydrogen-containing compound.
  • the reactor plant 6 produces methanol and, alternatively or additionally, ammonia. Accordingly, the hydrogen-containing substance 7 may be methanol or ammonia.
  • the reactor plant 6 may be divided into several sections with different functions in each case.
  • synthesis gas 11 e.g., including hydrogen and carbon oxides, is obtained in a synthesis gas section 10 of the reactor plant 6 .
  • the obtained synthesis gas 11 is supplied to a converting section 12 of the reactor plant 6 downstream of the synthesis gas section 10 , in which converting section 12 the obtained synthesis gas 11 is converted into the hydrogen-containing substance 7 .
  • the synthesis gas 11 may include hydrogen and carbon oxides, or substantially consists thereof.
  • the synthesis gas 11 may also contain nitrogen and smaller contents of noble gases, or contain hydrogen, carbon oxides, nitrogen and noble gases.
  • the synthesis gas 11 is converted in the converting section 12 into methanol and/or ammonia.
  • other starting materials may also be supplied to the converting section 12 , e.g. nitrogen for the production of ammonia. This may take place particularly if the synthesis gas 11 does not contain a sufficient amount of nitrogen.
  • the carbon-containing energy-carrier flow 8 is supplied to the synthesis gas section 10 for obtaining the synthesis gas 11 , that an oxygen-containing flow 13 is supplied to the synthesis gas section 10 , and that the synthesis gas 11 is obtained in the synthesis gas section 10 through a catalytic partial oxidation—which may also be referred to as autothermic reforming—by means of the oxygen-containing flow 13 .
  • the oxygen-containing flow 13 may substantially consist of oxygen and be obtained from an air separation device 14 of the reactor plant 6 .
  • the steam 5 is heated in the overheating step by means of heat from a reaction during the conversion of the obtained synthesis gas 11 into the hydrogen-containing substance 7 , e.g., into methanol and/or ammonia.
  • the reactions for forming methanol from synthesis gas 11 are exothermic, as is the reaction for obtaining ammonia from hydrogen and nitrogen, whereby the heat for heating the steam can thus be obtained.
  • FIG. 1 shows that the steam 5 is guided from the steam turbine 1 to the converting section 12 for heating—e.g., to a reactor 15 of the converting section 12 —and then back to the steam turbine 1 . Accordingly, the reactor 15 in this case forms the heating assembly 6 a . According to the illustration of FIG.
  • a product treatment unit 15 a of the converting section which obtains the hydrogen-containing substance 7 from the substance flow 16 exiting the reactor 15 , is connected downstream of the reactor 15 .
  • the product treatment unit 15 a may be configured for obtaining the hydrogen-containing flow 7 from the substance flow 16 by purifying the substance flow 16 .
  • the converting section 12 has the reactor 15 with a catalyst for at least partially converting the synthesis gas 11 into the hydrogen-containing substance 7 .
  • the converting section 12 may also have a heat exchanger—not shown in FIG. 1 herein—for cooling the substance flow 16 from the reactor 15 .
  • the substance flow 16 can include a raw-product flow with the hydrogen-containing substance 7 and possibly non-reacted synthesis gas.
  • the steam 5 is heated in the overheating step by heat from the reactor 15 or the heat exchanger.
  • the steam 5 supplied to the first pressure turbine stage 3 is already overheated and saturated. Therefore, a first saturated and overheated steam flow 17 may be supplied to the first pressure turbine stage 3 for driving the steam turbine 1 .
  • this first steam flow 17 may have any relationship with the steam 5 .
  • the first steam flow 17 may be separate from the steam 5 .
  • the steam flow 17 may also include the steam 5 or consist thereof.
  • the overheating of the steam 5 for the first pressure turbine stage 3 may have a higher temperature than the downstream overheating between the third pressure turbine stage 9 and the second pressure turbine stage 4 . Therefore, the exemplary embodiment shown here in FIG. 1 provides that the reactor plant 6 has a fired heating device 18 , which overheats the steam 5 , which is obtained in a saturated condition from the reactor plant 6 , for obtaining the first steam flow 17 . Apart from this overheating of the steam 5 , the fired heating device 18 may also have further functions.
  • the heating device 18 may be fed by the carbon-containing energy-carrier flow 8 .
  • the steam 5 is obtained in a saturated condition from the synthesis gas section 10 .
  • the steam 5 may be obtained from a process of draining water from the synthesis gas section 10 , for example.
  • the steam turbine 1 may be operated such that all its pressure turbine stages 3 , 4 , 9 are operated substantially only by the steam 5 that is already being supplied to the first pressure turbine stage 3 .
  • a second, in particular saturated, steam flow 19 is obtained from the reactor plant 6 , e.g., from the converting section 12 , which is overheated by the heating device 18 and which is supplied to the third pressure turbine stage 9 for driving the steam turbine 1 .
  • FIG. 1 As is shown in FIG.
  • the second steam flow 19 may be merged with the first steam flow 17 after the first steam flow 17 has exited the first pressure turbine stage 3 .
  • Pressures lower than those in the synthesis section 10 may occur in the converting section 12 . Therefore, the second steam flow 19 from the converting section 12 , which has a lower pressure compared with the first steam flow 17 , may be merged with the first steam flow 17 if the first steam flow 17 has already lost some pressure by flowing through the first pressure turbine stage 3 .
  • a process steam flow which may be a partial flow of the steam 5 , may also be extracted after exiting from the first pressure turbine stage 3 or from the third pressure turbine stage 9 .
  • the process steam flow is extracted prior to the supply to the third pressure turbine stage 9 of prior to the supply to the second pressure turbine stage 4 .
  • Such an extracted process steam flow is in at least some embodiments, supplied to the reactor plant 6 .
  • the extracted process steam flow may be supplied to the reactor plant 6 , and in at least some embodiments, to the synthesis gas section 10 or the converting section 12 , and in the illustrated embodiment to the product treatment unit 15 a .
  • the product treatment unit 15 a may comprise distillation columns for product treatment. The latter regularly require greater steam quantities, which can accordingly be provided by the extracted process steam flow.
  • the extracted process steam flow may be supplied as a heating medium and/or as a reaction medium in a chemical process.
  • the process steam flow may be mixed with a process flow of the reactor plant 6 .
  • the process steam flow may be used as a heating medium in a reboiler of the chemical plant.
  • the process steam flow condensates in the process and is supplied as a condensate to the condensed water from the condenser 25 —which is described in more detail below. As a consequence, the extracted process steam flow can no longer be returned to the steam turbine 1 .
  • the steam turbine 1 may be a condensing turbine, so that condensation arises in the exhaust steam of, in particular, the second pressure turbine stage 4 . Accordingly, in at least some embodiments, the second pressure turbine stage 4 relaxes the steam 5 supplied to it to form a wet steam 20 . This permits achieving a very high degree of efficiency with the steam turbine 1 .
  • the chemical plant comprises a generator 21 for producing an electrical turbine current, which generator 21 is driven by the shaft 2 .
  • a steam turbine 1 and in particular a condensing turbine, is operated with several pressure turbine stages 3 , 4 , 9 , then enough electrical power can be provided with it—and thus with a single steam turbine 1 —in order to operate all, or at least vital, electrical consumers of the reactor plant 6 .
  • excess electrical power generated by the generator 21 may even be provided to other consumers outside the reactor plant 6 . In that case, it is no longer necessary to use a plurality of steam turbines with, in each case, lower power.
  • the turbine current may be used for an arbitrary purpose. In at least some embodiments, however, that the turbine current drives the air separation device 14 of the reactor plant 6 . Also, the turbine current may drive a compressor assembly 26 and/or a pump assembly 22 of the reactor plant 6 .
  • the air separation device 14 is powered electrically and that it can be operated additionally or exclusively with power from a power grid.
  • the air separation device 14 may also produce, at least temporarily, oxygen for the oxygen-containing flow 13 and a surplus of oxygen beyond that.
  • the air separation device 14 then produces more oxygen than is required by the chemical plant and particularly the synthesis gas section 10 .
  • the oxygen surplus is then stored temporarily in a suitable storage unit, particularly in a liquid form.
  • the pump assembly 22 may have a boiler water pump 23 for providing water for a boiler 24 of the reactor plant 6 .
  • This boiler 24 may be included in the converting section 12 .
  • the boiler water pump 23 may be supplied with water from the condenser 25 of the chemical plant, which condenser 25 is supplied with the wet steam 20 .
  • the compressor assembly 26 may have a synthesis gas compressor for increasing the pressure in the reactor plant 6 .
  • the compressor assembly 26 and also the synthesis gas compressor, may serve for increasing the pressure of the synthesis gas 11 , i.e. particularly prior to being supplied to the reactor 15 .
  • the compressors of a compressor assembly 26 and the pumps of a pump assembly 22 may be driven by electric motors. If the power from the electrical power supply grid is fed to the latter, adjusting their rotation speed becomes difficult. For the rotation speed of an electric motor first depends on the frequency of the current, which in the power supply grid is fixed at 50 Hz, for example. Providing a mechanical transmission for adjusting the respective rotation speed is expensive and requires a design which is both complex and laborious to maintain.
  • the chemical plant may have a frequency converter assembly 27 which, with a power electronic system of the frequency converter assembly 27 , converts the turbine current, e.g., for driving the compressor assembly 26 and/or the pump assembly 22 .
  • the chemical plant may have a frequency converter assembly 27 with an adjustable output frequency.
  • the frequency converter assembly 27 may also have a plurality of individual frequency converters, e.g. at least one individual frequency converter is provided for each of the compressor assembly 26 , the pump assembly 22 and for the air separation device 14 .
  • Providing the frequency converter assembly 27 further permits the operation of the frequency converter assembly, and thus also of the compressor assembly 26 , the pump assembly 22 and/or the air separation device 14 , with power from the power supply grid when starting up the reactor plant 6 , i.e. when steam 5 from the reactor plant 6 is not yet provided to a sufficient extent for operating the steam turbine 1 .

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Organic Chemistry (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Analytical Chemistry (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
US17/286,418 2018-10-23 2019-10-17 Method for operating a chemical plant Active 2040-07-13 US12078086B2 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
EP18202126.1 2018-10-23
EP18202126.1A EP3643888B1 (de) 2018-10-23 2018-10-23 Verfahren zum betreiben einer chemischen anlage
PCT/EP2019/078232 WO2020083741A1 (de) 2018-10-23 2019-10-17 Verfahren zum betreiben einer chemischen anlage

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US20210301685A1 US20210301685A1 (en) 2021-09-30
US20220170389A2 true US20220170389A2 (en) 2022-06-02
US12078086B2 US12078086B2 (en) 2024-09-03

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WO2020083741A1 (de) 2020-04-30
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