EP2349922A1 - Production de gaz de procédé au moyen de récupération de chaleur à partir de chaleur d'échappement à basse température - Google Patents

Production de gaz de procédé au moyen de récupération de chaleur à partir de chaleur d'échappement à basse température

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Publication number
EP2349922A1
EP2349922A1 EP09748703A EP09748703A EP2349922A1 EP 2349922 A1 EP2349922 A1 EP 2349922A1 EP 09748703 A EP09748703 A EP 09748703A EP 09748703 A EP09748703 A EP 09748703A EP 2349922 A1 EP2349922 A1 EP 2349922A1
Authority
EP
European Patent Office
Prior art keywords
heat exchanger
process gas
heat
boiler feedwater
low
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP09748703A
Other languages
German (de)
English (en)
Inventor
Thilo Von Trotha
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
ThyssenKrupp Industrial Solutions AG
Original Assignee
Uhde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Uhde GmbH filed Critical Uhde GmbH
Publication of EP2349922A1 publication Critical patent/EP2349922A1/fr
Withdrawn legal-status Critical Current

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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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • 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
    • C01B3/32—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air
    • C01B3/34—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents
    • C01B3/48—Production of hydrogen or of gaseous mixtures containing a substantial proportion of hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents followed 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
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • 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
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/56—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with solids; Regeneration of used solids
    • 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
    • C01B2203/0205—Processes for making hydrogen or synthesis gas containing a reforming step
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/042—Purification by adsorption on solids
    • C01B2203/043—Regenerative adsorption process in two or more beds, one for adsorption, the other for regeneration
    • 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/047—Composition of the impurity the impurity being 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
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • 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
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0888—Methods of cooling by evaporation of a fluid
    • C01B2203/0894—Generation of steam
    • 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
    • C01B2203/12—Feeding the process for making hydrogen or synthesis gas
    • C01B2203/1205—Composition of the feed
    • C01B2203/1211—Organic compounds or organic mixtures used in the process for making hydrogen or synthesis gas
    • C01B2203/1235—Hydrocarbons
    • 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
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • the invention relates to a process for steam reforming of hydrocarbon-containing starting materials, which is in particular to the process gas production by means of heat recovery from low-temperature waste heat.
  • the invention relates to making better use of the energy of the process gas containing hydrogen and water vapor produced in a steam reforming process.
  • an apparatus for carrying out the method according to the invention should be the subject of the invention.
  • a reaction mixture of water vapor and hydrocarbon-containing starting materials is converted to a process gas which is enriched with hydrogen.
  • This process gas leaves the steam reforming process with a temperature above 100 0 C. Most of this temperature is in a range between 700 and 1000 0 C.
  • the process gas which may for example consist in a purification and / or an increase in the hydrogen content by pressure swing adsorption or membrane process, this must be cooled.
  • the temperature required for further processing is in a range of 20 ° to 5O 0 C.
  • further reaction steps which can react, for example carbon monoxide and water to carbon dioxide and hydrogen.
  • the amount of heat of the process gas is used in a typical conventional heat recovery process, which is integrated in a synthesis gas plant, usually characterized by that first a high pressure steam is generated in a waste heat boiler and the process gas is converted in a CO conversion unit to carbon dioxide and hydrogen. Thereafter, a variety of heat exchangers are often run through, for example, to heat the hydrocarbon-containing starting material, the boiler feed water and / or the make-up water. The remaining heat contained in the process gas is then usually released via the cooling section to the environment. The condensate accumulating in the cooling section is transferred to a water treatment unit where it is combined with make-up water and then passed into the boiler feedwater pre-heater, whereupon the heated stream is passed to the steam generation system.
  • a disadvantage of this conventional method of heat recovery is that the heat of the process gas leaving the CO conversion unit is largely the heat from a moisture condensation taking place. This condensation is subject to a Pinch effect by the further cooling, whereby the recovery of the heat contained is very difficult and a significant proportion is discharged through the cooling section to the environment.
  • the pinch effect is defined by the approach of the temperatures of two streams, whereby the temperature difference between the two streams is reduced and thus the driving force for heat exchange is minimized. As a result, a lot of energy from the process gas is lost unused.
  • a disadvantage of this system is that the heat exchange in the boiler feedwater heater 1, which is traversed by the process gas is subjected to a pinch effect and thereby the desired heat transfer takes place only to a very limited extent.
  • the greater the amount of boiler feed water that passes through this unit the greater the heat yield that can be utilized.
  • the division of the water flow, before passing through the boiler feedwater preheater 1 results in a limited amount of boiler feedwater passing through this unit and thus a significant fraction of the boiler feed water Heat contained in the process gas via the cooling section, which is usually realized via air cooler, is discharged to the environment and thus lost unused.
  • part of the heat of the flue gas is used to heat the boiler feed water. This heat content of the flue gas is thus no longer available for the actual steam generation.
  • the water treatment unit usually consists of a degasser. This is usually quasi-atmospheric or at a slight overpressure, typically at less than 5 bar (abs.) Operated to remove as much oxygen and other gases from the water.
  • the temperature of the water feed stream of this water treatment unit is typically limited to 80 ° to 95 ° C.
  • the water feed stream could be heated to a temperature greater than 100 ° C via the heat contained in the process gas. Therefore, an additional control device must ensure that the temperature of the inflow stream of the water treatment unit does not exceed the limit of 95 ° C.
  • the heat of the process gas can not be fully utilized and the residual heat contained is ultimately released unused to the environment.
  • the present invention has been developed against the background of the above-described prior art, wherein it is an object of the invention to provide a method for process gas generation, in which it no longer to the above problems in the heat recovery from the process gas contained heat quantity and in which the heat recovery is made even more efficient. Furthermore, it should be the subject of the invention to disclose an apparatus for carrying out the method according to the invention.
  • High-temperature conversion unit at least two units for pressure increase, at least one consumer and at least one unit for further processing of the resulting process gas.
  • High temperature conversion unit in which it is largely converted to carbon dioxide and hydrogen, after which the resulting heat-containing process gas is passed to a first heat exchanger for further heat transfer, and subsequently passes through at least two further heat exchangers operated as boiler feedwater pre-heaters, product condensate heat exchangers or low pressure evaporators, and which are connected in series in any order, wherein the process gas resulting from the low pressure evaporator is first passed into another boiler feedwater by heat energy is transferred to a partial flow of boiler feed water from the water treatment unit, after which the resulting process gas passes the cooling section in which the Process gas is cooled further and a condensate stream is generated and finally passed through at least one unit for further processing of the resulting process gas becomes.
  • a deionized stream is passed for heating in a second heat exchanger.
  • the deionized stream from the second heat exchanger is sent to the water treatment unit for degassing, the boiler feed water stream from the water treatment unit passes through a pressure increase unit and is split, with a first portion of the boiler feed water stream entering the water treatment unit
  • Low-pressure evaporator is passed, in which a low-pressure steam is generated, and the generated low-pressure steam is divided and a first partial flow of the low-pressure steam for heat transfer is performed in the water treatment unit and a second partial flow of low-pressure steam is passed into at least one consumer.
  • This second partial stream of low pressure steam may also be used to preheat other feeds, such as liquid feeds, or for use outside the plant.
  • a second part of the boiler feedwater stream is passed over the second heat exchanger for the purpose of energy transfer and then passed through one or more boiler feedwater preheaters for heating by means of the amount of heat contained in the process gas and finally passed to the steam generation.
  • the water treatment unit degassed the deionized in substantial parts of oxygen in the deaerator. Subsequently, other dosing agents such as ammonia can be added to adjust the pH.
  • the product resulting from this treatment is called boiler feed water.
  • the condensate stream from the cooling section is passed for heating by means of the amount of heat contained in the process gas via a unit for increasing the pressure in the product condensate heat exchanger, after which there is a further heating of the condensate stream.
  • the process gas from the first heat exchanger first passes through a first boiler feedwater pre-heater by heat energy is transferred to a boiler feedwater flow, then a
  • Low-pressure steam is generated from a boiler feedwater flow in order to continue from there through the defined process chain.
  • the process gas from the first heat exchanger first passes through a first boiler feedwater by heat energy is transferred to a boiler feedwater flow, then it is passed into the low pressure evaporator, in which by means of the amount of heat contained low pressure steam is generated from a boiler feedwater flow, and the resulting process gas passes from there to a product condensate heat exchanger, in which heat energy is transferred to a condensate stream in order to continue from there through the defined process chain.
  • the process gas from the first heat exchanger first passes through a product condensate heat exchanger in which heat energy is transferred to a condensate stream, from there it passes through the first boiler feedwater by transferring heat energy to a boiler feedwater stream, and thereafter it is transferred to the
  • Low-pressure evaporator passed, in which by means of the amount of heat contained low-pressure steam is generated from a boiler feedwater flow, and then the resulting process gas continues through the defined process chain as described above.
  • the process gas from the product condensate heat exchanger first passes through the first boiler feedwater pre-heater where heat energy is transferred to a boiler feedwater stream and is then passed through another product condensate heat exchanger before being directed into the low pressure evaporator from where it is defined Process chain continues to go through.
  • the process gas from the first heat exchanger first passes through a product condensate heat exchanger is transferred in the heat energy to a condensate stream and a partial flow of the boiler feedwater flow, is directed from there into the low-pressure evaporator, in which is generated by means of the amount of heat contained low-pressure steam from a boiler feedwater flow, and the resulting process gas then passes through the defined process chain on.
  • the process gas exiting the first heat exchanger is passed to another boiler feedwater preheater for further heat transfer, comprising a further substream resulting from further division of the second portion of the boiler feedwater stream, the water treatment unit, the pressure increase unit and the second boiler feedwater preheater has happened, is fed and thus continues to be heated.
  • the process gas leaving the first heat exchanger and / or the further boiler feed water is passed into a low-temperature conversion unit in which carbon dioxide and hydrogen is formed, from where it passes into one of the other heat exchanger of the defined process chain.
  • the process gas which has passed through a heat exchanger is subsequently passed through a separator and a resulting liquid stream is separated from the heat-containing process gas and combined with the condensate stream from the cooling section and other separators and this mixture is passed through a unit to increase the pressure and then by a
  • the corresponding device for steam reforming of hydrocarbon-containing starting materials by means of steam suitable to carry out a method according to claim 1, comprising an apparatus sequence for flow with process gas, comprising a high-temperature conversion unit, at least four Heat exchanger, a cooling section, and at least one unit for further processing of the resulting process gas, wherein transitions are provided, which connect the individual devices via the gas outlet and gas inlet for the transfer of the process gas with each other.
  • another heat exchanger in the apparatus for steam reforming are included, another heat exchanger, a water treatment unit, at least two booster units, at least one consumer, a device for introducing a Deionatstroms in the other heat exchanger, a device for transferring the Deionatstroms from the other heat exchanger in the water treatment unit, a device for the transfer of the
  • Low-pressure evaporator comprising a device for transferring a first partial flow of the generated low-pressure steam to the water treatment unit and a further device for transferring a second partial flow of the generated low-pressure steam into the further consumer, and a second supply line for transporting the second part of the
  • Kesselspeisewasserstroms is provided to the other heat exchanger, and from there a supply to the second boiler feedwater pre-heater is derived and from there a discharge to the first boiler feedwater or to a product condensate heat exchanger and / or directly provided for further steam generation, and a device for transferring the condensate flow from the cooling line via a unit is provided for increasing the pressure in one or more product condensate heat exchangers.
  • the apparatus sequence for the flow with process gas comprises a series circuit, a high-temperature conversion unit, a first heat exchanger, a first boiler feedwater pre-heater, a
  • Product condensate heat exchanger a low pressure evaporator, a second boiler feedwater pre-heater, a cooling section and at least one processing gas processing unit, in the order named.
  • the apparatus sequence for the flow through with process gas comprises a series circuit, a high-temperature conversion unit, a first heat exchanger, a first A boiler feedwater pre-heater, a low-pressure evaporator, a product condensate preheater, a second boiler feedwater pre-heater, a refrigeration section, and at least one processing gas-processing unit, in that order.
  • the apparatus sequence for flowing through process gas comprises a series circuit comprising a high temperature conversion unit, a first heat exchanger, a product condensate heat exchanger, a first boiler feedwater pre-heater, a low-pressure evaporator, a second boiler feedwater pre-heater, a cooling section and at least one processing gas processing unit named order.
  • the apparatus sequence for flowing through with process gas comprises a series circuit, a high-temperature conversion unit, a first heat exchanger, a product condensate heat exchanger, a low-pressure evaporator, a second boiler feedwater pre-heater, a cooling section and at least one unit for processing the resulting
  • Process gas in the order mentioned, wherein a device for transferring a first partial flow of the boiler feedwater from the second boiler feedwater is provided in a product condensate heat exchanger and another device for transferring the second partial flow of the boiler feedwater flow from the second boiler feedwater is provided directly for further steam generation.
  • Another possibility of the embodiment of the invention is that another third boiler feedwater is provided in the apparatus sequence for flow with process gas, the gas inlet is connected to the gas outlet of the first heat exchanger and its gas outlet to the gas inlet with an optional low-temperature conversion unit or subsequent heat exchanger is connected, and in which a device for transferring a further partial flow of the boiler feed water, which comes from the water treatment unit and the second boiler feedwater pre-heater opens.
  • a low-temperature conversion unit is provided in the apparatus sequence for the flow of process gas, the gas inlet is connected to the gas outlet of the first heat exchanger or the other third boiler feedwater pre-heater and the gas outlet is connected to a subsequent heat exchanger. It is advantageous in the apparatus sequence for flow through the process gas further separators are provided, the gas inlet is connected to the gas outlet of the respective upstream heat exchanger, and the gas outlet is connected to the in the process chain each subsequent heat exchanger, and each one Have discharge for the resulting liquid, which opens into the device for transferring the condensate stream from the cooling section in a product condensate heat exchanger and is passed through a pressure booster unit.
  • the second boiler feedwater pre-heater is integrated into a separator, which is optionally equipped with further fittings and / or packs, and which is provided with a discharge, the resulting process condensate in the device for the transfer of the condensate stream transported the cooling line in a product condensate heat exchanger.
  • Device is that further additional heat exchangers are provided in the apparatus sequence for flow through the process gas.
  • a further device for dividing the second stream of low-pressure steam may also be provided, so that a supply line for air preheating and a supply line to other consumers are provided.
  • FIG. 1 A process sketch according to the invention of the process for
  • FIG. 2 An alternative integration of the heat exchanger shown in Fig. 1 in the process for heat utilization in the steam reforming of hydrocarbon-containing starting materials by means of steam.
  • Fig. 3 A further advantageous variant of the method for heat utilization in the steam reforming of hydrocarbon-containing starting materials by means of steam, in which the product condensate heat exchanger is passed through with process gas before the first boiler feedwater pre-heater.
  • FIG. 4 Another embodiment of the interconnection of the inserted
  • FIGS. 1 to 3 Heat exchanger with each other.
  • the main difference to FIGS. 1 to 3 is that the first boiler feedwater pre-heater is dispensed with.
  • Fig. 5 A supplementary representation of Fig. 1, by various optional
  • Elements in the process such as a third boiler feed water heater, a low-temperature conversion unit, an optional additional separator and a heat exchanger, are integrated.
  • Fig. 1 shows a process diagram for heat utilization in the steam reforming of hydrocarbon-containing starting materials by means of steam, wherein the resulting heat-containing process gas 1a first passes through a high-temperature conversion unit 2, in which a part of the carbon monoxide is converted to carbon dioxide and hydrogen. The resulting heat-containing process gas 1b is then passed to a first heat exchanger 3 for further heat transfer. Thereafter, the heat-containing process gas 1c undergoes a first boiler feedwater pre-heater 4, the heat contained in the process gas having passed through preheated boiler feed water 14e originating from the water treatment unit 13 and the pressure-increasing unit 25, the heat exchanger 16, and the boiler feedwater pre-heater 8, is transmitted.
  • the deionized 12a is heated in the heat exchanger 16 and the heated deionized 12b is passed to the water treatment unit 13 for degassing.
  • the preheating of the deionized has the advantage that one side of the heat exchanger must be designed only at low pressures and a partial production of low alloy steel is sufficient, resulting in a cost savings.
  • the resulting boiler feedwater stream 14f is then sent for further steam generation processing.
  • the heat-containing process gas 1d resulting from the boiler feedwater preheater 4 is subsequently passed into the product condensate heat exchanger 5, in which it gives off heat to the process condensate 15a, which has passed the pressure increase unit 27 and originates from the cooling section 10.
  • the preheated process condensate 15b is then used for further heating.
  • the process condensate 15a is obtained in separators of the cooling section 10, which is composed for example of an air cooler and a water cooler, and is reheated in a product condensate heat exchanger 5.
  • This method could be carried out in a contact apparatus, which is supplied with water, wherein by direct cooling condenses at least a portion of the water vapor to be separated from the process gas, which is then eliminated with the water used for cooling.
  • the process condensate would be further preheated, which would be an advantage, since the higher the preheating of the process condensate, the more heat can be used in the flue gas for other media and steam generation.
  • the resulting from the product condensate heat exchanger 5 heat-containing process gas 1e is subsequently passed into the low-pressure evaporator 6, in which the heat is transferred to a part of the generated in the water treatment unit 13 boiler feedwater flow 14c, which has experienced an increase in pressure.
  • the low-pressure steam 19a thus obtained is returned to the water treatment unit 13 in a first partial stream 19b, while a second partial stream of the heated boiler feed water 19c is fed into a consumer, here into an air preheater 18, which heats ambient air 17, which then continues to be used as combustion air 20 place.
  • the heat-containing process gas 1f resulting from the low-pressure evaporator 6 is then fed to the boiler feedwater pre-heater 8 by the partial flow 14d of the in the Water treatment unit 13 is further preheated before it is transferred to the boiler feedwater 4.
  • the process gas 1g resulting from the boiler feedwater pre-heater 8 then passes into the cooling section 10, in which the process gas is further cooled and a condensate stream is generated, and the condensate stream 15a is passed into the product condensate heat exchanger 5.
  • FIG. 1 and FIG. 2 differ in that the heat-containing process gas 1d leaving the boiler feedwater preheater 4 first passes through the low-pressure evaporator 6 and then the product condensate heat exchanger 5 thereafter , The other interconnection of the individual appliances remains unaffected. However, it would be better to use the energy better in the variant shown in FIG.
  • FIG. 1 Another embodiment is shown in FIG. Starting from FIG. 1, the difference is that the heat-containing process gas 1 c resulting from the heat exchanger 3 first passes through the product condensate heat exchanger 5 and is subsequently passed through the boiler feed water preheater 4. The other interconnection of the individual apparatus remains unaffected and corresponds to that shown in Fig. 1 apparatus sequence.
  • the boiler feedwater preheater 4 is completely dispensed with.
  • the heat-containing process gas 1c originating from the heat exchanger 3 is led into the product condensate heat exchanger 5, from where the resulting heat-containing process gas 1d passes through the low-pressure evaporator 6 followed by the boiler feedwater pre-heater 8.
  • Boiler feedwater pre-heater 8 generated preheated boiler feed water 14e is divided in this example and a partial flow 14f is added together with the process condensate 15a via the product condensate heat exchanger 5, to then undergo further preheating.
  • the second partial flow 14g of the preheated boiler feed water is given to generate steam.
  • Fig. 5 further optional devices are included in the interconnection, which positively influence the process.
  • the starting point is the description and the illustration of differences from FIG.
  • the heat-containing process gas 1c from the heat exchanger 3 in an additional Boiler feedwater pre-heater 21 is fed, which is fed by a further partial flow 14g of the boiler feedwater flow undergoing preheating in the boiler feedwater pre-heater 8.
  • the resulting heated boiler feed water 14h is also routed to steam production and thus used further.
  • the resulting process gas is eliminated from the
  • Boiler feedwater pre-heater 21 is then passed into a low-temperature conversion unit 22 in which carbon dioxide and hydrogen are formed.
  • the resulting heat-containing process gas 1e then passes through the boiler feedwater preheater 4 and the product condensate preheater 5 as shown in FIG. 1.
  • the process gas 1g resulting from the product condensate preheater 5 subsequently passes into a separator 23 in which an emerging process condensate 15c is separated from the process gas is passed together with the other process condensate streams as process condensate 15d via a unit for pressure increase 27 in the product condensate heat exchanger 5.
  • Low-pressure evaporator 6 and the separator 7 go through.
  • the condensate stream 15e from the separator 7 is also conducted into the product condensate heat exchanger 5 together with the other condensate streams 15d resulting from the overall process.
  • the resulting from the low-pressure evaporator 6 low-pressure steam 19a is divided into three partial streams. It will be described below.
  • Partial flow 19b of the low-pressure steam is passed into the water treatment unit 13, 19c in the air preheater 18 and 19d in further consumers 26. After the separator 7, a further heat exchanger 24 is then connected for further energy transfer. Thereafter, the process chain described in Fig. 1, the boiler feedwater pre-heater 8, the cooling section 10 and the
  • Pressure swing adsorption unit 11 comprises.
  • a further heat exchanger 9 is provided between the boiler feedwater pre-heater 8 and the cooling section 10 in this embodiment.
  • FIG. 6 shows a further variant of FIG. 1.
  • the process condensate stream 15a which originates from the cooling section 10 and is passed via a unit for pressure increase 27 via a further additional product condensate heat exchanger 28 before it passes through the product condensate heat exchanger 5.
  • This has the advantage that the product condensate absorbs even more heat, which can be used in the further process for the heating of other media.
  • the additionally inserted in Fig. 5 apparatuses can be used combined as described in Figure 5, but also be integrated as individual components in the respective process chains.
  • FIG. 1 can serve as the basis of this apparatus integration, but all the figures can serve as the basis of the integration. From this it can be seen that the process offers many options to adapt the respective process to the individual needs of a plant operator and to integrate the corresponding plant components into existing plants. There is also the possibility of implementing these process variants in new plants.
  • the low-pressure evaporator could be equipped with a safety reverse and cool the process gas by generating and blowing off low-pressure steam in the event of shutdown.
  • the generated low-pressure steam can be used in addition to the air preheating and water treatment, as described above, for example, for the CO 2 in a CO 2 process gas scrubbing.
  • the temperature of the generated low-pressure steam is a maximum of 200 ° C.
  • the low-pressure evaporator 6 is dispensed with, as well as the boiler feedwater preheater 8, so that the boiler feedwater stream 14d is conducted directly into the boiler feedwater preheater 4.
  • the present invention positively affects energy utilization compared to this typical interconnection will be shown in the following table. In this case, some of the previously explained figures are used as the basis for the calculations. It is assumed that after the first four series-connected heat exchangers the apparatus sequence for the flow with process gas, a separator is connected. By way of example, a plant capacity of 33455 Nm 3 / h of hydrogen is assumed.
  • the interconnection variant of the invention which is reflected in FIGS. 3 and 6, is associated with a very high energy utilization in comparison to the interconnection typical in the prior art.
  • an increase in the total energy utilization of about 3270 kW is to be expected, which would be lost unused in the typical Verschaltungstine of the prior art.
  • FIGS. 7A to D The conditions on which the calculations are based are shown in FIGS. 7A to D as a graphic function of temperature and energy utilization.
  • the dashed line represents the temperature decrease of the process gas as a function of the energy contained, while the solid line represents the heating behavior of the individual media of the process.
  • the individual process steps represented by the graphs are reflected by the inserted reference numerals also used in the remaining Figures 1 to 6.
  • the further preheating of the process condensate in a product condensate heat exchanger causes more energy from the Flue gas for heating other media is available and can be used to generate steam.
  • the process condensate in the flue gas channel is preheated to boiling.
  • preheating the process condensate by process gas can be dispensed with the conventional heating in the flue gas duct, resulting in a simplification of the process concept.
  • the temperature and pressure conditions in the heat exchanger 16 prevent the risk of steam shock, thereby improving the reliability.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Inorganic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Hydrogen, Water And Hydrids (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

La présente invention porte sur un procédé d'utilisation de chaleur par reformage à la vapeur comprenant une unité de conversion à haute température, un premier échangeur de chaleur, et à la suite d'un dispositif de préchauffage d'eau d'alimentation de chaudière, d'un échangeur de chaleur de condensat produit et d'un évaporateur basse pression, un parcours de refroidissement, dans lequel le gaz de procédé est encore refroidi ensuite et un courant de condensat est produit et est mené à travers au moins une unité de traitement supplémentaire du gaz de procédé résultant. En outre, un courant de déionisation est produit et est mené à travers une unité de préparation d'eau, dans laquelle une première partie du courant d'eau d'alimentation de chaudière est menée dans l'évaporateur basse pression, et la vapeur basse pression générée est séparée et un premier courant partiel de la vapeur basse pression est conduit pour un transfert de chaleur dans l'unité de préparation d'eau et un deuxième courant partiel de la vapeur basse pression est mené dans au moins un consommateur. Une deuxième partie du courant d'eau d'alimentation de chaudière est menée sur un échangeur de chaleur et un ou plusieurs dispositifs de préchauffage d'eau d'alimentation de chaudière et finalement mené à la production de vapeur. Le courant de condensat sortant du parcours de refroidissement est mené sur une unité d'augmentation de pression dans l'échangeur de chaleur de condensat de produit.
EP09748703A 2008-11-10 2009-10-14 Production de gaz de procédé au moyen de récupération de chaleur à partir de chaleur d'échappement à basse température Withdrawn EP2349922A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102008056538A DE102008056538A1 (de) 2008-11-10 2008-11-10 Prozessgaserzeugung mittels Wärmerückgewinnung aus Niedertemperaturabwärme
PCT/EP2009/007368 WO2010051900A1 (fr) 2008-11-10 2009-10-14 Production de gaz de procédé au moyen de récupération de chaleur à partir de chaleur d'échappement à basse température

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EP2349922A1 true EP2349922A1 (fr) 2011-08-03

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US (1) US20110277962A1 (fr)
EP (1) EP2349922A1 (fr)
CN (1) CN102272039A (fr)
BR (1) BRPI0916065A2 (fr)
CA (1) CA2743089A1 (fr)
CO (1) CO6361983A2 (fr)
DE (1) DE102008056538A1 (fr)
EA (1) EA201190010A1 (fr)
MX (1) MX2011004916A (fr)
SG (1) SG171719A1 (fr)
WO (1) WO2010051900A1 (fr)
ZA (1) ZA201104320B (fr)

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US9163827B2 (en) * 2012-11-01 2015-10-20 General Electric Company System and method for using boiler feedwater
EP3124433B1 (fr) * 2015-07-27 2021-09-01 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Procédé de refroidissement de gaz de synthèse
EP3138810B1 (fr) 2015-09-03 2018-04-25 Air Products And Chemicals, Inc. Procédé de production d'hydrogène pour les climats froids
US9556026B1 (en) 2015-09-03 2017-01-31 Air Products And Chemicals, Inc. Hydrogen production process for cold climates
DE102016218438A1 (de) * 2016-09-26 2018-03-29 Thyssenkrupp Ag Verfahren und Anordnung zur Wärmeenergierückgewinnung in Anlagen umfassend wenigstens einen Reformer
CN110986649A (zh) * 2019-12-20 2020-04-10 乔治洛德方法研究和开发液化空气有限公司 合成气热量回收***
CN114735657B (zh) * 2022-04-22 2024-06-07 瑞切尔石化工程(上海)有限公司 一种用于制硫装置的冷凝器及基于克劳斯法的制硫装置、制硫工艺
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CO6361983A2 (es) 2012-01-20
BRPI0916065A2 (pt) 2015-11-10
US20110277962A1 (en) 2011-11-17
ZA201104320B (en) 2012-02-29
CN102272039A (zh) 2011-12-07
MX2011004916A (es) 2011-10-28
DE102008056538A1 (de) 2010-05-12
WO2010051900A1 (fr) 2010-05-14
EA201190010A1 (ru) 2012-02-28
SG171719A1 (en) 2011-07-28
CA2743089A1 (fr) 2010-05-14

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