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EP3891435B1 - Procédé d'utilisation de fumées et système d'utilisation de fumées - Google Patents

Procédé d'utilisation de fumées et système d'utilisation de fumées

Info

Publication number
EP3891435B1
EP3891435B1 EP19813478.5A EP19813478A EP3891435B1 EP 3891435 B1 EP3891435 B1 EP 3891435B1 EP 19813478 A EP19813478 A EP 19813478A EP 3891435 B1 EP3891435 B1 EP 3891435B1
Authority
EP
European Patent Office
Prior art keywords
flue gas
vapours
vapor
temperature
vapors
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.)
Active
Application number
EP19813478.5A
Other languages
German (de)
English (en)
Other versions
EP3891435C0 (fr
EP3891435A1 (fr
Inventor
Gerald GRÜNER
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.)
Standardkessel Baumgarte GmbH
Original Assignee
Standardkessel Baumgarte 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 Standardkessel Baumgarte GmbH filed Critical Standardkessel Baumgarte GmbH
Publication of EP3891435A1 publication Critical patent/EP3891435A1/fr
Application granted granted Critical
Publication of EP3891435C0 publication Critical patent/EP3891435C0/fr
Publication of EP3891435B1 publication Critical patent/EP3891435B1/fr
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/02—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment
    • F23G5/04—Incineration of waste; Incinerator constructions; Details, accessories or control therefor with pretreatment drying
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
    • F23G5/30—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having a fluidised bed
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/001—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for sludges or waste products from water treatment installations
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
    • F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
    • F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2206/00—Waste heat recuperation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2900/00—Special features of, or arrangements for incinerators
    • F23G2900/50213—Preheating processes other than drying or pyrolysis

Definitions

  • the invention relates to a method for utilizing vapors, wherein the vapors are introduced into a flue gas obtained during the combustion of a fuel in a combustion system. Furthermore, the invention relates to a vapor utilization system and a utilization plant.
  • Vapours are gases and/or air saturated with water vapor that are produced during the drying of solids.
  • vapours are produced during the drying of sewage sludge or industrial sludge.
  • vapors are frequently passed through condensers and condensed, whereby the released energy can, in the best case, be used at least partially for a district heating network.
  • the resulting vapor condensate is then usually fed (back) into a wastewater treatment plant or disposed of there.
  • plants that utilize vapors in the manner described above must have a wastewater treatment plant and/or a district heating network.
  • the question of vapor utilization is often a crucial point in the (planned) implementation of a project, especially if the resulting vapor condensate cannot be disposed of/used on-site and must be transported to a recycling facility at great expense.
  • EP 0 883 778 B1 discloses a method and a corresponding device for utilizing vapors. These vapors arise during the drying of sewage sludge. The vapors are introduced into a flue gas obtained from the combustion of the sewage sludge in a combustion system. The vapors are heated before being introduced into the flue gas.
  • the vapors are introduced into a flue gas obtained during the combustion of a fuel in a combustion system.
  • the solid is preferably sewage sludge.
  • flue gas refers here—as usual—to a dispersion of solid and/or liquid suspended particles in a gas obtained from the combustion of a fuel.
  • the fuel is preferably a solid fuel, but liquid and/or gaseous fuels can also be used, in particular a mixture of fuels.
  • liquid and/or gaseous fuels can also be used, in particular a mixture of fuels.
  • coal, natural gas, or preferably other materials suitable for thermal utilization could be used.
  • the dried solid or sludge itself i.e., a dry sludge obtained from the solid or sludge, in particular sewage sludge, during drying, is most preferably used as the fuel.
  • the vapors are now heated to a vapor introduction temperature of at least 500 °C for introduction into the flue gas, ie the process is carried out in a considerably higher vapor introduction temperature range than in the prior art, as will be explained later.
  • the "vapor introduction temperature” refers to the temperature of the vapors during and/or shortly before their introduction into the flue gas. More detailed explanations of the vapor introduction temperature will follow later.
  • the vapors can be fed into an incineration plant with up to 100% residue-free vapor introduction temperatures of more than 350 °C, without significantly lowering the flue gas temperature.
  • the process according to the invention can also be used in plants that neither have a sewage treatment plant nor are connected to a district heating network.
  • the vapor utilization process according to the invention can be used considerably more flexibly than previously known processes.
  • an incineration system such as a sewage sludge mono-incineration plant can operate without wastewater if the resulting vapors are fully utilized.
  • wastewater-free operation allows for site-independent operation, meaning that a sewage treatment plant is not necessarily required to be located in the immediate vicinity of the incineration plant in order to operate it.
  • a vapor utilization system for utilizing vapors obtained during the drying of a solid initially comprises a combustion system for combusting a fuel.
  • a combustion system comprises a plant for combusting or utilizing a fuel, wherein the combustion system can preferably be a fluidized-bed combustion plant, a grate furnace, or a rotary kiln.
  • the vapor utilization system comprises a vapor introduction device for introducing the vapors into the flue gas produced during the combustion of the fuel.
  • a vapor introduction device can comprise at least one vapor line system and, if appropriate, at least one nozzle connected thereto in the combustion system for introducing the vapors into the flue gas, wherein the vapors are preferably introduced entirely into the flue gas.
  • the vapor utilization system comprises a vapor heating device to heat the vapors to a vapor introduction temperature of at least 500 °C before or before they are introduced into the flue gas.
  • a vapor heating device comprises at least one heat exchanger, wherein the heat exchangers are preferably arranged in multiple stages. More detailed explanations of possible designs of such heat exchangers, as well as possible heating media, will be described in more detail later.
  • the vapor heating device can, for example, be part of the vapor introduction device, in which—as will be shown later with examples—heat exchangers or the like are interposed in the vapor line system.
  • the (thermal) energy required to heat the vapors is utilized from the same system to which the vapors are ultimately fed.
  • a large portion of the energy can be recovered through a "heat transfer system.”
  • the heat transfer system is implemented—as explained in detail later—by at least one, but preferably several, heat exchangers connected in series and/or in parallel.
  • a recycling plant or sludge recycling plant according to the invention comprises at least one dryer for the solids and a vapor recycling system according to the invention as described above.
  • the dryer can be connected to the vapor introduction device of the vapor recycling system in order to remove the vapors from the dryer and recycle them as described above.
  • the recycling plant is preferably a sewage sludge recycling plant, and the dryer is accordingly preferably a sewage sludge dryer.
  • the dryer in particular the sewage sludge dryer, is also connected to a fuel feed device of the combustion system of the vapor utilization system via a transport system for the dried (sewage) sludge (dry sludge), for example conveyor belts or the like, so that the dry sludge can be used as fuel to generate energy in the form of heat and, if suitable turbines are available, also electrical energy.
  • a transport system for the dried (sewage) sludge (dry sludge) for example conveyor belts or the like
  • the dry sludge can be used as fuel to generate energy in the form of heat and, if suitable turbines are available, also electrical energy.
  • at least a portion of the energy generated in the combustion system can be used to dry the solids or sludge, in particular sewage sludge, in the dryer or sewage sludge dryer.
  • process heat generated in the combustion system could be fed back to the dryer, preferably the sewage sludge dryer.
  • the invention requires a vapor introduction temperature of at least 500 °C.
  • the vapor introduction temperature is preferably at least 600 °C. At higher temperatures, larger quantities of vapor can be introduced into the flue gas at once without lowering its temperature too drastically.
  • the vapor introduction temperature is preferably at most 900 °C, preferably at most 800 °C, and particularly preferably at most 700 °C. These temperatures can be achieved, for example, by using the energy of the vapor heating system. Flue gas can be achieved without external energy - as will be explained in more detail later.
  • the vapors are introduced into the flue gas at a vapor introduction temperature in the range of 600 °C to 700 °C.
  • This vapor injection temperature range is particularly preferred in mono-combustion plants, i.e., in combustion systems that burn or utilize only one fuel, and particularly preferred in a mono-combustion plant that, as described above, uses only dried sludge, particularly sewage sludge, as fuel.
  • This temperature range is particularly suitable if, as mentioned above, the recycling plant or sewage sludge recycling plant is to be used completely autonomously and all sludge, particularly sewage sludge, and the resulting vapors are to be fully utilized.
  • the vapors could also be partially recycled in another thermal recovery plant using other fuels.
  • lower vapor injection temperatures of more than 350 °C, e.g., at least 360 °C, and no more than 600 °C, might be preferable. This is advisable if the thermal recovery plant is located nearby.
  • the vapors can preferably be heated to the desired vapor introduction temperature by means of thermal energy obtained from the at least partial combustion of the fuel in the combustion system.
  • the vapors can preferably be heated in a vapor heating system, which—as already mentioned at the beginning—can be constructed in several stages, i.e., can include several downstream heat exchangers.
  • a vapor heating system which—as already mentioned at the beginning—can be constructed in several stages, i.e., can include several downstream heat exchangers.
  • the vapors are gradually heated to increasing temperatures in various stages arranged one after the other in terms of the vapor transport path. This will be explained in more detail later using examples.
  • the (thermal) energy required to heat them is used from the same system to which the vapors are ultimately fed.
  • a large portion of the energy can be recovered through a heat transfer system, which can be implemented, for example, with one, but preferably several, heat exchangers.
  • the vapors can also be heated, at least partially, directly in the combustion chamber of an incineration plant.
  • at least a type of "heat exchanger" of the vapor heating device could be arranged directly in the combustion chamber of an incineration plant. If this is the case, this is preferably the aforementioned "final stage” in a multi-stage system, which ultimately heats the vapors to the vapor feed temperature.
  • Figure 1 shows a first embodiment of a sewage sludge utilization plant 100 with a vapor utilization system 9 according to the invention.
  • the sewage sludge utilization plant 100 here comprises a sewage treatment plant 2, which has a sewage sludge dryer 1 in which the recovered sewage sludge CS is dried. This drying process produces dry sludge TS (dried sewage sludge) and vapor B. This can be a conventional sewage sludge dryer 1.
  • a sewage sludge dryer 1 and the associated drying processes are known to those skilled in the art, so no further explanation is required here.
  • the combustion system 4 has a start-up burner 5 to bring the fluidized bed W to a sufficiently high temperature level.
  • the fuel TS is introduced into this fluidized bed W at a high temperature by a feeding device 6, here a throw-away feeder 6, and then burned in the fluidized bed W.
  • the vapor utilization system 9 has a vapor introduction device 18 with a vapor line 17 suitably connected to the sewage sludge dryer 1. Via this vapor line 17, the vapors B are sucked in by a blower 11 of the vapor utilization system 9.
  • a vapor introduction heater 13 (as a "final stage” 13) of the vapor heating device from the intermediate vapor temperature B T3 to a vapor introduction temperature B T4 .
  • This vapor introduction heater 13 or the final stage 13 is designed such that the vapors B reach a vapor introduction temperature B T4 of more than 350 °C, preferably a higher temperature, for example, of at least 600 °C.
  • a valve (not shown) could also be assigned to the final stage 13 in order to control the amount of vapor that is introduced into the flue gas from the final stage 13.
  • the vapors B can be introduced into the flue gas if required, for example temporarily, also with a (lower) vapor temperature, in extreme cases only with the intermediate vapor temperature B T3 , if the final stage is completely bypassed.
  • the vapors B heated to the desired vapor introduction temperature B T4 are fed as described in Figure 1 shown directly into the flue gas R in the "freeboard" 3 of the combustion chamber 7 of the fluidized bed combustion system 4.
  • the flue gas R which is about 870 °C hot, is, as in Figure 1 As shown, the flue gas is discharged from the combustion chamber 7 in the usual manner through a smoke outlet 19 adjoining the top of the combustion chamber 7 and (here in a first pass) passed over a first heating surface 21 to reduce the flue gas temperature. Behind this first heating surface 21, the flue gas temperature is approximately 800 °C.
  • This heating surface 21 is a heat exchanger 21 in which process steam generated in the plant itself is superheated by the flue gas R.
  • This process steam can, for example, be fed in the usual way to a turbine (e.g., a high-pressure turbine) to generate electricity.
  • a turbine e.g., a high-pressure turbine
  • at least a portion of this process steam can also be used as an exchange medium H to preheat the vapors B, as will be explained below.
  • the flue gas R is used to heat the vapours B directly in the vapour introduction heater 13 (i.e. the final stage 13) in a direct heat exchanger between the media "flue gas” and "vap” to the desired very high vapour introduction temperature B T4 .
  • the flue gas temperature is still approximately 600 °C.
  • the flue gas R is cooled again by a downstream heating surface 22.
  • This heating surface 22 can also be a heat exchanger 22, which can also be used to superheat the process steam generated in the plant itself.
  • This superheated process steam can, for example, then first be fed to the aforementioned heat exchanger 21 for further superheating. Depending on the temperature, it can also be fed directly to a turbine to generate electricity. Furthermore, at least a portion of this process steam can also be used as an exchange medium H to preheat the vapors B.

Landscapes

  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Water Supply & Treatment (AREA)
  • Fluidized-Bed Combustion And Resonant Combustion (AREA)

Claims (15)

  1. Procédé de valorisation des vapeurs (B) générées lors du séchage d'une matière solide (KS), préférentiellement d'une boue d'épuration (KS),
    - les vapeurs (B) étant introduites dans un gaz de fumée (R) lequel est généré lors de la combustion d'un combustible (TS) dans un système de combustion (4, 8), et
    - les vapeurs (B) étant chauffées à une température d'introduction de vapeurs (BT4) d'au moins à 500 °C pour être introduire dans les gaz de fumée (R).
  2. Procédé selon la revendication 1, la température d'introduction de vapeurs (BT4) étant d'au moins 600 °C.
  3. Procédé selon les revendications 1 ou 2, la température d'introduction de vapeurs (BT4) étant d'au plus 900 °C, de préférence d'au plus 800 °C et, avec une préférence particulière, d'au plus 700 °C.
  4. Procédé selon l'une des revendications précédentes, les vapeurs (B) étant introduites dans les gaz de fumée (R) à une température de gaz de fumée d'au moins 900 °C et/ou d'au plus 950 °C.
  5. Procédé selon l'une des revendications précédentes, les vapeurs (B) étant introduites dans les gaz de fumée (R) de manière à ce que, suite à l'introduction des vapeurs (B), les gaz de fumée (R) présentent une température d'au moins 850 °C.
  6. Procédé selon l'une des revendications précédentes, les vapeurs (B) étant introduites dans les gaz de fumée (R) au sein d'une chambre de combustion (7) du système de combustion (4, 8).
  7. Procédé selon l'une des revendications précédentes, les vapeurs (B) étant introduites dans les gaz de fumée (R) dans la zone d'un espace libre (3) située au-dessus d'un lit fluidisé (W) et/ou au niveau d'un organe d'alimentation en air secondaire.
  8. Procédé selon l'une des revendications précédentes, les vapeurs (B) étant réchauffées, préalablement à leur introduction dans les gaz de fumée (R), à une température d'introduction de vapeurs (BT4) en mettant en œuvre de l'énergie thermique produite par la combustion du combustible (TS) dans le système de combustion (4, 8),
    le réchauffement des vapeurs (B) étant réalisé de préférence, au moins partiellement, au moyen de gaz de fumée (R) du système de combustion (4, 8).
  9. Procédé selon la revendication 8, le réchauffement des vapeurs (B) étant réalisé, au moins partiellement, au moyen de gaz de fumée (R) du système de combustion (4, 8) lesquels sont mis en œuvre directement.
  10. Procédé selon les revendications 8 ou 9, le réchauffement des vapeurs (B) au moyen de gaz de fumée (R) du système de combustion (4, 8) étant réalisé, au moins partiellement de manière indirecte à travers un milieu d'échange (H).
  11. Procédé selon les revendications 8 ou 10, le réchauffement des vapeurs jusqu'à la température d'introduction de vapeurs (BT4) et/ou du milieu d'échange (H) jusqu'à une température de chauffe étant réalisé au moyen de gaz de fumée (R) dont la température de gaz de fumée est d'au plus 980 °C.
  12. Procédé selon l'une des revendications précédentes, le réchauffement des vapeurs (B) et/ou du milieu d'échange (H) étant réalisé, au moins partiellement, en dehors de la chambre de combustion (7) du système de combustion (4, 8).
  13. Système de valorisation des vapeurs (9) permettant de valoriser les vapeurs (B) qui sont générées lors du séchage d'une matière solide (KS), préférentiellement d'une boue d'épuration (KS), comportant
    - un système de combustion (4, 8) destiné à brûler un combustible (TS),
    - un dispositif d'introduction de vapeurs (18), disposé de manière à permettre d'introduire les vapeurs (B) dans des gaz de fumée (R) générés lors de la combustion du combustible (TS)
    et
    - un dispositif de réchauffement de vapeurs (14), disposé de manière à permettre de réchauffer les vapeurs (B) à une température d'introduction de vapeurs (BT4) d'au moins 500 °C, afin de les introduire dans les gaz de fumée (R).
  14. Système de valorisation de vapeurs (9) selon la revendication 13, le dispositif de réchauffement de vapeurs (14) comprenant au moins un échangeur de chaleur (13) dans lequel on met en œuvre les gaz de fumée (R) de manière directe pour réchauffer les vapeurs (B) à la température d'introduction de vapeurs (BT4) souhaitée.
  15. Installation de valorisation (100), de préférence installation de valorisation de boues d'épuration (100), comportant un dispositif de séchage (1), s'agissant préférentiellement d'un dispositif de séchage de boues d'épuration (1), et un système de valorisation de vapeurs (9) selon les revendications 13 ou 14.
EP19813478.5A 2018-12-05 2019-11-29 Procédé d'utilisation de fumées et système d'utilisation de fumées Active EP3891435B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102018131058.7A DE102018131058A1 (de) 2018-12-05 2018-12-05 Verfahren zur Brüdenverwertung und Brüdenverwertungssystem
PCT/EP2019/083088 WO2020114906A1 (fr) 2018-12-05 2019-11-29 Procédé d'utilisation de fumées et système d'utilisation de fumées

Publications (3)

Publication Number Publication Date
EP3891435A1 EP3891435A1 (fr) 2021-10-13
EP3891435C0 EP3891435C0 (fr) 2025-07-23
EP3891435B1 true EP3891435B1 (fr) 2025-07-23

Family

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Family Applications (1)

Application Number Title Priority Date Filing Date
EP19813478.5A Active EP3891435B1 (fr) 2018-12-05 2019-11-29 Procédé d'utilisation de fumées et système d'utilisation de fumées

Country Status (3)

Country Link
EP (1) EP3891435B1 (fr)
DE (1) DE102018131058A1 (fr)
WO (1) WO2020114906A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113915630B (zh) * 2021-09-18 2023-10-13 宁夏滨泽新能源科技有限公司 一种具有回收功能的化工尾气处理装置

Citations (3)

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Publication number Priority date Publication date Assignee Title
EP0832856A2 (fr) * 1996-09-26 1998-04-01 Andritz-Patentverwaltungs-Gesellschaft m.b.H. Procédé de séchage de matériaux indirectement chauffés, notamment de boues d'égout
EP0883778B1 (fr) * 1995-08-26 2001-05-16 L. & C. Steinmüller GmbH Procede d'incineration de boues d'epuration et installation correspondante
DE102016213954A1 (de) * 2016-07-28 2018-02-01 Floradry Gmbh Gestufte Feuerung

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Publication number Priority date Publication date Assignee Title
DE967629C (de) * 1950-08-27 1957-11-28 Gerhard Baumeister Anlage zum Trocknen und Verbrennen von Schlamm und zur Geruchsvernichtung der Brueden
DE4121968A1 (de) * 1991-06-28 1993-01-14 Noell K & K Abfalltech Verfahren zur kombinierten klaerschlamm- und muellverbrennung
DE19954764C1 (de) * 1999-11-15 2001-08-09 Roland Luecke Verfahren zur Aufarbeitung von ammoniakhaltigen Abgasen
DE10123402A1 (de) * 2001-05-14 2002-11-28 Fraunhofer Ges Forschung Verfahren zum Behandeln von ammoniakhaltigen Rauchgasen
DE102016213582A1 (de) 2016-07-25 2018-01-25 MaXXcon Energie GmbH & Co. KG Verwendung von bei einer Trocknung eines Schlamms entstehenden ammoniakhaltigen Brüden und Verfahren zur Verbrennung eines Schlamms

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0883778B1 (fr) * 1995-08-26 2001-05-16 L. & C. Steinmüller GmbH Procede d'incineration de boues d'epuration et installation correspondante
EP0832856A2 (fr) * 1996-09-26 1998-04-01 Andritz-Patentverwaltungs-Gesellschaft m.b.H. Procédé de séchage de matériaux indirectement chauffés, notamment de boues d'égout
DE102016213954A1 (de) * 2016-07-28 2018-02-01 Floradry Gmbh Gestufte Feuerung

Also Published As

Publication number Publication date
EP3891435C0 (fr) 2025-07-23
EP3891435A1 (fr) 2021-10-13
WO2020114906A1 (fr) 2020-06-11
DE102018131058A1 (de) 2020-06-10

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