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WO1999050599A1 - Procede d'incineration - Google Patents

Procede d'incineration Download PDF

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Publication number
WO1999050599A1
WO1999050599A1 PCT/CA1999/000245 CA9900245W WO9950599A1 WO 1999050599 A1 WO1999050599 A1 WO 1999050599A1 CA 9900245 W CA9900245 W CA 9900245W WO 9950599 A1 WO9950599 A1 WO 9950599A1
Authority
WO
WIPO (PCT)
Prior art keywords
furnace
heating
enclosure
compound
vapours
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.)
Ceased
Application number
PCT/CA1999/000245
Other languages
English (en)
Inventor
Jan Strmen
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.)
Individual
Original Assignee
Individual
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
Priority claimed from CA 2233475 external-priority patent/CA2233475A1/fr
Application filed by Individual filed Critical Individual
Priority to AU28236/99A priority Critical patent/AU2823699A/en
Publication of WO1999050599A1 publication Critical patent/WO1999050599A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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
    • 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
    • F23G7/008—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals for liquid waste
    • 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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/102—Combustion in two or more stages with supplementary heating
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2202/00—Combustion
    • F23G2202/10—Combustion in two or more stages
    • F23G2202/103—Combustion in two or more stages in separate chambers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
    • F23G2208/00—Safety aspects
    • F23G2208/10—Preventing or abating fire or explosion, e.g. by purging
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2217/00—Intercepting solids
    • F23J2217/50—Intercepting solids by cleaning fluids (washers or scrubbers)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J2219/00—Treatment devices
    • F23J2219/40—Sorption with wet devices, e.g. scrubbers

Definitions

  • This invention relates to a process and apparatus for incinerating certain volatile organic compounds especially odorants commonly used in the natural gas industry.
  • odorant as used in the natural gas industry refers to chemicals such as dimethyl sulfide, methyl ethyl sulfide, isopropyl mercaptan, normal propyl mercaptan, secondary butyl mercaptan, ethyl mercaptan, tetrahydrothiophene, and similar compounds.
  • odorant as used in the natural gas industry refers to chemicals such as dimethyl sulfide, methyl ethyl sulfide, isopropyl mercaptan, normal propyl mercaptan, secondary butyl mercaptan, ethyl mercaptan, tetrahydrothiophene, and similar compounds.
  • the above are all organic compounds containing sulfur, with an easily distinguishable odor used to odorize natural gas. All of these are volatile liquids.
  • Dismantling of contaminated metal containers has to be done in inert atmosphere or using other tools not generating sparks or open flame.
  • An object of the present invention is to provide for the safe and complete destruction of certain volatile organic compounds especially such compounds when disposed in metal containers.
  • Another object is to provide a multistage process, which separates evaporation from incineration and allows for safe, complete and environmentally sound destruction of these volatile organic compounds.
  • the process is believed to be superior in these respects from existing chemical or other thermal methods of destruction.
  • a process for the destruction of volatile organic compound(s) in accordance with the invention in one aspect comprises:
  • step (b) conducting the vapours of said compound(s) generated by heating step (a) from the first enclosure to a second enclosure and incinerating said vapour in the second enclosure.
  • the heating in step (a) effects a controlled temperature increase under conditions wherein there is insufficient oxygen to support combustion of said vapours in the first enclosure.
  • said compound(s) are in the form of a residue in a closed metal container with said metal container being positioned in said first enclosure prior to the heating in step (a) and connected to a system capable of conducting said vapours generated by heating step (a) from the interior of the metal container to the second enclosure.
  • the process includes the step of supplying inert gases under pressure to the interior of said metal container prior to commencement of heating step (a) and releasing the pressurized gases into said second enclosure prior to effecting heating step (a).
  • said heating step (a) preferably comprises gradually raising the temperature in said first enclosure to initially evaporate the lower boiling and more volatile compound(s) with evaporation of higher boiling compound(s) following thereafter as the temperature is raised to and held at higher levels for selected periods of time to complete the evaporation and to decompose and/or carbonize any remaining said compounds.
  • said first enclosure comprises a furnace having a heating means therein to generate the desired temperatures to effect said evaporation and wherein said second enclosure comprises a primary furnace wherein incineration of the vapours released during heating step (a) is effected.
  • the process also typically includes the step of passing combustion products from said primary furnace through an afterburner to complete the combustion process followed by scrubbing.
  • the compounds referred to above may comprise sulfur-containing odorants for natural gas as well as numerous other volatile organic materials.
  • Typical odorants include dimethyl sulfide, methyl ethyl sulfide, isopropyl mercaptan, normal propyl mercaptan, secondary butyl mercaptan, ethyl mercaptan, tetrahydrothiophene, and similar compounds.
  • the process of the invention is particularly advantageous for volatile substances such as mercaptans, other sulfur containing solvents and solvents in general, where temperature control of and subsequent feed control into the primary furnace must be strictly regulated. Temperature control, combustion products control, proper connection of treated containers to the primary furnace as well as safety features including the controlling of temperatures, pressures in treated containers and feed rates are important practical considerations.
  • Apparatus for the destruction of volatile organic compounds in accordance with a further aspect of the invention includes:
  • said first furnace has a heating means therein to generate the desired temperatures to effect said evaporation and said second furnace comprises a primary furnace having a supply of free -5- oxygen thereto and wherein incineration of the vapours released during the heating in the first furnace is effected.
  • said compound(s) are typically in the form of residues in a closed metal container with said first furnace being adapted to receive said metal container therein prior to the heating thereof, said vapour transporting system being capable of being attached to the metal container for conducting said vapours from the interior of the metal container to the second furnace.
  • a further feature of the invention is the use of a manifold system adapted to supply inert gases to the interior of said metal container to pressurize same prior to said heating, said vapour transporting system being adapted to subsequently release the pressurized inert gases into said second furnace also prior to commencement of the heating in said first furnace.
  • An afterburner through which combustion products from said primary furnace are passed to complete the combustion process is also a part of the preferred form of the equipment.
  • the preferred apparatus used includes a first (car bottom) furnace as a heating chamber, where precise temperature control during both low and high temperature process stages ensures a safe and controlled feed of volatile substances into a second (primary) furnace for incineration.
  • the combustion process is completed in an afterburner and all generated gases are scrubbed in a conventional wet scrubber.
  • the preferred form of the invention thus combines evaporation of the residual organic compounds from contaminated containers and subsequent high temperature treatment destroying all remnants of these compounds in the same furnace system.
  • the process provides for the combination of a low temperature treatment (e.g. 50 -200°C depending on the boiling range of the compounds) for evaporating volatile organic compounds from the containers followed by high temperature treatment (e.g.
  • Fig. 1 is a flow chart depicting the main steps in the process
  • Fig. 2 is a plan view showing the layout of the main pieces of equipment used
  • Fig. 3 is an elevation view of the equipment shown in Fig. 2;
  • Fig. 4 is a diagrammatic view showing connections between the manifold and tanks to be decontaminated
  • Fig. 5 is a schematic of the manifold system
  • Fig. 6 is a schematic view of the furnace temperature control system
  • Phases la and lb comprise evaporation and decomposition without combustion.
  • Heating of containers containing odorants and/or other odorant residues at temperatures below approximately 150°C is effected in a car bottom furnace to evaporate the odorant through a manifold (into the next phase, i.e. the primary furnace) without sufficient oxygen to support combustion or other chemical reactions which would otherwise generate excess heat and pressure; (since most odorants autoignite at approximately 200°C, a temperature of not exceeding about 150°C was chosen as a maximum evaporation temperature in phase la to effect evaporation while avoiding autoignition and possible -7- explosion).
  • Controlled heating of the containers of odorant and their residues from below or about 150°C up to about 600°C is effected.
  • the purpose of this stage is to continue evaporation and decomposition of odorants in the enclosed container in a non-combustion supporting environment prior to incineration.
  • Phases 2a and 2b involve incineration, afterburning and scrubbing.
  • the incinerated gases are directed from the primary furnace to the afterburner, completing the incineration process at about 980°C. Finally all gases go through a wet scrubbing process to remove SOx, particulate material, and/or any other acidic gas components using sodium hydroxide as the neutralizing agent.
  • a car-bottom furnace 10 (e.g. as manufactured by United Group Inc.of Topeka, Kansas) mounted on tracks 12 so that the furnace 10 may be rolled into and out of loading and operating positions.
  • Furnace 10 has an access door 14 at one end for loading and unloading of metal containers T (Fig. 4).
  • An exhaust stack 16 vents combustion products generated by the gas-fired heaters disposed within furnace 10.
  • Car bottom furnace 10 is equipped with 12 gas-fired burners B, 6 on the top of the furnace and six on the lower part to allow temperature control and heat distribution.
  • the control system of Fig. 6 effects the operation of the burners B in well-known fashion to achieve the desired result.
  • the control system of Fig. 6 may be of a standard commercially -8- available variety and includes a computerized process controller C receiving inputs from sensors CEM1 and CEM2 and temperature sensors Tl and T2 all located as indicated in Fig. 3.
  • Process controller C is programmed to produce outputs to the burner controls to control the temperature in the car bottom furnace in a manner to be described more fully hereafter.
  • a second furnace 20 termed the primary furnace (e.g. by United Group Inc.) is positioned a short distance from the car bottom furnace 10 when the latter is in the operating position and a manifold system 22 (Fig. 2) extends between them.
  • Primary furnace 20 is provided with a conventional gas burner and temperature controls (not shown) capable of maintaining temperatures of about 500-1200° C as required.
  • Manifold system 22 includes a nitrogen manifold 24 and a feedline manifold 26 (Fig. 4).
  • Nitrogen manifold 24 supplies nitrogen gas to the interiors of the containers T as described hereafter.
  • Feedline manifold 26 carries vaporized gases from the containers into the primary furnace 20 during operation..
  • Combustion products leaving the primary furnace 20 pass into a conventional afterburner 28 (Fig. 2) where combustion of gases is completed, with the exhaust gases thence passing through a scrubbing system including a quench and opposed blade venturi system 30 (e.g. by Anderson 2000 Inc. of
  • FIG. 4 the containers T containing the contaminants to be destroyed are loaded into the car bottom furnace 10 and positioned on cradles 36. Each container T has an inlet and an outlet opening 38 and 40 respectively. Inlets 38 are connected by metal piping 38a to nitrogen manifold 24 while outlets 40 are connected via metal pipes 40a to the feedline manifold 26 which -9- supplies the vaporized compounds to primary furnace 20.
  • Temperature control in car bottom furnace 10 allows controlled evaporation of organic solvents and regulates the feed of vapors into primary furnace 20 for incineration. As the temperature in the car bottom furnace 10 increases, higher boiling solvents are evaporated into primary furnace 20. As the content of low boiling solvents in containers T decreases, the temperature in car bottom furnace 10 is increased in increments to evaporate higher boiling solvents and pass same into primary furnace 20.
  • the temperature in the second (phase lb) part of the treatment is increased in 10°C increments up to about 300°C and above 300°C in about 30°C increments.
  • the temperature is raised in these increments generally up to about 600°C.
  • Containers T are kept at this temperature for at least an hour, or -10- until all residues of volatile components are incinerated.
  • the process temperature can be raised up to about 1000°C, in the event such temperatures are needed to purge low volatility high boiling components.
  • the treated containers T are then cooled down to ambient temperature, tested for volatile gases and then approved for dismantling, cutting and transport to metal recyclers.
  • Figs. 4 and 5 the containers T to be treated are placed on the cradles 36 of the car bottom furnace 10 and connected through valves 51 and 53, 54 (in lines 38a) to the nitrogen source. Valves 57 and 58 in lines 40a connect containers T to the feedline manifold 26, leading to the primary furnace 20. With valves 51, 53 and 57 open and valves 50, 52, 54, 55, 56, 58, 59, 60 and 61 closed, the nitrogen pressurizes container Tl to about 5-10 psi. Pressure gauge G on feed manifold 26 (Fig.4) indicates the pressure in the container Tl. Container Tl is kept at this pressure for 5 minutes.
  • the second step of the procedure i.e. release of the pressure into primary furnace 20 is to check to ensure free passage of gases through the system during operation, which prevents pressure build-up in container Tl .
  • This step for container Tl requires that nitrogen supply valves 51, 53 be closed and that valves 57, 60, 65 and 66 (Fig.5) be open to release the gases into primary furnace 20.
  • Container T2 is then tested for pressure and the pressure released using essentially the same procedure but using different valves as required.
  • the feed rate of evaporating solvents into primary furnace 20 is monitored as noted above by sensing the temperature of the primary furnace 20 and/or by the use of the SOx monitor in the afterburner stack, which indicates the concentration of the sulfur containing odorants being fed into the primary furnace 20.
  • the feed rate into primary furnace 20 is controlled by the control system of Fig.6 which varies the temperature setting in the car bottom furnace 10 by varying the temperature settings or number and positions of burners being fired.
  • the treated containers are kept at a low temperature, not exceeding about 150°C, until the sensed levels or SOx begin to decrease, thus indicating completion of the low temperature phase la .
  • the treated container(s) T still however contain vapors of evaporated solvents and these are further evaporated and incinerated in the subsequent high temperature phase lb.
  • more burners are switched on by the control system and the temperature in the car bottom furnace 10 is raised in increments of about 10°C.
  • the indication point for the next temperature increase is, again, a decreasing measured level of SOx in the afterburner stack and/or a decrease in the temperature of the primary furnace 20.
  • the temperature in the primary furnace 20 is generally constant, unless other sources of heat energy from car bottom furnace 10 are introduced.) If these compounds are present both SOx levels and temperatures must decrease before increasing the temperature in the primary furnace.
  • the process can be finished by raising the car bottom temperature to 600°C. Tanks/containers are typically kept at this temperature for one hour. The tanks are cooled then in the furnace, and after testing for presence of volatile compounds, (which test must prove the absence of these compounds), the tanks are cut and the metal is sent for recycling.
  • Peerless metal odorizer tanks containing liquid residues of odorant, consisting of tertiary butyl mercaptan, methylethylsulfide and accumulated higher boiling hydrocarbons.
  • the phase 1 a treatment is started by switching two burners of the car bottom furnace on and letting the temperature rise slowly, (within 90-120 minutes) up to 150°C at the stack entry. During this slow temperature rise, tertiary butylmercaptan and methylethylsulfide (boiling range 62 - 70°C) are evaporated slowly into the primary furnace. The feed is controlled by switching off burners, lowering temperature settings, or changing the positions of burners being -used in the car bottom furnace.
  • both tertiary butyl mercaptan, methylethyldisulfide and any low boiling hydrocarbons are evaporated into the primary furnace and only their vapors, (corresponding to the temperature of car bottom furnace) are present in the container T. SOx levels in afterburner and the temperature in the primary furnace then decrease indicating the end of the low temperature phase la (due to the reduced flow of vapors into the primary furnace).
  • the temperature in the car bottom furnace is initially raised by increments of 10°C.
  • the indication for the next temperature increase is a decreasing level of measured SOx and temperature in the primary furnace.
  • the primary reason for such a low rate of increase of the temperature is to avoid rapid decomposition of the remaining hydrocarbons in liquid or solid form, which would otherwise tend to overload the system.
  • Containers T are kept at final, 600°C temperature for at least an hour, or until all gases are evaporated and purged out of containers at this temperature. Final inspection of cut and dismantled tanks shows no residues inside of the containers, except for occasional, small amounts of carbonized material.
  • Example No.2
  • Pressure testing is performed on each tank separately as described above and if successful and complete, (with the primary furnace, afterburner and scrubber in operational mode) treatment is started. Temperature is raised slowly (within 90-120 minutes) up to 150° C at the stack entry.
  • kerosene, odorants and parts of other hydrocarbons are evaporated into the primary furnace for incineration.
  • the feed is controlled by the process_controller by switching off burners, changing temperature settings, or positions of burners used.
  • a temperature of 150°C most of the low boiling hydrocarbons are evaporated into the primary furnace. Higher boiling components are slowly being evaporated. SOx levels in the afterburner and the temperature in the primary furnace then decrease indicating the end of the low temperature stage.
  • phase lb temperature in the car bottom furnace is raised by increments of 10°C.
  • the indication for the next temperature increase is a decreasing level of SOx and decreasing temperature in the primary furnace.
  • the containers are kept at a final, 600°C temperature for at least an hour, or until all gases are evaporated and purged out of the containers at this temperature.
  • Final inspection of cut and dismantled tanks shows no residues inside of the containers except for occasional, small amounts of carbonized material.

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  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Developing Agents For Electrophotography (AREA)
  • Processing Of Solid Wastes (AREA)

Abstract

L'invention concerne un procédé et un appareil d'incinération de certains composés volatils organiques, notamment les odorisants couramment utilisés dans l'industrie du gaz naturel. Le procédé fait appel à un premier four (10) (à sole roulante) comme chambre de combustion dans laquelle une régulation précise de la température pendant les étapes du processus, tant les étapes à température élevée que les étapes à température réduite, garantit une introduction maîtrisée et sans risques des substances volatiles dans un second four (20) (primaire) pour procéder à leur incinération. Le processus de combustion s'achève dans un brûleur (28) à postcombustion et tous les gaz produits sont épurés dans un épurateur (30) par voie humide.
PCT/CA1999/000245 1998-03-27 1999-03-25 Procede d'incineration Ceased WO1999050599A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AU28236/99A AU2823699A (en) 1998-03-27 1999-03-25 Incineration process

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
CA 2233475 CA2233475A1 (fr) 1998-03-27 1998-03-27 Procede d'incineration
CA2,233,475 1998-03-27
CA2,234,200 1998-04-06
CA 2234200 CA2234200A1 (fr) 1998-03-27 1998-04-06 Procede d'incineration

Publications (1)

Publication Number Publication Date
WO1999050599A1 true WO1999050599A1 (fr) 1999-10-07

Family

ID=25680110

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CA1999/000245 Ceased WO1999050599A1 (fr) 1998-03-27 1999-03-25 Procede d'incineration

Country Status (3)

Country Link
AU (1) AU2823699A (fr)
CA (1) CA2234200A1 (fr)
WO (1) WO1999050599A1 (fr)

Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3639111A (en) * 1969-01-30 1972-02-01 Univ California Method and apparatus for preventing formation of atmospheric pollutants in the combustion of organic material
US4951583A (en) * 1989-07-27 1990-08-28 Mcgill Environmental Systems, Inc. Thermal destruction system for toxic substances
EP0437666A1 (fr) * 1989-09-08 1991-07-24 Paul H. Dr. Kydd Ensemble d'élimination des déchets solides
US5233933A (en) * 1991-03-25 1993-08-10 The United States Of America As Represented By The Administrator Of The Environmental Protection Agency Method of reducing transient emissions from rotary kiln incinerators and container for attaining the same
US5471937A (en) * 1994-08-03 1995-12-05 Mei Corporation System and method for the treatment of hazardous waste material

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3639111A (en) * 1969-01-30 1972-02-01 Univ California Method and apparatus for preventing formation of atmospheric pollutants in the combustion of organic material
US4951583A (en) * 1989-07-27 1990-08-28 Mcgill Environmental Systems, Inc. Thermal destruction system for toxic substances
EP0437666A1 (fr) * 1989-09-08 1991-07-24 Paul H. Dr. Kydd Ensemble d'élimination des déchets solides
US5233933A (en) * 1991-03-25 1993-08-10 The United States Of America As Represented By The Administrator Of The Environmental Protection Agency Method of reducing transient emissions from rotary kiln incinerators and container for attaining the same
US5471937A (en) * 1994-08-03 1995-12-05 Mei Corporation System and method for the treatment of hazardous waste material

Also Published As

Publication number Publication date
AU2823699A (en) 1999-10-18
CA2234200A1 (fr) 1999-09-27

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