US20060048514A1 - Process for the extraction of energy from flue gases - Google Patents

Process for the extraction of energy from flue gases Download PDF

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Publication number
US20060048514A1
US20060048514A1 US10/541,062 US54106205A US2006048514A1 US 20060048514 A1 US20060048514 A1 US 20060048514A1 US 54106205 A US54106205 A US 54106205A US 2006048514 A1 US2006048514 A1 US 2006048514A1
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Prior art keywords
heat exchange
flue gases
heat
exchange step
fresh air
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Abandoned
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US10/541,062
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English (en)
Inventor
Denise Bakker
Bernard Koeyvoets
Franciscus Moonen
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DSM IP Assets BV
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DSM IP Assets BV
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Assigned to DSM IP ASSETS B.V. reassignment DSM IP ASSETS B.V. ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: MOONEN, FRANCISCUS JOSEPHUS, BAKKER, DENISE MARIAN, KOEYVOETS, BERNARD GEERT MARIE
Publication of US20060048514A1 publication Critical patent/US20060048514A1/en
Abandoned legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23L—SUPPLYING AIR OR NON-COMBUSTIBLE LIQUIDS OR GASES TO COMBUSTION APPARATUS IN GENERAL ; VALVES OR DAMPERS SPECIALLY ADAPTED FOR CONTROLLING AIR SUPPLY OR DRAUGHT IN COMBUSTION APPARATUS; INDUCING DRAUGHT IN COMBUSTION APPARATUS; TOPS FOR CHIMNEYS OR VENTILATING SHAFTS; TERMINALS FOR FLUES
    • F23L15/00—Heating of air supplied for combustion
    • F23L15/04—Arrangements of recuperators
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07D—HETEROCYCLIC COMPOUNDS
    • C07D251/00—Heterocyclic compounds containing 1,3,5-triazine rings
    • C07D251/02—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings
    • C07D251/12—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members
    • C07D251/26—Heterocyclic compounds containing 1,3,5-triazine rings not condensed with other rings having three double bonds between ring members or between ring members and non-ring members with only hetero atoms directly attached to ring carbon atoms
    • C07D251/40—Nitrogen atoms
    • C07D251/54—Three nitrogen atoms
    • C07D251/56—Preparation of melamine
    • 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
    • F28D21/0001—Recuperative heat exchangers
    • F28D21/0003—Recuperative heat exchangers the heat being recuperated from exhaust gases
    • F28D21/001—Recuperative heat exchangers the heat being recuperated from exhaust gases for thermal power plants or industrial processes
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/34—Indirect CO2mitigation, i.e. by acting on non CO2directly related matters of the process, e.g. pre-heating or heat recovery

Definitions

  • the invention relates to a process for the extraction of energy from flue gases of a furnace which is operated with a fuel and which is used in a process for the production of melamine, the process comprising a first heat exchange step in which the flue gases are heat exchanged with a first process stream.
  • Such a process is known and is applied in many processes for the production of melamine.
  • the furnace is a salt furnace.
  • Fresh air and natural gas as fuel are supplied to burners.
  • flue gases are formed.
  • the flue gases are heat exchanged with a first process stream, i.e. molten salt.
  • energy is additionally extracted in the known process from the flue gases by means of heat exchange with fresh air; the heated air is subsequently fed to the burners of the furnace.
  • Energy efficiency is defined as the percentage of the energy released in the combustion of fuel that is absorbed by a particular stream or streams or by a total of streams.
  • the known process has the disadvantage that the heated air fed to the furnace leads to increased NO x emission in comparison with a furnace in which the fresh air is not preheated.
  • the increase in NO x emission as a result of the heated fresh air is observed with all types of burner.
  • the undesired increase in NO x emission can admittedly be limited by separating a proportion of the flue gases, combining that proportion with fresh air and thus heating a mixture of fresh air and recirculated flue gases and feeding it to the burners of the furnace.
  • the NO x emission remains undesirably high;
  • the NO x emission in the flue gases of the known process is generally 110 mg/Nm 3 or higher.
  • the unit Nm 3 stands for the volume of a gas under standardized conditions of pressure and temperature. These conditions are 273K and 0.1013 MPa.
  • the said object is attained by the flue gases being heat exchanged in a second heat exchange step with a second process stream.
  • An advantage of the process according to the invention is that the NO x emission decreases in comparison with the known process, while the combination of the first with the second heat exchange step allows energy to be efficiently extracted from the flue gases.
  • a furnace here means a furnace which is heated essentially with the aid of combustion; the fuels will in practice usually be natural gas or oil, although the process according to the invention is not limited thereto.
  • the furnace is used in a process for the production of melamine.
  • “Use” means that the energy which is released in the furnace is used as process heat.
  • An example of an application of process heat is heating the reactor in which melamine is prepared from urea in an endothermic reaction.
  • a process for the production of melamine here refers to any possible process. Examples of known processes for the production of melamine are described in for example Ullmann's Encyclopedia of Industrial Chemistry, Sixth Edition, 2001, Chapter ‘Melamine and Guanamines’, section 4.
  • Flue gases here refers to combustion gases resulting from the combustion of a fuel such as natural gas or oil.
  • the flue gases have a high temperature, usually of 600° C. to 800° C. to 1000° C., or even up to 1200° C. or higher.
  • Heat exchange may be direct; this means that the flue gases exchange heat with the process stream to be heated via at the most a fixed partition. Heat exchange may also be indirect; this means that the flue gases exchange heat with a heat transfer medium, after which the heat transfer medium is heat exchanged with the process stream to be heated in a separate heat exchange step.
  • heat transfer media are molten salt, Dowtherm® and steam.
  • a process stream here refers to a stream which is used or consumed in a process for the production of melamine.
  • a process stream are: feedstock streams such as urea; auxiliary streams such as ammonia, air in a pneumatic transport system, molten salt, Dowtherm, steam, boiler feedwater; reactor effluent and all downstream streams such as off-gases, melamine slurry, wet melamine crystals; sidestreams such as mother liquor. Fresh air for combustion in the furnace does not fall under the definition of a process stream.
  • the first and second process streams as meant in the process according to the invention will in general be two different process streams; however, they may also be one and the same stream.
  • the flue gases In order to obtain a high energy efficiency from the said first and second heat exchange steps it will usually be necessary to cool the flue gases to a relatively low temperature, for example to 350° C. to 300° C. or lower, say, 250° C. or even to 200° C. or lower. This can be accomplished using processes known per se.
  • An example of this is a combination of successive heat exchange steps with each subsequent heat exchange step delivering energy to a process stream at a lower temperature level.
  • An example of such a combination of heat exchange steps is the heating in the first heat exchange step of molten salt from approximately 420° C. to approximately 450° C., followed by the heating in the second heat exchange step of ammonia from approximately 150° C. to approximately 400° C.
  • Another example of such a combination of the first and the second heat exchange steps is heating molten salt from approximately 420° C. to approximately 450° C., followed by the heating of Dowtherm from 200° C. to 350° C.
  • a further example of such a combination of the first and the second heat exchange steps is heating ammonia from approximately 250° C. to approximately 450° C., followed by heating urea from approximately 135° C. to approximately 250° C.
  • the temperature of the flue gases can fall to such an extent that the energy efficiency in the process according to the invention is higher than 85%, preferably higher than 88%, more preferably higher than 90%, still more preferably higher than 92%, most preferably higher than 94%.
  • An energy efficiency up to 99.5% will be possible, although this will require considerable effort; an efficiency up to 99% or 97% or 96% will therefore often be accepted in practice.
  • the NO x emission in the process according to the invention decreases in comparison with the known process; the emission can decrease to less than 100 mg/Nm 3 , preferably less than 95 mg/Nm 3 , more preferably less than 90 mg/Nm 3 , most preferably less than 85 mg/Nm 3 , measured according to Clause 4 of the “Besluit emissie-eisen stookinstallaties milieubeheer A’ (Order stating emission requirements for combustion installations environmental management A’), also known as BEES (version valid from Nov. 23, 2000, Dutch Bulletin of Acts and Decrees 2000, 443).
  • BEES version valid from Nov. 23, 2000, Dutch Bulletin of Acts and Decrees 2000, 443
  • the process according to the invention preferably also comprises a third heat exchange step for the flue gases with fresh air; here the NO x emission in the flue gases is preferably less than 100 mg/Nm 3 .
  • Compliance with specified emission values does entail that preheating fresh air with the aid of the flue gases must be limited in such a way that the stated emission values are not exceeded. This can be accomplished by limiting the temperature increase of the fresh air.
  • preheating fresh air it may additionally be advantageous, as in the known process, to separate a proportion of the flue gases, to mix that proportion with fresh air and thus feed a mixture of fresh air and recirculated flue gases to the burners.
  • Preheating the fresh air with the flue gases by means of the third heat exchange step may be effected before, during or after the first or the second heat exchange steps with the first and the second process stream. If the fresh air is preheated prior to the first or the second heat exchange step, it is important to carefully verify that the energy efficiency and NO x emission remain within the limits indicated above. Therefore, the fresh air is preferably preheated during or after the first or the second heat exchange steps, most preferably after the second heat exchange step.
  • the furnace is preferably a salt furnace.
  • a salt furnace here means a furnace in which salt is melted via the first heat exchange step, if that had not been done yet, and is heated, after which the molten salt serves to supply process heat in a process for the production of melamine, so that there is mention here of indirect heat exchange.
  • Such salt furnaces are known per se.
  • the molten salt from the process usually enters the furnace at a temperature of between 400° C. and 440° C., in order to be heated to 450° C. or higher.
  • the flue gases usually still have a temperature of approximately 400° C. or higher; this temperature then is the inlet temperature for the second heat exchange step.
  • the process according to the invention comprises a first heat exchange step with molten salt, followed by a second direct heat exchange step with a process stream which consists essentially of ammonia.
  • ammonia is used and/or consumed in various places in processes for the production of melamine. In some of these places it is necessary for the ammonia to have a high temperature above 300° C., often approximately 350° C. to 400° C. or higher up to approximately 450° C. Examples hereof are the use of ammonia as the fluidization gas in the reactor of a gas-phase process for the production of melamine, or the use of ammonia in the reactor of a high-pressure liquid-phase process.
  • the ammonia to be heated may be gaseous, liquid or in supercritical condition.
  • the ammonia to be heated is liquid or in supercritical condition, because heat exchange to a liquid or supercritical medium is technically simpler to implement than heat exchange to a gaseous medium.
  • the process according to the invention comprises a first heat exchange step with molten salt, followed by a second direct heat exchange step with a process stream which consists essentially of urea.
  • urea can be heated by bringing the urea in direct contact with gases released in the reaction of urea to form melamine and which gases are usually eventually returned to a process for the preparation of urea.
  • there may still be a need for an additional method for heating urea for example in a non-steady state of the plant such as during start-up; also, the known process is not generally applicable in low-pressure processes for the production of melamine. It is therefore advantageous for urea to be used as the process stream in the process according to the invention.
  • the industrial applicability of the process according to the invention is to be found amongst other things in salt furnaces commonly used in practice.
  • the invention therefore also relates to an apparatus for supplying process heat in a process for the production of melamine, comprising a salt furnace which includes a heat exchange unit in which salt is heated; the first heat exchange step is carried out herein.
  • the apparatus according to the invention contains at least one further heat exchange unit which directly or indirectly heats a process stream: the second heat exchange step is carried out herein.
  • the presence of the at least one further heat exchange unit which heats a process stream contributes to achieving an energy efficiency of 85% or more, without the need to preheat fresh air.
  • the further heat exchange unit is a heat exchange unit for the direct heating of ammonia or urea.
  • the industrial applicability of the process according to the invention is further to be found in the optimization of an existing apparatus for the supply of process heat in a process for the production of melamine.
  • Application of the process according to the invention can be realized in an existing apparatus by adding at least one heat exchange unit for the direct or indirect heating of a process stream.
  • the addition of the at least one further heat exchange unit which heats a process stream contributes to achieving an energy efficiency of 85% or more without having to rely for this on preheating fresh air.
  • the added heat exchange unit is then used for the direct heating of a process stream which consists essentially of ammonia or urea.
  • the added heat exchange unit is preferably positioned such that the flue gases first pass through the added heat exchange unit before the flue gases preheat fresh air. Since fresh air extracts less energy and is thus preheated to a lesser extent, the NO x emission of the existing apparatus will decrease, with the eventually achieved emission value being dependent on the specific conditions of the existing apparatus.
  • a process stream such as a heat transfer medium or an auxiliary stream such as ammonia
  • a process stream is at the same time available at various temperature levels. Since the heat exchange steps with a process stream must be dimensioned to supply the highest desired temperature level to the process for the production of melamine, there is thus a need to provide a possibility of supplying that process stream also at a lower temperature level to the process for the production of melamine.
  • a fourth heat exchange step in which a process stream is heat exchanged with the flue gases, with the process stream supplied to the fourth heat exchange step having a higher temperature than the flue gases supplied to the fourth heat exchange step.
  • An example of such a fourth heat exchange step is first separating a proportion of a stream of molten salt which is supplied to, or discharged from, the first heat exchange step, followed by supplying to the fourth heat exchange step the separated stream of molten salt, with the flue gases, because of the second and possibly the third heat exchange step, having decreased in temperature such that the flue gases in the fourth heat exchange step are heated and the molten salt is cooled.
  • FIG. 1 shows an embodiment of the prior art, in which a fuel and fresh air are supplied to a burner; the flue gases are successively heat exchanged with molten salt and with fresh air.
  • FIG. 2 shows an embodiment according to the invention, in which the flue gases pass through two heat exchange steps with process streams before heat is exchanged with fresh air.
  • FIG. 3 shows an embodiment according to the invention, in which the flue gases, following heat exchange with molten salt, a process stream and with fresh air, are reheated somewhat by heat exchange with a proportion of the molten salt.
  • natural gas is supplied via line 102 to burner 104 , where the natural gas is combusted with the aid of combustion air supplied via 106 .
  • Flue gases are formed in this process.
  • the flue gases are conveyed through duct 108 to heat exchanger 110 , where the flue gases are heat exchanged with molten salt supplied through line 112 and, once heated, discharged through line 114 .
  • the flue gases are then supplied through duct 116 to heat exchanger 118 , where the flue gases are heat exchanged with fresh air.
  • the fresh air is supplied via line 120 , and, after heating, discharged through 106 as combustion air to burner 104 .
  • the flue gases are discharged through duct 122 .
  • a proportion of the flue gases is recirculated via 124 by mixing with the fresh air supplied through 120 .
  • the flue gases following heat exchange with a process stream (such as molten salt) are passed through 210 not directly to a heat exchange step with fresh air but first through duct 226 to heat exchanger 228 .
  • a process stream for example supercritical ammonia
  • the flue gases exchange heat again with a process stream (for example supercritical ammonia) supplied via line 230 and, after heating, are discharged via line 232 .
  • the flue gases are supplied through duct 234 to heat exchanger 218 .
  • the flue gases after heat exchange with fresh air in 318 , are supplied through duct 322 to heat exchanger 336 ; here the flue gases are heat exchanged with a proportion of the process stream that had been discharged through 314 ; this partial stream is supplied via line 338 .
  • the flue gases will be reheated somewhat, and the process stream will cool somewhat.
  • the cooled process stream is discharged via 340 ; the flue gases through duct 342 .
  • the invention is further elucidated with reference to an example and a comparative experiment.
  • An apparatus according to FIG. 2 in which the process according to the invention is applied comprises a salt furnace.
  • the first heat exchange step of the flue gases is carried out with molten salt in heat exchanger 210 ; the second heat exchange step with gaseous ammonia in heat exchanger 228 ; the third heat exchange step of the flue gases is carried out with fresh air in heat exchanger 218 .
  • a proportion of the flue gases is separated and mixed with fresh air via 224 .
  • the salt furnace is heated by means of combustion, in burner 204 , of 1625 Nm 3 /h natural gas with a mixture of approximately 90 vol. % fresh air and approximately 10 vol. % recirculated flue gases with a total volume of 20,850 Nm 3 /h.
  • the molten salt approximately 500 m 3 /h, is heated from 414° C. in line 212 to 450° C. in line 214 .
  • the gaseous ammonia approximately 22,500 kg/h, is heated from 210° C. in line 230 to 250° C. in line 232 .
  • the mixture of fresh air and recirculated flue gases is heated in heat exchanger 218 from 32° C. to 158° C.
  • the flue gases eventually emitted through 222 have a temperature of 220° C.
  • the overall energy efficiency is 91%; the NO x emission is 80 mg/Nm 3 .
  • An apparatus according to the state of the art, see FIG. 1 , comprises a salt furnace.
  • the flue gases are heat exchanged with molten salt in heat exchanger 110 .
  • the flue gases are eventually heat exchanged with fresh air in heat exchanger 118 .
  • a proportion of the flue gases is separated and mixed with fresh air via 124 .
  • the overall energy efficiency is 93%; allowance should be made here for the fact that in the apparatus according to the state of the art no ammonia stream has been heated as in Example I; this will require a separate heat exchange step in the process for the production of melamine, for example by means of steam or through electrical heating of the line carrying the ammonia to be heated, which has a negative effect on the efficiency given here. Also, in this embodiment the flue gases are cooled to a lower temperature, which leads also to a higher efficiency.
  • the NO x emission is 100 mg/Nm 3 .

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  • Engineering & Computer Science (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Mechanical Engineering (AREA)
  • Organic Chemistry (AREA)
  • Thermal Sciences (AREA)
  • Physics & Mathematics (AREA)
  • Combustion & Propulsion (AREA)
  • Treating Waste Gases (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
  • Chimneys And Flues (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Air Supply (AREA)
US10/541,062 2003-01-17 2003-12-17 Process for the extraction of energy from flue gases Abandoned US20060048514A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
NL1022414 2003-01-17
NL1022414A NL1022414C2 (nl) 2003-01-17 2003-01-17 Werkwijze voor het onttrekken van energie uit rookgassen.
PCT/NL2003/000897 WO2004065878A1 (en) 2003-01-17 2003-12-17 Process for the extraction of energy from flue gases

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US20060048514A1 true US20060048514A1 (en) 2006-03-09

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US10/541,062 Abandoned US20060048514A1 (en) 2003-01-17 2003-12-17 Process for the extraction of energy from flue gases

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US (1) US20060048514A1 (pl)
EP (1) EP1583931A1 (pl)
JP (1) JP2006513838A (pl)
KR (1) KR20050095851A (pl)
CN (1) CN100363702C (pl)
AU (1) AU2003290449B2 (pl)
CA (1) CA2511188A1 (pl)
EA (1) EA007943B1 (pl)
MX (1) MXPA05007608A (pl)
MY (1) MY141523A (pl)
NL (1) NL1022414C2 (pl)
NO (1) NO20053854L (pl)
PL (1) PL377737A1 (pl)
WO (1) WO2004065878A1 (pl)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100175689A1 (en) * 2009-01-13 2010-07-15 Hamilton Sundstrand Corporation Catalyzed hot gas heating system for pipes
CN112268465A (zh) * 2020-10-23 2021-01-26 鞍山绿冶热能工程技术有限公司 一种焦炉烟气脱硫脱硝余热回收系统及工艺
CN115010674A (zh) * 2022-07-05 2022-09-06 山东省舜天化工集团有限公司 一种三聚氰胺生产资源回收利用系统及回收利用方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1688411A1 (en) * 2005-02-04 2006-08-09 DSM IP Assets B.V. Process for the preparation of melamine

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US2943088A (en) * 1959-06-22 1960-06-28 Westfall Richard Howard Production of cyanuric acid from urea
US3426733A (en) * 1967-09-19 1969-02-11 Peter Von Wiesenthal Furnace and related process involving combustion air preheating
US4156080A (en) * 1977-01-19 1979-05-22 Stamicarbon, B.V. Process for the preparation of melamine
US4408046A (en) * 1982-04-07 1983-10-04 Stamicarbon, B.V. Process of preparing melamine
US4543110A (en) * 1983-07-06 1985-09-24 Kraftwerk Union Aktiengesellschaft Method and plant for reheating flue gases behind a wet flue-gas desulfurization plant
US4784069A (en) * 1985-11-01 1988-11-15 Foster Wheeler Usa Corporation Chemical process fired heaters, furnaces or boilers
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5384404A (en) * 1993-11-05 1995-01-24 Lee; Jing M. Process for manufacturing melamine from urea
US5474280A (en) * 1993-08-20 1995-12-12 Martin; Charles A. Apparatus for preheating a reactor feed
US6252074B1 (en) * 1997-06-27 2001-06-26 Eurotecnica Development & Licensing S.R.L. Process and apparatus for melamine manufacture
US6599119B1 (en) * 2001-02-13 2003-07-29 Entropy Technology And Environmental Consultants, Lp Apparatus and method to control emissions of nitrogen oxide

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DE889749C (de) * 1940-03-30 1953-09-14 American Cyanamid Co Verfahren zur Herstellung von Melamin und seinen Desaminierungsprodukten
GB2182395B (en) * 1985-11-01 1989-09-27 Foster Wheeler Energy Ltd Improvements in chemical process fired heaters, furnaces or boilers
NL1003709C2 (nl) * 1996-07-30 1998-02-05 Dsm Nv Werkwijze voor het bereiden van melamine.

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2943088A (en) * 1959-06-22 1960-06-28 Westfall Richard Howard Production of cyanuric acid from urea
US3426733A (en) * 1967-09-19 1969-02-11 Peter Von Wiesenthal Furnace and related process involving combustion air preheating
US4156080A (en) * 1977-01-19 1979-05-22 Stamicarbon, B.V. Process for the preparation of melamine
US4408046A (en) * 1982-04-07 1983-10-04 Stamicarbon, B.V. Process of preparing melamine
US4543110A (en) * 1983-07-06 1985-09-24 Kraftwerk Union Aktiengesellschaft Method and plant for reheating flue gases behind a wet flue-gas desulfurization plant
US4784069A (en) * 1985-11-01 1988-11-15 Foster Wheeler Usa Corporation Chemical process fired heaters, furnaces or boilers
US5247907A (en) * 1992-05-05 1993-09-28 The M. W. Kellogg Company Process furnace with a split flue convection section
US5474280A (en) * 1993-08-20 1995-12-12 Martin; Charles A. Apparatus for preheating a reactor feed
US5384404A (en) * 1993-11-05 1995-01-24 Lee; Jing M. Process for manufacturing melamine from urea
US6252074B1 (en) * 1997-06-27 2001-06-26 Eurotecnica Development & Licensing S.R.L. Process and apparatus for melamine manufacture
US6599119B1 (en) * 2001-02-13 2003-07-29 Entropy Technology And Environmental Consultants, Lp Apparatus and method to control emissions of nitrogen oxide

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20100175689A1 (en) * 2009-01-13 2010-07-15 Hamilton Sundstrand Corporation Catalyzed hot gas heating system for pipes
US8925543B2 (en) * 2009-01-13 2015-01-06 Aerojet Rocketdyne Of De, Inc. Catalyzed hot gas heating system for pipes
CN112268465A (zh) * 2020-10-23 2021-01-26 鞍山绿冶热能工程技术有限公司 一种焦炉烟气脱硫脱硝余热回收系统及工艺
CN115010674A (zh) * 2022-07-05 2022-09-06 山东省舜天化工集团有限公司 一种三聚氰胺生产资源回收利用系统及回收利用方法

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CA2511188A1 (en) 2004-08-05
KR20050095851A (ko) 2005-10-04
JP2006513838A (ja) 2006-04-27
MY141523A (en) 2010-05-14
CN100363702C (zh) 2008-01-23
AU2003290449A1 (en) 2004-08-13
EP1583931A1 (en) 2005-10-12
NO20053854D0 (no) 2005-08-17
WO2004065878A1 (en) 2004-08-05
EA007943B1 (ru) 2007-02-27
PL377737A1 (pl) 2006-02-20
CN1738998A (zh) 2006-02-22
NL1022414C2 (nl) 2004-07-20
AU2003290449B2 (en) 2009-07-16
EA200501141A1 (ru) 2006-04-28
MXPA05007608A (es) 2005-09-30
NO20053854L (no) 2005-08-17

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