EP2295734A2 - Procédé de production avec conversion de la chaleur résiduelle de plusieurs sources de chaleur résiduelle - Google Patents

Procédé de production avec conversion de la chaleur résiduelle de plusieurs sources de chaleur résiduelle Download PDF

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Publication number
EP2295734A2
EP2295734A2 EP10008825A EP10008825A EP2295734A2 EP 2295734 A2 EP2295734 A2 EP 2295734A2 EP 10008825 A EP10008825 A EP 10008825A EP 10008825 A EP10008825 A EP 10008825A EP 2295734 A2 EP2295734 A2 EP 2295734A2
Authority
EP
European Patent Office
Prior art keywords
cooling circuit
production process
waste heat
process according
fractionation
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Withdrawn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
EP10008825A
Other languages
German (de)
English (en)
Other versions
EP2295734A3 (fr
Inventor
Petrus Carolus van Beveren
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.)
Schutter Rotterdam BV
Original Assignee
Schutter Rotterdam BV
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 Schutter Rotterdam BV filed Critical Schutter Rotterdam BV
Publication of EP2295734A2 publication Critical patent/EP2295734A2/fr
Publication of EP2295734A3 publication Critical patent/EP2295734A3/fr
Withdrawn legal-status Critical Current

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K15/00—Adaptations of plants for special use
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B3/00—Refining fats or fatty oils
    • C11B3/12—Refining fats or fatty oils by distillation
    • C11B3/14—Refining fats or fatty oils by distillation with the use of indifferent gases or vapours, e.g. steam

Definitions

  • the present invention relates to a production process with the conversion of waste heat from multiple waste heat sources.
  • the crude palm oil is put in a process tank that is raised to a high temperature and mixed with stripping steam, whereby the volatile components evaporate from the palm oil and are fractionated immediately afterwards in a built-on fractionation pipe.
  • the fractionation process enables the volatile components of stearic acid and palmitic acid to be separated out selectively and separately, while even more volatile components such as lower hydrocarbons are removed.
  • the condensation of the stripping steam used also releases waste heat.
  • This condensation can be done with an ice condenser that sublimes the steam to ice, and ammonia is used as a coolant, or this condensation can be done by an alkaline vacuum system with a cooling unit that uses cold barometric water as a primary coolant and a mixture of water and ethylene glycol as an intermediate coolant, which in turn is cooled again in a cooling unit by a coolant such as freon or ammonia.
  • a coolant such as freon or ammonia.
  • a disadvantage of this process is that a quantity of energy is wasted in the form of waste heat, which increases the energy cost of the entire industrial process.
  • Another disadvantage is that the environment can be taken out of equilibrium by the release of the waste heat, with the attached costs for the environment.
  • the purpose of the present invention is to make optimum use of this waste heat by partly converting it into electrical energy, and by utilising it to heat liquids during the production process.
  • the invention relates to a production process with the conversion of waste heat from multiple waste heat sources in which the waste heat is partly converted into electrical energy by a main cooling circuit, whereby the waste heat from multiple waste heat sources is collected in the main cooling circuit, directly and/or via one or more intermediate auxiliary cooling circuits, in order to generate electrical energy.
  • An advantage of the present invention is that fewer external energy sources are needed for the production process, such as fossil fuels, which reduces the production costs, due to the conversion of part of the waste heat.
  • Another advantage of the present invention is that electrical energy is also generated in the production process, which may or may not be used then in the production process itself.
  • An additional advantage of the present invention is that less waste heat is released into the environment, such that the environment is spared more.
  • the main cooling circuit is a circuit of coolant that absorbs waste heat by directly cooling a production product, in this case the end product of stripped palm oil and the fractionation products from it, and also by cooling an auxiliary cooling circuit that absorbs waste heat from production sub-processes.
  • the auxiliary cooling circuit contains a mixture of water and ethylene glycol, by which waste heat is absorbed through a heat exchanger, originating from the fractionation condensers that are used for separating the fractionated products, such as stearic acid and palmitic acid.
  • Every auxiliary circuit can have its own coolant, different to the coolant of the main circuit for electricity generation, as well as other auxiliary cooling circuits such that every auxiliary cooling circuit can be optimised according to its function.
  • the waste heat absorbed in the main cooling circuit is now utilised to drive a turbine that is coupled to a generator to generate electrical energy.
  • the spent coolant is further cooled with a condenser and is further recycled to be heated again by the waste heat sources.
  • the auxiliary cooling circuit uses part of the absorbed waste heat to preheat liquids supplied to the production process, or in this case to preheat a part of the main cooling circuit.
  • the main cooling circuit cools a part of the auxiliary cooling circuit to cool a fractionation condenser in the fractionation process.
  • Figure 1 schematically shows a closed ammonia main cooling circuit 1 that contains a turbine 2 connected to an electrical power source 3, a condenser 4 and a receiving vessel 5, a pressure pump 6, and four heat exchangers 7, 8, 9 and 10.
  • Figure 1 also schematically shows a closed auxiliary cooling circuit 11 with a mixture of water and ethylene glycol that contains four heat exchangers 8, 9, 10 and 12, and two condensers 13 and 14.
  • Figure 1 further schematically shows a stripper process tank 15 with an input of palm oil 16 and an output of palm oil 17, an output pump 18, and a heat exchanger 7.
  • the process tank 15 is connected to a fractionation pipe 19, to two condensers 13 and 14, two output pumps 20 and 21, and a set of sprayers 22.
  • the fractionation pipe 19 opens out into a separator 23, connected to a vacuum installation 24 and an output pump 25.
  • unrefined palm oil is raised to a high temperature whereby more volatile components than palm oil are removed via a fractionation pipe 19, and stearic acid is separated at a temperature of 190°C in a condenser 14, and palmitic acid is separated in a subsequent condenser 13 at a temperature of 80°C.
  • the separated stearic acid is taken to a heat exchanger 12 via a pump 20, where the stearic acid is cooled to a temperature of 80°C and then taken to the storage.
  • the separated palmitic acid is injected downstream into the fractionation pipe, via a pump 21, with sprayers 22 that absorb the more volatile fractions insofar as they are not condensed in the condenser 13, and take them to a separator 23 for separation of the usable fractions that are then taken to the storage via pump 25.
  • the unusable lighter fractions are removed via a vacuum system 24.
  • the palm oil stripping and fractionation process produces waste heat that is absorbed by a closed water/ethylene glycol auxiliary cooling circuit 11.
  • a closed water/ethylene glycol auxiliary cooling circuit 11 The heat originating from the cooling of the fractionated stearic acid is absorbed in the heat exchanger 12, and the heat originating from the cooling of the fractionation condensers 18 and 19 is also absorbed, after which this heat is transferred to the main cooling circuit 1 with a coolant in the heat exchangers 8, 9 and 10.
  • the stripping and fractionation process produces waste heat from the cooling of the stripped palm oil itself that is transferred via the heat exchanger 7 directly to the main cooling circuit 1.
  • the main cooling circuit 1 collects the waste heat absorbed from a number of sources in the production process, after which this heat is utilised to drive a turbine 2 coupled to an electric generator 3 for the production of electrical energy.
  • the spent coolant is further cooled in a condenser 4 and further guided via a collection vessel 5 and a pressure pump 6 in the closed main cooling circuit 1 to reabsorb waste heat.
  • the main cooling circuit 1 extracts waste heat from the auxiliary cooling circuit 11 with a heat exchanger 8, such that the water/ethylene glycol mixture is brought to the right lower temperature of T3 (60°C) in order to cool the fractionation condensers 13 and 14.
  • the auxiliary cooling circuit 11 releases waste heat to the main cooling circuit 1 in the heat exchanger 9, whereby the coolant is evaporated before being combined with the other coolant supply that comes from heat exchanger 7, and is then further heated by the heat exchanger 10.
  • the coolant at T8 (123°C) is now ready to drive the turbine 2.
  • waste heat is also utilised directly to heat or cool liquids in the production process.
  • the main cooling circuit is heated by the auxiliary cooling circuit in heat exchanger 8, whereby the coolant of the auxiliary cooling circuit is brought to the right temperature T4 (60°C) for condensing palmitic acid in condenser 13.
  • the auxiliary cooling circuit is thus heated in heat exchanger 12 by the waste heat that is released from cooling the fractionated stearic acid, separated in condenser 18, after which the cooled stearic acid is taken to the storage at the desired temperature of T6 (80°C).
  • the present invention is not in any way limited to the embodiment described as an example and shown in the figures.
  • Such a process for converting waste heat from multiple sources in a production process to generate electrical energy and to directly heat liquids during the production process can be realised according to different variants, without acting outside the scope of the invention.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Microbiology (AREA)
  • Organic Chemistry (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Waste-Gas Treatment And Other Accessory Devices For Furnaces (AREA)
EP10008825A 2009-08-26 2010-08-25 Procédé de production avec conversion de la chaleur résiduelle de plusieurs sources de chaleur résiduelle Withdrawn EP2295734A3 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
BE2009/0519A BE1018869A3 (nl) 2009-08-26 2009-08-26 Productieproces met conversie van afvalwarmte uit meervoudige afvalwartebronnen.

Publications (2)

Publication Number Publication Date
EP2295734A2 true EP2295734A2 (fr) 2011-03-16
EP2295734A3 EP2295734A3 (fr) 2011-05-04

Family

ID=42235278

Family Applications (1)

Application Number Title Priority Date Filing Date
EP10008825A Withdrawn EP2295734A3 (fr) 2009-08-26 2010-08-25 Procédé de production avec conversion de la chaleur résiduelle de plusieurs sources de chaleur résiduelle

Country Status (2)

Country Link
EP (1) EP2295734A3 (fr)
BE (1) BE1018869A3 (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20220152522A1 (en) * 2019-03-08 2022-05-19 Solutherm B.V. Multi stage safe dry condensing

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1080057A (en) * 1964-10-15 1967-08-23 Giovanni Battista Martinenghi Refining process comprising deacidification and deodorization of glyceride oils and fats and equipment for said process
DE3227669C1 (de) * 1982-07-23 1983-07-07 Hermann Dr. 4400 Münster Stage Verfahren und Anlage zum Desodorieren und/oder Entsaeuern von Speiseoelen,Fetten und Estern
DE3522897A1 (de) * 1985-06-26 1987-01-08 Stage Hermann Verfahren und anlage zum desodorieren und/oder entsaeuern von hochsiedenden fluessigkeiten
US6526754B1 (en) * 1998-11-10 2003-03-04 Ormat Industries Ltd. Combined cycle power plant
DE102006043835A1 (de) * 2006-09-19 2008-03-27 Bayerische Motoren Werke Ag Wärmetauscheranordnung
DE102006057448A1 (de) * 2006-12-06 2008-06-12 Ibb Technology Gmbh Verfahren zur Erhöhung von Leistung und Wirkungsgrad im ORC-Kraftwerksprozess

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
None

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20220152522A1 (en) * 2019-03-08 2022-05-19 Solutherm B.V. Multi stage safe dry condensing
US12330087B2 (en) * 2019-03-08 2025-06-17 Solutherm B.V. Multi stage safe dry condensing

Also Published As

Publication number Publication date
EP2295734A3 (fr) 2011-05-04
BE1018869A3 (nl) 2011-10-04

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