EP3443265A2 - Procédé de production d'électricité - Google Patents

Procédé de production d'électricité

Info

Publication number
EP3443265A2
EP3443265A2 EP17765247.6A EP17765247A EP3443265A2 EP 3443265 A2 EP3443265 A2 EP 3443265A2 EP 17765247 A EP17765247 A EP 17765247A EP 3443265 A2 EP3443265 A2 EP 3443265A2
Authority
EP
European Patent Office
Prior art keywords
reactor
source
water
pressure
enable
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Withdrawn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
EP17765247.6A
Other languages
German (de)
English (en)
Inventor
Nico Smit
Frans BEZUIDENHOUT
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.)
Advance Carbon Technologies Pty Ltd
Original Assignee
Advance Carbon Technologies Pty Ltd
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 Advance Carbon Technologies Pty Ltd filed Critical Advance Carbon Technologies Pty Ltd
Publication of EP3443265A2 publication Critical patent/EP3443265A2/fr
Withdrawn legal-status Critical Current

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
    • F22B31/0007—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus with combustion in a fluidized bed
    • 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
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/061—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with combustion in a fluidised bed
    • F01K23/062—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle with combustion in a fluidised bed the combustion bed being pressurised

Definitions

  • the invention relates to a process for generating electricity, purifying water and for combusting carbon-based materials.
  • said process utilizes a gas-liquid interface inside a reactor.
  • a further disadvantage of the US process pertains to the complexity of the US process whereby further downstream process equipment is needed in order to remove the particulate matter from the flue gas and steam which results in further heat loss and therefore a further reduction in overall efficiency when compared to the instant invention.
  • a further disadvantage associated with the process described in the GB patent is that the non-combustible material in the fluidized bed may be blown out of the reactor, especially at high oxidising gas velocities, into downstream equipment.
  • the aforementioned circumstance necessitates the use of further expensive downstream equipment to remove such impurities in the steam and flue gas.
  • the heating of the non- combustible materials in the fluidized bed would require a substantial amount of energy which results in a reduction of the steam generation process.
  • an electricity generating process utilizing a gas-liquid interface, in a pressurized reactor including the steps consisting of:
  • a water purification process utilizing a gas-liquid interface, in a pressurized reactor, the process including the steps consisting of:
  • a combustion process utilizing a gas-liquid interface, in a pressurized reactor including the steps consisting of:
  • an accumulator for controlling the pressure of the resultant flue gas and steam.
  • a catalyst to enhance the combustion reaction.
  • the carbon source may be any one or more of a solid, a liquid and a gas.
  • the carbon may be mixed with water in ratios of between 15 percent and 86 percent by carbon weight.
  • the source of carbon may be coal.
  • the coal particles may have a diameter of less than 1 .0 millimeter.
  • the coal particles may have a particle size of 0.5 millimeter.
  • the coal particles may have a 30.0 weight percentage of coal in the source of water containing carbon, said coal being in suspension.
  • the source of water may comprise of any one or more of potable water, gray water, mine acid drainage waste water, recycled water and salt water or combinations thereof.
  • the activator may be in the form of a burner heating potable water, said water being in fluid flow communication with the reactor.
  • the water may be heated to between 180 °C and 520 °C and may be controllably fed at a temperature and pressure corresponding to the boiling conditions of the source of water containing carbon already present inside the reactor.
  • the fluid flow communication between the activator and reactor may be disabled before the introduction of step (iv).
  • the invention yet further provides for the source of oxygen to be introduced into the reactor may be air.
  • the air may be introduced into the liquid phase of the reactor to enable uniform distribution of the air inside the liquid phase.
  • the pressure of the air being introduced into the reactor during step (iv) may be at a pressure range of between 100 and 200 Bar.
  • the internal reactor temperature may be 280 °C and the internal pressure may be 100 Bar during step (iv) to step (vi) of the process.
  • the liquid phase is a reaction zone wherein the exothermic combustion occurs between the coal and the oxygen inside the liquid phase, such that the energy released from the combustion reaction may cause the water of the liquid phase to undergo a liquid to gas transformation.
  • the accumulator is in the form of a vessel to serve as a buffer between the reactor and the means for generating electricity.
  • Figure 1 shows the reactor setup (10), wherein the first step consists of preparing the reactor (14) for continuous reaction through an initial pressurization step (12) to establish a pressure of between 10 to 30 Bar inside the reactor.
  • Figure 1 further shows the introduction of a source of water containing carbon (16) into the reactor (14) and shows an activator (18) for conditioning the reactor (14) to achieve optimal conditions inside the reactor (14) and to enable the source of water containing carbon (16) to reach boiling point.
  • Figure 1 yet further shows the introduction of a source of oxygen (12) at a pressure and temperature to enable exothermic combustion to occur.
  • Figure 1 also shows an outlet (20) to enable fluid flow communication between the reactor (14) and accumulator (22) for controlling the pressure of the resultant flue gas and steam.
  • Figure 1 also depicts a means for generating electricity (24) in the form of a turbo generator (24).
  • Figure 1 further shows a discharge mechanism (30) for discharging particulate matter (32), gravitationally collected from the liquid phase (28), whilst the reactor is in use.
  • Figure 2 shows the reactor setup (34), wherein the first step consists of preparing the reactor (38) for continuous reaction through an initial pressurization step (36) to establish a pressure of between 10 to 30 Bar inside the reactor.
  • Figure 2 further shows the introduction of a source of water containing carbon (40) into the reactor (38) and shows an activator (42) for conditioning the reactor (38) to achieve optimal conditions inside the reactor (38) and to enable the source of water containing carbon (40) to reach boiling point.
  • Figure 2 yet further shows the introduction of a source of oxygen (36) at a pressure and temperature to enable exothermic combustion to occur.
  • Figure 2 also shows an outlet (42) from the reactor (38) for removing steam and flue gas from the reactor (38).
  • Figure 3 shows the purging of the reactor from time 12:00:01 to time 12:24:01 , during which time the valve (not shown in Figure 2) (labelled as "Valve Position” on Figure 3) which is located in the outflow (42) is in an open condition.
  • the reactor (38) has three temperature probes (not shown in Figure 2) which measures the temperature inside the reactor (38) at three regions thereof corresponding to a "bottom", “middle” and “top” region.
  • the temperature readings of the afore-mentioned temperature probes are shown in Figure 3 as "Bottom Temperature”, “Top Temperature” and “Dome Temperature”, respectively.
  • Figure 3 further shows the conditioning (increasing the temperature and pressure inside the reactor) of the reactor via the activator from time 12:33:37 to time 13:20:25. During this time, as shown on Figure 3, the steam produced by the activator reaches a temperature of more than 250 °C, which is then fed to the reactor (38) to heat the molasses and water mixture, and the liquid phase (46) contained therein.
  • FIG 3 at time 13:20:25, shows the shutdown of the activator (42) whereby the temperature and pressure of the said activator (42) drops significantly.
  • the source of oxygen (36) is introduced to the reactor (38) and the valve (not shown in Figure 2) located on the outflow (42) is opened in a step-wise fashion, where after the combustion reaction inside the reactor (38) occurs.
  • Evidence of this combustion reaction can be seen by the sharp increase in the readings of the "Dome Temperature" probe from time 13:20:25 and the initial increase of the reactor's (38) pressure.
  • a first advantage associated with the present process is the use of moderate pressures and temperatures inside the reactor, which results in an exothermic reaction occurring in the liquid phase and thereby increasing the heat transfer between the combustion reaction and water, thereby increasing the overall efficiency of the instant process up to 64 percent energy fed vs. energy gained.
  • the use of said moderate pressures and temperatures alleviates the need for increased apparatus specifications such as wall thickness of the reactor and accumulator.
  • a substantial cost saving in terms of process equipment will occur when compared to, inter alia, the patents described under the background of this specification.
  • a further advantage over the processes discussed under the background of this specification pertains to the simplicity of the design when compared to the US process, such as the redundancy of further downstream process equipment needed to remove the particulate matter from the flue gas and steam before it can be fed to the electricity generating means, thereby resulting in further cost savings.
  • a yet further advantage of the instant process resulting from the lower operating temperatures of the present invention when compared to the processes described under the background of this specification, is the absence of a stack whereby the flue gas is cooled prior to releasing it to the atmosphere.

Landscapes

  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)

Abstract

La présente invention concerne un procédé de production d'électricité, un procédé d'épuration des eaux et un procédé de combustion utilisant une interface gaz-liquide, dans un réacteur sous pression, le procédé comprenant les étapes consistant à préparer le réacteur pour une réaction continue, au moyen d'une étape de pressurisation initiale permettant d'établir une pression comprise entre 10 et 30 bars à l'intérieur du réacteur, à introduire une source d'eau contenant une source de carbone dans le réacteur et à utiliser un activateur pour conditionner le réacteur en vue d'obtenir des conditions optimales à l'intérieur du réacteur pour permettre à la source d'eau contenant du carbone d'atteindre le point d'ébullition. Le procédé consiste en outre à introduire une source d'oxygène à une pression et à une température permettant une combustion exothermique, à fournir en outre une source continue d'eau contenant du carbone et une source d'oxygène pour permettre une combustion exothermique continue et enfin à utiliser à la fois le gaz de combustion et la vapeur dans un moyen de production d'électricité ou d'épuration des eaux.
EP17765247.6A 2016-04-15 2017-04-13 Procédé de production d'électricité Withdrawn EP3443265A2 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
GB201606637 2016-04-15
PCT/IB2017/052136 WO2017179004A2 (fr) 2016-04-15 2017-04-13 Procédé de production d'électricité

Publications (1)

Publication Number Publication Date
EP3443265A2 true EP3443265A2 (fr) 2019-02-20

Family

ID=59856550

Family Applications (1)

Application Number Title Priority Date Filing Date
EP17765247.6A Withdrawn EP3443265A2 (fr) 2016-04-15 2017-04-13 Procédé de production d'électricité

Country Status (3)

Country Link
EP (1) EP3443265A2 (fr)
WO (1) WO2017179004A2 (fr)
ZA (1) ZA201806797B (fr)

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1537695A (en) * 1975-06-04 1979-01-04 Sterling Drug Inc Process and apparatus for energy recovery from wet oxidation
US5485728A (en) * 1985-12-26 1996-01-23 Enertech Environmental, Inc. Efficient utilization of chlorine and moisture-containing fuels
JP3354438B2 (ja) * 1996-06-04 2002-12-09 株式会社荏原製作所 有機物を含有する水媒体の処理方法及び水熱反応装置

Also Published As

Publication number Publication date
ZA201806797B (en) 2021-04-28
WO2017179004A2 (fr) 2017-10-19
WO2017179004A3 (fr) 2017-12-28

Similar Documents

Publication Publication Date Title
CN101555420B (zh) 煤催化气化反应的方法、系统及设备
CN100361889C (zh) 一种高浓度一氧化碳二级变换方法
CN101050390B (zh) 一种与粉煤气化配套的co变换工艺
CN102796561B (zh) 生物质燃料二氧化碳循环无氧气化方法及设备
JP5463524B2 (ja) バイオマスガス化方法、及びバイオマスガス化システム
WO2010060249A1 (fr) Procédé de gazéification haute température utilisant une biomasse pour produire un gaz de synthèse et système associé
CN103765986B (zh) 等离子电弧炉和应用
WO2010063206A1 (fr) Procédé de gazéification de la biomasse à température élevée et son système
WO2011056621A2 (fr) Préchauffage de gaz résiduaire psa
JP6070906B1 (ja) 超臨界水ガス化システムおよびガス化方法
CN111234876A (zh) 超临界水气化制氢的物料分级预热及超温保护系统与方法
WO2014048279A1 (fr) Catalyseur de craquage de la vapeur, son procédé de préparation, et procédé de combustion de l'hydrogène obtenu par craquage de la vapeur
US20150005399A1 (en) Method and device for producing synthetic gas and method and device for synthesizing liquid fuel
CN114058408A (zh) 一种超临界水制氢装置
CN102234545B (zh) 一种含炭质材料气化制合成气的方法
CN105836707A (zh) 非催化部分氧化-重整炉和利用其制备合成气的方法
WO2010063205A1 (fr) Procédé de gazéification à haute température avec de la biomasse et système correspondant
CN211896819U (zh) 煤炭超临界水气化制氢及固液残余无害化处理系统
JP2018510773A (ja) 有機物成分を含有するスラリを処理する方法およびシステム
EP3443265A2 (fr) Procédé de production d'électricité
CN111234877A (zh) 煤炭超临界水气化制氢及固液残余无害化处理系统与方法
CN105923635B (zh) 一种超临界态的生产方法和系统
CN103910330A (zh) 天然气、二氧化碳混合气催化部分氧化制合成气工艺
CN205773310U (zh) 非催化部分氧化-重整炉
Wicakso et al. Study of catalytic upgrading of biomass tars using Indonesian iron ore

Legal Events

Date Code Title Description
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: UNKNOWN

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE

PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

17P Request for examination filed

Effective date: 20181108

AK Designated contracting states

Kind code of ref document: A2

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE

DAV Request for validation of the european patent (deleted)
DAX Request for extension of the european patent (deleted)
STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: EXAMINATION IS IN PROGRESS

17Q First examination report despatched

Effective date: 20211013

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN

18D Application deemed to be withdrawn

Effective date: 20220426