WO2007067089A1 - Installation de traitement thermique de schiste a caloporteur solide - Google Patents

Installation de traitement thermique de schiste a caloporteur solide Download PDF

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Publication number
WO2007067089A1
WO2007067089A1 PCT/RU2006/000322 RU2006000322W WO2007067089A1 WO 2007067089 A1 WO2007067089 A1 WO 2007067089A1 RU 2006000322 W RU2006000322 W RU 2006000322W WO 2007067089 A1 WO2007067089 A1 WO 2007067089A1
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WO
WIPO (PCT)
Prior art keywords
separator
ash
heat
heat exchanger
mixer
Prior art date
Application number
PCT/RU2006/000322
Other languages
English (en)
Russian (ru)
Inventor
Eduard Petrovich Volkov
Dmitry Arkadievich Gilev
Dmitry Vasilevich Kogitsev
Sergey Viktorovich Onufrienko
Mikhail Sergeevich Petrov
Original Assignee
Obschestvo S Ogranichennoi Otvetstvennostyu Nauchno-Tehnichesky Centr 'ekosorb'
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
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First worldwide family litigation filed litigation Critical https://patents.darts-ip.com/?family=38123130&utm_source=google_patent&utm_medium=platform_link&utm_campaign=public_patent_search&patent=WO2007067089(A1) "Global patent litigation dataset” by Darts-ip is licensed under a Creative Commons Attribution 4.0 International License.
Application filed by Obschestvo S Ogranichennoi Otvetstvennostyu Nauchno-Tehnichesky Centr 'ekosorb' filed Critical Obschestvo S Ogranichennoi Otvetstvennostyu Nauchno-Tehnichesky Centr 'ekosorb'
Priority to BRMU8603045-0U priority Critical patent/BRMU8603045U2/pt
Priority to EEU200800059U priority patent/EE00813U1/xx
Publication of WO2007067089A1 publication Critical patent/WO2007067089A1/fr

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B53/00—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form
    • C10B53/06—Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of oil shale and/or or bituminous rocks
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10B—DESTRUCTIVE DISTILLATION OF CARBONACEOUS MATERIALS FOR PRODUCTION OF GAS, COKE, TAR, OR SIMILAR MATERIALS
    • C10B49/00—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated
    • C10B49/16—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form
    • C10B49/20—Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form
    • 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
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/10—Process efficiency
    • Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines

Definitions

  • a group of utility models (three options) relates to the energy sector, in particular to oil shale processing devices, which are used in energy technology plants using oil shale of various quality and its mixture with other components to produce fuel products with high calorific value and chemical products for various purposes.
  • a plant for the thermal processing of oil shale with a solid coolant was chosen [AC USSR 270684, publication date 05/12/1970].
  • the installation includes a dryer, a separator of dry shale, a screw, a reactor, a furnace, a coolant separator, an ash separator in the form of one or more cyclones, a mixing device and a separation chamber, in which a number of series-connected cyclones are mounted.
  • the dryer and the furnace are made of aero-fountain type
  • the reactor is in the form of a drum rotating around the horizontal axis.
  • the shale entering the dryer inlet is dried and heated due to the incoming hot flue gas from the bottom of the dryer.
  • a separator in which dry shale is released.
  • dry shale is conveyed by a screw to a mixing device, in which it is mixed with a combustible coolant, and then enters the reactor. Due to the heat of the combustible heat carrier, heating and thermal decomposition of oil shale occurs in the reactor.
  • the resulting vapor-gas decomposition products and semi-coke mixed with the coolant enter the separation chamber, from which the vapor-gas products are taken for cooling and condensation, and the mixture of the semi-coke and the coolant is transferred to the furnace.
  • the mixture of flue gases and heat transfer ash from the furnace enters the heat carrier separator, in which the necessary amount of heat carrier for the reactor is released.
  • the flue gases with an excess of coolant go from the coolant separator to the ash separator, and the ash cleaned in it goes to the dryer.
  • the flue gases purified from the ash in the separator enter the dryer, where they are used as a drying agent for the incoming shale. At the same time, this flue gas is also used for heating oil shale.
  • the temperature of the flue gases entering the dryer is 780-900 0 C, which is excessive for the process, because to dry shale, the temperature of the drying agent should not exceed 600 0 C, in order to avoid the onset of pyrolysis.
  • the installation has another drawback.
  • Ash removed from the cycle after the ash separator has an elevated temperature (about 900 0 C), which causes difficulties in its disposal or transportation.
  • the installation has a low thermal efficiency, which is expressed by a partial loss of generated heat during cooling of ash and flue gases.
  • the utility model is based on the task of utilizing the excess heat of products obtained during the operation of the installation and increasing the thermal efficiency of the installation.
  • the installation for the thermal processing of shale with a solid coolant includes a sequentially located loading hopper, aerial dryer, separator, conveying device (for example, auger), mixer, drum-type reactor with a horizontal axis of rotation, a separation a chamber, an air-fired type technological furnace, a coolant separator, the outlet of which is connected to the mixer.
  • the installation also contains an ash separator connected to a coolant separator.
  • the installation differs from the prototype in that it additionally contains a waste heat boiler installed between the ash separator and the airborne dryer and made to ensure the possibility of obtaining process steam.
  • the installation according to the first embodiment may also additionally contain an ash heat exchanger mounted on the ash output of the ash separator, while the heat transfer pipes of the heat exchanger are connected to the technological furnace.
  • the installation for the thermal processing of shale with a solid heat carrier incorporates a feed hopper, an aerofoil dryer, a separator, a conveying device (for example, an auger), a mixer, a drum-type reactor with a horizontal axis of rotation, a separation a chamber, an air-fired type technological furnace, a coolant separator, the outlet of which is connected to the mixer.
  • the installation also contains an ash separator connected to a coolant separator.
  • the installation differs from the prototype in that it additionally contains an ash heat exchanger mounted on the ash output of the ash separator, while the heat transfer pipes of the heat exchanger are connected to the technological furnace.
  • the installation may also further comprise a waste heat boiler installed between the ash separator and the airborne dryer and made with the possibility of obtaining process steam.
  • the task in the third embodiment is solved by the fact that the installation for the thermal processing of oil shale with a solid coolant incorporates a feed hopper, an aerofoil dryer, a separator, a conveying device (for example, an auger), a mixer, a drum-type reactor with a horizontal axis of rotation, a separation a chamber, an air-flow type fire chamber, a coolant separator, the outlet of which is connected to the mixer, and also contains an ash separator connected to the separator eplonositelya.
  • a feed hopper for example, an aerofoil dryer, a separator, a conveying device (for example, an auger), a mixer, a drum-type reactor with a horizontal axis of rotation, a separation a chamber, an air-flow type fire chamber, a coolant separator, the outlet of which is connected to the mixer, and also contains an ash separator connected to the separator eplonositelya.
  • the installation differs from the prototype in that it additionally contains a waste heat boiler installed between the ash separator and the airborne dryer and made with the possibility of producing process steam, and further comprises an ash heat exchanger installed at the ash outlet of the ash separator, this heat sink pipes of the heat exchanger are connected to the technological furnace.
  • Figure shows a schematic representation of a plant for the thermal processing of oil shale with a solid coolant.
  • the utility model according to the first embodiment includes sequentially located: feed hopper 1, aerial dryer 2, dry shale separator 3, conveying device 4, mixer 5, rotary drum reactor 6 with a horizontal axis, separation chamber 7, aero-fired technological furnace 8, separator 9 coolant, ash separator 10, recovery boiler 11 with afterburning device 12 and bypass duct 13 and valve 14 standing in the main line connecting the recovery boiler and the airborne dryer.
  • the device may also additionally contain an ash heat exchanger 15 mounted on the ash output of the ash separator 10, while the heat pipes of the heat exchanger 15 are connected to the process furnace 8.
  • the ash heat exchanger includes an intermediate air-water heat exchanger 16.
  • the utility model according to the second embodiment includes a feed hopper 1 in series, an aerial dryer 2, a dry shale separator 3, a conveying device 4, a mixer 5, a rotary drum reactor 6, a separation chamber 7, an aerial firing furnace 8, a coolant separator 9, a separator 10 ash and an ash heat exchanger 15 mounted on the ash output of the ash separator 10, while the heat pipes of the heat exchanger 15 are connected to the process furnace 8.
  • the ash heat exchanger contains Odita intermediate air-water heat exchanger 16.
  • the apparatus also may further comprise a waste-heat boiler 11 with afterburning device 12 with the bypass gas duct 13 and valve 14, standing in the line connecting the waste heat boiler and the dryer air-fountain
  • the utility model according to the third embodiment includes a sequentially located loading hopper 1, an aerial dryer 2, a dry shale separator 3, a conveying device 4, a mixer 5, a rotary drum reactor 6, a separation chamber 7, an aerial process furnace 8, a coolant separator 9, a separator 10 ash, recovery boiler 11, afterburner 12, bypass duct 13, valve 14, ash heat exchanger 15 and an intermediate air-water heat exchanger 16, which is part of the ash heat exchanger 15.
  • the output of the coolant separator 9 for ash removal is connected to the input of the mixer 5, and its second output for flue gas removal is connected to the input of the ash separator 10.
  • One of the outputs of the latter is connected to the ash heat exchanger 15, and the second to the waste heat boiler 11.
  • the output of the waste heat boiler 11 is connected to the air dryer 2 through the gas duct 13.
  • the output of the ash heat exchanger 15, which serves to remove hot blast air, is connected to the furnace 8 and to the afterburner 12.
  • Pre-crushed shale with a particle size of not more than 25 mm is fed through the feed hopper 1 to the airborne dryer 2, where it is dried and heated to a temperature of 110-150 0 C by exposure to flue gases also entering the dryer.
  • the air mixture of shale and flue gas enters the dry shale separator 3, in which dry shale is released from the gas subsequently discharged into the atmosphere.
  • the shale particles enter the mixer 5 by means of a conveying device 4 (for example, a screw).
  • a conveying device 4 for example, a screw
  • mixer 5 shale particles are mixed with hot heat carrier (ash) having a temperature of 800-850 0 C, after which the mixture enters reactor 6.
  • shale and coolant are also mixed, moving uniformly through it. Due to the heat of the hot heat carrier, heating occurs (up to a temperature of 500 0 C) and thermal decomposition (pyrolysis) of the combustible mass contained in them. AT As a result of pyrolysis, a vapor-gas mixture and a coke-ash residue are formed. The resulting mixture enters the separation chamber 7, in which the gas-vapor products are diverted for cooling and condensation, and the mixture of semi-coke and coolant is transferred to the process furnace 8. Hot (400-450 ° C) blast air is also supplied to the latter.
  • the coke ash residue is burned, and due to the heat generated during this process, the entire mass of coolant and ash of fresh semi-coke is heated to the required temperature (780-820 0 C).
  • the gas suspension resulting from the combustion of the coke ash residue is subjected to separation in a separator 9 into a heat carrier returned to the mixer 5 and into flue gases with an excess of heat carrier, which subsequently go from a heat carrier separator 9 to an ash separator 10. In the latter there is a separation into ash and flue gas.
  • the flue gas purified from the bulk of the ash enters the waste heat boiler 11 at a temperature of 780-820 0 C.
  • the amount of heat introduced into the waste heat boiler 11 depends on the quality and volume of the processed slate and the possibilities of impurities, ash content and the thermal processing mode.
  • sequential stepwise cooling and afterburning of the flue gas is carried out so that the temperature in the flue 13 does not exceed the limit value according to the conditions of slagging (900-950 0 C).
  • the cooling of the flue gas is carried out by means of heat exchange with feed water entering the pipe surface of the heat exchanger 11.
  • the process of multiple forced circulation and heat exchange of feed water with flue gas it is heated and then removed in the form of process steam.
  • the aforementioned burning of flue steam is carried out by the afterburning device 12, which is in demand in order to control the temperature of the process steam discharged from the waste heat boiler 11.
  • flue gases are used to dry 2 shale entering the dryer.
  • the amount of heat allocated for drying the shale depends on its consumption and humidity, and changes during operation.
  • bypassing of the heated furnace is provided gas so that the temperature behind the air dryer 2 corresponds to safety requirements.
  • the flue gas in this case is carried out by means of a bypass duct 13.
  • the ash separated in the separator 10 from the flue gas enters the ash heat exchanger 15 at a temperature of about 800-850 0 C.
  • the ash is cooled by a counter flow of blast air entering the multisection tube surface of the heat exchanger 15 with a temperature of not more than 50-70 0 C This allows to obtain ash of an acceptable temperature (up to 150-200 0 C) at the outlet of the specified heat exchanger for its further disposal or transportation.
  • high-temperature (400-450 0 C) process blast air enters the outlet of the multisectional tube surface of the heat exchanger 15, then it enters the furnace 8 and afterburner 12.
  • the design of the described installation provides for the possibility of intermediate cooling of the blast air in the intermediate air-water heat exchanger 16, which includes in the composition of the ash heat exchanger 15.
  • cooling of the blast air can be carried out by heat exchange with feed water entering the pipe surface t heat exchanger 16.
  • the specified feed water can also be used for heat transfer in the waste heat boiler 11, which will significantly increase the useful steam output of the heat recovery boiler 11.
  • by changing the flow rate of blast air through the heat exchanger 15 it is possible to control the heat removal in the heat exchanger 16 by maintaining a certain temperature of the blast air at the outlet of the multisectional tube surface of the heat exchanger 15.
  • the inventive installation for the thermal processing of shale with a solid heat carrier can reduce the loss of generated heat during cooling of ash and / or flue gases in the respective heat exchangers, to increase the thermal efficiency of the installation as a whole, as well as to obtain process steam, which can be used as an additional energy product.
  • the utility model according to the first embodiment makes it possible to efficiently utilize the excess heat of the flue gases to produce process steam.
  • the utility model according to the second embodiment makes it possible to efficiently utilize the residual heat of the ash to produce high-temperature process blast air.
  • the utility model according to the third option allows us to solve the combined problem of efficient utilization of excess heat of ash and flue gas to produce process blast air and water vapor, respectively.
  • the utilization of the heat of the flue gas (due to its afterburning) can reduce harmful emissions of carbon monoxide into the atmosphere during production.

Abstract

La présente invention relève du génie énergétique, et se rapporte à des installations de traitement de schiste, qui utilisent du schiste de diverses qualités et des mélanges de schiste et d'autres composants afin d'obtenir des produits combustibles à fort pouvoir calorifique et des produits chimiques destinés à divers usages. Une installation selon invention comprend successivement une trémie de chargement (1), un appareil de séchage à jet d'air (2), un séparateur (3), un dispositif de transport (4), un mélangeur (5), un réacteur (6) de type à tambour doté d'un axe de rotation horizontal, une chambre de séparation (7), un four de traitement (8) de type à jet d'air, un séparateur de caloporteur (9), dont la sortie est reliée au mélangeur (5), et un séparateur de cendres (10) relié au séparateur de caloporteur (9). L'installation selon l'invention comprend également : une chaudière de récupération (11), qui est placée entre le séparateur de cendres (10) et le dispositif de séchage à jet d'air (2), et est conçue pour recevoir la vapeur de traitement ; et un échangeur de chaleur à cendres (15), qui est placé au niveau de la sortie des cendres du séparateur de cendres (10), les conduits d'évacuation de la chaleur de l'échangeur de chaleur étant reliés au four de traitement (8). La présente invention permet de récupérer l'excédent de chaleur généré par les produits obtenus lors du fonctionnement de l'installation, tout en augmentant le rendement thermique de ladite installation.
PCT/RU2006/000322 2005-12-05 2006-06-20 Installation de traitement thermique de schiste a caloporteur solide WO2007067089A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
BRMU8603045-0U BRMU8603045U2 (pt) 2005-12-05 2006-06-20 usina de termotratamento de xisto proporcionada com um transportador de calor sàlido
EEU200800059U EE00813U1 (et) 2005-12-05 2006-06-20 Seade p?levkivi termiliseks t””tlemiseks tahke soojuskandja kasutamisel

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
RU2005137842 2005-12-05
RU2005137842 2005-12-05

Publications (1)

Publication Number Publication Date
WO2007067089A1 true WO2007067089A1 (fr) 2007-06-14

Family

ID=38123130

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Application Number Title Priority Date Filing Date
PCT/RU2006/000322 WO2007067089A1 (fr) 2005-12-05 2006-06-20 Installation de traitement thermique de schiste a caloporteur solide

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BR (1) BRMU8603045U2 (fr)
EE (1) EE00813U1 (fr)
UA (1) UA41368U (fr)
WO (1) WO2007067089A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102533296A (zh) * 2011-12-26 2012-07-04 上海交通大学 油页岩回转窑干馏与循环流化床燃烧工艺
CN112708432A (zh) * 2020-12-08 2021-04-27 陕西德信祥能源科技有限公司 一种新型固体热载体提升管油回收方法

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3318798A (en) * 1964-08-21 1967-05-09 Mobil Oil Retorting of oil shale
US3976558A (en) * 1974-06-26 1976-08-24 Hall Robert N Method and apparatus for pyrolyzing oil shale
RU2094447C1 (ru) * 1994-12-28 1997-10-27 Саратовский государственный технический университет Способ термической переработки сернистых сланцев

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3318798A (en) * 1964-08-21 1967-05-09 Mobil Oil Retorting of oil shale
US3976558A (en) * 1974-06-26 1976-08-24 Hall Robert N Method and apparatus for pyrolyzing oil shale
RU2094447C1 (ru) * 1994-12-28 1997-10-27 Саратовский государственный технический университет Способ термической переработки сернистых сланцев

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102533296A (zh) * 2011-12-26 2012-07-04 上海交通大学 油页岩回转窑干馏与循环流化床燃烧工艺
CN112708432A (zh) * 2020-12-08 2021-04-27 陕西德信祥能源科技有限公司 一种新型固体热载体提升管油回收方法

Also Published As

Publication number Publication date
EE00813U1 (et) 2009-04-15
BRMU8603045U2 (pt) 2008-12-30
UA41368U (ru) 2009-05-25

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