[go: up one dir, main page]

WO2008111750A1 - Procédé et système de craquage catalytique de contact dans lesquels est utilisé un lit catalytique mobile vertical à flux ascendant - Google Patents

Procédé et système de craquage catalytique de contact dans lesquels est utilisé un lit catalytique mobile vertical à flux ascendant Download PDF

Info

Publication number
WO2008111750A1
WO2008111750A1 PCT/KR2008/001201 KR2008001201W WO2008111750A1 WO 2008111750 A1 WO2008111750 A1 WO 2008111750A1 KR 2008001201 W KR2008001201 W KR 2008001201W WO 2008111750 A1 WO2008111750 A1 WO 2008111750A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
catalytic cracking
synthetic resin
waste synthetic
regenerator
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/KR2008/001201
Other languages
English (en)
Inventor
Jae Sak Koo
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
Application filed by Individual filed Critical Individual
Publication of WO2008111750A1 publication Critical patent/WO2008111750A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/08—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal with moving catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/082—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
    • C10G1/10—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal from rubber or rubber waste
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/16—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "moving bed" method
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
    • C10G2300/40—Characteristics of the process deviating from typical ways of processing
    • C10G2300/4087—Catalytic distillation
    • 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
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/62—Plastics recycling; Rubber recycling

Definitions

  • the present invention relates to a method and system for contact catalytic cracking by which hydrocarbons can be efficiently decomposed, and, more particularly, to a method and system for contact catalytic cracking using an upward moving-bed catalyst, in which hydrocarbons are decomposed using an upward moving-bed catalyst, and the catalyst is regenerated using an electric heating method, thereby increasing the efficiency of the decomposition of hydrocarbons and the efficiency of the regeneration of the catalyst, and in which catalyst circulation can be accurately controlled, and decomposed hydrocarbon gases cannot be fired, so that methods for treating waste synthetic resin can be widely used.
  • the catalyst that is used in the present invention is a catalyst generally used in the contact catalytic cracking of hydrocarbons, and is a solid acid catalyst including spherical particles the same as those of a zeolite catalyst.
  • the contact catalytic cracking method which is compared to thermal cracking, is a technology for decomposing heavy oil, such as asphalt, into light oil in large quantities in a short period of time using a solid acid catalyst having acidic characteristics and a large porous area of about 200 ⁇ 800 mVg, in which heat necessary for decomposing hydrocarbon polymers is supplied to the process together with a solid acid catalyst having the same form as a zeolite catalyst.
  • the contact catalytic cracking method is a continuous circulation-loop type catalytic cracking method in which a catalyst can be continuously used by regenerating the catalyst by oxidizing carbon remaining in pores of the catalyst, the carbon being produced by the decomposition of hydrocarbons, using air.
  • oil refining companies modify this contact catalytic cracking into fluid catalytic cracking (FCC), and this fluid catalytic cracking (FCC) is used in the process of decomposing asphalt, which is a final residue in vacuum distillation, into light oils, such as gasoline, kerosene, diesel oil, etc., without leaving behind any asphalt.
  • FCC fluid catalytic cracking
  • a fluid bed is made in a fluid catalytic cracking reaction tube (Riser) by shooting powdered catalyst upwards at a speed of 25 m/sec, and when asphalt is injected into the fluid bed, the asphalt is decomposed into gas oil in several seconds by a solid acid catalyst, and then the gas oil is separated from the solid acid catalyst in a cyclone located at the upper portion of the reaction tube, and then the separated gas oil is converted into various kinds of light oils through subsequent condensing, distilling and refining processes and finally recovered.
  • iser fluid catalytic cracking reaction tube
  • a fluid catalytic cracking apparatus includes a reaction tube and a cyclone, the sum of the height of the reaction tube and the height of the cyclone being about 30 ⁇ 50 m, and has a treatment capacity of 30,000 ⁇ 100,000 barrels per day. Therefore, this fluid catalytic cracking apparatus is a large sized apparatus, and it is basically impossible to manufacture a small sized fluid catalytic cracking apparatus, so that it has been limited to develop the fluid catalytic cracking apparatus in other uses. Moreover, in the fluid catalytic cracking apparatus, a catalyst regeneration tower also has a heavy weight of about 600 ⁇ 1,000 tons.
  • gas heated by a burner is blown into a highly-concentrated fluid bed catalyst, flowing downwards, and then from down to up at high pressure, and thus carbon deposited on the fluid bed catalyst or non-vaporized hydrocarbons are fired, and then continuously fired by the blowing air.
  • the fluid bed catalyst in order to uniformly regenerate the fluid bed catalyst, the fluid bed catalyst must maintain the fluid bed structure, and air flow must be of a plug flow type without causing a channeling phenomenon. Therefore, in order to maintain the air flow under high pressure, it is required to manufacture a large-sized fluid catalytic cracking apparatus.
  • gas oil which is a product obtained by decomposing synthetic resins through a catalytic cracking process
  • gas oil is an inflammable gas which can leak easily, unless the gas oil is completely separated from a catalyst regenerator filled with air
  • methods or apparatuses for solving these problems are not proposed.
  • a first object of the present invention is to provide a contact catalytic cracking method, which enables decomposed gases to become easily detached from the catalyst and easily vaporized by preventing the catalyst from continuously lying on a moving bed due to the downward movement of the catalyst, and which can naturally increase thermal efficiency by controlling the flow of the catalyst and the flow of decomposed gas oil.
  • a second object of the present invention is to provide an economical catalyst regeneration technology, which can exhibit a fluid bed effect even in a moving bed catalyst regeneration tower, and in which the heat of combustion of a catalyst is used as an ignition source, and thus a supply of heat is not required.
  • a third object of the present invention is to provide a technology allowing stable circulation of a catalyst.
  • a fourth object of the present invention is to provide a technology of basically preventing the ignition of fluids when the fluids move between apparatuses through pores of a particulate catalyst due to the difference in pressure between the apparatuses.
  • the present invention provides a contact catalytic cracking method, in which a catalyst flows from a down location upwards, contrary to conventional catalytic cracking methods, so that the heat supplied to the catalyst flows from a down location upwards and simultaneously enables the decomposed gas detached from the catalyst to naturally vaporize, and in which the size of a catalyst moving bed is minimized, so that the catalyst is prevented from lying on the catalyst moving bed, with the result that decomposed gas can be easily detached from the catalyst.
  • the present invention provides a contact catalytic cracking apparatus using an upward moving bed catalyst (referred to as a bucket elevating cracker) provided therein with a bucket elevator transferring a catalyst from a down location upwards and an electric heater controlling the temperature in the upward catalytic cracking apparatus.
  • This bucket elevator includes a bucket filled with the catalyst, a conveyor link forming a transfer pathway while moving up and down and rotating, and a sprocket gear transmitting power to the conveyor link from the outside or supporting the movement of the conveyor link.
  • the bucket may have a volume of below 50 L, and the outer wall of the bucket is formed of meshed screen, so that decomposed gas oil formed in the catalyst can be easily detached therefrom.
  • the size and number of the bucket elevators is very important to determine reaction time. It is preferred that the reaction time in the catalytic cracking apparatus be 3 ⁇ 10 minutes. In consideration of the reaction time, the size and number of the buckets and the length of the conveyor link are to be determined.
  • a temperature control unit provided in the contact catalytic cracking apparatus serves to maintain reaction temperature. In order to prevent the ignition of the decomposed gas oil due to the introduction of oxygen, a heater emitting radiant heat is used as the temperature control unit. It is preferred that the reaction temperature be controlled in a range of 450 ° C ⁇ 550 ° C .
  • the present invention provides an apparatus for sucking decomposed gas oil produced in the contact catalytic cracking apparatus and then rapidly discharging the decomposed gas oil to the outside.
  • This apparatus includes a pressure transmitter measuring the pressure of the decomposed gas oil and a suction blower discharging the decomposed gas oil, and serves to collect the decomposed gas oil without causing the difference in pressure between a contact catalytic cracking reactor and a catalyst regenerator.
  • a moving-bed catalyst regeneration tower is manufactured in a vertical fashion such that the combustion heat flowing upward from the catalyst regeneration tower can easily burn carbon in the catalyst lying on the upper portion of the catalyst regeneration tower, and a multi-stage air supply unit is vertically provided in the catalyst regeneration tower such that the flow of air on a moving bed is the same as the flow of air on a fluid bed, and further, electric heaters having the same number as the air distributors are provided in the catalyst regeneration tower.
  • the present invention provides a vertical catalyst regeneration tower, the inner diameter and capacity of which is designed such that it takes 3 ⁇ 10 minutes to regenerate a catalyst, and the inner wall of which is provided with a castable refractory material in order to prevent it from being overheated by combustion heat .
  • the present invention provides multi-stage air distributors and electric heaters, which are vertically provided in the catalyst regeneration tower.
  • the multi ⁇ stage air distributors are uniformly distributed in the catalyst regeneration tower, and enable air to uniformly flow in a catalyst moving bed as well as in a catalyst fluid bed, and are provided in the catalyst regeneration tower together with the electric heaters such that the air distributor and electric heater make a pair.
  • the electric heaters are provided right over the respective air distributors in order to efficiently supply heat and to prevent the electric heaters from being damaged by the air becoming overheated owing to the accumulation of air.
  • the amount of the catalyst loaded in a catalyst regenerator and catalyst storage units are accurately measured in real time, and thus the catalyst regenerator and catalyst storage units are operated such that these measured data are combined with the control speed of a catalyst transfer unit.
  • the present invention provides a load cell unit measuring the weight of two catalyst storage units (referred to as "catalyst hoppers" ) located between a catalyst reactor and a catalyst regenerator.
  • the load cell unit In order for the load cell unit not to be influenced by the change in weight of the two catalyst storage units, the change in weight thereof being caused by pipes connected to the catalyst storage units, the catalyst storage units are connected to each other using flexible pipes.
  • the present invention provides an apparatus for measuring the level of a catalyst in the upper portion of a catalyst generator.
  • This apparatus measures the height of a catalyst in the upper portion of a catalyst regenerator using a laser, and is provided with an additional measuring tube to compensate for the measuring error caused by dusts and flame generated from a combustion furnace in the upper portion of the catalyst generator.
  • the present invention provides screw feeders provided at the lower ends of the catalyst storage units and the catalyst regenerator and the above mentioned bucket elevator in the catalytic cracking reactor. These screw feeders and bucket elevator are operated by a reduction motor controlled by a frequency control unit, and their speeds are controlled by the weight of the load cell and the values measured by a laser sensor.
  • a catalytic cracking reactor may not be controlled by measuring and controlling the amounts of the catalysts charged in the catalyst regenerator and the catalyst storage units.
  • the present invention provides the above mentioned catalyst storage unit, which is a physical device serving to compensate for the ununiform flow of a catalyst and to basically prevent the phenomenon in which decomposed gas oil charged in the contact catalytic cracking reactor is brought into contact with air charged in the catalyst regenerator, and thus the decomposed gas oil is fired.
  • the height of the catalyst stored in this apparatus must be determined by pressure loss design.
  • the present invention provides a heat exchanger, which is provided at the rear end of a combustion gas outlet in order to remove excess positive pressure caused by the thermal expansion of combustion gas in the upper portion of the catalyst regenerator, and which serves to enable the combustion gas to be easily discharged by greatly decreasing the volume of the combustion gas, and provides a pressure balancing pipe which serves to transfer the high-pressure air coming out of the lower end of the catalyst regenerator in the direction in which discharged gases flow without applying any pressure load to the catalyst storage unit.
  • the contact catalytic cracking system using a upward moving bed catalyst according to the present invention is advantageous in that it can overcome the problems of a decrease in decomposition efficiency, ununiform catalyst generation, uneconomical thermal efficiency, an unreliable catalyst circulation control method, and the ignition of decomposed gases in the contact catalytic cracking system, and further in that it can maintain the rapid decomposition of raw materials and the uniform regeneration performance of the catalyst, and in that it can be variously designed in small size.
  • FIG. 1 is a schematic view showing a contact catalytic cracking system according to an embodiment of the present invention.
  • the system for catalytic cracking using a moving bed catalyst includes a mixer for mixing a molten polymer, which is a raw material used for cracking, with a catalyst; a catalytic cracking apparatus using an upward moving bed catalyst (referred to as a bucket elevating cracker); a vertical catalyst regenerator; two catalyst storage units (referred to as catalyst hoppers); three catalyst transfer units (referred to as screw feeders); and the like.
  • the mixer 1 serves to mix a molten hydrocarbon polymer, which is a raw material used for cracking, with a regenerated catalyst. Since the catalyst introduced into the mixer 1 from a catalyst transfer unit 12 supplies most of heat necessary for cracking, the catalyst is referred to as a contact catalyst.
  • the mixing ratio of the catalyst to the raw material is determined in consideration of total decomposition heat and evaporation heat. In the present invention, it is preferred that the mixing ratio of the catalyst to the raw material be 3 ⁇ 10: 1.
  • the temperature of the catalyst is in a range of 450 ° C ⁇ 550 ° C
  • the temperature of the raw material is in a range of 300 ° C ⁇ 350 ° C .
  • the mixer 1, having a cylindrical shape, is provided therein with a zigzag multi-stage slope way such that a catalyst curtain is formed when a catalyst flows through the multi-stage slope way and falls down.
  • the raw material is introduce into the middle portion of the mixer 1, and then mixed with the catalyst.
  • wax materials which are formed into azeotropes and vaporized by low molecular weight gas, are instantaneously produced. These wax materials move toward the top of the mixer 1, and simultaneously come into contact with the catalyst on the catalyst curtain, so that they are decomposed again.
  • a discharge line is connected to the upper portion of the mixer 1 such that decomposed gases are discharged therethrough.
  • the contact catalytic cracking apparatus 2 is provided therein with electric heaters in order to compensate for thermal loss. These electric heaters emit radiant heat to prevent the ignition of decomposed gas oil.
  • the temperature of the contact catalytic cracking apparatus 2 is in a range of 350°C ⁇ 450°C .
  • a suction blower 14 is provided over the contact catalytic cracking apparatus 2.
  • the suction blower 14 serves to forcibly discharge excess decomposed gas oil produced in the catalytic cracking apparatus 2 to maintain the temperature of the catalytic cracking apparatus 2 constant. Due to this action of the suction blower 14, reaction yield can be increased without performing a steam stripping process and an oil separation process in fluid catalytic cracking.
  • the catalytic cracking apparatus 2 is completely sealed such that decomposed gas oil is not brought into contact with external air. After the decomposition reaction, the catalyst is transferred to a regenerative catalyst storage unit 3 (referred to as a catalyst hopper).
  • Regenerative catalyst storage unit (catalyst hopper) ⁇ 62> After the decomposition reaction, the catalyst is transferred to a regenerative catalyst storage unit 3 from the contact catalytic cracking apparatus 2 along a sloping path.
  • the regenerative catalyst storage unit 3 is provided in consideration of being placed at a sufficient height such that it can prevent the movement of fluid due to the difference in pressure between the catalytic cracking apparatus 2 and a catalyst regenerator 4.
  • the regenerative catalyst storage unit 3 has a function of measuring the change in weight of the catalyst. In order to accurately measure the change in weight of the catalyst, the regenerative catalyst storage unit 3 is connected to outer apparatuses using a flexible pipe. Further, the regenerative catalyst storage unit 3 has another function of refilling a new catalyst corresponding to the loss of the circulated catalyst.
  • a horizontal screw feeder 10 serves to control the total amount of the catalyst.
  • the catalyst discharged from the catalyst storage unit is introduced into a catalyst regenerator 4 by the catalyst transfer unit 10, and the carbon deposited in the pores of the catalyst is burned.
  • Electric heaters 7 are used as the ignition source.
  • the electric heaters 7 are disposed in the catalyst generator 4 at regular intervals to uniformly regenerate the catalyst.
  • Air distributors 8 are disposed right under the respective electric heaters 7, and serve to uniformly diffuse the heat generated from the electric heater 7 and to supply air into the catalyst generator 4.
  • the carbon deposited on the catalyst can be continuously burned by the heat generated from the electric heaters 7 and the air supplied from the air distributors 8.
  • the normal operating temperature of the catalyst regenerator 4 is 650°C ⁇ 750°C .
  • the catalyst regenerator 4 Since the catalyst regenerator 4 is provided with a heat exchanger for cooling air at the rear end thereof, combustion air is easily discharged due to the pressure difference, so that back pressure does not occur, thereby decreasing the load of the entire process.
  • a laser reflection type level measuring device 13 is provided in the top portion of the catalyst regenerator 4. This level measuring device 13 is particularly fabricated using an air-purging type laser in order to remove the measurement error caused by dust and flame.
  • the time taken to regenerate the catalyst in the catalyst regenerator 4 is determined by a horizontal screw feeder 11 provided under the catalyst regenerator 4. It is preferred that the time taken to regenerate the catalyst be in a range of 3 ⁇ 10 minutes.
  • the catalyst regenerated in the catalyst regenerator 4 is transferred to a reactive catalyst storage unit 5 by a catalyst transfer unit 11.
  • this reactive catalyst storage unit 5 serves to prevent the air in the catalyst regenerator 4 from being brought into contact with the decomposed gas in the catalyst cracking apparatus 2, and serves to solve the excessive heat and pressure in the catalyst. Therefore, unlike the regenerative catalyst storage unit 3, the reactive catalyst storage unit 5 is provided therein with a heat exchanger for cooling a catalyst, so that the catalyst is made to have a temperature necessary for reaction, thereby preventing the introduction of overheated catalyst. Further, the reactive catalyst storage unit 5 is configured to be pressure- balanced with a flue gas line such that the positive-pressure air introduced into the reactive catalyst storage unit 5 from the catalyst regenerator 4 does not flow into the catalytic cracking apparatus 2 and can be safely discharged.
  • the catalyst in the reactive catalyst storage unit 5 is introduced into the mixer 1 by a catalyst transfer unit 12 at a predetermined flow rate, while the weight of the catalyst being maintained constant.
  • waste synthetic resins are difficult to collect in large quantities in one place, considering transportation expenses, collection routes, and the like, they are actually treated in small quantities at every place from which the waste synthetic resins are collected. Further, since waste synthetic resins are difficult to select because they are mixed with other waste materials or foreign materials, the ratio of recycled synthetic resins is very limited. These waste synthetic resins which cannot be recycled incur environmental pollution and increase treatment expenses.
  • the contact catalytic cracking apparatus using a upward moving bed catalyst according to the present invention is designed such that waste synthetic resins, which are collected in small quantities and have low recycle ratio, are more efficiently decomposed and treated. Since this contact catalytic cracking apparatus functions to prevent the deterioration of catalytic performance by separating undecomposed inorganic materials from a catalyst in a catalytic cracking process, it can be very usefully used to decompose and treat waste vinyl products which are very difficult to treat in agricultural villages.
  • the present invention provides an apparatus for converting waste synthetic resins, which are difficult to recycle, into higher value-added fuel oils. Since this apparatus does not produce decomposed residues, like fluid catalytic cracking apparatuses, it contributes to environmental conservation.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Wood Science & Technology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

La présente invention concerne un procédé de production de pétroles légers, comprenant la décomposition de polymères d'hydrocarbures par un processus de craquage catalytique de contact et, plus particulièrement, un procédé de décomposition de pétroles lourds en pétroles légers par craquage catalytique en lit fluidisé (FCC) ou par craquage catalytique en lit mobile (MBCC) classique, le procédé pouvant être mis en oeuvre dans un appareil de petite taille. La présente invention concerne un procédé permettant de décomposer et de traiter en continu une résine synthétique usée, ce procédé faisant intervenir une structure de circulation du catalyseur et consistant: à soumettre une résine de synthèse usée à un craquage catalytique de contact à l'aide d'un catalyseur en lit mobile à flux ascendant avec un élévateur à godets; et à régénérer le catalyseur à l'aide d'un régénérateur de catalyseur à flux ascendant à chauffage électrique. Des unités de stockage du catalyseur sont fournies pour chacune des étapes du procédé.
PCT/KR2008/001201 2007-03-15 2008-03-03 Procédé et système de craquage catalytique de contact dans lesquels est utilisé un lit catalytique mobile vertical à flux ascendant Ceased WO2008111750A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
KR1020070025332A KR100791216B1 (ko) 2007-03-15 2007-03-15 상향식 이동상 촉매에 의한 접촉촉매분해 방법과 그장치
KR10-2007-0025332 2007-03-15

Publications (1)

Publication Number Publication Date
WO2008111750A1 true WO2008111750A1 (fr) 2008-09-18

Family

ID=39216551

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/KR2008/001201 Ceased WO2008111750A1 (fr) 2007-03-15 2008-03-03 Procédé et système de craquage catalytique de contact dans lesquels est utilisé un lit catalytique mobile vertical à flux ascendant

Country Status (2)

Country Link
KR (1) KR100791216B1 (fr)
WO (1) WO2008111750A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3144345A4 (fr) * 2014-07-31 2017-05-31 JFE Steel Corporation Procédé de décomposition thermique de substances organiques
CN115305107A (zh) * 2022-08-29 2022-11-08 中国石油化工股份有限公司 一种流化床轻烃加工装置的再生器外补热设备

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101001012B1 (ko) 2009-07-30 2010-12-15 구재삭 폐플라스틱의 고압접촉촉매 분해에 의한 가스화 방법과 그 장치
KR101846479B1 (ko) 2016-12-12 2018-04-09 한국지역난방공사 고온 버켓 엘리베이터를 이용한 순환 유동층 반응기

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4578370A (en) * 1985-04-25 1986-03-25 Uop Inc. Gas circulation method for moving bed catalyst regeneration zones
KR20050000069A (ko) * 2003-06-23 2005-01-03 최영철 폐합성수지에서 탄화수소류를 회수하기 위한 다중낙하촉매열분해공법
US6884400B1 (en) * 2001-06-22 2005-04-26 Uop Llc Reaction and regeneration system

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09310075A (ja) * 1996-05-22 1997-12-02 Densen Sogo Gijutsu Center ゴム・プラスチック廃棄物の処理方法および処理装置

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4578370A (en) * 1985-04-25 1986-03-25 Uop Inc. Gas circulation method for moving bed catalyst regeneration zones
US6884400B1 (en) * 2001-06-22 2005-04-26 Uop Llc Reaction and regeneration system
KR20050000069A (ko) * 2003-06-23 2005-01-03 최영철 폐합성수지에서 탄화수소류를 회수하기 위한 다중낙하촉매열분해공법

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP3144345A4 (fr) * 2014-07-31 2017-05-31 JFE Steel Corporation Procédé de décomposition thermique de substances organiques
CN115305107A (zh) * 2022-08-29 2022-11-08 中国石油化工股份有限公司 一种流化床轻烃加工装置的再生器外补热设备

Also Published As

Publication number Publication date
KR100791216B1 (ko) 2008-01-03

Similar Documents

Publication Publication Date Title
CN106362651B (zh) 混合物热处理反应器及其制造方法、使用工艺和所得产品的用法
RU2763026C2 (ru) Печь
CN105219406B (zh) 一种设备和用于转化含烃材料的方法
CN113939578B (zh) 用于将塑料废物转化成石化产品的塑料油化设备、相应的裂解反应器以及相关的方法
CN101495808B (zh) 带有横向传送系统的水平取向气化器
US6534689B1 (en) Process for the conversion of waste plastics to produce hydrocarbon oils
KR101682734B1 (ko) 연속적 촉매 재생을 위한 염소화 영역에서의 배플의 사용 방법
KR101908540B1 (ko) 소량의 콘라드슨 탄소를 갖는 분획을 처리하기 위한 촉매 크래킹 방법
US20120137939A1 (en) Processes and systems for producing heat for rapid thermal processing of carbonaceous material
JP2012505931A (ja) 各種の有機材料の熱分解用装置および方法
CN101855165A (zh) 循环流化床重整装置
EP0403381A1 (fr) Procédé et dispositif de régulation ou controle du niveau thermique d'un solide pulverulent, comportant un échangeur de chaleur à compartiments en lit fluidisé ou mobile
WO2008111750A1 (fr) Procédé et système de craquage catalytique de contact dans lesquels est utilisé un lit catalytique mobile vertical à flux ascendant
CA2870361A1 (fr) Cornue verticale de surface et procede pour obtenir de l'huile et du gaz a partir de schiste pyrobitumineux et/ou de matieres contenant des composes carbones organiques
KR20040048368A (ko) 플라스틱의 유화방법 및 유화플랜트
CN101778927B (zh) 提炼含油固体的方法和装置
RU2347139C1 (ru) Способ газификации конденсированных топлив и устройство для его осуществления
WO2013119187A2 (fr) Procédé de décomposition thermique de matières organiques et équipement pour sa mise en œuvre
CN1249809A (zh) 反应器
US12344801B2 (en) Reactor fluid supply systems
KR100241543B1 (ko) 폐플라스틱의 분해처리방법과 그 장치
CN101007961B (zh) 渣油烃的热解
CN206996619U (zh) 一种催化裂化再生系统
JP2969417B2 (ja) 廃プラスチックの分解方法
US20230285920A1 (en) Method and device for recycling waste materials containing valuable metals

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08723239

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 08723239

Country of ref document: EP

Kind code of ref document: A1