CN101130469B - Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol - Google Patents

Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol Download PDF

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CN101130469B
CN101130469B CN200610112557XA CN200610112557A CN101130469B CN 101130469 B CN101130469 B CN 101130469B CN 200610112557X A CN200610112557X A CN 200610112557XA CN 200610112557 A CN200610112557 A CN 200610112557A CN 101130469 B CN101130469 B CN 101130469B
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reaction
heat
temperature
heat absorption
catalyst
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CN101130469A (en
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刘中民
齐越
吕志辉
何长青
许磊
张今令
王贤高
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SYN ENERGY TECHNOLOGY Co Ltd
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Dalian Institute of Chemical Physics of CAS
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Priority to AU2007291786A priority patent/AU2007291786A1/en
Priority to JP2009524885A priority patent/JP2010501495A/en
Priority to PCT/CN2007/002537 priority patent/WO2008025247A1/en
Priority to ZA200901045A priority patent/ZA200901045B/en
Priority to BRPI0715687-1A2A priority patent/BRPI0715687A2/en
Priority to KR1020097005634A priority patent/KR20090057027A/en
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    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • 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
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • 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
    • C10G51/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only
    • C10G51/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only
    • C10G51/04—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more cracking processes only plural serial stages only including only thermal and catalytic cracking steps
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
    • 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
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/40—Ethylene production

Abstract

The invention discloses a recycling method of regenerative heat in the low-carbon olefin making course from carbinol through fluid bed technique, which is characterized by the following: entering the high-temperature catalyst into one cracking reacting endothermic area to contact hydrocarbon before contacting carbinol; using the heat to adsorb catalyst from hydrocarbon cracking reaction to reduce the temperature of the catalyst to the temperature of the needed transformation temperature of carbinol.

Description

The recovery method of reactivation heat in a kind of process of preparing low carbon olefinic hydrocarbon with methanol
Technical field
The present invention relates to a kind of recovery method of reactivation heat, specifically, relate to the recovery method of reactivation heat in a kind of process of preparing low carbon olefinic hydrocarbon with methanol.
Background technology
Low-carbon alkene such as ethene, propylene is the basic material of chemical industry.The source of ethene and propylene mainly is the hydrocarbon vapours cracking traditionally, and raw materials used is petroleum naphtha, solar oil and hydrocracking tail oil etc.In recent years, along with sharp rising of oil price, the production cost that adopts above-mentioned raw materials to obtain ethene, propylene constantly rises.Simultaneously, produced in conventional processes ethene and propylene mainly adopt the high temperature process furnances cracking technology, and energy consumption is than higher.These factors impel people to develop the novel process of olefin production.Adopting non-petroleum to produce low-carbon alkene is the operational path that receives more concern in recent years.Wherein, be converted into methyl alcohol, and then become the operational path of low-carbon alkene to be subjected to paying close attention to widely by methanol conversion by coal or natural gas via synthetic gas.Selectivity generates the process of low-carbon (LC) (C2-C4) alkene to methyl alcohol (or by methyl alcohol dehydration generation earlier dme) on molecular sieve catalyst, is commonly referred to the MTO process.In recent years, adopt successive reaction-regenerated fluidized-bed MTO technology to obtain more concern.The ultimate principle of fluidized-bed process is material benzenemethanol to be mixed in reactor with catalyzer make its fluidisation, and is converted into mixture of products such as containing ethene, propylene at a certain temperature, and catalyzer produces carbon distribution and part or all of inactivation after reacting.Gaseous reaction products flows out from reactor and enters tripping device, and decaying catalyst then flows out from reactor continuously and enters revivifier and regenerate, and promptly carbon distribution is removed in burning in oxygen-containing atmosphere, gets back to reactor then and contacts with reaction raw materials.
In above successive reaction-regenerated fluidized-bed process, the area carbon of decaying catalyst is to remove in the mode of high-temp combustion.Usually, the temperature of the reaction of making charcoal is higher than 600 ℃, reaches as high as more than 700 ℃.If disregard the loss of heat radiation, then the heat of the burning of carbon distribution generation migrates out revivifier in two ways: the high temperature regeneration flue gas of discharge is taken away a part of heat, and the heated catalyzer of another part heat is taken away.On the one hand, the heat that the pyritous regenerated flue gas is taken out of, usually recycled to produce methods such as steam or generating, for example, U.S. Pat 20050238543A1 discloses a kind of method that reclaims heat from regenerated flue gas, comprise that with regenerated flue gas through heat exchange repeatedly and lower the temperature, the heat of taking-up is used to produce steam etc.On the other hand, the heat taken out of of the catalyzer after the heating usually is used to react heat supply.Traditionally, fluidized-bed reaction technology is applied to thermo-negative reaction such as catalytic cracking of hydrocarbon usually, and the part of reaction heat provides by heated catalyzer in the regenerative process.Be that carbon distribution is removed in burning in the oxygen-containing atmosphere of decaying catalyst in revivifier, obtain regeneration and heating, get back to reactor then, simultaneously heat is passed to the latter by the former, so that partial reaction heat at least to be provided.But, the mode of this Btu utilization and not to be suitable for methanol conversion be olefine reaction.Because it is strong exothermal reaction that methanol conversion generates alkene, catalyzer is heated in reactor, and the catalyst temperature that only enters reactor is lower than the temperature of reaction bed, could keep the stable of temperature of reaction.Methanol conversion is that the optimization temperature of reaction of low-carbon alkene is 350-600 ℃, is lower than catalyzer coke-burning regeneration temperature (600-700 ℃).Therefore, the catalyzer that regeneration finishes must be emitted the heat that obtains in the regenerative process, enters reactor after the cooling again, and could satisfy methanol conversion is the needs of low-carbon alkene reaction.
Summary of the invention
The object of the present invention is to provide the recovery method of reactivation heat in a kind of process of preparing low carbon olefinic hydrocarbon with methanol.
For achieving the above object, the recovery method of reactivation heat in the process of preparing low carbon olefinic hydrocarbon with methanol provided by the invention, be that the high temperature catalyst after the regeneration is flowed into a scission reaction heat absorption district, the heat that carries by hydrocarbon catalytic cracking reaction absorbing catalyst in this heat absorption district, catalyst temperature enters methanol conversion after descending.
Described method, wherein the catalyzer of Cai Yonging is a Si-Al zeolite or/and SAPO-34, SAPO-11 molecular sieve catalyst, its micropore size is 0.3-0.6nm.
Described method, wherein the substrate material of catalyzer is one or more in silicon oxide, aluminum oxide or the clay.
Described method, wherein the temperature in scission reaction heat absorption district is 400-700 ℃.
Described method, wherein the temperature head of catalyzer between the entrance and exit in scission reaction heat absorption district is 50-300 ℃.
Described method, wherein the hydro carbons that feeds in the scission reaction heat absorption district is that methyl alcohol generates the above product of C4 in the olefine reaction, or/and the hydro carbons of other C4-C20.
Described method, wherein the hydro carbons that feeds in the scission reaction heat absorption district is that petroleum naphtha, gasoline, condensate oil, solar oil, hydrogenation tail oil are or/and kerosene.
Described method, wherein the product that contains ethene and propylene of scission reaction heat absorption district generation is integrated with in the product of methanol conversion generation.
Embodiment
According to the present invention, can adopt the hydrocarbon cracking of heat absorption to react the partial regeneration heat that reclaims in the process of preparing low carbon olefinic hydrocarbon with methanol.Characteristics of the present invention are: for the process of preparing low carbon olefinic hydrocarbon with methanol of the reaction with successive reaction characteristics-regeneration fluidized-bed process, before contacting with methyl alcohol, high temperature catalyst after the regeneration is introduced into a scission reaction heat absorption district, catalyzer after feeding the C4-C20 hydro carbons and regenerate in this heat absorption district contacts, the heat that utilizes hydrocarbon cracking reaction absorbing catalyst to carry, catalyst temperature enters methanol conversion after reducing to the needed temperature of methanol conversion.Low-carbon alkene that scission reaction produces can join in the olefin product of methyl alcohol generation simultaneously.
The invention provides the method for the partial regeneration heat in the following recovery process of preparing low carbon olefinic hydrocarbon with methanol: in the process of preparing low carbon olefinic hydrocarbon with methanol that adopts fluidized-bed process, methanol feedstock mixes in reactor with catalyzer makes its fluidisation, and is converted into the product mixtures that contains ethene, propylene and other hydro carbons at a certain temperature; Produce carbon distribution and part or all of inactivation behind the catalyst reaction; Gaseous reaction products flows out from reactor and enters tripping device, and decaying catalyst then flows out from reactor continuously and enters revivifier and regenerate; Decaying catalyst is carried device through gas earlier before entering revivifier, removes hydro carbons residual on the catalyzer with rare gas elementes such as water vapour, and carbon distribution is removed in burning in the oxygen-containing atmosphere in revivifier then; Heat is emitted in the carbon distribution burning, and this part heat part is taken out of by regenerated flue gas, and another part is then taken out of by the catalyzer after the regeneration; At the catalyzer of revivifier internal heating to 600-700 ℃, after removing residual oxygen through rare gas elementes such as water vapour, enter a scission reaction heat absorption district, this endothermic heat of reaction district can be an independent close phase reaction section, also can be with the lifting section of catalyst transport to methanol conversion simultaneously.In this endothermic heat of reaction district, hydrocarbon raw material contact the heat that generation cracking absorbing catalyst carries with catalyzer after the regeneration.The temperature in this endothermic heat of reaction district is 400-700 ℃, catalyzer is after flowing out above-mentioned endothermic heat of reaction district, temperature reduces 50-300 ℃ than this ingress, heat absorption district, and reaching methanol conversion is the desired temperature of olefin hydrocarbon reactor, enters the reactor that methanol conversion is an alkene then.The product that comprises ethene and propylene that generates in the above-mentioned scission reaction heat absorption district can merge in the product of methanol conversion.Above-mentioned catalyzer comprises Si-Al zeolite that micropore size is 0.3-0.6nm or/and the silicophosphate molecular sieve catalyst, as ZSM-5, ZSM-11, SAPO-34, SAPO-11 etc., and their element modified product.Above-mentioned catalyzer also comprises substrate material, is in silicon oxide, aluminum oxide or the clay one or more; The carbon number of above-mentioned endothermic heat of reaction hydro carbons that the district adopts is between 4-20, and it can be that methyl alcohol generates the above product of C4 in the olefine reaction, can be the hydro carbons of other C4-C20 also, comprises petroleum naphtha, gasoline, condensate oil, solar oil, hydrogenation tail oil and kerosene etc.
Specific embodiment
By the following examples the present invention is made detailed description, but the present invention is not limited to these embodiment.
Embodiment 1:
Conversion reaction result and the reaction heat of butene-2 on molecular sieve catalyst is as shown in table 1.Temperature of reaction is 500 ℃.As can be known from the table data, under this condition in the reaction product selectivity of ethene and propylene be 78.1%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 471KJ/Kg.
Butene-2 cleavage reaction product and reaction heat among table 1: the embodiment 1 (500 ℃)
Figure DEST_PATH_GSB00000302469000021
Embodiment 2:
Conversion reaction result and the reaction heat of butene-2 on molecular sieve catalyst is as shown in table 2.Temperature of reaction is 550 ℃.As can be known from the table data, under this condition in the reaction product selectivity of ethene and propylene be 82.21%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 704KJ/Kg.
Butene-2 cleavage reaction product and reaction heat among table 2: the embodiment 2 (550 ℃)
Figure S061B2557X20060901D000061
Embodiment 3:
Conversion reaction result and the reaction heat of butene-2 on molecular sieve catalyst is as shown in table 3.Temperature of reaction is 600 ℃.As can be known from the table data, under this condition in the reaction product selectivity of ethene and propylene be 80.97%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 825KJ/Kg.
Butene-2 cleavage reaction product and reaction heat among table 3: the embodiment 3 (600 ℃)
Figure S061B2557X20060901D000062
Embodiment 4:
Conversion reaction result and the reaction heat of kerosene on molecular sieve catalyst is as shown in table 4.Temperature of reaction is 550 ℃.The thermodynamic(al)function of kerosene is in n-dodecane.As can be known from the table data, under this condition in the reaction product selectivity of ethene and propylene be 28.91%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 2238KJ/Kg.
Kerosene cleavage reaction product and reaction heat among table 4: the embodiment 4 (550 ℃)
Figure S061B2557X20060901D000071
Embodiment 5:
Conversion reaction result and the reaction heat of kerosene on molecular sieve catalyst is as shown in table 5.Temperature of reaction is 600 ℃.The thermodynamic(al)function of kerosene is in n-dodecane.As can be known from the table data, under this condition in the reaction product selectivity of ethene and propylene be 36.97%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 2821KJ/Kg.
Kerosene cleavage reaction product and reaction heat among table 5: the embodiment 5 (600 ℃)
Embodiment 6:
Conversion reaction result and the reaction heat of gasoline on molecular sieve catalyst is as shown in table 6.Temperature of reaction is 640 ℃.The thermodynamic(al)function of gasoline is in various amylene mean values.As can be known from the table data, under this condition in the reaction product yield of ethene and propylene be 44.01%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 361KJ/Kg.
Naphtha cracking reaction product and reaction heat among table 6: the embodiment 6 (640 ℃)
Figure S061B2557X20060901D000073
Embodiment 7:
Conversion reaction result and the reaction heat of gasoline on molecular sieve catalyst is as shown in table 7.Temperature of reaction is 610 ℃.The thermodynamic(al)function of gasoline is in various amylene mean values.As can be known from the table data, under this condition in the reaction product yield of ethene and propylene be 39.68%, under this products distribution condition, the endothermic heat of reaction of scission reaction is 367KJ/Kg.
Naphtha cracking reaction product and reaction heat among table 7: the embodiment 7 (610 ℃)
Figure S061B2557X20060901D000081

Claims (7)

1. the recovery method of reactivation heat in the process of preparing low carbon olefinic hydrocarbon with methanol, the catalyzer that adopts is that micropore size is that the Si-Al zeolite of 0.3-0.6nm is or/and SAPO-34, SAPO-11 molecular sieve catalyst, high temperature catalyst after the regeneration is flowed into a scission reaction heat absorption district, the heat that carries by hydrocarbon catalytic cracking reaction absorbing catalyst in this heat absorption district, catalyst temperature enters methanol conversion after descending.
2. the method for claim 1, wherein the substrate material of catalyzer is in silicon oxide, aluminum oxide or the clay one or more.
3. the method for claim 1, wherein the temperature in scission reaction heat absorption district is 400-700 ℃.
4. the method for claim 1, wherein the temperature head of catalyzer between the entrance and exit in scission reaction heat absorption district is 50-300 ℃.
5. the method for claim 1, wherein the interior hydro carbons that feeds in scission reaction heat absorption district is that methyl alcohol generates the above product of C4 in the olefine reaction, or/and the hydro carbons of other C4-C20.
6. the method for claim 1, wherein the interior hydro carbons that feeds in scission reaction heat absorption district is that petroleum naphtha, gasoline, condensate oil, solar oil, hydrogenation tail oil are or/and kerosene.
7. the method for claim 1, wherein the product that contains ethene and propylene of scission reaction heat absorption district generation is integrated with in the product of methanol conversion generation.
CN200610112557XA 2006-08-23 2006-08-23 Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol Active CN101130469B (en)

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Application Number Priority Date Filing Date Title
CN200610112557XA CN101130469B (en) 2006-08-23 2006-08-23 Method for recovering reactivation heat in process of preparing low carbon olefinic hydrocarbon with methanol
JP2009524885A JP2010501495A (en) 2006-08-23 2007-08-22 Method for recovering regenerative heat in the process of producing lower olefins from methanol
PCT/CN2007/002537 WO2008025247A1 (en) 2006-08-23 2007-08-22 A process for recovering regenerated heat during the production of lower olefins from methanol
ZA200901045A ZA200901045B (en) 2006-08-23 2007-08-22 A process for recovering regenerated heat during the production of lower olefins from methanol
AU2007291786A AU2007291786A1 (en) 2006-08-23 2007-08-22 A process for recovering regenerated heat during the production of lower olefins from methanol
BRPI0715687-1A2A BRPI0715687A2 (en) 2006-08-23 2007-08-22 METHOD FOR RECOVERING HEAT REGENERATION IN A PROCESS PREPARING LOWER OLEFINS FROM METHANOL.
KR1020097005634A KR20090057027A (en) 2006-08-23 2007-08-22 A process for recovering regenerated heat during the production of lower olefins from methanol

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BRPI0715687A2 (en) 2014-12-23
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