WO2005105710A1 - 低級オレフィンの製造法 - Google Patents
低級オレフィンの製造法 Download PDFInfo
- Publication number
- WO2005105710A1 WO2005105710A1 PCT/JP2005/008067 JP2005008067W WO2005105710A1 WO 2005105710 A1 WO2005105710 A1 WO 2005105710A1 JP 2005008067 W JP2005008067 W JP 2005008067W WO 2005105710 A1 WO2005105710 A1 WO 2005105710A1
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- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- producing
- rare earth
- zeolite
- earth element
- Prior art date
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C4/00—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms
- C07C4/02—Preparation of hydrocarbons from hydrocarbons containing a larger number of carbon atoms by cracking a single hydrocarbon or a mixture of individually defined hydrocarbons or a normally gaseous hydrocarbon fraction
- C07C4/06—Catalytic processes
-
- 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
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the present invention relates to a method for producing a lower-order olefin, mainly ethylene and propylene, in a high yield over a long period of time by catalytically cracking a hydrocarbon raw material using a catalyst.
- Lower-order olefins such as ethylene and propylene are important substances as basic raw materials for various types of danigaku products.
- these lower-olefins have been produced by using gaseous hydrocarbons such as ethane, propane, butane or liquid hydrocarbons such as naphtha as raw materials and thermally decomposing them in a steam furnace in an externally heated tubular furnace.
- the method is widely practiced.
- this method requires a high temperature of 800 ° C or higher to increase the olefin yield, and requires the use of expensive equipment materials. It has disadvantages.
- various catalytic cracking methods for hydrocarbons using a catalyst have been studied. Among them, many examples have been reported when a solid acid, particularly zeolite, is used as a catalyst because it can be decomposed at a relatively low temperature (350 to 700 ° C).
- Patent Document 1 discloses a catalytic cracking method of naphtha using a ZSM-5 type catalyst in which the acid amount and the acid strength are controlled to specific ranges! This method produces a large amount of aromatic components (benzene, toluene, xylene) and cannot obtain olefins efficiently.
- Patent Document 2 discloses a catalytic cracking method of paraffin using mordenite supporting silver. However, there is a problem that the decomposition temperature is high at 720 ° C.
- Patent Literature 3 and Patent Literature 4 disclose catalytic cracking methods for paraffin using ZSM-5 supporting copper, cobalt, silver, and the like. It is reported that this method produces a total of 40-70% of ethylene and propylene in a pulsed reaction of a very dilute raw material, which makes commercial practice difficult. Also, the ethylene yield is as low as 20%.
- Patent Literature 5 and Patent Literature 6 disclose ZSM-5 supporting rare earth elements and phosphorus. Discloses a catalytic cracking method for paraffins and naphtha. In this technique, the production of by-products such as aromatic hydrocarbons and heavy substances is suppressed by the addition of rare earth elements, and the durability of the catalyst is improved by supporting phosphorus. However, according to Non-Patent Document 1, even when this catalyst is used, the yield of the target lower olefin is not always good.
- Patent document 1 JP-A-6-34602
- Patent document 2 U.S. Pat.No. 4,172,816
- Patent Document 3 JP-A-2-1413
- Patent Document 4 Japanese Patent Laid-Open No. 2-184638
- Patent Document 5 JP-A-11-180902
- Patent Document 6 JP-A-11-253807
- Non-Patent Document 1 "1999 Next-Generation Chemical Process Technology Development Results Report (pp. 226-235)"
- the present inventors have conducted intensive studies to solve the above-mentioned problems, and as a result, have used a fixed-bed reactor filled with a crystalline aluminosilicate zeolite catalyst having a specific size and carrying a rare earth element.
- a fixed-bed reactor filled with a crystalline aluminosilicate zeolite catalyst having a specific size and carrying a rare earth element.
- the present invention is characterized by the following gist.
- Catalytic cracking of hydrocarbon raw materials with 2 or more carbon atoms in a fixed-bed reactor filled with catalyst In producing low-level olefins, a crystalline aluminosilicate zeolite containing a rare earth element is used as a catalyst, the size of the catalyst is 14 mesh (1.2 mm) or more, and the pressure loss of the catalyst layer in the reactor is 0.02 MPa.
- a method for producing a low-grade olefin comprising:
- the rare earth element is at least one selected from the group consisting of lanthanum, cerium, praseodymium, neodymium, samarium, gadolinium, and disprosium.
- hydrocarbon raw material is a paraffin having 2 to 30 carbon atoms or a hydrocarbon raw material containing the same as a main component.
- a crystalline aluminosilicate zeolite catalyst having a size of 14 mesh (1.2 mm) or more carrying a rare earth element or a rare earth element and phosphorus is used, and a catalyst layer in a fixed bed reactor is used.
- hydrocarbon raw material used in the present invention gaseous or liquid hydrocarbons at normal temperature and normal pressure can be used.
- a paraffin having 2 to 30, preferably 2 to 20 carbon atoms or a hydrocarbon raw material containing this as a main component (10 wt% or more) is used.
- hydrocarbon raw materials include paraffins such as ethane, propane, butane, pentane and hexane, and light hydrocarbon fractions such as naphtha and light oil.
- the raw material components are not limited to saturated hydrocarbons, and those having components having unsaturated bonds can also be used. Further, an aromatic component may be contained.
- the catalyst of the present invention contains zeolite supporting a rare earth element as a main component.
- zeolite a high silica type zeolite, particularly ZSM-5 or ZSM-11, is preferred.
- Zeolite SiO / Al O-dani preferably 25-800, more preferably 30-600, specially 40
- the rare earth element preferably, lanthanum, cerium, brassodymium, neodymium, samarium, gadolinium, disprosium and the like can be mentioned.
- the rare earth elements may be used alone or in combination of two or more.
- the catalyst is a proton-type zeolite in a solution of various salts of rare earth elements, for example, acetate, nitrate, halide, sulfate, carbonate, or water or ethanol in which alkoxide, acetyl acetonate or the like is dissolved. Can be easily prepared by impregnation, drying and baking.
- a part of the rare earth element enters the pores of the zeolite and a part exchanges ions with the protons of the zeolite, but most of the rare earth elements are supported on the zeolite as oxides.
- the rare earth element needs to be supported on zeolite, and the effect of the present catalyst is hardly obtained only by physically mixing zeolite and rare earth oxide.
- the supported amount of the rare earth element is preferably 0.4 to 20, more preferably 0.6 to 10, and particularly preferably 0.8 to 5 by atomic ratio with respect to aluminum in the zeolite. It is.
- the supported amount is less than 0.4, the formation of aromatic hydrocarbons and heavy substances is not suppressed, and when the supported amount is larger than 20, the catalytic activity decreases, and The yield is lower.
- the catalyst of the present invention may contain components other than zeolite and rare earth elements, for example, alkali metals, alkaline earth metals, transition metals, noble metals, halogens, phosphorus, binders and the like.
- rare earth elements Phosphorus can be supported by impregnating the present catalyst supporting the same with an aqueous solution of diammonium hydrogen phosphate.
- the supported phosphorus is preferably present in the form of an oxidant.
- phosphorus is contained in the present catalyst in an amount of 0.1 to 10% by mass, more preferably 1 to 7% by mass, particularly preferably 2 to 5% by mass in terms of elemental phosphorus.
- the present catalyst can be used by mixing with a filler such as silica, alumina, quartz sand and the like.
- the size of the catalyst packed in the fixed bed reactor and the pressure loss of the catalyst in the reactor are controlled.
- the pressure loss of the catalyst layer in the reactor can be reduced by reducing the flow rate, but it is not industrial. Also, by increasing the diameter of the reactor, the pressure loss of the catalyst layer can be reduced, but this is not practical because the cost of the reaction equipment increases.
- the size of the catalyst to be used is controlled, and the pressure loss of the catalyst is reduced by forming a solid (ring, hollow, or the like) having a predetermined size or more from fine powder.
- the size of the catalyst needs to be more than a certain value, and the size needs to be 14 mesh (1.2 mm) or more, preferably 10 mesh (1. 7 mm) or more, particularly preferably 7 mesh (2.8 mm) or more.
- the size of the catalyst is measured by a Tyler standard sieve.
- 14 mesh or more means a size that does not pass through a 14 mesh sieve.
- the size of the catalyst is usually preferably 60 mm or less, particularly preferably 40 mm or less.
- the shape of the catalyst can be selected from various shapes such as a sphere, a cylinder, a cylinder, a ring, a prism, and a prism.
- the pressure loss of the catalyst layer in the reactor is controlled.
- the pressure loss of the catalyst layer in the reactor is reduced to 0.02 MPa or less. More preferably, the pressure is set to 0.001 MPa or less, particularly preferably 0.008 MPa or less. If the pressure loss force of the catalyst layer is too high, the drift of the raw material gas may occur, so the pressure loss of the catalyst layer is preferably at least 0.001 MPa, particularly preferably at least 0.002 MPa.
- the production of by-products is suppressed by vigor, and a low-level olefin, which is a reaction product, can be obtained in high yield.
- a low-level olefin which is a reaction product
- this performance is maintained for a long time.
- the size of the catalyst and the pressure loss of the catalyst layer in the reactor are not maintained within the above ranges, the secondary reaction of olefins generated on the catalyst and the formation of coat components cannot be suppressed, and lower olefins cannot be produced.
- the selectivity is not improved, and the durability of the catalyst is reduced.
- the catalytic cracking reaction of the present invention is carried out by using a fixed-bed reactor and supplying a hydrocarbon raw material to a catalyst bed filled with the above-mentioned catalyst.
- the hydrocarbon raw material may be diluted with nitrogen, hydrogen, helium, steam, or the like.
- especially steam has an effect of maintaining the activity of the catalyst, and the preferable supply amount of steam is 0.1 to 1, more preferably 0.3 to 0.7 by mass ratio to the raw material hydrocarbon. It is.
- the reaction temperature is usually 350 to 780. C, preferably 500-750. C, more preferably 600-720. C range. Temperatures above 780 ° C are feasible, but methane and coat production will increase sharply. In addition, if the temperature is lower than 350 ° C, sufficient activity cannot be obtained, so that the yield of olefins per pass decreases.
- the obtained white powder was compression-molded and pulverized to a size of 10 to 14 mesh (not passing through a 14-mesh sieve, but passing through a 10-mesh sieve, and having a size of 1.2 to 1.7 mm. This has the same meaning in the examples.)
- 10% La-ZSM-5 catalyst was used. [0019] 1.5 g of this catalyst was diluted with quartz sand and filled into a stainless reaction tube (made of SUS 316) having an inner diameter of 10 mm and a length of 460 mm so that the catalyst layer had a length of 110 mm. The top and bottom of the catalyst layer were filled with stone sand. The temperature of the catalyst layer was increased to 650 ° C.
- Raw material conversion rate (1-unreacted raw material weight Z feed raw material weight) x 100
- the pressure loss of the catalyst layer in the reactor during the above reaction was 0.005 to 0.01 MPa. Table 1 shows the reaction results one hour after starting the supply of the raw materials.
- Example 1 The reaction was carried out in the same manner as in Example 1 except that the size of the catalyst was changed to 14 to 30 mesh (0.5 to 1.2 mm). The pressure loss of the catalyst layer in the reactor during the reaction was 0.04 to 0.05 MPa. Table 1 shows the reaction results one hour after starting the supply of the raw materials.
- the reaction was carried out in the same manner as in Example 1 except that the size of the catalyst was changed to 100 mesh (0.15 mm) or less.
- the pressure loss of the catalyst layer in the reactor during the reaction was 0.11 to 0.14 MPa. Table 1 shows the reaction results one hour after starting the supply of the raw materials.
- this catalyst was impregnated with an aqueous solution of diammonium hydrogen phosphate (0.439 g of ammonium hydrogen phosphate dissolved in 50 g of ion-exchanged water), and stirred at 40 ° C. for 1 hour.
- the resulting slurry was stirred at 40 to 60 ° C. under reduced pressure to evaporate water for about 1 hour to obtain a white powder.
- the obtained powder was dried in air at 120 ° C. for 12 hours, then heated to 600 ° C. in a tubular furnace under air circulation over 4 hours and calcined at 600 ° C. for 5 hours.
- the resulting white The color solid was compression molded, pulverized, and sieved to 10 to 14 mesh (1.2 to 1.7 mm) to obtain a 2% -P-10% La-ZSM-5 catalyst.
- the durability of a catalyst supporting a rare earth element and phosphorus from a gaseous or liquid hydrocarbon can be increased, and a low-level olefin such as ethylene or propylene can be efficiently produced. It becomes possible.
- the size of the catalyst by setting the size of the catalyst to 14 mesh (1.2 mm) or more and the pressure loss of the catalyst layer to 0.02 MPa or less, even after 18 hours from the start of the raw material supply, the raw material transfer rate and The yield power of ethylene and propylene is only 0.93% lower than that after 1 hour, and the durability of the catalyst can be increased.
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- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Catalysts (AREA)
Abstract
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Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2004136460A JP2005314339A (ja) | 2004-04-30 | 2004-04-30 | 低級オレフィンの製造法 |
JP2004-136460 | 2004-04-30 |
Publications (1)
Publication Number | Publication Date |
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WO2005105710A1 true WO2005105710A1 (ja) | 2005-11-10 |
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PCT/JP2005/008067 WO2005105710A1 (ja) | 2004-04-30 | 2005-04-27 | 低級オレフィンの製造法 |
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JP (1) | JP2005314339A (ja) |
WO (1) | WO2005105710A1 (ja) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101348407B (zh) * | 2007-07-18 | 2010-12-22 | 中国石油化工股份有限公司 | 催化裂解制乙烯和丙烯的方法 |
CN110975928A (zh) * | 2019-12-06 | 2020-04-10 | 陕西延长石油(集团)有限责任公司 | 一种无粘结剂zsm-11 分子筛催化剂的改性方法和应用 |
Families Citing this family (8)
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JP5094506B2 (ja) * | 2008-03-28 | 2012-12-12 | 出光興産株式会社 | 軽質オレフィンの製造方法 |
JP5288255B2 (ja) * | 2008-10-29 | 2013-09-11 | 独立行政法人産業技術総合研究所 | 低級オレフィン製造用触媒、その製造方法及びこれを用いた低級オレフィンの製造方法 |
CN102802792A (zh) | 2009-06-22 | 2012-11-28 | 日挥株式会社 | 低级烯烃制造用催化剂及使用其制造低级烯烃的方法 |
JP5188484B2 (ja) | 2009-10-01 | 2013-04-24 | 日本電波工業株式会社 | 恒温型の水晶発振器 |
CN104056654B (zh) * | 2013-03-22 | 2016-07-06 | 中国石油化工股份有限公司 | 一种zsm-5分子筛组合物、制备方法及其应用 |
CN104056652B (zh) * | 2013-03-22 | 2016-05-25 | 中国石油化工股份有限公司 | 一种核壳型zsm-5分子筛小球催化剂 |
CN104056655B (zh) * | 2013-03-22 | 2016-07-06 | 中国石油化工股份有限公司 | 一种核壳型小球催化剂 |
CN103752229B (zh) * | 2014-01-26 | 2015-10-21 | 惠生工程(中国)有限公司 | 一种含氧化合物制烯烃的固定床反应器 |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5629919B2 (ja) * | 1974-06-28 | 1981-07-11 | ||
JPH11180902A (ja) * | 1997-12-16 | 1999-07-06 | Agency Of Ind Science & Technol | 低級オレフィンの製造方法 |
JPH11253807A (ja) * | 1998-03-09 | 1999-09-21 | Agency Of Ind Science & Technol | 低級オレフィン製造用触媒 |
-
2004
- 2004-04-30 JP JP2004136460A patent/JP2005314339A/ja not_active Withdrawn
-
2005
- 2005-04-27 WO PCT/JP2005/008067 patent/WO2005105710A1/ja active Application Filing
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5629919B2 (ja) * | 1974-06-28 | 1981-07-11 | ||
JPH11180902A (ja) * | 1997-12-16 | 1999-07-06 | Agency Of Ind Science & Technol | 低級オレフィンの製造方法 |
JPH11253807A (ja) * | 1998-03-09 | 1999-09-21 | Agency Of Ind Science & Technol | 低級オレフィン製造用触媒 |
Non-Patent Citations (1)
Title |
---|
YAMANAKA T.: "Shokubai Kagaku", 1964, THE NIKKAN KOGYO SHINBUN, LTD., pages: 246 - 251, XP002994418 * |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101348407B (zh) * | 2007-07-18 | 2010-12-22 | 中国石油化工股份有限公司 | 催化裂解制乙烯和丙烯的方法 |
CN110975928A (zh) * | 2019-12-06 | 2020-04-10 | 陕西延长石油(集团)有限责任公司 | 一种无粘结剂zsm-11 分子筛催化剂的改性方法和应用 |
CN110975928B (zh) * | 2019-12-06 | 2022-11-01 | 陕西延长石油(集团)有限责任公司 | 一种无粘结剂zsm-11分子筛催化剂的改性方法和应用 |
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