97 results about "Mole ratio" patented technology

The invention discloses an NZP-high-entropy (Ln1 / n) PO4 monazite type multiphase ceramic solidified body and a preparation method thereof, the chemical general formula of the NZP-high-entropy (Ln1 / n) PO4 monazite type multiphase ceramic solidified body is (1-x) Sr0. 5Zr2 (PO4) 3-x (Ln1 / n) PO4, x represents molar percentage, the value range is 0.1-0.9, x represents molar percentage, and the value range is 0.1-0.9. The NZP-high-entropy (Ln1 / n) PO4 monazite type multiphase ceramic solidified body is NZP-high-entropy (Ln1 / n) PO4 monazite type multiphase ceramic solidified body. N represents the number of element types of Ln lattice sites in the high-entropy (Ln1 / n) PO4 monazite type, and n is an integer and is larger than or equal to 5 and smaller than or equal to 7; the Ln element types comprise La, Nd, Sm, Eu, Gd, Ho, Er, Sr0. 5Zr2 (PO4) 3 and (Ln1 / n) PO4, and the molar ratio of the Ln element types to the Sr0. 5Zr2 (PO4) 3 to the (Ln1 / n) PO4 can be freely regulated and controlled. The NZP-high-entropy (Ln1 / n) PO4 monazite type multiphase ceramic solidified body adopts an in-situ preparation process, and integration of crystal phase synthesis and sintering densification can be realized. The preparation method comprises the following steps: uniformly mixing the raw materials, pretreating, adding a sintering aid, mixing again, granulating and aging the obtained powder, molding, removing plastic, and sintering to obtain the NZP-high-entropy (Ln1 / n) PO4 monazite type composite ceramic solidified body. The preparation process disclosed by the invention has the advantages of flexible composition design, capability of simultaneously curing various fission products and (sub) actinide series nuclides, short preparation period, low production energy consumption, high product compactness and the like.

The invention provides a feeding control method and device for an arsenic hydride reaction kettle, equipment and a storage medium, and belongs to the technical field of arsenic hydride reaction, and the method comprises the following steps: determining an initial feeding mode of raw materials at the initial reaction stage based on the volume of the reaction kettle and an expected reaction molar ratio; the raw materials comprise zinc arsenide and dilute sulphuric acid; the desired reaction molar ratio is the desired molar ratio between zinc arsenide and dilute sulphuric acid; in response to the situation that the pressure change rate in the reaction kettle is smaller than a preset change rate value, the initial feeding mode is switched into a constant-speed feeding mode of raw materials in the middle stage of reaction; in response to the condition that the generation rate of the arsenic hydride is lower than a preset generation rate value, switching the constant-speed feeding mode into a final feeding mode of raw materials at the end of the reaction; according to the arsenic hydride reaction kettle feeding control method and device, the equipment and the storage medium provided by the invention, the feeding opportunity and the feeding speed of the reaction kettle can be accurately grasped.

A SCM-33 molecular sieve has a schematic chemical composition as shown in the formula “SiO2·1 / x XO1.5·m MO0.5”, wherein X is a framework trivalent element, the Si / X molar ratio x is ≥5, M is a framework equilibrium cation, and the M / Si molar ratio is 0<m≤1. The molecular sieve is a novel molecular sieve with RTE topology and the molecular sieve requires short preparation time, involves a low synthesis cost and can be used as adsorbent or catalyst.

The invention provides a Raman analysis method of mixed gas content and an ethylene cracking gas detection method and system, and belongs to the technical field of gas mixture online detection.The analysis method comprises the steps that mixed gas is split into n key components, and reference components are determined; performing spectral signal processing on the original Raman spectrum to obtain a normalized spectrum, and determining the relative Raman peak heights of the n key components; based on the relative Raman peak heights and the regression coefficients of the n-1 key components, determining the molar ratios of the n-1 key components relative to the reference component; the molar fractions of the n key components are determined based on the molar ratios of the n-1 key components relative to the reference component. The detection method comprises the following steps: taking an ethylene independent Raman peak near 1345cm <-1 > as a reference peak, and determining the content of each component of the ethylene cracking gas by adopting the analysis method. According to the method provided by the invention, the complex ethylene cracking gas composition can be accurately and rapidly detected.

The application provides a hydrogen arsenide reaction kettle feeding control method and device, equipment and storage medium, and belongs to the technical field of hydrogen arsenide reaction. The method comprises the following steps: determining an initial feeding mode of raw materials in the initial stage of reaction based on the volume of the reaction kettle and an expected reaction molar ratio; the raw materials comprise zinc arsenide and dilute sulfuric acid; the expected reaction molar ratio is an expected molar ratio between the zinc arsenide and the dilute sulfuric acid; in response to a pressure change rate in the reaction kettle being less than a preset change rate value, switching the initial feeding mode to a uniform feeding mode of the raw materials in the middle stage of reaction; and in response to a generation rate of hydrogen arsenide being lower than a preset generation rate value, switching the uniform feeding mode to a final feeding mode of the raw materials in the late stage of reaction. The hydrogen arsenide reaction kettle feeding control method and device, equipment and storage medium provided by the application can accurately grasp the feeding time and feeding speed of the reaction kettle.

This invention relates to a selective gold-based oxidation catalyst, its preparation method, and its application; the catalyst comprises components represented by general formula (1): Au-Sc a / Si b Ce c X d O e In formula (1), a is the molar ratio of Sc to Au, with a value of 0.1 to 1.0; b is the molar ratio of Si to Au, with a value of 100 to 500; c is the molar ratio of Ce to Au, with a value of 1.0 to 30.0; d is the molar ratio of X to Au, with a value of 0.1 to 2.0; e is the number of oxygen atoms required to satisfy the oxidation states of each element in the active component; X is selected from at least one of Li, Na, K, Rb, and Cs. The catalyst of the present invention is used for selective oxidation, with high yield of target product and high conversion rate of raw materials. For example, it has the characteristics of high conversion rate of methacrolein and high yield of methyl methacrylate in the synthesis of alkyl acrylates.

The invention discloses small-particle spherical cerium carbonate, the median diameter D0.5 of the small-particle spherical cerium carbonate is 1.98 to 3.65 [mu] m, the particle size distribution PDI is 0.77 to 1.11, and the sphericity degree S of the small-particle spherical cerium carbonate is 0.91 to 0.96. The cerium carbonate with spherical morphology and particle median diameter of 1.98-3.65 mu m is successfully obtained by adjusting the influence of hydrothermal reaction crystallization temperature, reaction crystallization time, reactant concentration and molar ratio factors on the crystal form of the cerium carbonate.

A method for manufacturing solketal ((2,2-Dimethyl-1,3-dioxolan-4-yl)methanol) includes: (1) milling starting reagents, including at least: glycerol, a catalyst selected from a hard Lewis acid including at least one transition metal, and acetone, the molar ratio (glycerol):(acetone) being less than or equal to 0.8; preferably less than or equal to 0.7, at an ambient temperature greater than or equal to 50° C., preferably greater than or equal to 56° C., in a three-dimensional microbead mill in a liquid phase for a residence time less than or equal to 15 minutes, preferably less than or equal to 10 minutes, and in particular less than or equal to 5 minutes; (2) recovering, as output from the mill, a final composition including solketal and, where appropriate, one or more sub-products corresponding to the starting reagents that have not reacted and / or to 1,3-O-isopropylidene-glycerol, and (3) optionally, separating the solketal from the one or more sub-products.

The invention provides a liquid treatment method, device and equipment, the liquid treatment method comprises a first liquid supply assembly, and the method comprises the following steps: obtaining a current concentration value of a target element in a to-be-treated liquid; wherein the to-be-treated liquid has a preset flow rate, the target element has a molar coefficient, the target element interacts with a reaction element in the reaction liquid, the reaction element has a preset concentration value, and the target element and the reaction element have a molar ratio; determining the target flow of the reaction liquid according to the current concentration value and the molar coefficient of the target element, the preset flow of the liquid to be treated, and the preset concentration value and the molar ratio of the reaction element; according to the target flow of the reaction liquid, a control signal is generated, and the control signal is used for changing the flow of the reaction liquid. By adopting the technical scheme, the dosage of the reaction solution can be adjusted, and the treatment efficiency is improved.

The invention discloses a modified small-grain Y-type molecular sieve as well as a preparation method and application thereof. The total molar content of 0-NNN aluminum and 1-NNN aluminum in the modified small-grain Y-type molecular sieve is 89% or above, preferably 92% or above, based on the total molar weight of X-NNN aluminum; the molar ratio of the 0-NNN aluminum to the 1-NNN is 2.1 to 7.5, and preferably, the molar ratio is 2.3 to 6.0. The modified small-grain Y-type molecular sieve has the advantages that the content and proportion of 0-NNN aluminum and 1-NNN aluminum are high, the crystallinity is high, and the pore volume proportion of 4-8nm mesopores is large; when the modified small-grain Y-type molecular sieve is applied to a hydrocracking catalyst, the yield and quality of middle distillate can be improved.

An one component (1K) composition comprising: a) thermally-expandable thermoplastic microspheres; b) at least one epoxide compound; c) at least one compound which provides at least two amine hydrogens reactive toward epoxide groups; and, d) at least one accelerator, wherein the composition is characterized by a molar ratio of epoxide-reactive groups to epoxide groups from 0.6:1 to 1.2:1, preferably from 0.95: 1 to 1.1:1. The present disclosure envisages the use of this one component (1K) composition in providing an adhesive within a bonded structure upon curing of said composition under conditions in which the constituent microspheres retain their capacity to thermally expand.

The application discloses a continuous Saucy-Marbet ketonization reaction process of allyl alcohol compounds. Specifically provided is a preparation method of compound II, which comprises the following steps: reacting compound I and 2-methoxy propylene in the presence of an acid in a tubular reactor to generate compound II; and the acid is added in the following manner: in the first stage, the molar ratio of the acid to the compound I is 0.005-0.015; in the second stage, the molar ratio of the acid to the compound I is 0.006-0.020; and in the third stage, the molar ratio of the acid to the compound I is 0.009-0.025. The preparation method disclosed by the application has one or more of the following advantages: (1) high yield, (2) high purity, (3) few side reactions, (4) simple operation and (5) low cost.

The invention relates to the technical field of analytical chemistry and hydrometallurgy, in particular to a method for measuring coordination number of organic acid and RE < 3 + > by using a molar ratio method. The method comprises the following steps: S1, preparing a plurality of organic acid solutions of CY with different concentrations, preparing a RE3 + solution of CM, mixing the organic acid solutions and the RE3 + solution in an isovolumetric manner, adjusting the pH value, and carrying out a complexation reaction; s2, carrying out ultraviolet spectrophotometric measurement, determining the maximum absorption wavelength, and determining the absorbance A of the solutions after the complexation reaction under the maximum absorption wavelength; s3, drawing by taking the molar ratio n = [CY] / [CM] as a horizontal coordinate and the absorbance A as a vertical coordinate, and finding out an interval in which the absorbance linearly rises along with the increase of n and an interval in which the absorbance reaches a platform or the slope is obviously changed; linear fitting is conducted on the data points of the two intervals, two straight lines are obtained, and the value of an abscissa n corresponding to the intersection point of the two straight lines is the coordination ratio of the complex. The method is reliable in result, low in cost, easy to popularize, convenient and fast.

Provided is a method for producing an alkane, which performs a reaction at a relatively low reaction temperature and reaction pressure, suppresses carbon reduction with respect to an alcohol, and has excellent conversion rate and selectivity. A method for producing an alkane from an alcohol having 8-24 carbon atoms, said method comprising: a step in which the alcohol having 8-24 carbon atoms and hydrogen are reacted in the presence of a zeolite catalyst and a noble metal from Group 8-10 of the periodic table under the conditions of a reaction temperature of 160 DEG C or higher and a hydrogen pressure of 3 MPa or less in terms of gauge pressure; the zeolite catalyst is of an H-beta type or an H-ZSM-5 type, and the molar ratio (SiO2 / Al2O3) of silica (SiO2) to alumina (Al2O3) is 20-35.

A two component (2K) composition comprising: a first component comprising: a) at least one epoxide compound; and, a second component comprising: b) at least one compound which provides at least one epoxide-reactive group; c) at least one accelerator, wherein the composition further comprises: d) at least one particulate liquid-absorbent polymer, and wherein the composition is characterized by a molar ratio of epoxide groups to epoxide-reactive groups (ER) of from 0.6:1 to 1.2:1, for example from 0.9:1 to 1.1:1.

This application relates to a fluid water-in-oil emulsion comprising: A) at least one polyester, which is a reaction product of the following components (i), (ii) and (iii): (i) at least one polyglycerol-3; (ii) at least one dimer acid; and (iii) at least one fatty monocarboxylic acid having 8 to 30 carbon atoms, wherein the reacting components (i), (ii) and (iii) are in a molar ratio of 1 mole of polyglycerol-3, 0.5 to 1 mole of dimer acid, and 0.1 to less than 2.0 moles of fatty monocarboxylic acid; B) at least one continuous oil phase comprising: 1) at least one volatile hydrocarbon oil; and 2) optionally at least one non-volatile oil; and C) at least one aqueous phase dispersed in the oil phase, wherein the liquid component of the aqueous phase accounts for at least 50% by weight of the total weight of the composition; and D) At least one nonionic surfactant with an HLB of less than 8.0, the chemical structure of which is generated by the reaction of at least one polyhydroxystearic acid and / or at least one polyricinoleic acid with a polyol containing at least two alcohol functional groups; the weight ratio of nonionic surfactant D) to polyester A) is greater than or equal to 0.9 and preferably greater than or equal to 1.0.

The present invention is composition comprising a mixture of a mica and a TR-DRR resin, where each R is independently phenyl or methyl, wherein the mole-to-mole ratio of DRR units to TR units is in the range of from 30:70 to 80:20; and wherein the weight-to-weight ratio of mica to the TR-DRR resin is in the range of 20:80 to 80:20. The composition of the present invention is useful as a coating for a substrate, wherein the coating exhibits good adhesion, and crack-resistance when subjected to high temperatures for several weeks.

A composition containing: (a) a polyether with an average of 1.4 or more unsaturated carbon-carbon bonds per molecule; (b) one or more silyl-hydride functional polysiloxane crosslinker that is free of phenyl groups and that comprises 90 mole-percent or more of a combination of the following siloxane units: H(R3)2SiO1 / 2, SiO4 / 2 and optionally (R3)3SiO1 / 2 where the average number per molecule of H(R3)2SiO1 / 2 units is 2 or more, the average number per molecule of SiO4 / 2 units is one or more and the average number per molecule of (R3)3SiO1 / 2 units is such that the number of (R3)3SiO1 / 2 units divided by the sum of H(R3)2SiO1 / 2 and (R3)3SiO1 / 2 units is less than 0.7; where R3 is independently in each occurrence selected from hydrocarbyl groups having from one to 8 carbon atoms; and (c) a hydrosilylation catalyst; where the molar ratio of SiH / C═C in the composition is in a range of 0.3 to 10.

The application discloses a method for regulating bubble size in a high-temperature molten salt bubbling tower, comprising the following steps: according to the diameter range of the target bubble required by the bubbling tower, a single-hole bubbling experimental device is built by selecting a bubble distributor with a corresponding characteristic aperture; according to the component of the molten salt required by the bubbling tower, a database of the relationship between the molar ratio of each chemical component of the molten salt and the physical properties is established; in the single-hole bubbling experimental device, a regulation mode is selected according to the size of the characteristic aperture of the bubble distributor, the adjustable range of the bubble diameter is adjusted to the diameter range of the target bubble required by the bubbling tower; and the obtained regulation mode is applied to the bubbling tower; the application can reveal a comprehensive solution of the synergistic mechanism among multiple parameters, so as to realize accurate and predictable control of the bubble size from microns to millimeters, and solve the technical problems from laboratory research to industrial device amplification.

The invention relates to a method for continuously producing n-butyl(meth)acrylate by reacting (meth)acrylic acid with n-butanol in the presence of an acid catalyst and a polymerization inhibitor. In a first embodiment, the method has the steps of: *carrying out an esterification within a reactor (A) comprising a column (B) installed thereon, wherein the components (meth)acrylic acid and n-butanol are used in a molar ratio ranging from 1.0:1.0 to 10:2.0, preferably 1.0:1.1 to 1.0:1.5, and the esterification is carried out at a temperature ranging from 80 to 150° C., preferably 100 to 130° C., and an absolute pressure ranging from 0.2 to 5.0 bar, preferably 0.4 to 1.5 bar, whereby a resulting reaction product (6) and a vapor flow are obtained at the head of the column (B), *discharging the vapor flow at the head of the column (B), *condensing the vapor flow in a condenser (C), thereby forming an organic phase, which is enriched with n-butyl(meth)acrylate, and an aqueous phase, *continuously separating the organic phase from the aqueous phase by means of a phase separator (D), *supplying the resulting reaction product (6) to a rectification column (E), *separating the azeotrope within the rectification column (E) consisting of: a) water and n-butyl(meth)acrylate, b) n-butanol and n-butyl(meth)acrylate, c) n-butanol and water, and d) n-butanol, n-butyl(meth)acrylate, and water, wherein the rectification column (E) is operated at a sump temperature ranging from 80 to 150° C. and at a temperature at the head ranging from 70 to 130° C. and an absolute pressure ranging from 0.2 to 5 bar, preferably 0.4 to 1.5 bar, *discharging a gas flow enriched with the azeotrope at the head of the rectification column (E), *condensing the gas flow in a condenser (F), thereby forming an organic phase, which is enriched with n-butyl(meth)acrylate, and an aqueous phase, *continuously separating the organic phase from the aqueous phase by means of a phase separator (G), *continuously discharging at least one part of the organic phase out of the phase separator (G), said discharged part of the n-butyl(meth)acrylate-enriched organic phase constituting the raw product flow (15), *discharging a high-boiling sump discharge (23) out of the sump of the rectification column (E), the mass flow ratio of the high-boiling sump discharge (23) to the (meth)acrylic acid supplied to the reactor (A) as a reactant ranging from 0.5 to 5, *supplying a high-boiling sub-flow (7) of the discharged high-boiling sump discharge (23) to a mixer (H), the mass flow ratio of the high-boiling sub-flow (7) to the high-boiling sump discharge (23) ranging from 0.01 to 0.5, preferably 0.05 to 0.08, *supplying a mixture (10) resulting from the mixer (H) to an extraction phase separator (I) arranged downstream thereof, and *continuously separating the mixture in the extraction phase separator (I), thereby obtaining an organic raffinate (11) and an aqueous catalyst-containing extract (12), said aqueous extract (12) being at least partly recirculated to the reactor (A) and / or the rectification column (E), wherein—a sub-flow of the aqueous phase (18) from the phase separator (G), —a sub-flow of the aqueous phase (26) from the phase separator (D) and / or —a sub-flow of the aqueous phase (5) from the phase separator (D) is supplied to the phase separator (G), and subsequently a sub-flow of the aqueous phase (18) from the phase separator (G) is supplied to the mixer (H). The mass flow ratio of the sub-flow of the aqueous phase (18) to the high-boiling sub-flow (7) of the discharged high-boiling sump discharge (23) ranges from 0.08 to 0.50, and the mass flow ratio of the sub-flow of the aqueous phase (5) to the high-boiling sub-flow (7) of the discharged high-boiling sump discharge (23) ranges from 0.08 to 0.50.

The present invention relates to a process for preparing a polyester of glycerol and a dicarboxylic acid, the process comprising: (a) contacting monomers comprising at least glycerol and dicarboxylic acid in the presence of water in an inert atmosphere at a temperature of less than 100 DEG C wherein the molar ratio of glycerol / dicarboxylic acid ranges from 0.5 / 1 to 10 / 1; (b) carrying out esterification in an inert atmosphere at a temperature higher than 110 DEG C; (c) at a temperature higher than 110 DEG C, vacuumizing the reaction medium to a pressure lower than 100 mbar; (d) maintaining a vacuum and a temperature above 110 DEG C to carry out polycondensation, said process comprising: at the end of the esterification of step (b), before or after the evacuation of step (c), introducing a polycondensation catalyst in an amount of less than or equal to 5000 ppm with respect to the total weight of monomers, said catalyst being a tin-based food grade catalyst, the organic tin compounds are selected from organic tin compounds containing carboxyl functional groups (-C (O) OH), organic tin compounds containing functional groups (-Sn (O) OH) and mono-butyltin tris (2-ethylhexanoate). The present invention relates to a process for synthesizing glycerol polyesters having a residual monomer content of less than 5% by weight, based on the weight of the polymer, a high number average molar mass Mn of greater than 2500 g / mol, a dispersity of less than or equal to 10 and a 1, 2, 3-triacylglyceride unit content of less than 15 mol% with respect to all units of the polymer, in particular to the synthesis of glycerol polyesters having a residual monomer content of less than 5% by weight, based on the weight of the polymer, a high number average molar mass Mn of greater than 2500 g / mol.

The present invention discloses an SCM-38 molecular sieve and a preparation method thereof. The SCM-38 molecular sieve is a new type of molecular sieve, and its chemical composition includes, in molar ratio: SiO2: Al2O3: P2O5 = 0-0.1: 0.8-1.5: 1, and the XRD pattern of the SCM-38 molecular sieve includes X-ray diffraction peaks at 2θ of 7.20 ± 0.1, 10.81 ± 0.1, 11.60 ± 0.1, 14.32 ± 0.1, 21.39 ± 0.1, 21.83 ± 0.1, 27.31 ± 0.1, and 28.72 ± 0.1, wherein 2θ is 7.20 ± 0.1 as the strongest peak. The SCM-38 molecular sieve provided by the present invention can be used in adsorbents or catalysts.

The invention relates to a composition containing a novolak and water. In one embodiment, a composition is provided comprising novolak and water with the percentage of ortho linkages of the phenol rings of the novolak is greater than that of para linkages, the novolak having a phenolic compound and an aldehyde molar ratio of from 1:0.2 to 1:0.45 and the composition having from 2% to 20% by weight of water based on the weight of the sum of the novolak and the water.

Disclosed is γ-2CaO∙SiO2-containing fired product which is characterized by satisfying the requirements (a) to (c) described below.　(a) The ratio C' / S' (molar ratio) expressed by ([CaO] - 4[Fe2O3]) / [SiO2] is 1.90 to 2.10.　(b) The ratio Fe2O3 / Al2O3 (molar ratio) is 0.90 to 1.10.　(c) Fe2O3 is 20.00 mass% or less.

The present invention discloses a eutectic aluminophosphate material and a preparation method thereof. The chemical composition of the eutectic aluminophosphate material, in terms of molar ratio, is SiO2:Al2O3:P2O5 = 0 - 0.10:0.88 - 1.30:1. The XRD pattern of the eutectic aluminophosphate material contains a broad peak appearing between 2θ of 4.60 ± 0.05 and 5.70 ± 0.05, and X-ray diffraction peaks appearing at 2θ of 7.20 ± 0.1, 10.81 ± 0.1, 11.60 ± 0.1, 14.32 ± 0.1, 21.39 ± 0.1, 21.83 ± 0.1, 27.31 ± 0.1, 28.72 ± 0.1, where the peak at 2θ of 7.20 ± 0.1 is the strongest peak. The eutectic aluminophosphate material provided by the present invention is a novel eutectic material and can be applied in adsorbents or catalysts.

The present invention relates to a process for NH3 reforming, the process comprising: (i) providing a reactor containing an NH3 reforming catalyst C1, the NH3 reforming catalyst comprising a metal M1 selected from the group consisting of Groups 6 to 11 of the Periodic Table, including mixtures of two or more thereof; (ii) preparing a feed gas stream F1 comprising NH3; (iii) feeding F1 into the reactor and contacting F1 with C1, wherein the reactor has a temperature of 100 DEG C or higher; obtaining a product gas stream P1 comprising H2O and an NH3 reforming catalyst C2; wherein the feed according to (ii) begins at the point in time t1; wherein at point in time t2, the molar ratio of H2O in P1 to H2O in F1 is greater than 1: 1, and wherein the difference between t2 and t1 is in the range of 5 s to 10 days.

The invention provides an SCM-44 molecular sieve as well as a preparation method and application thereof. The chemical composition of the SCM-44 molecular sieve is xSiO2.y GeO2, the molar ratio of SiO2 to GeO2 is x / y, x / y is larger than or equal to 40, and preferably x / y is larger than or equal to 50. The framework of the SCM-44 molecular sieve contains an Si element and other optional elements, and the SCM-44 molecular sieve has flaky morphology, high specific surface area, large micropore volume and excellent adsorption and catalytic performance.

This inorganic compound includes M, O, and F, in which M is one or more kinds of transition metal elements, when defining a molar ratio of O as “b” and defining a molar ratio of F as “c”, (b / c) is 0.60 or more and 2.30 or less, and a half-value width of a diffraction peak of a (110) plane obtained by X-ray diffraction analysis is 0.60° or less. Also, the inorganic compound includes M, O, and F, in which M is one or more kinds of transition metal elements, when defining a molar ratio of O as “b” and defining a molar ratio of F as “c”, (b / c) is 1.50 or less, and a half-value width of a diffraction peak of a (110) plane obtained by X-ray diffraction analysis is 0.45° or more.

To provide a method for producing propylene capable of producing propylene with a comparatively excellent yield.SOLUTION: A method for producing propylene pertaining to the present invention includes: a reaction process A of obtaining a crude product (A) from a raw material including ethanol in the presence of a catalyst (A); and a reaction process B of obtaining a crude product (B) from the crude product (A) in the presence of a catalyst (B), where compositions of the catalyst (A) and the catalyst (B) are mutually different, the catalyst (A) includes at least two metals M and N selected from the group consisting of zirconium or the like, the mole ratio of the metal M to the metal N is less than 100, and the amount of an acid sites of the catalyst (B) is 50 μ mol / g or more.SELECTED DRAWING: None

A calcine containing γ-2CaO·SiO2, characterized in that it satisfies the following conditions of a) to c). a) C' / S' (molar ratio) represented by {[CaO]-4[Fe2O3]} / [SiO2] is 1.90 to 2.10. b) Fe2O3 / Al2O3 (molar ratio) is 0.90 to 1.10. c) Fe2O3 is 20.00 mass% or less.