Initialization method for a process to prepare an olefin oxide, process to prepare an olefin oxide, and, olefin oxide

Description

/ 73 INITIALIZATION METHOD FOR A PROCESS TO PREPARE AN OLEFIN OXIDE, PROCESS TO PREPARE AN OLEFIN OXIDE, AND, OLEFIN OXIDE

[001] In a first aspect, the invention relates to a start-up method for a process for preparing an olefin oxide comprising a normal operating stage, wherein the normal operating stage comprises providing olefin, hydrogen peroxide and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, so that a reaction mixture comprising olefin, hydrogen peroxide and organic solvent is formed, and subjecting the reaction mixture to the epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide and organic solvent; wherein the initiation method comprises (a) providing olefin and organic solvent for a first time period P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; and (b) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst.A second aspect of the invention is directed to a process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, wherein the normal operation stage comprises (A) providing olefin, hydrogen peroxide, water and organic solvent in a zone of. Petition 870250090577, dated 03 / 10 / 2025, page 101 / 173 / 73 epoxidation comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide, water and organic solvent is formed; (B) subjecting the reaction mixture of (A) to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide, water and organic solvent; and (C) removing an effluent stream from the epoxidation zone, comprising olefin oxide, water and organic solvent; wherein the initialization stage comprises steps (a) and (b) of the method of the first aspect. In a third aspect, the invention relates to an olefin oxide obtained or obtainable from the process of the second aspect.

[002] Olefin oxides, such as propylene oxide, are important intermediates in the chemical industry.A suitable process for the preparation of olefin oxide starts with the respective olefin and makes use of hydrogen peroxide as an oxidizing agent, organic solvents, water, and heterogeneous epoxidation catalysts such as titanium-containing zeolites. Due to its importance for industrial-scale processes, it is desirable to carry out such epoxidation reactions as efficiently as possible.

[003] Any process, and even more importantly, every process on an industrial scale, comprises at least three stages, which are an initialization stage, in which the reaction is initiated, a normal operation stage, in which the reaction is carried out so that the desired product is obtained, and finally, a shutdown stage, in which the reaction is terminated and the reaction vessel can be emptied, for example, to allow catalyst regeneration, replacement, etc.

[004] The initialization stage, since it defines the conditions under which the catalyst in the reactor must operate, is of great importance. Especially when, as is often the case, epoxidations are carried out in several reactors in parallel, the initialization is relevant, since normally, any epoxidation process is part of a system Petition 870250090577, dated 03 / 10 / 2025, page 102 / 173 / 73 highly integrated, in which the reactors are started and shut down sequentially. If one of a plurality of reactors has to be started while one or more of the others are in operation, it is mandatory that this reactor does not negatively affect the overall equilibrium.

[005] One option for starting a reactor is described in the document WO 2017 / 162446 A1 (Evonik Degussa GmbH et al.), which describes a process for the epoxidation of propylene by the continuous reaction of propylene with hydrogen peroxide in a methanol solvent and in the presence of a molded titanium silicalite catalyst with a starting stage, wherein the methanol solvent is fed to the reaction tubes at a feed rate of 50 to 100% of a feed rate for full reactor loading; hydrogen peroxide is fed to the reaction tubes at a feed rate that starts with no more than 10% of a feed rate for full reactor loading and is increased continuously or gradually up to the rate for full reactor loading; and propylene is fed to the reaction tubes at a feed rate of 20 to 100% of a feed rate for full reactor loading.

[006] The technical problem underlying the present invention was, therefore, to provide an improved method for initiating an epoxidation reaction.

[007] A first aspect of the invention relates to a method of starting up a process for preparing an olefin oxide comprising a normal operating stage, wherein the normal operating stage comprises providing olefin, hydrogen peroxide and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide and organic solvent is formed and subjecting the reaction mixture to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide. Petition 870250090577, dated 03 / 10 / 2025, page 103 / 173 / 73 olefin and organic solvent; wherein the initiation method comprises (a) providing olefin and organic solvent for a first period of time Pi to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b) after the first time period, provide olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and bring the second mixture 2 into contact during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst.

[008] “Essentially free of hydrogen peroxide” in relation to the mixture in (a) means that said mixture comprises less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, of hydrogen peroxide, based on the total weight of the mixture.

[009] It has been surprisingly demonstrated that the use of a startup procedure with a propylene feed initiation before the hydrogen peroxide feed initiation significantly helped to minimize propylene oxide losses during the startup phase, i.e., it improves selectivity with respect to propylene oxide and was therefore superior to a startup procedure with hydrogen peroxide feed initiation before propylene feed initiation. Furthermore, the inventive process surprisingly results in slower catalyst deactivation over time. Petition 870250090577, dated 03 / 10 / 2025, page 104 / 173 / 73 of time and proves effective in reducing the formation of by-products.

[0010] In some preferred embodiments of the initialization method, the amount of olefin provided in (a) is less than the amount intended to be provided in the normal operating stage.

[0011] In some preferred embodiments of the initialization method, the amounts of olefin and hydrogen peroxide provided in (b) are less than the respective amounts intended to be provided in the normal operating stage, wherein, preferably, the molar amount of olefin provided in (b) is greater than the molar amount of hydrogen peroxide provided in (b).

[0012] In some preferred embodiments of the initialization method, step (b) comprises (b') after the first time period Pi, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operating stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operating stage, so that a mixture 2' is formed, and contacting the mixture 2' during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst;wherein, preferably, the molar quantity of olefin initially provided is greater than the molar quantity of hydrogen peroxide initially provided, and the molar quantity of olefin provided during the increase is greater than the molar quantity of hydrogen peroxide provided during the increase. Petition 870250090577, dated 03 / 10 / 2025, page 105 / 173 / 73

[0013] In mixture 2', due to the increase in the amount of hydrogen peroxide and the amount of olefin over the time period P2', the concentrations of hydrogen peroxide and olefin increase over P2'.

[0014] In some preferred embodiments of the initialization method, the olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operating stage in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:1.

[0015] In some preferred embodiments of the initialization method, the olefin and hydrogen peroxide are provided in (b) or in (b'), respectively, such that the molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[0016] In the normal operating stage of the process for preparing an olefin oxide, the olefin is preferably used in a molar excess compared to hydrogen peroxide. The expression “olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operating stage” means, for the initial method, that for each mole of hydrogen peroxide intended to be used in the normal operating stage, the excess molar amount of olefin relative to a 1:1 ratio of olefin:hydrogen peroxide is provided in (a) and therefore contained in the first mixture 1 formed in (a). In other words, the molar amount of olefin provided in (a) is (molar amount of hydrogen peroxide intended to be used in the normal operating stage) - (molar amount of olefin intended to be used in the normal operating stage).For example, if the molar ratio of olefin to hydrogen peroxide intended for use in the normal operating stage is 1.1:1, then the excess molar quantity of olefin intended... Petition 870250090577, dated 03 / 10 / 2025, page 106 / 173 / 73 to be used in the normal operation stage is 0.1.

[0017] Using a molar excess of propylene relative to the hydrogen peroxide used or intended to be used in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:1 in step (a) and preferably also a molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1, surprisingly provides improved performance, as the selectivity with respect to the olefin oxide formed in step (b) (removed as described in more detail below in (b.2) or (b'.2)) can be maintained, while the selectivities with respect to four of the main by-products, namely, acetaldehyde (AA), 1-methoxy-2-propanol (PM-2), 2-methoxy-1-propanol (PM-1), and hydroxyacetone (acetol) are drastically reduced compared to a process variant where the aforementioned specific excess ratio is not applied.

[0018] The point in time at which step (a) begins is t1, while the point in time at which step (b) or (b') begins is t2. The first time period P1 is therefore the time period between t2 and t1, i.e., P1 = t2 — t1. When the quantities of all components (olefin, organic solvent, and hydrogen peroxide) are as high as intended for the normal operating stage, this indicates the beginning of the normal operating stage, which occurs at a point in time t3. The second time period P2 or P2' in the case of (b') is then the time period between t3 and t2, i.e., P2 = t3-t2 (or P2' = t3-t2).

[0019] The molar quantities of hydrogen peroxide and olefin initially provided in (b') are preferably each in the range of 1 to 50% of the quantity intended to be used in the normal operating stage. During P2', the quantities of hydrogen peroxide and olefin are increased up to 100% of the quantities intended to be used in the stage Petition 870250090577, dated 03 / 10 / 2025, page 107 / 173 / 73 of normal operation, in which the increase is carried out gradually or continuously, so that the mixture formed in (b') comprises increasing amounts of olefin and hydrogen peroxide compared to the amounts initially provided in (b'), while the molar ratio of olefin:hydrogen peroxide during P2 or P2' is preferably maintained in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[0020] As also indicated below, the amount of hydrogen peroxide provided in the normal operating stage is adjusted so that the molar ratio of olefin:hydrogen peroxide in the reaction mixture formed is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1. Therefore, in (b), (b') preferably an excess of olefin is used compared to hydrogen peroxide, while in (a), only the excess molar amount of olefin compared to the molar amount of hydrogen peroxide - relative to what is intended to be used in the normal operating stage - is provided.

[0021] In some preferred embodiments of the initialization method, (a) comprises (a.1) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (a.2) remove, during P1, an effluent stream from the epoxidation zone, the effluent stream comprising olefin and organic solvent.

[0022] Step (a.2) is directly connected to (a.1).

[0023] In some preferred modalities of the method of Petition 870250090577, dated 03 / 10 / 2025, page 108 / 173 / 73 initialization, (b) comprises (b.1) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent; and / or wherein (b') comprises (b'.1) after the first time period P1, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operating stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operating stage, so that a mixture 2' is formed, and contacting the mixture 2' during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b'.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent.

[0024] Step (b.2) or (b'.2) is directly connected to (b.1) or Petition 870250090577, dated 03 / 10 / 2025, page 109 / 173 / 73 (b'.1). Additive

[0025] In some preferred embodiments of the initialization method, in any one of (a), (a.1), (b), (b'), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), an additive is provided to the epoxidation zone, wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof; wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, ammonia and mixtures of two or more thereof, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more thereof; wherein the additive comprises, most preferably, at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein, most preferably, 95 to 100% by weight of the additive is dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate.

[0026] Preferably, in the case of ammonia, the additive is provided in pure form or in aqueous solution, wherein the additive is selected from the group consisting of a potassium salt of an inorganic acid, a potassium salt of an organic acid, or an ammonium salt of an acid. Petition 870250090577, dated 03 / 10 / 2025, page 110 / 173 / 73 inorganic, ammonium salt of an organic acid or any mixture comprising two or more of the same or any mixture comprising ammonia and at least one of the same, provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NHZ and NH3.

[0027] Etidronic acid is a tetrabasic acid with pK values ​​of 1.35 ± 0.08; 2.87; 7.03 ± 0.01; 11.3. Each of the ammonia, potassium salts and ammonium salts mentioned above, when in aqueous solution, dissociates to release or forms at least to some extent anion(s) and one or more cations. For example, ammonia forms NH3 to some extent, ammonium salts dissociate to some extent into NH4+, and one or more potassium anions or salts dissociate to some extent to release K+ and one or more anions, the positive charge being compensated by the appropriate equivalent of anions. With respect to ammonia and ammonium salts, due to the dissociation equilibrium between NH3 and NH4+, the sum of NH3 and NH4+ must be considered for M.In some preferred embodiments, the aqueous additive solution comprises a range of 0.01 to 5% by weight, preferably a range of 0.5 to 3% by weight, and more preferably a range of 1 to 2% by weight, of additive, based on the total weight of the aqueous solution.

[0028] In some preferred embodiments of the initialization method, the additive is preferably premixed with the organic solvent or with hydrogen peroxide, preferably with the organic solvent, before being provided to the epoxidation zone. In some preferred embodiments of the initialization method, the additive is provided in any one of (a), (b), (b'), (a.1), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), in a molar ratio M:hydrogen peroxide Petition 870250090577, dated 03 / 10 / 2025, page 111 / 173 / 73 hydrogen in the range of 1 x 10-5:1 to 1 x 10-3:1. When the additive is provided in (a), then the molar ratio M:hydrogen peroxide applies to the hydrogen peroxide that is intended to be provided in the normal operating stage. Time periods

[0029] In some preferred embodiments of the initialization method, the first time period P1 is preferably a time period in the range of 1 minute to 5 hours, more preferably in the range of 5 minutes to 1 hour, most preferably in the range of 10 minutes to 30 minutes; and / or wherein the second time period P2 or P2' respectively is preferably a time period in the range of 30 minutes to 24 hours, more preferably in the range of 2 to 18 hours, most preferably in the range of 4 to 12 hours.

[0030] In some preferred embodiments, the initialization method further comprises, before (a), (x) providing a stream of organic solvent for a period of time Px to the epoxidation zone, wherein Px is preferably a period of time in the range of 10 minutes to 24 hours.

[0031] The organic solvent stream provided in (x) is essentially free of olefin and hydrogen peroxide, wherein “essentially free of” means that the respective compound is contained in said stream at less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, based on the total weight of the stream. Preferably, the organic solvent stream provided in (x) is also essentially free of additive, wherein “essentially free of” means that the additive is contained in said stream at less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, based on the total weight of the stream. In some preferred embodiments, the organic solvent is provided in each of (a), Petition 870250090577, dated 03 / 10 / 2025, page 112 / 173 / 73 (b), (a.1), (a.2) and (b') in the range of 50 to 100%, preferably in the range of 70 to 100%, more preferably in the range of 90 to 100%, of the quantity intended to be used in the normal operating stage. Reaction conditions

[0032] In some preferred embodiments, the initialization method is performed continuously.

[0033] In some preferred embodiments of the initiation method, contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at an absolute pressure in the epoxidation zone in the range of 0.5 to 5.0 MPa, preferably in the range of 1.5 to 3.0 MPa, more preferably in the range of 1.8 to 2.8 MPa.

[0034] In some preferred embodiments of the initiation method, contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at a temperature in the epoxidation zone in the range of 20 to 75°C, preferably in the range of 22 to 75°C, more preferably in the range of 24 to 70°C, most preferably in the range of 25 to 65°C.

[0035] In some preferred embodiments of the initiation method, the epoxidation reaction conditions comprise drip bed conditions.

[0036] In some preferred alternative embodiments of the initiation method, the epoxidation reaction conditions comprise fixed bed conditions. Catalyst

[0037] In some preferred embodiments of the initialization method, the heterogeneous epoxidation catalyst comprises a zeolitic material having a framework structure comprising Si, O and Ti. Petition 870250090577, dated 03 / 10 / 2025, page 113 / 173 / 73

[0038] In some preferred embodiments of the initialization method, the zeolitic material comprises Ti in an amount in the range of 0.2 to 5% by weight, preferably in the range of 0.5 to 4% by weight, more preferably in the range of 0.7 to 3% by weight, calculated as elemental Ti and based on the total weight of the zeolitic material.

[0039] In some preferred embodiments of the method of initialization, the zeolite material with an arcabouch structure comprising Si, O and Ti comprising the epoxidation catalyst is a titanium zeolite having an arcabouch structure of ABW, ACOI, AE, AET, AENG, AENG, AENG, AAF, AFI, AFN, AFO, AFR, AFS, AFT, AFX, AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AWO, AWW, BCT, BEA, BEC, BIK, BOG, BPH, BRE, CAN, CAS, CDO, CHA, CLO, CLO, CGF, CGF CON, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI, EMT, EPI, ERI, ESV, ETR, EUO, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFR, ISV, ITE, ITH, ITQ, ITW, IWR, IW, LW, LW, JB, LAW LIO, LOS, LOV, LTA, LTL, LTN, MAR, MAZ, MCM-22(S), MCM-36, MCM-56, MEI, MEL, MEP, MER, MIT-1, MMFI, MFS, MON, MOR, MSE, MSO, MTF, MTN, MTT, MTT, MW, NW, NW, NPO, NPO, NPO OBW, OFF, OSI, OSO, PAR, PAU, PHI, PON, RHO, RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAO, SAS, SAT, SAV, SBE, SBS, SBT, SFE, SFF, SFG, SFH, SFN SFO, SGT, SOD, SSY, STF, STFSTI, STT, TER, THO, TON, TSC, UEI, UFI, UOZ, USI, UTL, VET, VFI, VNI, VSV, WEI, WEN, YUG, ZON, SVR, SVY or a mixed structure of two or more of these framework types; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type, a MEL framework type, an MWW framework type, an MCM-22 (S) framework type, an MCM-56 framework type, an IEZ-MWW framework type, an MCM-36 framework type, an ITQ framework type, a BEA framework type, a, Petition 870250090577, dated 03 / 10 / 2025, page 114 / 173 / 73 type of framework MOR or a mixed structure of two or more of these types of frameworks; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI type framework or an MWW type framework; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti has the MFI type framework; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium silicalite-1 (TS-1).

[0040] In some preferred embodiments of the initialization method, the heterogeneous epoxidation catalyst further comprises a binder, which preferably comprises silicon dioxide.

[0041] In some preferred embodiments of the initialization method, the heterogeneous epoxidation catalyst is in the form of a mold, preferably in the form of a wire or a granule. A wire has a cross-section in which the cross-section preferably has a hexagonal, rectangular, square, triangular, trilobular, oval, or circular shape. In some preferred embodiments, the mold has the form of a wire having a circular cross-section, which is more preferably formed by extrusion (cylindrical extrude). A granule preferably comprises particles having a shape selected from cylindrical, spherical, trilobular (particle having a trilobular cross-section), and mixed shapes of two or more of these shapes, wherein the granule comprises particles of one shape as well as mixtures of particles having two or more of these shapes. A “sphere” comprises an ideal sphere shape, but also spheroidal shapes.A "cylinder" comprises shapes having a high h that is greater than the radius of the circle's area, as well as shapes having a high h that is less than the radius of the circle's area (tablet shape).

[0042] In some preferred modalities of the method of Petition 870250090577, dated 03 / 10 / 2025, p. 115 / 173 / 73 initialization, from 95 to 100% by weight, preferably from 98 to 100% by weight, more preferably from 99 to 100% by weight, more preferably from 99.5 to 100% by weight, more preferably from 99.9 to 100% by weight of the molding consist of the zeolitic material and the binder.

[0043] In some preferred embodiments of the initialization method, 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, more preferably 99.9 to 100% by weight of the binder comprised in the molding consists of Si and O.

[0044] In some preferred embodiments of the initialization method, the heterogeneous epoxidation catalyst, preferably the molding, comprises the binder, calculated as SiO2, in an amount in the range of 1 to 95% by weight, preferably in the range of 3 to 70% by weight, more preferably in the range of 5 to 50% by weight, most preferably in the range of 10 to 30% by weight, based on the total weight of the epoxidation catalyst, preferably based on the total weight of the molding and / or wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the zeolitic material in an amount in the range of 5 to 99% by weight, preferably in the range of 30 to 97% by weight, more preferably in the range of 50 to 95% by weight, most preferably in the range of 70 to 90% by weight, based on the total weight of the epoxidation catalyst. heterogeneous, preferably based on the total weight of the molding. Hydrogen peroxide

[0045] In some preferred embodiments of the startup method, hydrogen peroxide is provided as an aqueous hydrogen peroxide solution, which preferably has a total organic carbon (TOC) content in the range of 100 to 800 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, preferably Petition 870250090577, dated 03 / 10 / 2025, page 116 / 173 / 73 in the range of 120 to 750 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, more preferably in the range of 150 to 700 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, determined in accordance with DIN EN 1484 (April 2019).

[0046] In some preferred embodiments of the initialization method, hydrogen peroxide has a pH in the range of 0 to 3.0, preferably in the range of 0.1 to 2.5, more preferably in the range of 0.5 to 2.3, determined with a pH-sensitive glass electrode according to the CEFIC PEROXYGENS H2O2 AM-7160 standard (2003).

[0047] In some preferred embodiments of the initialization method, hydrogen peroxide comprises 20 to 85% by weight, preferably 30 to 75% by weight, more preferably 40 to 70% by weight of hydrogen peroxide, relative to the total weight of the aqueous hydrogen peroxide solution.

[0048] In some preferred embodiments of the initialization method, hydrogen peroxide is obtained or obtainable from an anthraquinone process. Solvent

[0049] In some preferred embodiments of the initialization method, the organic solvent is an organic epoxidation solvent, preferably the organic solvent is selected from the group consisting of alcohol, acetonitrile, propionitrile and mixtures of two or more thereof; more preferably selected from the group consisting of alcohol, acetonitrile and mixtures of alcohol and acetonitrile; more preferably the organic solvent comprises at least one alcohol, wherein the alcohol is preferably a C1 to C5 monoalcohol or a mixture of two or more C1 to C5 alcohols, more preferably the alcohol comprises at least methanol, wherein the organic solvent comprises more preferably methanol. Petition 870250090577, dated 03 / 10 / 2025, page 117 / 173 / 73 less than 90% by weight, more preferably at least 95% by weight, more preferably at least 98% by weight, more preferably at least 99% by weight, of methanol. Olefin (oxide)

[0050] In some preferred embodiments of the initialization method, the olefin is a C2-C10 alkene, preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene. The olefin oxide, especially the olefin oxide removed from the epoxidation zone with the effluent stream comprising olefin oxide, water and organic solvent in (C), as described in more detail below, is a C2-C10 alkene oxide, preferably a C2-C5 alkene oxide, more preferably a C2-C4 alkene oxide, more preferably ethylene oxide or propylene oxide, more preferably propylene oxide. 2nd aspect - process for preparing an olefin oxide

[0051] A second aspect of the invention relates to a process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, wherein the normal operation stage comprises (A) providing olefin, hydrogen peroxide, water and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide, water and organic solvent is formed; (B) subjecting the reaction mixture from (A) to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide, water and organic solvent; (C) remove an effluent stream from the epoxidation zone, comprising olefin oxide, water and organic solvent; in which the initialization stage comprises Petition 870250090577, dated 03 / 10 / 2025, page 118 / 173 / 73 (a) provide olefin and organic solvent for a first period of time Pi to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contact the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b) after the first time period, provide organic solvent, olefin and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and bring the second mixture 2 into contact during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst.

[0052] “Essentially free of hydrogen peroxide” in relation to the mixture in (a) means that said mixture comprises less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, of hydrogen peroxide, based on the total weight of the mixture. All details, preferred embodiments and alternative preferred embodiments indicated above in the section relating to the first aspect also apply to the second aspect, especially for the initial stage included in the process for preparing an olefin oxide.

[0053] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, the amount of olefin provided in (a) is less than the amount intended to be provided in the normal operation stage.

[0054] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, the amounts of olefin and hydrogen peroxide provided in (b) are less than the respective amounts intended for Petition 870250090577, dated 03 / 10 / 2025, page 119 / 173 / 73 to be provided in the normal operating stage, wherein, preferably, the molar quantity of olefin provided in (b) is greater than the molar quantity of hydrogen peroxide provided in (b).

[0055] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, step (b) comprises (b') after the first time period Pi, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operation stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operation stage, so that a mixture 2' is formed,and bring mixture 2' into contact during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; wherein, preferably, the molar amount of olefin initially provided is greater than the molar amount of hydrogen peroxide initially provided and the molar amount of olefin provided during the increase is greater than the molar amount of hydrogen peroxide provided during the increase.

[0056] In mixture 2', due to the increase in the amount of hydrogen peroxide and the amount of olefin over the time period P2', the concentrations of hydrogen peroxide and olefin increase over P2'.

[0057] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the olefin is provided in (a) in a molar ratio Petition 870250090577, dated 03 / 10 / 2025, page 120 / 173 / 73 relating to the molar quantity of hydrogen peroxide intended to be used in the normal operating stage in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:1.

[0058] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the olefin and hydrogen peroxide are provided in (b) or in (b'), respectively, such that the molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[0059] In the normal operating stage of the process for preparing an olefin oxide, the olefin is preferably used in a molar excess compared to hydrogen peroxide. The expression “the olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operating stage” means, for the initial method, that for each mole of hydrogen peroxide intended to be used in the normal operating stage, the excess molar amount of olefin relative to a 1:1 ratio of olefin:hydrogen peroxide is provided in (a) and therefore contained in the first mixture 1 formed in (a). In other words, the molar amount of olefin provided in (a) is (molar amount of hydrogen peroxide intended to be used in the normal operating stage) - (molar amount of olefin intended to be used in the normal operating stage).For example, if the molar ratio of olefin to hydrogen peroxide intended for use in the normal operating stage is 1.1:1, then the excess molar quantity of olefin intended for use in the normal operating stage is 0.1.

[0060] The point in time where step (a) begins is t1, while the point in time where step (b) or (b') begins is t2. The first time period P1 is therefore the time period between t2 and t1, that is, P1 = t2 - t1. Petition 870250090577, dated 03 / 10 / 2025, page 121 / 173 / 73 When the quantities of all components (olefin, organic solvent, and hydrogen peroxide) are as high as intended for the normal operating stage, this indicates the start of the normal operating stage, which occurs at a point in time t3. The second time period P2 or P2' in the case of (b') is then the time period between t3 and t2, i.e., P2 = t3-t2 (or P2' = t3-t2).

[0061] The molar quantities of hydrogen peroxide and olefin initially provided in (b') are preferably each in the range of 1 to 50% of the quantity intended to be used in the normal operating stage. During P2', the quantities of hydrogen peroxide and olefin are increased up to 100% of the quantities intended to be used in the normal operating stage, wherein the increase is carried out gradually or continuously, so that the mixture formed in (b') comprises increasing quantities of olefin and hydrogen peroxide compared with the quantities initially provided in (b'), while the molar ratio of olefin:hydrogen peroxide during P2 or P2' is preferably maintained in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[0062] As also indicated below, the amount of hydrogen peroxide provided in the normal operating stage is adjusted so that the molar ratio of olefin:hydrogen peroxide in the reaction mixture formed is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1. Therefore, in (b), (b') preferably an excess of olefin is used compared to hydrogen peroxide, while in (a), only the excess molar amount of olefin compared to the molar amount of hydrogen peroxide - relative to what is intended to be used in the normal operating stage - is provided.

[0063] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a Petition 870250090577, dated 03 / 10 / 2025, page 122 / 173 / 73 initialization stage, step (a) comprises (a.1) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (a.2) remove, during P1, an effluent stream from the epoxidation zone, the effluent stream comprising olefin and organic solvent.

[0064] Step (a.2) is directly connected to (a.1).

[0065] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, step (b) comprises (b.1) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent; and / or wherein (b') comprises (b'.1) after the first time period P1, provide organic solvent and olefin and hydrogen peroxide in initial quantities to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide. Petition 870250090577, dated 03 / 10 / 2025, page 123 / 173 / 73 hydrogen, in which the quantities of hydrogen peroxide and olefin are less than the quantities intended to be provided in the normal operating stage, and increase the quantity of hydrogen peroxide and the quantity of olefin over the time period P2' until the quantities intended to be provided in the normal operating stage are reached, so that a mixture 2' is formed, and bring the mixture 2' into contact during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b'.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent.

[0066] Step (b.2) or (b'.2) is directly connected to (b.1) or (b'.1). Additive

[0067] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, in any one of (a), (a.1), (b), (b'), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), an additive is provided to the epoxidation zone, wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof; wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, ammonia and mixtures of two or more of these. Petition 870250090577, dated 03 / 10 / 2025, page 124 / 173 / 73 same, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more of the same; wherein the additive comprises, most preferably, at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein, most preferably, 95 to 100% by weight of the additive is dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate.

[0068] Preferably, in the case of ammonia, the additive is provided in pure form or in aqueous solution, wherein the additive is, if selected from the group consisting of a potassium salt of an inorganic acid, a potassium salt of an organic acid, an ammonium salt of an inorganic acid, an ammonium salt of an organic acid, or any mixture comprising two or more of the same, or any mixture comprising ammonia and at least one of the same, provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NHZ and NH3.

[0069] Etidronic acid is a tetrabasic acid with pK values ​​of 1.35 ± 0.08; 2.87; 7.03 ± 0.01; 11.3. Each of the ammonia, potassium salts and ammonium salts mentioned above, when in aqueous solution, dissociates to release or forms at least to some extent anion(s) and one or more cations. For example, ammonia forms NH3 to a certain extent, ammonium salts dissociate to a certain extent into NH3, and one or more potassium anions or salts dissociate to a certain extent to release K+ and one or more anions, the positive charge being compensated by the appropriate equivalent of anions. Regarding Petition 870250090577, dated 03 / 10 / 2025, page 125 / 173 / 73 to ammonia and ammonium salts, due to the dissociation equilibrium between NH3 and NH4+, the sum of NH3 and NH4+ must be considered for M. In some preferred embodiments, the aqueous additive solution comprises in the range of 0.01 to 5% by weight, preferably in the range of 0.5 to 3% by weight, more preferably in the range of 1 to 2% by weight, of additive, based on the total weight of the aqueous solution.

[0070] Preferably, the additive is preferably premixed with the organic solvent or with hydrogen peroxide, preferably with the organic solvent, before being provided to the epoxidation zone.

[0071] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, the additive is provided in any one of (a), (b), (b'), (a.1), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), in a molar ratio M:hydrogen peroxide in the range of 1 x 10-5:1 to 1 x 10-3:1.

[0072] When the additive is provided in (a), then the molar ratio M:hydrogen peroxide applies to the hydrogen peroxide that is intended to be provided in the normal operating stage. Time periods

[0073] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the first time period P1 is preferably a time period in the range of 1 minute to 5 hours, more preferably in the range of 5 minutes to 1 hour, most preferably in the range of 10 minutes to 30 minutes; and / or wherein the second time period P2 or P2' respectively is preferably a time period in the range of 30 minutes to 24 hours, more preferably in the range of 2 to 18 hours, most preferably in the range Petition 870250090577, dated 03 / 10 / 2025, page 126 / 173 / 73 from 4 to 12 hours.

[0074] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the process further comprises, before (a), (x) providing a stream of organic solvent for a period of time Px to the epoxidation zone, wherein Px is preferably a period of time in the range of 10 minutes to 24 hours.

[0075] The organic solvent stream provided in (x) is essentially free of olefin and hydrogen peroxide, wherein “essentially free of” means that the respective compound is contained in said stream at less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, based on the total weight of the stream. Preferably, the organic solvent stream provided in (x) is also essentially free of additive, wherein “essentially free of” means that the additive is contained in said stream at less than 0.2% by weight, preferably less than 0.1% by weight, more preferably less than 0.05% by weight, based on the total weight of the stream. In some preferred embodiments, the organic solvent is provided in each of (a), (b), (a.1), (a.2) and (b') in the range of 50 to 100%, preferably in the range of 70 to 100%, more preferably in the range of 90 to 100%, of the amount intended to be used in the normal operating stage. Reaction conditions

[0076] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, the process is carried out continuously, i.e., preferably, the normal operation stage and the start-up stage are carried out continuously.

[0077] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and a Petition 870250090577, dated 03 / 10 / 2025, page 127 / 173 / 73 initialization stage, the contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at an absolute pressure in the epoxidation zone in the range of 0.5 to 5.0 MPa, preferably in the range of 1.5 to 3.0 MPa, more preferably in the range of 1.8 to 2.8 MPa.

[0078] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at a temperature in the epoxidation zone in the range of 20 to 75°C, preferably in the range of 22 to 75°C, more preferably in the range of 24 to 70°C, most preferably in the range of 25 to 65°C.

[0079] In some preferred embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the epoxidation reaction conditions comprise drip bed conditions.

[0080] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the epoxidation reaction conditions comprise fixed bed conditions. Catalyst

[0081] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the heterogeneous epoxidation catalyst comprises a zeolitic material having a framework structure comprising Si, O and Ti.

[0082] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the zeolitic material comprises Ti in Petition 870250090577, dated 03 / 10 / 2025, page 128 / 173 / 73 an amount in the range of 0.2 to 5% by weight, preferably in the range of 0.5 to 4% by weight, more preferably in the range of 0.7 to 3% by weight, calculated as elemental Ti and based on the total weight of the zeolitic material.

[0083] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the zeolitic material having a framework structure comprising Si, O and Ti comprised in the epoxidation catalyst is a titanium zeolite having a framework structure of ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR, AFS, AFT, AFX, AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AWO, AWW, BCT, BEA, BEC, BIK, BOG, BPH, BRE, CAN, CAS, CDO, CFI, CGF, CGS, CHA, CHI, CLO, CON, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI, EMT, EPI, ERI, ESV, ETR, EUO, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFR, ISV, ITE, ITH, ITQ, ITW, IWR, IWW, JBW, KFI, LAU, LEV, LIO, LOS, LOV, LTA, LTL, LTN, MAR, MAZ, MCM-22(S) RRO, RSN, RTE,RTH, RUT, RWR, RWY, SAO, SAS, SAT, SAV, SBE, SBS, SBT, SFE, SFF, SFG, SFH, SFN SFO, SGT, SOD, SSY, STF, STI, STT, TER, THO, TON, TSC, UEI, UFI, UOZ, USI, UTL, VET, VFI, VNI, VSV, WEI, WEN, YUG, ZON SVR, SVY or a mixed structure of two or more of these types of framework; More preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type, a MEL framework type, an MWW framework type, an MCM22(S) framework type, an MCM-56 framework type, an IEZ-MWW framework type, an MCM-36 framework type, an ITQ framework type, a BEA framework type, an MOR framework type or a mixed structure of two or more, Petition 870250090577, dated 03 / 10 / 2025, page 129 / 173 / 73 of these framework types; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type or an MWW framework type; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti has the MFI framework type; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium silicalite-1 (TS-1).

[0084] Preferably, the heterogeneous epoxidation catalyst further comprises a binder, preferably comprising silicon dioxide.

[0085] Preferably, the heterogeneous epoxidation catalyst is in the form of a mold, preferably in the form of a wire or a granule.

[0086] A wire has a cross-section in which the cross-section preferably has a hexagonal, rectangular, square, triangular, trilobular, oval, or circular shape. In some preferred embodiments, the molding has the shape of a wire having a circular cross-section, which is most preferably formed by extrusion (cylindrical extrudate). A granule preferably comprises particles having a shape selected from cylindrical, spherical, trilobular (particle having a trilobular cross-section), and mixed shapes of two or more of these shapes, wherein the granule comprises particles of one shape as well as mixtures of particles having two or more of these shapes. A “sphere” comprises an ideal sphere shape, but also spheroidal shapes. A “cylinder” comprises shapes having a high h that is greater than the radius of the area of ​​the circle, as well as shapes having a high h that is less than the radius of the area of ​​the circle (tablet shape).

[0087] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising an operation stage Petition 870250090577, dated 03 / 10 / 2025, page 130 / 173 / 73 normal and an initial stage, from 95 to 100% by weight, preferably from 98 to 100% by weight, more preferably from 99 to 100% by weight, more preferably from 99.5 to 100% by weight, more preferably from 99.9 to 100% by weight of the molding consist of the zeolitic material and the binder.

[0088] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, most preferably 99.9 to 100% by weight of the binder comprising in the molding consists of Si and O.

[0089] Preferably, the heterogeneous epoxidation catalyst, preferably the molding, comprises the binder, calculated as SiO2, in an amount in the range of 1 to 95% by weight, preferably in the range of 3 to 70% by weight, more preferably in the range of 5 to 50% by weight, most preferably in the range of 10 to 30% by weight, based on the total weight of the epoxidation catalyst, preferably based on the total weight of the molding and / or wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the zeolitic material in an amount in the range of 5 to 99% by weight, preferably in the range of 30 to 97% by weight, more preferably in the range of 50 to 95% by weight, most preferably in the range of 70 to 90% by weight, based on the total weight of the heterogeneous epoxidation catalyst, preferably based on the total weight of the molding. Hydrogen peroxide

[0090] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, hydrogen peroxide is provided as an aqueous hydrogen peroxide solution, which preferably has a Petition 870250090577, dated 03 / 10 / 2025, page 131 / 173 / 73 total organic carbon (TOC) content in the range of 100 to 800 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, preferably in the range of 120 to 750 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, more preferably in the range of 150 to 700 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, determined in accordance with DIN EN 1484 (April 2019). In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the hydrogen peroxide has a pH in the range of 0 to 3.0, preferably in the range of 0.1 to 2.5, more preferably in the range of 0.5 to 2.3, determined with a pH-sensitive glass electrode according to the CEFIC standard PEROXYGENS H2O2 AM-7160 (2003).In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the hydrogen peroxide comprises 20 to 85% by weight, preferably 30 to 75% by weight, more preferably 40 to 70% by weight of hydrogen peroxide, relative to the total weight of the aqueous hydrogen peroxide solution. In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the hydrogen peroxide is obtained or obtainable from an anthraquinone process. Solvent

[0091] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the organic solvent is an organic epoxidation solvent, preferably the organic solvent is selected from the group consisting of alcohol, acetonitrile, propionitrile and mixtures of two or more thereof; more preferably selected from the group Petition 870250090577, dated 03 / 10 / 2025, page 132 / 173 / 73 consisting of alcohol, acetonitrile and mixtures of alcohol and acetonitrile; more preferably the organic solvent comprises at least one alcohol, wherein the alcohol is preferably a C1 to C5 monoalcohol or a mixture of two or more C1 to C5 alcohols, more preferably the alcohol comprises at least methanol, wherein the organic solvent comprises more preferably at least 90% by weight, more preferably at least 95% by weight, more preferably at least 98% by weight, more preferably at least 99% by weight, of methanol. Olefin (oxide)

[0092] In some preferred alternative embodiments of the process for preparing an olefin oxide comprising a normal operation stage and an initialization stage, the olefin is a C2-C10 alkene, preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene. The olefin oxide, especially the olefin oxide removed from the epoxidation zone with the effluent stream comprising olefin oxide, water and organic solvent in (C), is a C2-C10 alkene oxide, preferably a C2-C5 alkene oxide, more preferably a C2-C4 alkene oxide, more preferably ethylene oxide or propylene oxide, more preferably propylene oxide.

[0093] The above description for the second aspect process applies equally to steps such as (A), (B), (C) of the normal operation stage and to steps such as (a), (b) of the initialization stage. 3rd aspect - olefin oxide

[0094] In a third aspect, the invention is directed to an olefin oxide, preferably propylene oxide, obtained or obtainable from the process of the second aspect.

[0095] The present invention is further illustrated by the following embodiments and combinations of embodiments, as indicated by Petition 870250090577, dated 03 / 10 / 2025, pp. 133 / 173 / 73 respective dependencies and subsequent references. In particular, it should be noted that in each case where a series of modalities is mentioned, for example, in the context of a term such as “A ... of any of the modalities 1 to 4”, each modality in that series must be explicitly described for the expert, i.e., the formulation of this term must be understood by the expert as synonymous with “A ... of any of the modalities 1, 2, 3 and 4”.

[0096] 1. A start-up method for a process for preparing an olefin oxide comprising a normal operating stage, wherein the normal operating stage comprises providing olefin, hydrogen peroxide and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide and organic solvent is formed, and subjecting the reaction mixture to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide and organic solvent; wherein the initiation method comprises (a) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b) after the first time period, provide olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and bring the second mixture 2 into contact during P2 under epoxidation reaction conditions in the epoxidation zone with the epoxidation catalyst. Petition 870250090577, dated 03 / 10 / 2025, page 134 / 173 / 73 heterogeneous.

[0097] 2. The initialization method of mode 1, wherein the amount of olefin provided in (a) is less than the amount intended to be provided in the normal operating stage.

[0098] 3. The initialization method of embodiment 1 or 2, wherein the amounts of olefin and hydrogen peroxide provided in (b) are less than the respective amounts intended to be provided in the normal operating stage, wherein, preferably, the molar amount of olefin provided in (b) is greater than the molar amount of hydrogen peroxide provided in (b).

[0099] 4. The initialization method of any of the embodiments in 3, wherein (b) comprises (b') after the first time period Pi, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operating stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operating stage, so that a mixture 2' is formed, and contacting the mixture 2' during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst;wherein, preferably, the molar quantity of olefin initially provided is greater than the molar quantity of hydrogen peroxide initially provided, and the molar quantity of olefin provided during the increase is greater than the molar quantity of hydrogen peroxide provided during the increase. Petition 870250090577, dated 03 / 10 / 2025, pages 135 / 173 / 73

[00100] 5. The initialization method of any of the embodiments in 4, wherein the olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operating stage in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:1.

[00101] 6. The initialization method of any of the embodiments in 5, wherein the olefin and hydrogen peroxide are provided in (b) or in (b'), respectively, such that the molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[00102] 7. The initialization method of any of the embodiments in 6, wherein (a) comprises (a.1) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (a.2) remove, during P1, an effluent stream from the epoxidation zone, the effluent stream comprising olefin and organic solvent.

[00103] 8. The initialization method of any of the embodiments in 7, wherein (b) comprises (b.1) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under Petition 870250090577, dated 03 / 10 / 2025, page 136 / 173 / 73 epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent; and / or wherein (b') comprises (b'.1) after the first time period Pi, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operating stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operating stage, so that a mixture 2' is formed, and contacting the mixture 2' during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b'.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent.

[00104] 9. The initialization method of any of the embodiments in 8, wherein in any one of (a), (a.1), (b), (b'), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), an additive is provided to the epoxidation zone, wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, salt of Petition 870250090577, dated 03 / 10 / 2025, page 137 / 173 / 73 ammonium of an organic acid and mixtures of two or more of the same; wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, ammonia and mixtures of two or more thereof, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more thereof; wherein the additive comprises, most preferably, at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein, most preferably, 95 to 100% by weight of the additive is dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate.

[00105] 10. The initialization method of embodiment 10, wherein the additive is, in the case of ammonia, provided in pure form or in aqueous solution, wherein the additive is, in the case of being selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonium salt of an inorganic acid, ammonium salt of an organic acid or any mixture comprising two or more of the same or any mixture comprising ammonia and at least one of the same, provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NH3 and NH3.

[00106] 11. The initialization method of embodiment 9 or 10, wherein the additive is preferably premixed with the organic solvent or with the Petition 870250090577, dated 03 / 10 / 2025, page 138 / 173 / 73 hydrogen peroxide, preferably with the organic solvent, before being provided to the epoxidation zone.

[00107] 12. The initialization method of any of the embodiments 9 to 11, wherein the additive is provided in any one of (a), (b), (b'), (a.1), (b.1), (b'.1), preferably in at least any one of (b), (b'), (b.1), (b'.1), more preferably in each one of (b), (b'), (b.1), (b'.1), in a molar ratio M:hydrogen peroxide in the range of 1 x 10-5:1 to 1 x 10-3:1.

[00108] 13. The initialization method of any of the modalities 1 to 12, wherein the first time period P1 is preferably a time period in the range of 1 minute to 5 hours, more preferably in the range of 5 minutes to 1 hour, most preferably in the range of 10 minutes to 30 minutes; and / or wherein the second time period P2 or P2' respectively is preferably a time period in the range of 30 minutes to 24 hours, more preferably in the range of 2 to 18 hours, most preferably in the range of 4 to 12 hours.

[00109] 14. The initialization method of any of embodiments 1 to 13 further comprising, before (a), (x) providing a stream of organic solvent for a period of time Px to the epoxidation zone, wherein Px is preferably a period of time in the range of 10 minutes to 24 hours.

[00110] 15. The initialization method of any of the modes 1 to 14, which is performed continuously.

[00111] 16. The initiation method of any of the embodiments 1 to 15, in which contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at an absolute pressure in the epoxidation zone in the range of 0.5 to 5.0 MPa, preferably in the range of 1.5 to 3.0 MPa, more preferably in the Petition 870250090577, dated 03 / 10 / 2025, page 139 / 173 / 73 range of 1.8 to 2.8 MPa.

[00112] 17. The initialization method of any of the embodiments 1 to 16, in which contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at a temperature in the epoxidation zone in the range of 20 to 75°C, preferably in the range of 22 to 75°C, more preferably in the range of 24 to 70°C, most preferably in the range of 25 to 65°C.

[00113] 18. The initiation method of any of the modalities 1 to 17, wherein the epoxidation reaction conditions comprise drip bed conditions.

[00114] 19. The initiation method of any of the embodiments 1 to 17, in which the epoxidation reaction conditions comprise fixed bed conditions.

[00115] 20. The initialization method of any of the embodiments 1 to 19, wherein the heterogeneous epoxidation catalyst comprises a zeolitic material having a framework structure comprising Si, O and Ti.

[00116] 21. The initialization method of embodiment 20, wherein the zeolitic material comprises Ti in an amount in the range of 0.2 to 5% by weight, preferably in the range of 0.5 to 4% by weight, more preferably in the range of 0.7 to 3% by weight, calculated as elemental Ti and based on the total weight of the zeolitic material.

[00117] 22. The initialization method of embodiment 20 or 21, wherein the zeolitic material having a framework structure comprising Si, O and Ti comprised in the epoxidation catalyst is a titanium zeolite having a framework structure of ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR, AFS, AFT, AFX, AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AWO, AWW, BCT, BEA, BEC, BIK, BOG, BPH, BRE, CAN, CAS, CDO, CFI, CGF, CGS, CHA, CHI, CLO, Petition 870250090577, dated 03 / 10 / 2025, pp. 140 / 173 / 73 CON, CZP, DAC, DDR, DFO, DFT, DOH, DON, EAB, EDI, EMT, EPI, ERI, ESV, ETR, EUO, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFR, ISV, ITE, ITH, ITQ, ITQ, IWR, IWW, JW, JW, KW, LAW LEV, LIO, LOS, LOV, LTA, LTL, LTN, MAR, MAZ, MCM-22(S), MCM-36, MCM-56, MEI, MEL, MEP, MER, MIT-1, MMFI, MFS, MON, MOR, MSE, MSO, MTF, MTN, MTT, MTW, NW, NW, NW, NW, NW NPO, OBW, OFF, OSI, OSO, PAR, PAU, PHI, PON, RHO, RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAO, SAS, SAT, SAV, SBE, SBS, SBT, SFE, SFF, SFG, SFH, SFN, SFO, SGT, SGT, SGT, STTY, STTY TER, THO, TON, TSC, UEI, UFI, UOZ, USI, UTL, VET, VFI, VNI, VSV, WEI, WEN, YUG, ZON SVR, SVY or a mixed structure of two or more of these types of arcabouço;More preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type, a MEL framework type, an MWW framework type, an MCM-22(S) framework type, an MCM-56 framework type, an IEZ-MWW framework type, an MCM-36 framework type, an ITQ framework type, a BEA framework type, an MOR framework type or a mixed structure of two or more of these framework types; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type or an MWW framework type; More preferably, the zeolitic material having a framework structure comprising Si, O, and Ti has the MFI framework type; more preferably, the zeolitic material having a framework structure comprising Si, O, and Ti is a titanium silicalite-1 (TS-1).

[00118] 23. The initialization method of any of the embodiments 20 to 22, in which the heterogeneous epoxidation catalyst additionally comprises a binder, preferably comprising silicon dioxide. Petition 870250090577, dated 03 / 10 / 2025, pp. 141 / 173 / 73

[00119] 24. The initialization method of embodiment 23, in which the heterogeneous epoxidation catalyst is in the form of a mold, preferably in the form of a wire or a granule.

[00120] 25. The initialization method of embodiment 23 or 24, wherein 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, more preferably 99.9 to 100% by weight of the molding consists of the zeolitic material and the binder.

[00121] 26. The initialization method of any of the embodiments 23 to 25, wherein 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, more preferably 99.9 to 100% by weight of the binder comprised in the molding consists of Si and O.

[00122] 27. The initialization method of embodiment 26, wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the binder, calculated as SiO2, in an amount in the range of 1 to 95% by weight, preferably in the range of 3 to 70% by weight, more preferably in the range of 5 to 50% by weight, most preferably in the range of 10 to 30% by weight, based on the total weight of the epoxidation catalyst, preferably based on the total weight of the molding and / or wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the zeolitic material in an amount in the range of 5 to 99% by weight, preferably in the range of 30 to 97% by weight, more preferably in the range of 50 to 95% by weight, most preferably in the range of 70 to 90% by weight, based on the total weight of the catalyst of heterogeneous epoxidation, preferably based on the total weight of the molding.

[00123] 28. The initialization method of any of the embodiments 1 to 27, in which hydrogen peroxide is provided as a solution. Petition 870250090577, dated 03 / 10 / 2025, page 142 / 173 / 73 of aqueous hydrogen peroxide, which preferably has a total organic carbon (TOC) content in the range of 100 to 800 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, preferably in the range of 120 to 750 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, more preferably in the range of 150 to 700 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, determined in accordance with DIN EN 1484 (April 2019).

[00124] 29. The initialization method of any of the embodiments 1 to 28, wherein the hydrogen peroxide has a pH in the range of 0 to 3.0, preferably in the range of 0.1 to 2.5, more preferably in the range of 0.5 to 2.3, determined with a pH-sensitive glass electrode in accordance with the CEFIC PEROXYGENS H2O2 AM-7160 (2003) standard.

[00125] 30. The initialization method of any of the embodiments 1 to 29, wherein hydrogen peroxide comprises 20 to 85% by weight, preferably 30 to 75% by weight, more preferably 40 to 70% by weight of hydrogen peroxide, relative to the total weight of the aqueous hydrogen peroxide solution.

[00126] 31. The initiation method of any of the embodiments 1 to 30, in which hydrogen peroxide is obtained or obtainable from an anthraquinone process.

[00127] 32. The initialization method of any of embodiments 1 to 31, wherein the organic solvent is an organic epoxidation solvent, preferably the organic solvent is selected from the group consisting of alcohol, acetonitrile, propionitrile and mixtures of two or more thereof; more preferably selected from the group consisting of alcohol, acetonitrile and mixtures of alcohol and acetonitrile; most preferably the organic solvent comprises at least one alcohol, wherein the alcohol is preferably a C1 to C5 monoalcohol or a mixture of Petition 870250090577, dated 03 / 10 / 2025, page 143 / 173 / 73 two or more C1 to C5 alcohols, more preferably the alcohol comprises at least methanol, wherein the organic solvent comprises more preferably at least 90% by weight, more preferably at least 95% by weight, more preferably at least 98% by weight, more preferably at least 99% by weight, of methanol.

[00128] 33. The initialization method of any of the embodiments 1 to 33, wherein the olefin is a C2-C10 alkene, preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene.

[00129] 34. A process for preparing an olefin oxide comprising a normal operation stage and a start-up stage, wherein the normal operation stage comprises (A) providing olefin, hydrogen peroxide, water and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide, water and organic solvent is formed; (B) subjecting the reaction mixture from (A) to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide, water and organic solvent; (C) remove an effluent stream from the epoxidation zone, comprising olefin oxide, water and organic solvent; wherein the initialization stage comprises (a) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b) after the first time period, provide solvent Petition 870250090577, dated 03 / 10 / 2025, page 144 / 173 / 73 organic, olefin and hydrogen peroxide to the epoxidation zone for a second period of time P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst.

[00130] 35. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 34, wherein the amount of olefin provided in (a) is less than the amount intended to be provided in the normal operation stage.

[00131] 36. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of embodiment 34 or 35, wherein the amounts of olefin and hydrogen peroxide provided in (b) are less than the respective amounts intended to be provided in the normal operation stage, wherein, preferably, the molar amount of olefin provided in (b) is greater than the molar amount of hydrogen peroxide provided in (b).

[00132] 37. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of any of the embodiments 34 to 36, wherein (b) comprises (b') after the first time period P1, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operation stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts Petition 870250090577, dated 03 / 10 / 2025, page 145 / 173 / 73 intended to be provided in the normal operation stage, so that a mixture 2' is formed, and to bring the mixture 2' into contact during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; wherein, preferably, the molar quantity of olefin initially provided is greater than the molar quantity of hydrogen peroxide initially provided and the molar quantity of olefin provided during the increase is greater than the molar quantity of hydrogen peroxide provided during the increase.

[00133] 38. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 37, wherein the olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operation stage in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:1.

[00134] 39. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 38, wherein the olefin and hydrogen peroxide are provided in (b) or in (b'), respectively, such that the molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[00135] 40. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 39, wherein (a) comprises (a.1) providing olefin and organic solvent for a first period of time P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 for P1 under epoxidation reaction conditions in the epoxidation zone with the epoxidation catalyst Petition 870250090577, dated 03 / 10 / 2025, pp. 146 / 173 / 73 heterogeneous; (a.2) remove, during Pi, an effluent stream from the epoxidation zone, the effluent stream comprising olefin and organic solvent.

[00136] 41. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of any of the embodiments 34 to 40, wherein (b) comprises (b.1) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent; and / or wherein (b') comprises (b'.1) after the first time period Pi, provide organic solvent and olefin and hydrogen peroxide in initial quantities to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the quantities of hydrogen peroxide and olefin are less than the quantities intended to be provided in the normal operating stage, and increase the quantity of hydrogen peroxide and the quantity of olefin over the time period P2' until the quantities intended to be provided in the normal operating stage, so that a mixture 2' is formed, and bring mixture 2' into contact during P2' under Petition 870250090577, dated 03 / 10 / 2025, page 147 / 173 / 73 epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b'.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent.

[00137] 42. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 41, wherein in any one of (a), (a.1), (b), (b'), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), an additive is provided to the epoxidation zone, wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof; wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, ammonia and mixtures of two or more thereof, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more thereof; wherein the additive most preferably comprises at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein most preferably 95 to 100% by weight of the additive is dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate. Petition 870250090577, dated 03 / 10 / 2025, pages 148 / 173 / 73 dipotassium and dipotassium hydrogen phosphate.

[00138] 43. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 42, wherein the additive is, in the case of ammonia, provided in pure form or in aqueous solution, wherein the additive is, in the case of being selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonium salt of an inorganic acid, ammonium salt of an organic acid or any mixture comprising two or more of the same or any mixture comprising ammonia and at least one of these, provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NH4+ and NH3.

[00139] 44. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 42 or 43, wherein the additive is preferably premixed with the organic solvent or with hydrogen peroxide, preferably with the organic solvent, before being provided to the epoxidation zone.

[00140] 45. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 42 to 44, wherein the additive is provided in any one of (a), (b), (b'), (a.1), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), in a molar ratio M:hydrogen peroxide in the range of 1 x 10-5:1 to 1 x 10-3:1.

[00141] 46. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 45, wherein the first time period P1 is preferably a time period in the range of 1 minute to 5 Petition 870250090577, dated 03 / 10 / 2025, p. 149 / 173 / 73 hours, more preferably in the range of 5 minutes to 1 hour, more preferably in the range of 10 minutes to 30 minutes; and / or where the second time period P2 or P2' respectively is preferably a time period in the range of 30 minutes to 24 hours, more preferably in the range of 2 to 18 hours, more preferably in the range of 4 to 12 hours.

[00142] 47. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of any of the embodiments 34 to 46, further comprising, before (a), (x) providing a stream of organic solvent for a period of time Px to the epoxidation zone, wherein Px is preferably a period of time in the range of 10 minutes to 24 hours.

[00143] 48. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 41, which is carried out continuously.

[00144] 49. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 48, wherein contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at an absolute pressure in the epoxidation zone in the range of 0.5 to 5.0 MPa, preferably in the range of 1.5 to 3.0 MPa, more preferably in the range of 1.8 to 2.8 MPa.

[00145] 50. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of any of the embodiments 34 to 49, wherein contact under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst is carried out at a temperature in the epoxidation zone in the range of 20 to 75°C, preferably in the range of 22 to 75°C, more preferably in the Petition 870250090577, dated 03 / 10 / 2025, page 150 / 173 / 73 range of 24 to 70°C, more preferably in the range of 25 to 65°C.

[00146] 51. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 50, wherein the epoxidation reaction conditions comprise drip bed conditions.

[00147] 52. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 51, wherein the epoxidation reaction conditions comprise fixed bed conditions.

[00148] 53. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 52, wherein the heterogeneous epoxidation catalyst comprises a zeolitic material having a framework structure comprising Si, O and Ti.

[00149] 54. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 53, wherein the zeolitic material comprises Ti in an amount in the range of 0.2 to 5% by weight, preferably in the range of 0.5 to 4% by weight, more preferably in the range of 0.7 to 3% by weight, calculated as elemental Ti and based on the total weight of the zeolitic material.

[00150] 55. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of embodiment 53 or 54, wherein the zeolitic material having a framework structure comprising Si, O and Ti comprised in the epoxidation catalyst is a titanium zeolite having a framework structure of ABW, ACO, AEI, AEL, AEN, AET, AFG, AFI, AFN, AFO, AFR, AFS, AFT, AFX, AFY, AHT, ANA, APC, APD, AST, ASV, ATN, ATO, ATS, ATT, ATV, AWO, AWW, BCT, BEA, BEC, BIK, BOG, BPH, BRE, CAN, CAS, CDO, CFI, CGF, CGS, CHA, CHI, CLO, CON, CZP, DAC, DDR, Petition 870250090577, dated 03 / 10 / 2025, pages 151 / 173 / 73 DFO, DFT, DOH, DON, EAB, EDI, EMT, EPI, ERI, ESV, ETR, EUO, FAU, FER, FRA, GIS, GIU, GME, GON, GOO, HEU, IFR, ISV, ITE, ITH, ITQ, ITW, IWR, IWW, JBW, KFI, LEV, LIO, LOU, LIO LTA, LTL, LTN, MAR, MAZ, MCM-22(S), MCM-36, MCM-56, MEI, MEL, MEP, MER, MIT-1, MMFI, MFS, MON, MOR, MSE, MSO, MTF, MTN, MTT, MTW, MWW, NABES, NAT, NAT, NPO, OFF, OFF, OFF OSO, PAR, PAU, PHI, PON, RHO, RON, RRO, RSN, RTE, RTH, RUT, RWR, RWY, SAO, SAS, SAT, SAV, SBE, SBS, SBT, SFE, SFF, SFG, SFH, SFN SFO, SGT, SOD, SOD, SSY, STF, STI, STER, STER, TON, TON, TON UEI, UFI, UOZ, USI, UTL, VET, VFI, VNI, VSV, WEI, WEN, YUG, ZON SVR, SVY or a mixed structure of two or more of these types of arcabouço;More preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type, a MEL framework type, an MWW framework type, an MCM-22(S) framework type, an MCM-56 framework type, an IEZ-MWW framework type, an MCM-36 framework type, an ITQ framework type, a BEA framework type, an MOR framework type or a mixed structure of two or more of these framework types; more preferably, the zeolitic material having a framework structure comprising Si, O and Ti is a titanium zeolite having an MFI framework type or an MWW framework type; More preferably, the zeolitic material having a framework structure comprising Si, O, and Ti has the MFI framework type; more preferably, the zeolitic material having a framework structure comprising Si, O, and Ti is a titanium silicalite-1 (TS-1).

[00151] 56. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 53 to 55, wherein the heterogeneous epoxidation catalyst further comprises a binder, which Petition 870250090577, dated 03 / 10 / 2025, pp. 152 / 173 / 73 preferably includes silicon dioxide.

[00152] 57. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 56, wherein the heterogeneous epoxidation catalyst is in the form of a mold, preferably in the form of a wire or a granule.

[00153] 58. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 56 or 57, wherein 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, most preferably 99.9 to 100% by weight of the molding consist of the zeolitic material and the binder.

[00154] 59. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 56 to 58, wherein 95 to 100% by weight, preferably 98 to 100% by weight, more preferably 99 to 100% by weight, more preferably 99.5 to 100% by weight, most preferably 99.9 to 100% by weight of the binder comprised in the molding consists of Si and O.

[00155] 60. The process for preparing an olefin oxide comprising a normal operation stage and an initialization stage of embodiment 59, wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the binder, calculated as SiO2, in an amount in the range of 1 to 95% by weight, preferably in the range of 3 to 70% by weight, more preferably in the range of 5 to 50% by weight, most preferably in the range of 10 to 30% by weight, based on the total weight of the epoxidation catalyst, preferably based on the total weight of the molding and / or wherein the heterogeneous epoxidation catalyst, preferably the molding, comprises the zeolitic material in a Petition 870250090577, dated 03 / 10 / 2025, page 153 / 173 / 73 quantity in the range of 5 to 99% by weight, preferably in the range of 30 to 97% by weight, more preferably in the range of 50 to 95% by weight, more preferably in the range of 70 to 90% by weight, based on the total weight of the heterogeneous epoxidation catalyst, preferably based on the total weight of the molding.

[00156] 61. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 60, wherein hydrogen peroxide is provided as an aqueous hydrogen peroxide solution, which preferably has a total organic carbon (TOC) content in the range of 100 to 800 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, preferably in the range of 120 to 750 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, more preferably in the range of 150 to 700 mg per kg of hydrogen peroxide comprised in the aqueous hydrogen peroxide solution, determined in accordance with DIN EN 1484 (April 2019).

[00157] 62. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 61, wherein the hydrogen peroxide has a pH in the range of 0 to 3.0, preferably in the range of 0.1 to 2.5, more preferably in the range of 0.5 to 2.3, determined with a pH-sensitive glass electrode in accordance with the CEFIC PEROXYGENS H2O2 AM7160 (2003) standard.

[00158] 63. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 62, wherein the hydrogen peroxide comprises 20 to 85% by weight, preferably 30 to 75% by weight, more preferably 40 to 70% by weight of hydrogen peroxide, relative to the total weight of the aqueous hydrogen peroxide solution. Petition 870250090577, dated 03 / 10 / 2025, pages 154 / 173 / 73

[00159] 64. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 63, wherein hydrogen peroxide is obtained or obtainable from an anthraquinone process.

[00160] 65. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 64, wherein the organic solvent is an organic epoxidation solvent, preferably the organic solvent is selected from the group consisting of alcohol, acetonitrile, propionitrile and mixtures of two or more thereof; more preferably selected from the group consisting of alcohol, acetonitrile and mixtures of alcohol and acetonitrile; More preferably, the organic solvent comprises at least one alcohol, wherein the alcohol is preferably a C1 to C5 monoalcohol or a mixture of two or more C1 to C5 alcohols; more preferably, the alcohol comprises at least methanol, wherein the organic solvent comprises more preferably at least 90% by weight, more preferably at least 95% by weight, more preferably at least 98% by weight, more preferably at least 99% by weight, of methanol.

[00161] 66. The process for preparing an olefin oxide comprising a normal operation stage and a start-up stage of any of the embodiments 34 to 65, wherein the olefin is a C2C10 alkene, preferably a C2-C5 alkene, more preferably a C2-C4 alkene, more preferably ethylene or propylene, more preferably propylene.

[00162] 67. The process for preparing an olefin oxide according to any of the embodiments 34 to 66, wherein the epoxidation in (B) is carried out at an absolute pressure in the reaction zones in the range of 0.5 to 5.0 MPa, preferably in the range of 1.5 to 3.0 MPa, more preferably in the range of 1.8 to 2.8 MPa.

[00163] 68. The process for preparing an olefin oxide according to Petition 870250090577, dated 03 / 10 / 2025, p. 155 / 173 / 73 with any of the embodiments 34 to 67, in which the epoxidation in (B) is carried out at a temperature in the reaction zones in the range of 20 to 75°C, preferably in the range of 25 to 75°C, more preferably in the range of 28 to 70°C, most preferably in the range of 30 to 65°C.

[00164] 69. The process for preparing an olefin oxide according to any one of embodiments 34 to 68, wherein the molar ratio of olefin:hydrogen peroxide (w / w) in the reaction mixture formed in (A) is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:1.

[00165] 70. The process for preparing an olefin oxide according to any one of embodiments 34 to 69, wherein the weight ratio of organic solvent:hydrogen peroxide (w / w) in the reaction mixture formed in (A) is in the range of 15:1 to 5:1, preferably in the range of 12:1 to 6:1, more preferably in the range of 12:1 to 8.5:1 or in the range of 8:1 to 6:1.

[00166] 71. The process for preparing an olefin oxide according to any one of embodiments 34 to 70, wherein the organic solvent:olefin weight ratio (w / w) in the reaction mixture formed in (A) is in the range of 10:1 to 1:0.1, preferably in the range of 9:1 to 1:1, more preferably in the range of 7:1 to 4:1 or in the range of 1.5:1 to 1:1.

[00167] 72. The process for preparing an olefin oxide according to any of the embodiments 34 to 71, wherein an additive is provided in (A), wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof; wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, Petition 870250090577, dated 03 / 10 / 2025, page 156 / 173 / 73 diammonium hydrogen phosphate, ammonia and mixtures of two or more thereof, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more thereof; wherein the additive comprises, most preferably, at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein, most preferably, 95 to 100% by weight of the additive is dipotassium etidronate.

[00168] 73. The process for preparing an olefin oxide according to embodiment 72, wherein the additive is, in the case of ammonia, provided in pure form or in aqueous solution, wherein the additive is, in the case of being selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonium salt of an inorganic acid, ammonium salt of an organic acid or any mixture comprising two or more of the same or any mixture comprising ammonia and at least one of the same, provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NHZ and NH3.

[00169] 74. The process for preparing an olefin oxide according to embodiment 72 or 73, wherein the aqueous solution of additive comprises in the range of 0.01 to 5% by weight, preferably in the range of 0.5 to 3% by weight, more preferably in the range of 1 to 2% by weight, of additive, based on the total weight of the aqueous solution.

[00170] 75. The process for preparing an olefin oxide according to any of the embodiments 72 to 74, wherein the additive is Petition 870250090577, dated 03 / 10 / 2025, page 157 / 173 / 73 preferably premixed with the organic solvent or with hydrogen peroxide, more preferably premixed with the organic solvent, before being provided to the epoxidation zone in (A).

[00171] 76. The process for preparing an olefin oxide according to any one of embodiments 34 to 75, wherein the additive is provided in (A) in a molar ratio M:hydrogen peroxide in the range of 1 x 10-5:1 to 1 x 10-3:1.

[00172] 77. The process for preparing an olefin oxide according to any of the embodiments 34 to 76, wherein the epoxidation reaction conditions according to (B) comprise fixed bed conditions.

[00173] 78. The process for preparing an olefin oxide according to any of the embodiments 34 to 76, wherein the epoxidation reaction conditions according to (B) comprise trickle bed conditions.

[00174] 79. Olefin oxide, preferably propylene oxide, obtained or obtainable from the process of any of the embodiments 34 to 78.

[00175] The present invention is further illustrated by the following reference examples, comparative examples and examples. Examples Table 1 Chemicals Methanol CH3OH Propylene C3H5 (C3) Oxygen O2 Nitrogen N2 Hydrogen peroxide H2O2 Dipotassium hydrogen phosphate K2HPO4 Colloidal silica at 40% by weight in water Ludox® AS-40 Titanium silicalite zeolite-1 TS-1

[00176] The TS-1 catalyst was prepared in accordance with Reference Example 2 of document WO 2022 / 263437 A1 and was used in wire form. Petition 870250090577, dated 03 / 10 / 2025, page 158 / 173 / 73 extrudates having a diameter of 1.5 mm (circular cross-section). The extrudates contained 75% by weight of TS-1 and 25% by weight of silicon dioxide (from Ludox®). Analytical methods Determination of organic constituents

[00177] The concentration of the constituents of the effluent stream (product) from the 2nd separator (see Reference Example 1) was analyzed by Gas Chromatography (GC) Determination of oxygen and nitrogen concentration

[00178] The ventilation stream flow after the 2nd separator (see Reference Example 1) was measured using a Brunkhorst flow meter and the oxygen concentration was measured using a Dräger Polytron 7000 detector with an electrochemical sensor. Determination of water concentration

[00179] The water concentration was determined by Karl Fischer titration. Determination of hydrogen peroxide

[00180] Hydrogen peroxide was determined photometrically in accordance with DIN38409, part 15 (June 1897). Determination of total peroxides

[00181] Total peroxides (organic ROOH and H2O2) were provided as the active oxygen content. The active oxygen content in the samples was determined by iodometry. A general description of how the determination was performed is provided below.

[00182] Approximately 5 g of the sample, weighed to a precision of 0.1 mg, were placed in a reaction flask, washed with argon, and 40 ml of a 1:1 acetic acid / chloroform mixture were added to dissolve the sample. The reaction flask was fitted with a chiller and placed on a preheated heating block at 80°C. One Petition 870250090577, dated 03 / 10 / 2025, page 159 / 173 / 73 A weak argon flow was passed through the cooler to prevent air from entering. After temperature equilibration, 5.0 ml of a saturated potassium iodide solution (approximately 60.0 g of potassium iodide dissolved in 100 ml of deionized water) were added through the cooler and the mixture was boiled under reflux for 10 min. In the next step, 40.0 ml of deionized water were added and the sample solution was titrated with a 0.01 M thiosulfate solution, using a platinum electrode as an endpoint indicator. Hydrogen peroxide conversion calculation

[00183] The conversion of H2O2 in % was calculated according to the following equation (I): H2O2 Conversion [%] = [(mmol of hydrogen peroxide (feed) - mmol of hydrogen peroxide (effluent)) / mmol of hydrogen peroxide (feed)]*100 % (I) where “mmol of hydrogen peroxide (feed)” means the amount in mmol of H2O2 in the reactor feed stream and “mmol of hydrogen peroxide (effluent)” means the amount in mmol of H2O2 in the effluent stream leaving the reactor. Selectivity calculation

[00184] The selectivity of a compound X in % mol was calculated based on the following equation (II): Compound X [%] = (mmol of compound X (effluent) per hour / mmol total (effluent) per hour)*100 % (II) where X is a compound selected from PO, AA, PM-2, PM-1, acetol, MPG and ROOH, “mmol compound X (effluent)” means the amount in mmol of said compound in the effluent stream leaving the reactor and “mmol total (effluent)” means the sum of the amount in mmol of propylene (C3) converted into PO + AA + PM-2 + PM-1 + acetol + MPG + ROOH in the effluent stream leaving the reactor per hour. Petition 870250090577, dated 03 / 10 / 2025, pages 160 / 173 / 73 Reference Example 1: Experimental Reactor Configuration for Example 1 and Comparative Example 1

[00185] 140 g of TS-1 catalyst were loaded into a reaction tube of a mini-plant with a length of 180 cm and a volume of 300 ml. The tube diameter was 1.905 cm (0.75 inch), with a wall thickness of 0.19 cm (0.07 inch). In the center of the reaction tube was installed a smaller tube (0.3175 cm (0.125 inch)), containing thermocouples to measure the temperature over the catalyst bed. The critical point, i.e., the zone where the maximum reaction occurs, is normally located in the first half of a catalytic bed and, preferably, most of the thermocouples used are located in the first half of the catalytic bed.

[00186] Propylene was stored in 50 l gas cylinders containing immersion tubes, facilitating transfer to the mini-plant via a nitrogen pressure of 2,500 kPa (25 bar). The precise quantity was measured using a Brunkhorst flow meter with a range of 0 to 500 g / h. The flow was controlled by a Flowserve control valve. Hydrogen peroxide was transferred to the reactor using a Grundfos DME2 pump. The quantity was determined using a scale. The measurement showed liters / minute. The respective additive solution was fed to the reactor using an LC hydrogen peroxide pump. The precise quantity was determined using a scale. A Lewa pump with a range of 0 to 1,500 ml / h was used to feed the methanol. Feed control was performed using a Lewa KMM. Nitrogen was fed using a Flowserve control valve. The quantity was measured using a Brunkhorst flow meter with a range of 0 to 200 Nl / h.“Nl / h” means standard liter per hour, where 1 standard liter is the amount of gas that fills 1 litre at 0°C and 101.3 kPa (1,013 mbar) (see DIN 1343 of January 1990). Petition 870250090577, dated 03 / 10 / 2025, pages 161 / 173 / 73

[00187] The reagents, solvents, and additives, as indicated in detail in Example 1 and Comparative Example 1, all entered the reaction tube by means of a static mixer [0.635 cm (0.25 inch) mixer], so that a combined feed stream was formed and fed into the reaction tube, in which the feed direction was from the bottom to the top of the reaction tube.

[00188] The reactor effluent was passed through a 2-micrometer filter to remove fine particles (catalyst) before passing to the first separator. The bottom level valve controlled a 25% level in the first separator, while the top pressure valve established a pressure of 2,000 kPa (20 bar) throughout the upstream reaction system. The second separator was also operated at a 25% liquid level, while the top pressure valve reduced the pressure to 200 kPa (2 bar). This lower pressure served to allow the evaporation of unconverted propylene, allowing for safe sample collection and providing an additional safety buffer. The two separators had a volume of 2 liters each and were maintained at a temperature of 5°C using cooling water.A nitrogen stream with a gas flow rate of 5 NI / h was fed through the entire system (reactor -> 1st separator -> 2nd separator -> venting system) to maintain sufficient gas flow in the venting direction to verify if traces of oxygen, formed by the partial decomposition of H2O2, had evaporated and could be analyzed at the end of the vent pipe. A flow meter was installed in the vent line, through which the gaseous vent stream from the 2nd separator flows, to measure the flow and quantify the amount of oxygen. The liquid effluent stream (product) from the 2nd separator was analyzed by Gas Chromatography (GC) for the compounds it contained and their respective quantities and concentrations. Petition 870250090577, dated 03 / 10 / 2025, pages 162 / 173 / 73 Example 1: Startup process with propylene feed starting before the start of aqueous hydrogen peroxide solution feed. Startup stage.

[00189] The reactor of Reference Example 1 was purged with nitrogen and pressurized to 2,000 kPa (20 bar). Initially (tstart-up = 0 h), methanol was fed at a rate of 370 g / h through the static mixer into the reaction tube, so that the reaction tube was initially flooded with methanol, with the feed direction being from the bottom to the top of the reaction tube. 15 minutes later (tstart-up = 15 minutes), the addition of propene was initiated via the static mixer at a rate of 54 g / h, so that a combined stream comprising methanol and propene was fed into the reaction tube.After a further 15 minutes (tstart-up = 30 minutes), the feeding of an aqueous hydrogen peroxide solution (40% by weight H2O2) at a flow rate of 47 g / h (50% of the flow rate used for normal operation) and additive solution (aqueous K2HPO4 solution, 0.3% by weight K2HPO4) with a flow rate adjusted to maintain 130 micromol K+ / mol of hydrogen peroxide to the static mixer was initiated, so that a combined stream of methanol, propylene, water, hydrogen peroxide and additive (K2HPO4) was fed to the reaction tube. — from this moment, the production time was counted (tstart-up = 30 minutes corresponds to ton stream = 0h). After four hours of production, the flow rate of the aqueous hydrogen peroxide solution was increased to 65 g / h (70% of the flow rate used for normal operation) and the additive flow rate was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream.After 23 hours in production, the flow rate of the aqueous hydrogen peroxide solution was increased to 94 g / h (100% of the flow rate used for normal operation) and the additive flow rate was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream. Petition 870250090577, dated 03 / 10 / 2025, pages 163 / 173 / 73 Normal operating stage

[00190] The reaction was then carried out under normal operating conditions with a combined feed stream to the propylene-based reactor fed at 54 g / h, aqueous H2O2 solution (40 wt% H2O2) fed at a rate of 94 g / h, methanol fed at a rate of 370 g / h and an additive solution of 4 g / h aqueous K2HPO4 solution (0.3 wt% K2HPO4), wherein the flow rate of the additive solution was adjusted to maintain 130 micromol K+ / mol hydrogen peroxide. Normal operation was continued for at least 72 h in production.

[00191] During the initialization stage and the normal operation stage - during the first 48 hours in production - the water temperature setpoint was kept constant at 30°C and only then was it increased to achieve a hydrogen peroxide conversion of 90% using a water-cooled jacket circuit.

[00192] During the initialization stage and the normal operation stage, samples were collected from the liquid effluent (product) stream downstream of the 2nd separator at production times of 7h, 23h, 31h, 47h, 55h and 71h and analyzed by GC.

[00193] The selectivities to propylene oxide (PO) and several characteristic byproducts were calculated based on the amount of PO or the respective byproduct in the effluent stream withdrawn from the reactor per hour relative to the total amount of propylene (C3) converted to PO and all byproducts per hour according to Equation (II). The results are shown below in Table 2 and are graphically represented in Figure 1 (PO selectivity) and Figure 3 (overview of the average selectivities listed in Table 2 for AA, PM-2, PM-1, acetol, MPG and ROOH).

[00194] The conversion of hydrogen peroxide was calculated based on the amount of hydrogen peroxide contained in the effluent stream withdrawn from the reactor in relation to the amount of hydrogen peroxide Petition 870250090577, dated 03 / 10 / 2025, pages 164 / 173 / 73 included in the liquid feed stream provided to the reactor according to Equation (I) and the results are shown graphically in Figure 2. Table 2 Selectivities for PO and by-products ____________________________ Time [h] PO [%] AA [%] PM-2 [%] PM-1 [%] Acetol [%] MPG [%] ROOH [%] 7 92.78 0.26 2.53 3.61 0.10 0.72 0.00 23 94.25 0.31 1.84 2.57 0.12 0.51 0.40 31 95.09 0.38 1.55 1.84 0.13 0.44 0.57 47 96.17 0.35 1.01 0.96 0.16 0.29 1.06 55 96.26 0.41 1.03 0.97 0.18 0.29 0.86 71 96.56 0.42 0.96 0.90 0.18 0.27 0.71 Average 95.19 0.36 1.49 1.81 0.15 0.42 0.60 Production time in hours PO [%] Propylene-based selectivity for PO in % by mole AA [%] Propylene-based selectivity for acetaldehyde in % by mole PM-2 [%] Propylene-based selectivity for 1-methoxy-2-methanol in mol% PM-1 [%] Propylene-based selectivity for 2-methoxy-1-methanol in mol% Acetol [%] Propylene-based selectivity for hydroxyacetone in % mol MPG [%] Propylene-based selectivity for 1,2-propanediol in % by mole ROOH [%] Propylene-based selectivity for hydroperoxypropanols in % by mole Comparative Example 1: Startup process with aqueous hydrogen peroxide solution feed starting before propylene feed begins. Startup stage

[00195] The reactor of Reference Example 1 was purged with nitrogen and pressurized to 2,000 kPa (20 bar). Initially (tstart-up = 0 h), methanol was fed at a rate of 370 g / h through the static mixer into the reaction tube, so that the reaction tube was initially flooded with methanol, with the feed direction from the bottom to the top of the reaction tube. After 15 minutes (tstart-up = 15 minutes), a feed of an aqueous hydrogen peroxide solution (40 wt% H2O2) was added at a rate of 47 g / h (50% of the flow rate used for normal operation) and an additive solution (aqueous K2HPO4 solution, 0.3 wt% K2HPO4) at a flow rate adjusted to maintain 130 micromol K+ / mol of Petition 870250090577, dated 03 / 10 / 2025, page 165 / 173 / 73 Hydrogen peroxide in the static mixer was initiated, so that a combined stream of methanol, water, hydrogen peroxide and additive (K2HPO4) was fed to the reaction tube. After another 15 minutes (tstart-up = 30 minutes), propylene was added via the static mixer at a flow rate of 54 g / h, so that a combined stream comprising methanol, hydrogen peroxide, water, K2HPO4 and propylene was fed to the reaction tube - from this point in time, the production time was counted (tstart-up = 30 minutes corresponds to ton stream = 0h). After four hours of production (ton-stream = 4h), the flow rate of the aqueous hydrogen peroxide solution was increased to 65 g / h (70% of the flow rate used for normal operation) and the additive flow rate was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream.During 24 hours of production (ton-stream = 24h), the flow rate of the aqueous hydrogen peroxide solution was increased to 94 g / h (100% of the flow rate used for normal operation) and the additive flow rate was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream. Normal operating stage

[00196] The reaction was then carried out under normal operating conditions with a combined feed stream to the propylene-based reactor fed at 54 g / h, aqueous H2O2 solution (40 wt% H2O2) fed at a rate of 94 g / h, methanol fed at a rate of 370 g / h and an additive solution of 4 g / h aqueous K2HPO4 solution (0.3 wt% K2HPO4), wherein the flow rate of the additive solution was adjusted to maintain 130 micromol K+ / mol hydrogen peroxide. Normal operation was continued for at least 72 h in production.

[00197] During the initialization stage and the normal operation stage - during the first 48 hours in production - the water temperature setpoint was kept constant at 30°C and only afterwards was Petition 870250090577, dated 10 / 03 / 2025, pp. 166 / 173 / 73 increased to achieve a target hydrogen peroxide conversion of 90% using a water-cooled jacket circuit.

[00198] During the initialization stage and the normal operation stage, samples were collected from the effluent (product) stream downstream of the 2nd separator at production times of 8h, 24h, 32h, 48h, 56h and 72h.

[00199] The selectivities for propylene oxide (PO) and several characteristic byproducts were calculated based on the amount of PO or the respective byproduct in the effluent stream withdrawn from the reactor relative to the total amount of PO and all byproducts according to Equation (II). The results are shown below in Table 3 and are graphically represented in Figure 1 (PO selectivity) and Figure 3 (overview of average selectivities listed in Table 2 for AA, PM-2, PM-1, acetol, MPG and ROOH).

[00200] The hydrogen peroxide conversion was calculated based on the amount of hydrogen peroxide contained in the effluent stream withdrawn from the reactor relative to the amount of hydrogen peroxide contained in the liquid feed stream supplied to the reactor according to Equation (I) and the results are shown graphically in Figure 2. Table 3 Selectivity for PO and by-products Time [h] PO [%] AA [%] PM-2 [%] PM-1 [%] Acetol [%] MPG [%] ROOH [%] 8 91.99 0.29 2.76 4.12 0.11 0.73 0.00 24 93.77 0.39 1.76 2.41 0.16 0.58 0.93 32 94.60 0.40 1.51 1.56 0.22 0.50 1.21 48 95.69 0.47 1.32 1.25 0.24 0.35 0.68 56 96.00 0.51 1.13 1.09 0.23 0.34 0.70 72 96.00 0.61 1.11 1.02 0.26 0.34 0.66 Average 94.68 0.45 1.60 1.91 0.20 0.47 0.70 Production time in hours PO [%] Propylene-based selectivity for PO in % by mole AA [%] Propylene-based selectivity for acetaldehyde in % by mole PM-2 [%] Propylene-based selectivity for 1-methoxy-2-methanol in mol% Petition 870250090577, dated 03 / 10 / 2025, pages 167 / 173 / 73 PM-1 [%] Acetol [%] MPG [%] ROOH [%] Propylene-based selectivity for 2-methoxy-1-methanol in mol% Propylene-based selectivity for hydroxyacetone in mol% Propylene-based selectivity for 1,2-propanediol in mol% Propylene-based selectivity for hydroperoxypropanols in mol% Example 2: Initialization process with propylene feed initiated before the start of aqueous hydrogen peroxide solution feed; excess molar quantity of propylene compared to the hydrogen peroxide provided or intended to be provided, respectively. Startup stage

[00201] The reactor of Reference Example 1 was purged with nitrogen and pressurized to 2,000 kPa (20 bar). Initially (tstart-up = 0 h), methanol was fed at a rate of 370 g / h through the static mixer into the reaction tube, so that the reaction tube was initially flooded with methanol, with the feed direction being from the bottom to the top of the reaction tube. 15 minutes later (tstart-up = 15 minutes), the addition of propylene was initiated via the static mixer at a rate of 17 g / h, so that a combined stream comprising methanol and propylene was fed to the reaction tube; the molar ratio of propene:hydrogen peroxide (intended to be provided in normal operation) was 0.3.After a further 15 minutes (tstart-up = 30 minutes), the feeding of an aqueous hydrogen peroxide solution (40% by weight H2O2) at a flow rate of 55 g / h and an additive solution (aqueous K2HPO4 solution, 0.3% by weight K2HPO4) at a flow rate adjusted to maintain 130 micromol K+ / mol of hydrogen peroxide in the static mixer was started; simultaneously, the propylene feed was increased to 44 g / h, so that a combined stream of methanol, propylene, water, hydrogen peroxide and additive (K2HPO4) was fed into the reaction tube - from this point in time, the production time was counted (tstart-up = 30 minutes corresponds to ton stream = 0h); the propylene:hydrogen peroxide molar ratio was 1.6. After four hours in production, a. Petition 870250090577, dated 03 / 10 / 2025, page 168 / 173 / 73: the flow rate of the aqueous hydrogen peroxide solution was increased to 80 g / h; the flow rate of the additive was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream, while simultaneously, the propylene feed was increased to 56 g / h; the propylene:hydrogen peroxide molar ratio was 1.4. After 23 hours and 45 minutes of production, the flow rate of the aqueous hydrogen peroxide solution was increased to 94 g / h (100% of the flow rate used for normal operation) and the additive flow rate was increased accordingly to maintain 130 micromol K+ / mol of hydrogen peroxide in the combined feed stream, while simultaneously, the propylene feed was increased to 66 g / h (100% of the flow rate used for normal operation); the propylene:hydrogen peroxide molar ratio was 1.3. Normal operating stage

[00202] The reaction was then carried out under normal operating conditions with a combined feed stream to the propylene-based reactor fed at 54 g / h, aqueous H2O2 solution (40 wt% H2O2) fed at a rate of 94 g / h, methanol fed at a rate of 370 g / h and an additive solution of 4 g / h aqueous K2HPO4 solution (0.3 wt% K2HPO4), wherein the flow rate of the additive solution was adjusted to maintain 130 micromol K+ / mol hydrogen peroxide. Normal operation was continued for at least 72 h in production.

[00203] During the initialization stage and the normal operation stage - during the first 48 hours in production - the water temperature setpoint was kept constant at 30°C and only then was it increased to achieve a hydrogen peroxide conversion of 90% using a water-cooled jacket circuit.

[00204] During the initialization stage and the normal operation stage, samples were collected from the liquid effluent (product) stream downstream of the 2nd separator at a time during production, as indicated in Petition 870250090577, dated 03 / 10 / 2025, pages 169 / 173 / 73 Table 3, and analyzed using GC.

[00205] The selectivities to propylene oxide (PO) and several characteristic byproducts were calculated based on the amount of PO or the respective byproduct in the effluent stream withdrawn from the reactor per hour relative to the total amount of propylene (C3) converted to PO and all byproducts per hour according to Equation (II). For PO, the average propylene-based selectivity was 95.3% (mol %), while for the byproducts AA, PM-1, PM-2 and acetol, the average selectivities were AA: 0.18% (mol %), PM-2: 1.66% (mol %), PM-1 2.02% (mol %), and acetol: 0.09% (mol %).

[00206] The conversion of hydrogen peroxide was calculated based on the amount of hydrogen peroxide contained in the effluent stream removed from the reactor in relation to the amount of hydrogen peroxide contained in the liquid feed stream provided to the reactor according to Equation (I). Results - Comparison of procedures according to Examples 1 and 2 versus the procedure according to Comparative Example 1.

[00207] In the startup procedure according to Example 1, based on an initial methanol stream, the propylene feed was started before the start of the aqueous hydrogen peroxide solution feed, whereas in Comparative Example 1, the startup procedure was done in reverse, i.e., based on an initial methanol stream, the aqueous hydrogen peroxide solution feed was started before the start of the propylene feed.

[00208] The selectivity of propylene oxide (PO) based on converted propylene was always higher when following the procedure of Example 1 compared to Comparative Example 1, which indicated that an initialization with the start of propylene feeding before the start of hydrogen peroxide feeding was superior. Petition 870250090577, dated 03 / 10 / 2025, pages 170 / 173 / 73

[00209] Regarding hydrogen peroxide conversion, it was observed that hydrogen peroxide conversion was 100% in the first 24 hours of production and almost identical (~97 to 98%) after 32 hours of production for Example 1 and Comparative Example 1. Even though during the first 48 hours of production the water temperature setpoint was kept constant at 30°C and only then increased to achieve the target hydrogen peroxide conversion of 90%, a greater drop in hydrogen peroxide conversion was observed after these first 48 hours of production – and before the start of the water temperature increase – in the procedure according to Comparative Example 1 (88%) compared to the procedure of Example 1 (93%). This shows that starting with hydrogen peroxide feed before propylene feed resulted in faster catalyst deactivation.

[00210] Regarding the selectivities over time for the main byproducts acetaldehyde (AA), 1-methoxy-2-propanol (PM-2), 2-methoxy-1-propanol (PM-1), hydroxyacetone (acetol), 1,2-propanediol (MPG), and hydroperoxypropanols (ROOH), it was observed that the average selectivity for each byproduct was always higher when the procedure of Comparative Example 1 was used compared to the procedure according to Example 1. This demonstrated that an initialization with the start of hydrogen peroxide feeding before the start of propylene feeding resulted in an increase in byproduct formation.

[00211] Looking more closely at Example 2, it became evident that when comparing Example 1 and Example 2, Example 2, which was based on a propylene start before the hydrogen peroxide start, combined with a gradual increase of propylene and hydrogen peroxide under consideration of a molar excess of propylene relative to the hydrogen peroxide used or intended to be used in the range of 0.1:1 to 4:1 - here 0.3 - and Petition 870250090577, dated 03 / 10 / 2025, page 171 / 173 / 73 preferably also a molar ratio of olefin:hydrogen peroxide since the hydrogen peroxide feed was initiated in the range of 1.1:1 to 5:1 - here 1.6:1, 1.4:1 and 1.3:1, respectively - resulted in even more improved performance: Although the selectivity of PO was as good as in Example 1, the selectivities with respect to four of the main by-products, namely, acetaldehyde (AA), 1-methoxy-2-propanol (PM2), 2-methoxy-1-propanol (PM-1), hydroxyacetone (acetol), were drastically reduced.

[00212] Overall, it was demonstrated that using a startup procedure with propylene feed initiation before hydrogen peroxide feed initiation significantly helped to minimize propylene oxide losses during the startup phase and was therefore superior to a startup procedure with hydrogen peroxide feed initiation before propylene feed initiation. Brief Description of the Figures

[00213] Figure 1 shows the PO selectivity achieved according to the Example 1 procedure over time versus the PO selectivity achieved according to the Comparative Example 1 procedure over time, where production time is shown on the x-axis in hours and PO selectivity in % is shown on the y-axis.

[00214] Figure 2 shows the hydrogen peroxide conversion achieved according to the procedure of Example 1 over time versus the hydrogen peroxide conversion achieved according to the procedure of Comparative Example 1 over time, where the production time is shown on the x-axis in hours and the hydrogen peroxide conversion in % is shown on the y-axis.

[00215] Figure 3 shows the average selectivities for various byproducts achieved according to the procedure in Example 1 versus Petition 870250090577, dated 03 / 10 / 2025, pp. 172 / 173 / 73 the average selectivities for these by-products achieved according to the procedure of Comparative Example 1. Literature Cited

[00216] - WO 2017 / 162446 A1 - WO 2022 / 263437 A1 Petition 870250090577, dated 03 / 10 / 2025, page 173 / 173

Claims

1 / 6 CLAIMS 1. Startup method for a process for preparing an olefin oxide comprising a normal operation stage, wherein the normal operation stage comprises providing olefin, hydrogen peroxide and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, such that a reaction mixture comprising olefin, hydrogen peroxide and organic solvent is formed, and subjecting the reaction mixture to epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide and organic solvent;characterized in that the initialization method comprises (a) providing olefin and organic solvent for a first time period P1 to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; wherein the amount of olefin provided in (a) is less than the amount intended to be provided in the normal operating stage.

2. Startup method according to claim 1, characterized in that the amounts of olefin and hydrogen peroxide provided in (b) are less than the respective amounts intended to be provided in the normal operating stage, wherein, preferably, the molar amount of olefin provided in (b) is greater than the molar amount of hydrogen peroxide provided in (b).

3. Initialization method according to claim 1 or 2, characterized in that (b) comprises (b') after the first time period Pi, providing organic solvent and olefin and hydrogen peroxide in initial amounts to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the amounts of hydrogen peroxide and olefin are less than the amounts intended to be provided in the normal operating stage, and increasing the amount of hydrogen peroxide and the amount of olefin over the time period P2' until the amounts intended to be provided in the normal operating stage, so that a mixture 2' is formed, and contacting the mixture 2' during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst;wherein, preferably, the molar quantity of olefin initially provided is greater than the molar quantity of hydrogen peroxide initially provided, and the molar quantity of olefin provided during the increase is greater than the molar quantity of hydrogen peroxide provided during the increase.

4. Startup method according to any one of claims 1 to 3, characterized in that the olefin is provided in (a) in a molar ratio relative to the molar amount of hydrogen peroxide intended to be used in the normal operating stage in the range of 0.1:1 to 4:1, preferably in the range of 0.1:1 to 1:1 or in the range of 2.1 to 4:

1.

5. Initialization method according to any of claims 1 to 4, characterized in that the olefin and hydrogen peroxide are provided in (b) or in (b'), respectively, such that the molar ratio of olefin:hydrogen peroxide in the second mixture 2 formed in (b) or in the mixture formed in (b'), respectively, is in the range of 1.1:1 to 5:1, preferably in the range of 1.1:1 to 2:1 or in the range of 3:1 to 5:

1.

6. A method of initiation according to any one of claims 1 to 5, characterized in that (b) comprises (b.1) after the first time period, providing olefin, organic solvent and hydrogen peroxide to the epoxidation zone for a second time period P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b.2) removing, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent; and / or wherein (b') comprises (b'.1) After the first time period P1, provide organic solvent and olefin and hydrogen peroxide in initial quantities to the epoxidation zone for a time period P2', so that a mixture is formed, comprising organic solvent, olefin and hydrogen peroxide, wherein the quantities of hydrogen peroxide and olefin are less than the quantities intended to be provided in the normal operating stage, and increase the quantity of hydrogen peroxide and the quantity of olefin over the time period P2' until the quantities intended to be provided in the normal operating stage, so that a mixture 2' is formed, and bring mixture 2' into contact during P2' under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst; (b'.2) remove, during the respective time period, an effluent stream from the epoxidation zone, the effluent stream comprising olefin oxide and organic solvent.

7. A method of initiation according to any one of claims 1 to 6, characterized in that, in any one of (a), (a.1), (b), (b'), (b.1), (b'.1), preferably in at least one of (b), (b'), (b.1), (b'.1), more preferably in each of (b), (b'), (b.1), (b'.1), an additive is provided to the epoxidation zone, wherein the additive is selected from the group consisting of potassium salt of an inorganic acid, potassium salt of an organic acid, ammonia, ammonium salt of an inorganic acid, ammonium salt of an organic acid and mixtures of two or more thereof;wherein the additive is preferably selected from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, potassium formate, potassium acetate, potassium hydrogen carbonate, dipotassium etidronate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, ammonia and mixtures of two or more thereof, more preferably from the group consisting of potassium dihydrogen phosphate, dipotassium hydrogen phosphate, dipotassium etidronate, ammonia and mixtures of two or more thereof; wherein the additive comprises, more preferably, at least dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate, wherein, more preferably in the range of 95 to 100% by weight of the additive, dipotassium etidronate or dipotassium hydrogen phosphate or a mixture of dipotassium etidronate and dipotassium hydrogen phosphate are present. Petition 870250090577, dated 03 / 10 / 2025, page 93 / 173 5 / 6; 8. A method of initiation according to claim 7, characterized in that the additive, in the case of ammonia, is provided in pure form or in aqueous solution, wherein the additive, if selected from the group consisting of a potassium salt of an inorganic acid, a potassium salt of an organic acid, an ammonium salt of an inorganic acid, an ammonium salt of an organic acid, or any mixture comprising two or more of the same, or any mixture comprising ammonia and at least one of the same, is provided in aqueous solution; wherein the additive in aqueous solution releases or forms one or more cations M, wherein M represents, in the case of a potassium salt, K+, or, in the case of ammonia or ammonium salts, M represents the sum of NH3 and NH3.

9. Initiation method according to any one of claims 1 to 8, characterized in that it further comprises, before (a), (x) providing a stream of organic solvent for a period of time Px to the epoxidation zone, wherein Px is preferably a period of time in the range of 10 minutes to 24 hours.

10. Process for preparing an olefin oxide, characterized in that it comprises a normal operation stage and an initialization stage, wherein the normal operation stage comprises (A) providing olefin, hydrogen peroxide, water and organic solvent in an epoxidation zone comprising a heterogeneous epoxidation catalyst, so that a reaction mixture comprising olefin, hydrogen peroxide, water and organic solvent is formed; (B) subjecting the reaction mixture of (A) to the epoxidation reaction conditions in the epoxidation zone, thereby obtaining a mixture comprising olefin oxide, water and organic solvent; (C) removing an effluent stream from the epoxidation zone, Petition 870250090577, dated 03 / 10 / 2025, page 94 / 173 6 / 6 comprising olefin oxide, water and organic solvent;wherein the initialization stage comprises (a) providing olefin and organic solvent for a first period of time Pi to the epoxidation zone, so that a first mixture 1 is formed, which is essentially free of hydrogen peroxide, and contacting the first mixture 1 during P1 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst, wherein the amount of olefin provided in (a) is less than the amount provided in the normal operating stage; (b) after the first period of time, providing organic solvent, olefin and hydrogen peroxide to the epoxidation zone for a second period of time P2, so that a second mixture 2 is formed, comprising olefin, organic solvent and hydrogen peroxide, and contacting the second mixture 2 during P2 under epoxidation reaction conditions in the epoxidation zone with the heterogeneous epoxidation catalyst.

11. Olefin oxide, preferably propylene oxide, characterized in that it is obtained or obtainable by the process as defined in claim 10. Petition 870250090577, dated 03 / 10 / 2025, page 95 / 173

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