Multistage Reactor Systems and Processes for Oxygenate Conversion

Description

1 / 61 Multistage Reactor Systems and Processes for Oxygenate Conversion REFERENCE TO RELATED PATENT APPLICATION

[001] This patent application grants priority to the application for Provisional Patent No. 63 / 488,867 filed on March 7, 2023, the full content of which is hereby expressed by reference in this document. TECHNICAL FIELD

[002] Multistage reactor systems and processes for the conversion of oxygenates (e.g., alcohols or ethers) are presented, and more specifically, adiabatic processes that result in the conversion of oxygenates into olefins. BACKGROUND

[003] Multistage reactor systems and processes for the conversion of oxygenates (e.g., alcohols or ethers), and more specifically, adiabatic processes resulting in the conversion of oxygenates to olefins are provided.

[004] Fixed-bed adiabatic reactors are among the least expensive reactors available, but they present a challenge for processes that release or absorb significant amounts of heat. Endothermic reactions reduce the process temperature as a function of the extent of the reaction and can quench the processes without the addition of heat. Exothermic reactions increase the process temperature as a function of the extent of the reaction and can cause the reaction to lose selectivity or proceed uncontrollably without heat removal. Adding or removing heat in such processes requires expensive heat exchange equipment, ultimately increasing the net heat demand, increasing the system pressure drop, and increasing the difficulty of controlling the process. In processes with high heat exchange demand, it is typical Petition 870250078935, dated 04 / 09 / 2025, page 11 / 101 2 / 61 ca the segmentation of a fixed bed and the addition of heating or cooling stages, or the use of generally more expensive multitubular fixed-bed reactors where the reactor itself serves as a heat exchanger. However, such systems can be inefficient, and furthermore the applicability of such systems can be severely limited (e.g., steam reforming of methane or partial oxidation of propylene to acrylic acid, among others) and generally cannot support systems consisting of a combination of exothermic and endothermic steps.

[005] Consequently, there continues to be a need for improved, efficient, economical and more versatile systems and processes that involve and can combine endothermic and exothermic reactions. BRIEF DESCRIPTION OF THE DRAWINGS

[006] The attached drawings, which are incorporated into this descriptive report and form part thereof, show certain aspects of the object disclosed in this document and, together with the description, help to explain some of the principles associated with the disclosed implementations. In the drawings:

[007] FIGURE 1 is a schematic illustration of an exemplary system for the conversion of oxygenates where the first input feed includes at least ethanol; and

[008] FIGURE 2 is a schematic illustration of another exemplary system for the conversion of oxygenates where the first input feed includes at least methanol and ethanol.

[009] When practicable, similar reference numbers denote similar structures, features, or elements. SUMMARY

[0010] In certain aspects of the present object, the challenges associated with the conversion of oxygenates may be encountered Petition 870250078935, dated 04 / 09 / 2025, p. 12 / 101 3 / 61 by the inclusion of one or more of the features described in this document or comparable / equivalent approaches as shall be understood by a person normally versed in the state of the art. The aspects of the present object relate to processes and systems for [converting] one or more oxygenates into one or more olefins.

[0011] In some respects, one or more of the following features may be optionally included in any practicable combination.

[0012] Exemplary processes are disclosed for the conversion of one or more oxygenates into one or more olefins. In an exemplary aspect, the process includes introducing a first feedstock at a first end of an adiabatic multistage reactor, wherein the first feedstock includes one or more first oxygenates and one or more first olefins, and the multistage reactor has at least one first reaction stage and one second reaction stage. The first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed.The process also includes placing the first feedstock in contact with the first reactor bed to thereby maintain a first reactor bed temperature within a first temperature range of about 300°C to 550°C and to produce a first reaction mixture, introducing a second feedstock into the multi-stage reactor downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feedstock to produce a first effluent that has a different composition relative to the first reaction mixture, and the second feedstock includes one or more se. Petition 870250078935, dated 04 / 09 / 2025, page 13 / 101 4 / 61 oxygenated seconds. The process also includes placing the first effluent in contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of approximately 300°C to 550°C and thereby produce a second reaction mixture.

[0013] In some respects, the multistage reactor may have a third reaction stage, wherein the third reaction stage has a third reactor bed. In this case, the process may also include the introduction of a third feedstock into the multistage reactor downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture may be mixed with the third feedstock to produce a second effluent which has a different composition relative to the second reaction mixture, and the third feedstock includes one or more oxygenated thirds. The process also includes placing the second effluent in contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and thereby produce a third reaction mixture.

[0014] In some respects, during each reaction stage and between reaction stages, external heat is not added to the multistage reactor. In some respects, during each reaction stage and between reaction stages, heat is not removed from the multistage reactor. In some respects, the first effluent is not removed from the multistage reactor. In some respects, the second effluent is not removed from the multistage reactor. In some respects, heat is not removed from the first reaction mixture before it is mixed with the second inlet feed. In some respects, heat is not removed from the second reaction mixture before it is removed from the multistage reactor or subsequently mixed. Petition 870250078935, dated 04 / 09 / 2025, page 14 / 101 5 / 61 fearfully with the third feed charge. In some respects, heat is not removed from the third reaction mixture before being removed from the multistage reactor or subsequently mixed with a fourth feed charge.

[0015] In some respects, one or more first oxygenates include a predominant first oxygenate, and one or more first olefins include a predominant first olefin, wherein the predominant first oxygenate may be ethanol and the predominant first olefin may be ethylene. In some respects, the ethylene:ethanol molar ratio may be from about 0.25 to 10 in the first feed charge. In some respects, the ethylene:ethanol molar ratio may be from about 0.25 to 5 in the first feed charge. In some respects, the first temperature range may be from about 350°C to 500°C. In some respects, the second temperature range may be from about 350°C to 500°C. In some respects, the third temperature range may be from about 350°C to 500°C.

[0016] In some respects, at least one of the first reactor bed or the second reactor bed may be a fixed bed. In some respects, the third reactor bed may be a fixed bed. In some respects, at least one of the first reactor bed or the second reactor bed may be a fluidized bed. In some respects, the third reactor bed may be a fluidized bed. In some respects, at least one of the first reactor bed or the second reactor bed may be a moving bed. In some respects, the third reactor bed may be a moving bed.

[0017] In some respects, one or more primary oxygenated particles and one or more secondary oxygenated particles may be the same. In some respects, one or more primary oxygenated particles, one or more secondary oxygenated particles, and one or more tertiary oxygenated particles may be the same. In some respects, one or more primary oxygenated particles include one or Petition 870250078935, dated 04 / 09 / 2025, page 15 / 101 6 / 61 plus C2+ alcohols. In some respects, one or more second oxygenated elements include one or more C2+ alcohols. In some respects, one or more third oxygenated elements include one or more C2+ alcohols.

[0018] In some respects, one or more first oxygenates include a predominant first oxygenate, wherein the predominant oxygenate may be ethanol. In some respects, one or more second oxygenates include a predominant second oxygenate, wherein the predominant oxygenate may be ethanol. In some respects, one or more third oxygenates include a predominant third oxygenate, wherein the predominant oxygenate may be ethanol.

[0019] In some aspects, the process may also include the introduction of the second reaction mixture into a single-stage reactor, wherein the single-stage reactor includes one or more catalysts, and the bringing of the second reaction mixture into contact with one or more catalysts to produce an output stream that includes one or more product olefins. Prior to the introduction of the second reaction mixture into the single-stage reactor, the process may include lowering the temperature of the second reaction mixture.

[0020] In some respects, the process may also include introducing the output stream into a separation subsystem to produce a first stream and a second stream.

[0021] In some respects, the second stream may include at least one C3+ olefin. In some respects, the process may also include combining the first stream with one or more first oxygenates to produce the first feedstock. In some respects, the first stream may include a predominant olefin, wherein the predominant olefin may be ethylene.

[0022] In some respects, the process may also include condensing the output stream into a condensed output stream and introducing the condensed output stream into a subsystem. Petition 870250078935, dated 04 / 09 / 2025, page 16 / 101 7 / 61 separation theme to produce a first stream and a second stream. In some aspects, the process may also include combining the first stream with one or more first oxygenates to produce the first feedstock. In some aspects, the first stream may include a predominant olefin, where the predominant olefin may be ethylene. In some aspects, the second stream may include at least one C3+ olefin.

[0023] In some respects, the process may also include the introduction of the third reaction mixture into a single-stage reactor, wherein the single-stage reactor includes one or more catalysts, and the bringing of the third reaction mixture into contact with one or more catalysts to produce an output stream that includes one or more product olefins.

[0024] In some aspects, prior to the introduction of the third reaction mixture into the single-stage reactor, the process may also include lowering the temperature of the third reaction mixture. In some aspects, the process may also include introducing the outlet stream into a separation system to produce a first stream and a second stream. In some aspects, the process may also include combining the first stream with one or more first oxygenates to produce the first feed. In some aspects, the first stream may include a predominant olefin, wherein the predominant olefin may be ethylene. In some aspects, the second stream may include at least one C3+ olefin.

[0025] In some aspects, the process may also include condensing the outlet stream into a condensed outlet stream and introducing the condensed reaction mixture into a separation subsystem to produce a first stream and a second stream. In some aspects, the process may also include Petition 870250078935, dated 04 / 09 / 2025, page 17 / 101 8 / 61 combination of the first stream with one or more first oxygenates to produce the first feedstock. In some respects, the first stream may include a predominant olefin, where the predominant olefin may be ethylene. In some respects, the second stream may include at least one C3+ olefin.

[0026] In some respects, before the introduction of the first inlet stream into the adiabatic multistage reactor, the process may also include the superheating of one or more first oxygenates. In some respects, before the introduction of the second inlet stream into the adiabatic multistage reactor, the process may also include the superheating of one or more second oxygenates. In some respects, before the introduction of the third inlet stream into the adiabatic multistage reactor, the process may also include the superheating of one or more third oxygenates.

[0027] In some respects, the multistage reactor may be at a gauge pressure of 0 to about 30 bar. In some respects, the multistage reactor may be at a weight-hour space velocity (WHSV) of about 0.25 to 15.

[0028] In some respects, at least one of the first reactor bed or the second reactor bed may include a mixture of catalysts. In some respects, the catalyst mixture may include a zeolite and an alcohol dehydration catalyst. In some respects, the third reactor bed may include a mixture of catalysts. In some respects, the catalyst mixture of the third reactor bed may include a zeolite and an alcohol dehydration catalyst.

[0029] In some respects, the second feed charge may be introduced into the adiabatic multistage reactor at a temperature that may be higher than the temperature of the first mix. Petition 870250078935, dated 04 / 09 / 2025, page 18 / 101 9 / 61 of the reaction. In some respects, the third feedstock can be introduced into the adiabatic multistage reactor at a temperature that may be higher than the temperature of the second reaction mixture.

[0030] In some respects, the multistage reactor may include one or more additional reaction stages downstream of the third reaction stage, wherein each of the additional reaction stages has a corresponding reactor bed. In this case, the process may also include the introduction of a subsequent inlet feed into the multistage reactor downstream of the previous reaction stages in such a way that, upon exiting the previous reaction stage, a previous reaction mixture may be mixed with the subsequent inlet feed to produce an additional effluent that has a different composition than the previous reaction mixture, wherein the subsequent inlet feed includes one or more additional oxygenates.The process may also include bringing the previous effluent into contact with the respective reactor bed of one or more additional reaction stages to maintain a temperature of the respective reactor bed within a temperature range of about 300°C to 550°C and thereby produce an additional reaction mixture downstream of the previous reaction stages.

[0031] In some respects, one or more first oxygenates may include ethanol and methanol. In some respects, one or more first olefins may include ethylene, propylene, butene, or any combination thereof.

[0032] In some respects, one or more first oxygenated compounds do not include methanol. In some respects, one or more second oxygenated compounds do not include methanol. In some respects, one or more third oxygenated compounds do not include methanol.

[0033] In another aspect, another process is presented. Petition 870250078935, dated 04 / 09 / 2025, p. 19 / 101 10 / 61 to convert one or more oxygenates into one or more olefins. In some respects, the process involves introducing a first feedstock at a first end of an adiabatic multistage reactor, wherein the first feedstock includes one or more first oxygenates, and one or more first oxygenates include ethanol and at least one of methanol or dimethyl ether, the multistage reactor has at least one first reaction stage and a second reaction stage, wherein the first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed.The process also includes placing the first feedstock in contact with the first reactor bed to thereby maintain a first reactor bed temperature within a first temperature range of about 300°C to 550°C and to produce a first reaction mixture, and introducing a second feedstock into the multi-stage reactor downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feedstock to produce a first effluent that has a different composition relative to the first reaction mixture, wherein the second feedstock includes one or more second oxygenates.The process also includes bringing the first effluent into contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of approximately 300°C to 550°C, thereby producing a second reaction mixture.

[0034] In some respects, the multistage reactor may have a third reaction stage which has a third reactor bed and the process may also include the introduction of a third feedstock into the multistage reactor downstream of the second stage. Petition 870250078935, dated 04 / 09 / 2025, page 20 / 101 11 / 61 of the reaction in such a way that, upon exiting the second reaction stage, the second reaction mixture can be mixed with the third feedstock to produce a second effluent that has a different composition relative to the second reaction mixture, wherein the third feedstock includes one or more third oxygenates. The process may also include bringing the second effluent into contact with the third reactor bed to thereby maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and to produce a third reaction mixture. In some respects, one or more first oxygenates may include ethanol and methanol. In some respects, one or more first oxygenates may include ethanol or dimethyl ether. In such respects, one or more first oxygenates may also include methanol.

[0035] In some respects, one or more second oxygenates may include ethanol, methanol, or a combination thereof. In some respects, one or more second oxygenates do not include methanol.

[0036] In some respects, one or more third oxygenated compounds may include ethanol, methanol, or a combination thereof. In some respects, one or more third oxygenated compounds do not include methanol.

[0037] In another aspect, a system is presented arranged to convert one or more oxygenates into one or more olefins by using the processes described above. In some aspects, the system may include the adiabatic multistage reactor described above.

[0038] In another aspect, a process for the conversion of one or more oxygenates into one or more [olefins] may include an initial feed at one end of the adiabatic multistage reactor assembly, wherein the initial feed Petition 870250078935, dated 04 / 09 / 2025, p. 21 / 101 12 / 61 input may include one or more first oxygenates and at least one or more first olefins and methanol, wherein the multistage reactor set has at least one first reaction stage and one second reaction stage, and the first reaction stage is upstream of the second reaction stage. The first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed.The process also includes placing the first feedstock in contact with the first reactor bed to maintain a first reactor bed temperature within a first temperature range of approximately 300°C to 550°C and thereby produce a first reaction mixture, and introducing a second feedstock into the multi-stage reactor array downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feedstock to produce a first effluent that has a different composition relative to the first reaction mixture. The second feedstock includes one or more second oxygenates.The process also includes bringing the first effluent into contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of approximately 300°C to 550°C, thereby producing a second reaction mixture.

[0039] In some aspects, the multistage reactor set may have a third reaction stage, where the third reaction stage has a third reactor bed. In such aspects, the process may include the introduction of a third inlet feed into the multistage reactor set downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture may be mixed with the third inlet feed to produce a second effluent which may have a Petition 870250078935, dated 04 / 09 / 2025, page 22 / 101 13 / 61 different composition in relation to the second reaction mixture. The third inlet feed may include one or more third oxygenates. The process may also include placing the second effluent in contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and thereby produce a third reaction mixture.

[0040] In some respects, the multistage reactor set may include two or more reactors, wherein the first and second stages may be loaded within the first reactor and the third stage may be run in the second reactor.

[0041] In some aspects, the multistage reactor set may include two or more reactors, wherein the first reactor bed may be positioned in a first reactor and the second reactor bed may be positioned in a second reactor. In such aspects, the third reactor bed may be positioned in a third reactor.

[0042] In some respects, the first feed charge may include one or more first oxygenates, one or more first olefins, and methanol.

[0043] In some respects, the first feed charge may include one or more oxygenated firsts and methanol.

[0044] In some respects, the first intake charge may include one or more first oxygenates and one or more first olefins.

[0045] In some respects, one or more oxygenated seconds in do not include methanol.

[0046] In some respects, one or more oxygenated third parties do not include methanol.

[0047] In some respects, one or more first olefins may Petition 870250078935, dated 04 / 09 / 2025, p. 23 / 101 14 / 61 include one or more recycled olefins, wherein one or more recycled olefins may include ethylene, propylene, butenes, pentenes, or any combination thereof. DETAILED DESCRIPTION

[0048] Certain illustrative aspects will now be described to provide a comprehensive understanding of the principles of structure, function, manufacture, and use of the systems and processes disclosed herein. One or more examples of such aspects are illustrated in the accompanying drawings. Those skilled in the art will understand that the systems and processes specifically described herein and illustrated in the accompanying drawings are illustrative, not limiting, embodiments and that the scope of the present invention is not defined solely by the claims. The features illustrated or described in relation to one illustrative aspect may be combined with the features of other aspects. Such modifications and variations lend themselves to being included within the scope of the present invention.

[0049] The dehydration of alcohols into olefins (e.g., ethanol to ethylene) is particularly challenging in economic terms. This is a significant issue, for example, since the production of ethylene from ethanol is the first step in the production of many of the available volume renewable chemicals (e.g., biocompound-based polyethylene or biocompound-based ethylene), as well as the first step in multiple commercial processes for producing renewable hydrocarbon fuels from ethanol, especially sustainable aviation fuel (SAF). Due to the fact that dehydration reactions consist of multiple highly endothermic reaction stages, very high recycling rates or low feed concentrations are generally required to achieve conversion rates. Petition 870250078935, dated 04 / 09 / 2025, page 24 / 101 15 / 61 are high. All conventional approaches involve very high equipment and energy costs.

[0050] In the present systems and processes described in this document, one or more oxygenates (e.g., C1+ alcohol(s), dimethyl ether, or mixtures thereof) and, optionally, a concomitant olefin feedstock, are converted into a mixture of olefins. The conversion process involves a combination of endothermic alcohol or ether dehydration or ether into olefins followed by a net exothermic oligomerization and cracking of the resulting number of lower carbon olefins into a number of higher carbon olefins.To maximize the potential for heat integration between these reactions and to minimize equipment cost as well as the overall process heat demand, the present systems and processes are designed to control the relative rates of these two reactions to balance the heat released or adsorbed from the overall process by means of the staged addition of one or more oxygenates while the overall process is still running.

[0051] In the present invention, a multi-stage adiabatic reactor is designed to balance the endothermic oxygenate dehydration and the exothermic olefin oligomerization by separating the oxygenate feedstock through multiple stages in an adiabatic reactor in such a way that the endothermic oxygenate dehydration reaction is used to divert the heat generated by the exothermic olefin oligomerization process and to maintain the reactor's internal temperatures within the desired limits through the reactor beds. In this way, the conversion process through the present multi-stage adiabatic reactors therefore occurs in a more consistent temperature profile compared to conventional conversion processes that involve only Petition 870250078935, dated 04 / 09 / 2025, page 25 / 101 16 / 61 a single dose of oxygenates. Furthermore, this heat diversion eliminates the need for interstage removal of reactor material during use, significant recycling of unconverted or partially converted oxygenates, or excessive dilution of the oxygenates charge, which would otherwise be necessary if the oxygenates charge were supplied as a single dose. It should be noted that the reactor contents can be cooled or heated without heat removal or addition by employing a secondary charge at a temperature lower or higher than the reactor contents at that stage.

[0052] In general, the present systems disclosed in this document for converting one or more oxygenates into one or more olefins include an adiabatic multistage reactor having multiple inlets (e.g., at least first and second inlet feeds), at least one first reaction stage and a second reaction stage, where the first reaction stage is upstream of the second reaction stage. The first reaction stage includes a first reactor bed and the second reaction stage includes a second reactor bed. In use, a first inlet feed can be fed at a first end (e.g., an inlet) of the adiabatic multistage reactor and subsequently brought into contact with the first reactor bed to produce a first reaction mixture.A second inlet feed can be introduced into the adiabatic multistage reactor downstream of the first reaction stage, which then mixes with the first reaction mixture to produce a first effluent that has a different composition compared to the first reaction mixture. The first effluent can then subsequently come into contact with the second reactor bed to produce a second reaction mixture. This second reaction mixture can then be passed through the... Petition 870250078935, dated 04 / 09 / 2025, page 26 / 101 17 / 61 reactor outlet, or in other cases to a subsequent reaction stage (e.g., the third reaction stage) of the reactor.

[0053] In some respects, during each reaction stage and between reaction stages, external heat is not added to the adiabatic multistage reactor. The term external heat is the heat that is supplied to the adiabatic multistage reactor that is not otherwise generated by a chemical reaction within the adiabatic multistage reactor nor supplied by any input feed (e.g., the first, second, or third input feed). Alternatively or additionally, during each reaction stage and between reaction stages, heat is not removed from the adiabatic multistage reactor.

[0054] In some respects, the first effluent is not removed from the adiabatic multistage reactor. The compositional combination of the first effluent may include water, oxygenates, and byproducts. Alternatively or additionally, in some respects, the second effluent is not removed from the adiabatic multistage reactor. The compositional combination of the second effluent may include water, oxygenates, olefins, and byproducts (e.g., paraffin and aromatic compounds).

[0055] In some respects, heat is not removed from the first reaction mixture before it is mixed with the second feedstock. Alternatively or additionally, in some respects, heat is not removed from the second reaction mixture before it is removed from the adiabatic multistage reactor or subsequently mixed with a third feedstock.

[0056] The first feedstock includes one or more first oxygenates. For the purposes of the present invention, an oxygenate is a hydrocarbon that contains oxygen as part of its chemical structure. Non-limiting examples of first oxygenates include Petition 870250078935, dated 04 / 09 / 2025, p. 27 / 101 18 / 61 in methanol, ethanol, butanols, pentanols, one or more esters and / or one or more ethers. In some respects, one or more first oxygenates do not include methanol. In some respects, one or more first oxygenates may include the same oxygenate, and in other respects, one or more first oxygenates may include a mixture of different oxygenates. As an example, in some respects, one or more first oxygenates may include a predominant first oxygenate, for example, ethanol. In such respects, one or more first oxygenates may also include one or more other oxygenates, for example, methanol, propanol, one or more esters and / or one or more ethers.As used in this document, a predominant first oxygenate may be present in a higher percentage by weight than any other individual oxygenate in one or more first oxygenates, for example, present in an amount that is at least 25 percent by weight, at least 50 percent by weight, or at least 75 percent by weight of one or more first oxygenates. In some respects, the predominant first oxygenate may be present in an amount of 25 percent by weight to 99 percent by weight of one or more first oxygenates, in an amount of 25 percent by weight to 90 percent by weight of one or more first oxygenates, in an amount of 50 percent by weight to 99 percent by weight of one or more first oxygenates, or in an amount of 75 percent by weight to 99 percent by weight of one or more first oxygenates. It is also contemplated that the first predominant oxygenated element may be present among any of these recited ranges.

[0057] In some respects, one or more first oxygenates may include ethanol and methanol. Alternatively or additionally, one or more first oxygenates may include dimethyl ether. Furthermore, the molar ratio between methanol and ethanol in the first inlet charge Petition 870250078935, dated 04 / 09 / 2025, p. 28 / 101 19 / 61 could be approximately 0.5 to 6, or the molar ratio could be approximately 1 to 5, or the molar ratio could be approximately 2 to 5, or the molar ratio could be approximately 3 to 6, or the molar ratio could be approximately 3 to 5.

[0058] One or more first oxygenates may be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some aspects, the temperature of one or more first oxygenates may be from about 300°C to 550°C or from about 400°C to 500°C. In another aspect, the temperature of one or more first oxygenates may be from about 300°C to 480°C. In another aspect, the temperature of one or more first oxygenates may be from about 480°C to 550°C or from about 450°C to 500°C. It is also contemplated that the temperature of one or more first oxygenates does not fall outside these stated ranges. It is also contemplated that the temperature of one or more first oxygenates may lie between any of these stated ranges.

[0059] The first input charge may also include other materials such as, for example, one or more first olefins. Non-limiting examples of first olefins include ethylene, propylene, butenes, and others. In some respects, one or more first olefins may include the same olefin, and in other respects, one or more first olefins may include a mixture of different olefins. By way of example, in some respects, one or more first olefins may include a predominant first olefin, for example, ethylene. As used herein, a predominant first olefin may be present in a greater percentage by weight than any other individual olefin in one or more first olefins, for example, present in an amount that is at least 25 percent by weight, at least 50 percent by weight, or at least 75 percent by weight of a Petition 870250078935, dated 04 / 09 / 2025, page 29 / 101 20 / 61 or more first olefins. In some respects, the predominant first olefin may be present in an amount of 25 percent by weight to 99 percent by weight of one or more first olefins, in an amount of 25 percent by weight to 90 percent by weight of one or more first olefins, in an amount of 50 percent by weight to 99 percent by weight of one or more first olefins, or in an amount of 75 percent by weight to 99 percent by weight of one or more first olefins. It is also contemplated that the predominant first olefin may be present within any of these recited ranges. In some respects, the first input load may include ethanol and ethylene. For example, the molar ratio of ethylene:ethanol may be about 0.25 to 10 in the first inlet charge, or the molar ratio of ethylene:ethanol may be about 0.25 to 5 in the first inlet charge.

[0060] In some aspects, at least one or more first olefins is provided by means of a recycled olefin within the adiabatic multistage system. Such olefins are referred to herein as a recycled olefin. Non-limiting examples of suitable recycled olefins include ethylene, propylene, butenes, pentenes, or any combination thereof. By way of example, in some aspects at least one or more of the first olefins may include ethylene, alone or in combination with other olefins, for example, one or more C3+ olefins, by means of recycling ethylene produced within the adiabatic multistage reactor and combining it with one or more first oxygenates (e.g., ethanol) to form the first feedstock.In some respects, at least one of one or more first olefins may include a mixture of recycled C2-C4 olefins, whereas in other respects at least one of one or more first olefins may include C2-C5 olefins. Petition 870250078935, dated 04 / 09 / 2025, p. 30 / 101 21 / 61

[0061] The first inlet charge may be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some respects, the temperature of the first inlet charge may be from about 300°C to 550°C or from about 400°C to 500°C. It is also contemplated that the temperature of the first inlet charge does not fall outside these stated ranges. It is also contemplated that the temperature of the first inlet charge may lie between any of these stated ranges.

[0062] In use, the compositional combination of the first feed charge is designed to maintain a first reactor bed temperature within a given temperature range. In some respects, the first temperature range may be approximately 300°C to 550°C. In some respects, the first temperature range may be approximately 300°C to 500°C, approximately 350°C to 500°C, approximately 300°C to 400°C, approximately 350°C to 450°C, approximately 400°C to 460°C, approximately 400°C to 480°C, or approximately 370°C to 480°C. It is also contemplated that the first temperature does not fall outside of these stated ranges. It is also contemplated that the first temperature may lie between any of these stated ranges.

[0063] In addition to the compositional combination of the first feed charge, the temperature of the first reactor bed may also be dependent on at least the compositional combination of the first reactor bed. The first reactor bed may include one or more first catalysts. Thus, in some respects, the first reactor bed may include a single catalyst, while in other respects the first reactor bed includes a mixture of two or more catalysts. It should be noted that the first reactor bed should be designed to avoid excessive conversion of one or more first oxygenates and one or more olefins (e.g., lower carbon content olefins) present within the first feed charge. Petition 870250078935, dated 04 / 09 / 2025, page 31 / 101 22 / 61 feedstock, which must overcool or overheat the first reaction stage, respectively. Thus, the compositional combination of the first reactor bed can be designed based on the desired rate and composition of one or more first olefins relative to the total flow of one or more first oxygenates.

[0064] In some respects, one or more first catalysts include a doped or undoped zeolite catalyst.Non-limiting examples of suitable zeolite catalysts include pentasyl types such as ZSM-5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON having a Si / Al ratio greater than 10; or a dealuminized crystalline silicate of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON having a Si / Al ratio greater than 10; or a phosphorus- and / or boron-modified crystalline silicate of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON having a Si / Al ratio greater than 10; or molecular sieves of the type... Silicoaluminophosphate from the AEL group. Non-limiting examples of suitable zeolite catalyst dopants include phosphorus and / or boron. In some respects, the zeolite catalyst may be a zeolite doped with boron and phosphorus.Additional additives for mixing with doped zeolites include SiO2 supports doped with metal dopants which may include sodium (Na), potassium (K), lithium (Li), beryllium (Be), magnesium (Mg), calcium (Ca), strontium (Sr), barium, radium, iron (Fe), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), iridium (Ir), tungsten (W), copper (Cu), manganese (Mn), vanadium (V), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag), indium (In), or any combination thereof. Petition 870250078935, dated 04 / 09 / 2025, page 32 / 101 23 / 61

[0065] In other respects, one or more first catalysts may also include a specific alcohol or ether dehydration catalyst, for example, solid acids, a doped or undoped alumina, such as zirconia alumina, gamma-alumina, high-purity gamma-alumina, or doped gamma-alumina, or doped or undoped zeolites with limited olefin oligomerization activity (for example, where such zeolite must dehydrate an alcohol into its corresponding olefin with at least 80 molar % selectively under the applied conditions), for example, H-MFI type zeolites with high Si / Al2 ratios (e.g., > 190) or which have been dealuminated, and under certain conditions, Si / Al2 ratios, HFER, H-BEA or HY type zeolites may also be considered as monofunctional dehydration catalysts.

[0066] Exemplary catalyst combinations, physically mixed within the reactor first bed, may include a portion (e.g., a first catalyst of one or more first catalysts) of doped zeolites, such as crystalline silicates of the SM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON having a Si / Al ratio greater than 10, or a dealuminated crystalline silicate of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON having a Si / Al ratio greater than 10, or a phosphorus- and / or boron-modified crystalline silicate of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON which have a Si / Al ratio greater than 10, or silico-aluminophosphate type molecular sieves of the AEL group.The additives for mixing with doped zeolites consist of SiO2 supports doped with metal dopants including iron (Fe), strontium (Sr), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), and iridium. Petition 870250078935, dated 04 / 09 / 2025, page 33 / 101 24 / 61 (Ir), magnesium (Mg), tungsten (W), copper (Cu), manganese (Mn), vanadium (Va), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag), indium (In), or any combination thereof. A second part of the catalyst mixture (for example, a second catalyst for one or more first catalysts) may include a specific alcohol or ether dehydration catalyst as discussed above.

[0067] The first reactor bed can have a variety of structural configurations. For example, in some respects, the first reactor bed is a fixed reactor bed. In some respects, the fixed-bed reactor is an axial-flow fixed-bed reactor. In some respects, the fixed-bed reactor is a radial-flow fixed-bed reactor. In other respects, the first reactor bed is a fluidized bed. In still other respects, the first reactor bed is a moving bed.

[0068] The second feedstock includes one or more second oxygenates, so named because they are the second oxygenates introduced into the reactor in the second stage or reactor bed. Non-limiting examples of second oxygenates include methanol, ethanol, butanols, pentanols, one or more esters and / or one or more ethers. In some respects, one or more second oxygenates do not include methanol. In some respects, one or more second oxygenates may include the same oxygenate, and in other respects one or more second oxygenates may include a mixture of different oxygenates. By way of example, in some respects, one or more second oxygenates may include a predominant second oxygenate, for example, ethanol.As used in this document, a second predominant oxygenate may be present in a higher percentage by weight than any other individual oxygenate in one or more second oxygenates, for example, present in an amount that is at least 25 percent by weight. Petition 870250078935, dated 04 / 09 / 2025, page 34 / 101 25 / 61 at least 50 percent by weight, or at least 75 percent by weight of one or more oxygenated seconds. In some respects, the predominant oxygenated second may be present in an amount of 25 percent by weight to 99 percent by weight of one or more oxygenated seconds, in an amount of 25 percent by weight to 90 percent by weight of one or more oxygenated seconds, in an amount of 50 percent by weight to 99 percent by weight of one or more oxygenated seconds, or in an amount of 75 percent by weight to 99 percent by weight of one or more oxygenated seconds. It is also contemplated that the predominant oxygenated second may be present within any of these recited ranges.

[0069] In general, one or more second oxygenates are the same as one or more first oxygenates in such a way that the total conversion process within the adiabatic multistage reactor includes two or more oxygenate injections, and more specifically a separate oxygenate injection at different reaction stages. This allows the system to control the reactor bed temperatures, thereby maximizing heat integration through the adiabatic multistage reactor. In some respects, the predominant second oxygenate of one or more second oxygenates may include ethanol. In such respects, one or more second oxygenates may also include one or more other oxygenates, for example, methanol, propanols, butanols, pentanols, one or more esters and / or one or more ethers.

[0070] One or more second oxygenators may be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some aspects, the temperature of one or more second oxygenators may be from about 300°C to 550°C or from about 400°C to 500°C. In one aspect, the temperature of one or more second oxygenators may be from about 300°C to 480°C. In Petition 870250078935, dated 04 / 09 / 2025, p. 35 / 101 26 / 61 Another aspect, the temperature of one or more oxygenated seconds may be from approximately 480°C to 550°C or from approximately 450°C to 500°C. It is also contemplated that the temperature of one or more oxygenated seconds does not fall outside these recited ranges. It is also contemplated that the temperature of one or more oxygenated seconds may fall between any of these recited ranges.

[0071] The second feed charge may be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some aspects, the temperature of the second feed charge may be from about 200°C to 550°C, from about 200°C to 500°C, from about 300°C to 500°C, from about 360°C to 400°C, from about 400°C to 500°C, or from about 450°C to 550°C. It is also contemplated that the temperature of one or more second feed charges does not fall outside these stated ranges. It is also contemplated that the temperature of the second feed charge may lie between any of these stated ranges. In some aspects, the second feed charge is introduced into the adiabatic multistage reactor at a temperature that may be higher than the temperature of the first reaction mixture.

[0072] In use, the compositional combination of the second feed charge is designed so as to maintain a second reactor bed temperature within a second temperature range. In some respects, the second temperature range may be from about 300°C to 550°C. In some respects, the second temperature range may be from about 300°C to 500°C, from about 350°C to 500°C, from about 300°C to 400°C, from about 350°C to 450°C, from about 400°C to 480°C, or from about 380°C to 450°C. It is also contemplated that the second temperature does not fall outside these stated ranges. It is also contemplated that the second temperature may lie between any of these stated ranges. Petition 870250078935, dated 04 / 09 / 2025, page 36 / 101 27 / 61

[0073] In addition to the compositional combination of the second feedstock, the temperature of the second reactor bed may also be dependent on at least the compositional combination of a bifunctional catalyst or a specific mixture of catalysts in the second reactor bed. The second reactor bed may include one or more second catalysts. Thus, in some respects, the second reactor bed may include a single catalyst, while in other respects the second reactor bed includes a mixture of two or more types of mono- or bifunctional catalysts. It should be noted that the second reactor bed must be designed to avoid excessive conversion of one or more second oxygenates and one or more second olefins (e.g., lower carbon olefins) present within the first reaction mixture, which excessively cool or overheat the second reaction stage, respectively.Thus, the compositional combination of the second reactor bed can be designed based on the desired rate and composition of one or more second olefins relative to the total flow of one or more second oxygenates.

[0074] In some respects, one or more secondary catalysts include a doped or undoped zeolite catalyst. Non-limiting examples of suitable zeolite catalysts include pentasyl types such as ZSM-5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Si / Al ratio greater than 10; or a dealuminated crystalline silicate from the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Si / Al ratio greater than 10; or a phosphorus- and / or boron-modified crystalline silicate from the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Si / Al ratio greater than 10; or molecular sieves of silica type Petition 870250078935, dated 04 / 09 / 2025, page 37 / 101 28 / 61 AEL group aluminum phosphate. Non-limiting examples of suitable zeolite catalyst dopants include phosphorus and / or boron. Additional additives for mixing with doped zeolites include SiO2 supports doped with metal dopants, which may include sodium (Na), potassium (K), lithium (Li), beryllium (Be), magnesium (Mg), calcium (Ca), strontium (Sr), barium, radium, iron (Fe), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), iridium (Ir), tungsten (W), copper (Cu), manganese (Mn), vanadium (V), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag), and / or indium (In).

[0075] In other respects, one or more second catalysts may also include a specific alcohol or ether dehydration catalyst, for example, solid acids, a doped or undoped alumina, such as zirconia alumina, gamma-alumina, high-purity gamma-alumina, or doped gamma-alumina, or a doped or undoped zeolite with limited olefin oligomerization activity (for example, where such zeolite must dehydrate an alcohol into its corresponding olefin with at least 80 molar % selectively under the applied conditions), for example, H-MFI type zeolites with high Si / Al2 ratios (e.g., > 190) or that have been dealuminated, and under certain conditions the Si / Al2 ratios, H-FER, H-BEA or HY type zeolites may also be considered as monofunctional dehydration catalysts.

[0076] Exemplary catalyst combinations, physically mixed within the second reactor bed, may include a portion (e.g., a first catalyst of one or more second catalysts) of doped zeolites such as crystalline silicates of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, Zsm-48, MTT or TON having a Si / Al ratio Petition 870250078935, dated 04 / 09 / 2025, page 38 / 101 29 / 61 greater than 10, or a dealuminated crystalline silicate of the ZSM5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON that has a Si / Al ratio greater than 10, or a phosphorus- and / or boron-modified crystalline silicate of the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON that has a Si / Al ratio greater than 10, or silico-aluminophosphate type molecular sieves of the AEL group. Additional additives for mixing with doped zeolites consist of SiO2 supports doped with metal dopants that include iron (Fe), strontium (Sr), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), iridium (Ir), magnesium (Mg), tungsten (W), copper (Cu), manganese (Mn), vanadium (V), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag) and / or indium (In).A second part of the catalyst mixture (for example, a second catalyst for one or more first catalysts) may include a specific alcohol or ether dehydration catalyst as discussed above.

[0077] The second reactor bed can have a variety of structural configurations. For example, in some respects, the second reactor bed is a fixed reactor bed. In some respects, the fixed-bed reactor is an axial-flow fixed-bed reactor. In some respects, the fixed-bed reactor is a radial-flow fixed-bed reactor. In other respects, the second reactor bed is a fluidized bed. In still other respects, the second reactor bed is a moving bed.

[0078] In some respects, the adiabatic multistage reactor may include one or more additional reaction stages, each of which has its own reactor bed. For example, the adiabatic multistage reactor may include a third reaction stage that has a third reactor bed. The third reactor bed may Petition 870250078935, dated 04 / 09 / 2025, page 39 / 101 30 / 61 can have a variety of configurations. For example, in some aspects, the third reactor bed is a fixed reactor bed. In some aspects, the fixed-bed reactor is an axial-flow fixed-bed reactor. In some aspects, the fixed-bed reactor is a radial-flow fixed-bed reactor. In other aspects, the third reactor bed is a fluidized bed. In still other aspects, the third reactor bed is a moving bed.

[0079] In use, a third inlet feed is introduced into the adiabatic multistage reactor downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture can be mixed with the third inlet feed to produce a second effluent that has a different composition relative to the second reaction mixture. The second effluent then comes into contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and to thereby produce a third reaction mixture. In some respects, heat is not removed from the third reaction mixture before it is removed from the adiabatic multistage reactor or subsequently mixed with a fourth inlet feed.

[0080] The third feedstock includes one or more third oxygenates, so named because they are the third oxygenates introduced into the reactor at the third stage or reactor bed. Non-limiting examples of third oxygenates include methanol, ethanol, propanols, butanols, pentanols, one or more esters and / or one or more ethers. In some respects, one or more third oxygenates do not include methanol. In some respects, one or more third oxygenates may include the same oxygenate, and in other respects one or more third oxygenates may include a mixture of different oxygenates. As an example, in some respects, Petition 870250078935, dated 04 / 09 / 2025, p. 40 / 101 31 / 61 One or more third oxygenates may include a predominant third oxygenate, for example, ethanol. As used herein, a predominant third oxygenate may be present in a higher percentage by weight than any other individual oxygenate in one or more third oxygenates, for example, present in an amount that is at least 25 percent by weight, at least 50 percent by weight, or at least 75 percent by weight of one or more third oxygenates. In some respects, the predominant third oxygenate may be present in an amount of 25 percent by weight to 99 percent by weight of one or more third oxygenates, in an amount of 25 percent by weight to 90 percent by weight of one or more third oxygenates, in an amount of 50 percent by weight to 99 percent by weight of one or more third oxygenates, or in an amount of 75 percent by weight to 99 percent by weight of one or more third oxygenates.It is also contemplated that the predominant third oxygenated element may be present among any of these recited ranges.

[0081] In general, one or more third oxygenates are the same as one or more first oxygenates and one or more second oxygenates in such a way that the total conversion process within the adiabatic multistage reactor includes two or more oxygenate injections, and more specifically, a separate oxygenate injection at different reaction stages. This also allows the system to control the reactor bed temperatures, thereby maximizing heat integration throughout the adiabatic multistage reactor. In some respects, the predominant third oxygenate of one or more third oxygenates may include ethanol. In such respects, one or more third oxygenates may also include one or more other oxygenates, for example, methanol, propanol, Petition 870250078935, dated 04 / 09 / 2025, page 41 / 101 32 / 61 one or more esters and / or one or more ethers.

[0082] One or more third oxygenates may be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some aspects, the temperature of one or more third oxygenates may be from about 300°C to 550°C or from about 400°C to 500°C. In one aspect, the temperature of one or more third oxygenates may be from about 300°C to 480°C. In another aspect, the temperature of one or more third oxygenates may be from about 480°C to 550°C or from about 450°C to 500°C. It is also contemplated that the temperature of one or more third oxygenates does not fall outside these stated ranges. It is also contemplated that the temperature of one or more third oxygenates may lie between any of these stated ranges.

[0083] The third feed can be introduced into the adiabatic multistage reactor at a variety of temperatures. For example, in some respects, the temperature of the third feed can be from about 200°C to 550°C, from about 200°C to 500°C, or from about 300°C to 500°C. In some respects, the third feed is introduced into the adiabatic multistage reactor at a temperature that may be higher than the temperature of the second reaction mixture.

[0084] In use, the compositional combination of the third feedstock is designed to maintain a third reactor bed temperature within a third temperature range. In some respects, the third temperature range may be from about 300°C to 550°C. In some respects, the third temperature range may be from about 300°C to 500°C, from about 350°C to 500°C, from about 300°C to 400°C, from about 350°C to 450°C, from about 400°C to 460°C, from about 400°C to 480°C, or from about 370°C to 480°C. It is also contemplated that the third temperature does not fall below Petition 870250078935, dated 04 / 09 / 2025, p. 42 / 101 33 / 61 of these recited ranges. It is also contemplated that the second temperature may fall between any of these recited ranges.

[0085] In addition to the compositional combination of the third feedstock, the temperature of the third reactor bed may also be dependent on at least the compositional combination of the third reactor bed. The third reactor bed may include one or more third catalysts (e.g., bifunctional type catalyst(s)). Thus, in some respects, the third reactor bed may include a single catalyst, while in other respects the third reactor bed includes a mixture of two or more catalysts. It should be noted that the third reactor bed should be designed to avoid excessive conversion of one or more oxygenated third catalysts and one or more olefins (e.g., lower carbon olefins) present within the second reaction mixture, which excessively cool or overheat the third reaction stage, respectively.Thus, the compositional combination of the reactor's third bed can be designed based on the desired rate and composition of one or more third olefins relative to the total flow of one or more third oxygenates.

[0086] In some respects, one or more third catalysts include a doped or undoped zeolite catalyst. Non-limiting examples of suitable zeolite catalysts include pentasil types such as ZSM-5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Si / Al ratio greater than 10; or a dealuminated crystalline silicate from the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Si / Al ratio greater than 10; or a phosphorus- and / or boron-modified crystalline silicate from the ZSM-5 group (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT, or TON that have a Petition 870250078935, dated 04 / 09 / 2025, page 43 / 101 34 / 61 Si / Al ratio greater than 10, or molecular sieves of the silicoaluminophosphate type of the AEL group. Non-limiting examples of suitable zeolite catalyst dopants include phosphorus and / or boron. In some respects, the zeolite catalyst may be a zeolite doped with boron and phosphorus. Additional additives for mixing with doped zeolites include SiO2 supports doped with metal dopants which may include sodium (Na), potassium (K), lithium (Li), beryllium (Be), magnesium (Mg), calcium (Ca), strontium (Sr), barium, radium, iron (Fe), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), iridium (Ir), tungsten (W), copper (Cu), manganese (Mn), vanadium (V), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag) and / or indium (In).

[0087] In other respects, one or more third catalysts may also include a specific alcohol or ether dehydration catalyst, for example, solid acids, a doped or undoped alumina, such as zirconia alumina, gamma-alumina, high-purity gamma-alumina, or doped gamma-alumina, or a doped or undoped zeolite with limited olefin oligomerization activity (for example, where such zeolite must dehydrate an alcohol into its corresponding olefin with at least 80 molar percentage selectively under the applied conditions), for example, H-MFI type zeolites with high Si / Al2 ratios (e.g., > 190) or which have been dealuminated, and under certain conditions, Si / Al2 ratios of H-FER, H-BEA or HY type zeolites may also be considered as monofunctional dehydration catalysts.

[0088] Exemplary catalyst combinations, physically mixed within the reactor's third bed, may include a portion (e.g., a first catalyst of one or more third catalysts) of doped zeolites such as crystalline silicates of Petition 870250078935, dated 04 / 09 / 2025, page 44 / 101 35 / 61 group ZSM-5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON having a Si / Al ratio greater than 10, or a dealuminated crystalline silicate of group ZSM5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON having a Si / Al ratio greater than 10, or a phosphorus and / or boron modified crystalline silicate of group ZSM-5 (MFI or BEA structures), CHA, FER, FAU, MWW, ANSR, EUO, MFS, ZSM-48, MTT or TON having a Si / Al ratio greater than 10, or silico-aluminophosphate type molecular sieves of group AEL.Additional additives for mixing with doped zeolites consist of SiO2 supports doped with metal dopants including iron (Fe), strontium (Sr), cobalt (Co), nickel (Ni), lanthanum (La), chromium (Cr), zirconium (Zr), ruthenium (Ru), molybdenum (Mo), iridium (Ir), magnesium (Mg), tungsten (W), copper (Cu), manganese (Mg), vanadium (V), zinc (Zn), titanium (Ti), rhodium (Rh), rhenium (Re), gallium (Ga), palladium (Pd), silver (Ag), and / or indium (In). A second part of the catalyst mixture (e.g., a second catalyst for one or more first catalysts) may include a specific alcohol or ether dehydration catalyst as discussed above.

[0089] As noted above, the adiabatic multistage reactor may contain any number of reaction stages equal to or greater than two in order to obtain a desired outlet composition. In other respects, the multistage reactor includes one or more additional reaction stages downstream of the third reaction stage. Each of the one or more additional reaction stages has a respective reactor bed. In use, a subsequent inlet feed is introduced into the multistage reactor downstream of the previous stage reactors (e.g., first, second, and third reaction stages) in such a way that, upon exiting the stage of Petition 870250078935, dated 04 / 09 / 2025, page 45 / 101 36 / 61 previous reaction (e.g., the third reaction stage), a previous reaction mixture (e.g., a third reaction mixture) is mixed with the subsequent feed to produce an additional effluent that has a different composition from the previous reaction mixture. The subsequent feed may include one or more additional oxygenates. The previous effluent may then come into contact with the respective reactor bed of one or more additional reaction stages to thereby maintain a temperature of the respective reactor bed within a temperature range (e.g., from about 300°C to 550°C) and to produce an additional reaction mixture downstream of the previous reaction stages.

[0090] Although the above discussion of the adiabatic multistage reactor includes all beds in a single adiabatic multistage reactor, this document also contemplates that each reactor bed can be positioned with a separate adiabatic reactor. For example, in some aspects, each of the first, second, and third reactor beds discussed above is positioned in a respective adiabatic reactor. Such an approach should allow the use of movable beds, as well as provide the ability to access and service specifically or replace each bed individually. This document also contemplates implementations where two or more adiabatic reactors include two or more catalyst beds.For example, in some respects, a first adiabatic reactor includes a first reactor bed and a second reactor bed, and a second adiabatic reactor includes a third reactor bed and optionally a fourth reactor bed.

[0091] In examples where there are two or more adiabatic reactors, these reactors may be referred to collectively in this document as a reactor set (e.g., two or more reactors). Petition 870250078935, dated 04 / 09 / 2025, page 46 / 101 37 / 61 multistage adiabatic reactors may be collectively referred to herein as a set of multistage adiabatic reactors. In some respects, a process for converting one or more oxygenates into one or more olefins may include the introduction of a first feedstock at a first end of the multistage adiabatic reactor set, wherein the multistage reactor set has at least one first reaction stage and a second reaction stage, wherein the first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed. The first feedstock may include one or more first oxygenates and at least one of one or more first olefins or methanol.The process may also include placing the first feedstock in contact with the first reactor bed to maintain a first reactor bed temperature within a first temperature range of about 300°C to 550°C and thereby produce a first reaction mixture, and introducing a second feedstock into the multi-stage reactor array downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feedstock to produce a first effluent that has a different composition relative to the first reaction mixture. The second feedstock may include one or more second oxygenates.The process may also include placing the first effluent in contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of approximately 300°C to 550°C, thereby producing a second reaction mixture.

[0092] In some respects, the set of multiple reactors Petition 870250078935, dated 04 / 09 / 2025, page 47 / 101 38 / 61 stages may include a third reaction stage, wherein the third reaction stage has a third reactor bed. In such aspects, the process may also include the introduction of a third inlet feed into the multi-stage reactor system downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture is mixed with the third inlet feed to produce a second effluent that has a different composition relative to the second reaction mixture. The third inlet feed may include one or more oxygenated thirds. The process may also include bringing the second effluent into contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and thereby produce a third reaction mixture.

[0093] In some respects, the multistage reactor set may include two or more reactors, wherein the first and second stages may be loaded within the first reactor and the third stage may be run in the second reactor.

[0094] In some aspects, the multistage reactor set may include two or more reactors, wherein the first reactor bed may be positioned in a first reactor and the second reactor bed may be positioned in a second reactor. In such aspects, the third reactor bed may be positioned in a third reactor.

[0095] In aspects where the adiabatic multistage reactor includes only two reactor beds, the outlet of the adiabatic multistage reactor is the second reaction mixture. The compositional combination of the second reaction mixture may include oxygenates, for example, alcohol(s) and / or ether(s), olefins, for example, C5+ olefins, water, and byproduct(s), for example, saturated. In some aspects Petition 870250078935, dated 04 / 09 / 2025, page 48 / 101 39 / 61 tos, the alcohol(s) includes(s) ethanol, propanols, butanols, and others.

[0096] In aspects where the adiabatic multistage reactor includes three reactor beds, the outlet of the adiabatic multistage reactor is the third reaction mixture. The compositional combination of the third reaction mixture may include oxygenates, for example, alcohol(s) and / or ether(s), olefins, for example, C5+ olefins, water, and byproduct(s), for example, saturated. In some aspects, the alcohol(s) include(s) ethanol, propanols, butanols, and others.

[0097] Present systems for the conversion of oxygenates may include additional elements. For example, present systems may include, in addition to the adiabatic multistage reactor, one or more of the following: a single-stage reactor, one or more heat exchange units, a condenser, a separation subsystem (e.g., a distillation system), one or more furnaces, or any combination thereof. Although not discussed in detail in this document, it should be noted that other elements present within the system are also contemplated in this document.

[0098] In some aspects, the system may include a single-stage reactor comprising a reactor bed having one or more catalysts. In use, the outlet of the adiabatic multi-stage reactor (e.g., the second reaction mixture or the third reaction mixture) may be introduced into a single-stage reactor and brought into contact with one or more catalysts to produce an outlet stream comprising one or more product olefins. One or more product olefins may include C2-C7 olefins, for example, ethylene, propylene, butenes, pentenes, and others, or any combination thereof. In one aspect, one or more product olefins may include at least ethylene. Petition 870250078935, dated 04 / 09 / 2025, page 49 / 101 40 / 61

[0099] In aspects where the adiabatic multistage reactor includes only two reactor beds, before the introduction of the second reaction mixture into the single-stage reactor, the temperature of the second reaction mixture can be lowered. In aspects where the adiabatic multistage reactor includes only three reactor beds, before the introduction of the third reaction mixture into the single-stage reactor, the temperature of the third reaction mixture can be lowered. In either case, this temperature reduction can be achieved, for example, by a heat exchange unit.

[00100] In some aspects, the output stream can be introduced into a separation subsystem to produce a first stream and a second stream. In certain aspects, prior to the introduction of the output stream into the separation subsystem, the output stream can be condensed as a condensed output stream, and the condensed output stream can be introduced into the separation subsystem. The separation subsystem may include a variety of separation units, such as a distillation system, a liquid-liquid separation system, a liquid extraction system, a membrane separation system, and an adsorbent system(s) to perform the separation processes to produce the first and second streams.

[00101] The first stream may include ethylene, propylene, butane(s), or any combination thereof. In one aspect, the first stream may include a predominant olefin, for example, ethylene. As used herein, a predominant olefin may be present in a greater percentage by weight than any other individual olefin in the first stream, for example, present in an amount that is at least 50 percent by weight, at least 75 percent by weight, or at least 95 percent by weight of the olefins within the first stream. In some Petition 870250078935, dated 04 / 09 / 2025, p. 50 / 101 41 / 61 aspects, the predominant olefin may be present in an amount of 25 percent by weight to 99 percent by weight of the olefins within the first stream, in an amount of 25 percent by weight to 90 percent by weight of the olefins within the first stream, in an amount of 35 percent by weight to 90 percent by weight of the olefins within the first stream, in an amount of 40 percent by weight to 90 percent by weight of the olefins within the first stream, in an amount of 45 percent by weight to 90 percent by weight of the olefins within the first stream, in an amount of 50 percent by weight to 99 percent by weight of the olefins within the first stream, in an amount of 55 percent by weight to 99 percent by weight of the olefins within the first stream, in an amount of 60 percent by weight to 99 percent by weight of the olefins within the first stream current,or in an amount of 75 percent by weight to 99 percent by weight of the olefins within the first chain. In some respects, the predominant olefin may be present in an amount of 35 percent by weight to 65 percent by weight of the olefins within the first chain. It is also contemplated that the predominant olefin may be present within any of these recited ranges.

[00102] The second stream may include C3+ olefins, such as at least one C3 to C7 olefin. In addition, in some respects, the second stream may include by-products, such as aromatic(s) and saturated(s).

[00103] In aspects where a recycled olefin is incorporated into the system, the first stream can be combined with one or more first oxygenates to produce the first feed. In some aspects, before the introduction of the first feed stream into the multi-stage adiabatic reactor, one or more first oxygenates can be heated, for example, to a temperature Petition 870250078935, dated 04 / 09 / 2025, p. 51 / 101 42 / 61 from about 200°C to 500°C, from about 200°C to 500°C, from about 375°C to 500°C, from about 360°C to 550°C, or from about 400°C to 500°C. Alternatively or additionally, before the introduction of the second inlet stream into the adiabatic multi-stage reactor, one or more second oxygenates may be heated, for example, to a temperature of about 200°C to 500°C, from about 200°C to 500°C, from about 375°C to 500°C, from about 360°C to 550°C, or from about 400°C to 500°C. Alternatively or additionally, before the introduction of the third inlet stream into the adiabatic multi-stage reactor, one or more second oxygenates may be heated, for example, to a temperature of about 200°C to 500°C, about 200°C to 500°C, about 375°C to 500°C, about 360°C to 550°C, or about 400°C to 500°C.In some respects, one or more first oxygenates, one or more second oxygenates, and / or one or more third oxygenates can be heated by a single heat exchanger, for example, a single furnace. In other respects, one or more first oxygenates, one or more second oxygenates, and / or one or more third oxygenates can be heated by two or more heat exchangers, for example, the respective furnaces.

[00104] In some respects, the adiabatic multistage reactor may be at a weight-hour space velocity (WHSV) of about 0.25 to 15. As used in this document, weight-hour space velocity is defined as the weight of hydrocarbon compounds flowing per hour to the total weight of catalysts in the multistage reactor.

[00105] It should be appreciated that the net thermodynamics of the oxygenate(s) to olefin(s) conversion process depends at least on the identity of the oxygenate, the desired mixture of the olefin product, and the presence of any side reactions. For example, in some respects, especially at higher recycling rates Petition 870250078935, dated 04 / 09 / 2025, page 52 / 101 43 / 61 of lower olefins, the liquid process can be exothermic and heat needs to be removed from the system. This cooling can be accomplished in multiple ways. For example, a heat exchanger can be used to lower the outlet temperature of the adiabatic multistage reactor before subjecting it to a final stage, or stages, of olefin oligomerization and cracking. This heat exchanger can be separate from the adiabatic multistage reactor or integrated within the reactor. The final reaction stage(s) can be carried out in a separate vessel, such as in a single reactor downstream of the adiabatic multistage reactor, or a side stream from the adiabatic multistage reactor can be cooled and then reintroduced into the adiabatic multistage reactor. Another approach would involve lower temperature second and third oxygenate inlet feeds that cool the respective reactor beds.

[00106] In some respects, particularly at low to zero recycling rates of lower olefins or in cases where the initial feedstock includes smaller amounts of methanol or lower olefins, the liquid process may be endothermic and heat must be added to the system. This heating can be accomplished in multiple ways. One approach is to heat one or more first oxygenates above the temperature of the first reactor bed. Some amount of recycling of one or more olefins (e.g., recycling of lower olefin(s)) may be necessary to maintain process temperatures in the initial stage or stages of the adiabatic multistage reactor. Subsequent additions of one or more oxygenates (e.g., one or more second oxygenates and / or one or more third oxygenates) may be heated above the desired maximum temperature for the adiabatic multistage reactor to reach the process temperature. Petition 870250078935, dated 04 / 09 / 2025, p. 53 / 101 44 / 61 total before each reaction stage high enough to continue to simultaneously dehydrate one or more oxygenates and oligomerize the olefins present in the reaction mixtures (e.g., the first reaction mixture, the second reaction mixture, and / or the third reaction mixture). The recycling of lower net olefin can be reduced, in some cases to almost negligible values, by increasing the number of reaction stages, although the selectivity for olefins may be decreased when the olefins are exposed to the catalyst for longer periods of time.

[00107] An exemplary schematic diagram of a system 100 for the conversion of oxygenates is illustrated in FIGURE 1. For simplification purposes only, this exemplary system 100 is discussed with respect to one or more first, second and third oxygenates consisting of ethanol and one or more olefins consisting of ethylene. A person skilled in the art should appreciate that this exemplary system can be used for other oxygenates and olefins, and is therefore not limited to ethanol or ethylene.

[00108] In the illustrated system 100, the system 100 includes an ethanol source 102, an optional heat integration subsystem 104, and an adiabatic multistage reactor 106. Although the adiabatic multistage reactor 106 may have two or more reaction stages, in this illustrated example the adiabatic multistage reactor includes three reaction stages. The first reaction stage includes a first reactor bed 108, the second reaction stage includes a second reactor bed 110, and the third reaction stage includes a third reactor bed 112. Each reactor bed 108, 110, 112 includes one or more catalysts. As will be described in more detail below, in this illustrated system, heated ethanol is fed into the adiabatic multistage reactor 106 in three portions. Although the sub Petition 870250078935, dated 04 / 09 / 2025, page 54 / 101 45 / 61 heat integration system can have a variety of configurations, in this illustrated system the heat integration subsystem includes a preheater that is configured to preheat the ethanol, for example, to a temperature of about 450°C, and a condenser that is configured to condense an output stream (for example, the output stream from the single-stage reactor) as a condensed output stream.

[00109] In use, ethanol 102 is introduced into the preheater (not shown) and heated. A first portion of heated ethanol 102a is then combined with a recycled ethylene stream 114 (e.g., a first stream) to generate a first feed 116, which is then introduced into a first end 118 (e.g., a first inlet) of the adiabatic multistage reactor 106. The first feed 116 then comes into contact with the first reactor bed 108 to maintain a first reactor bed temperature 108 within a first temperature range and thereby produce a first reaction mixture (not shown). The first reactor bed 108 is designed such that the heat produced from the expected exothermic olefin oligomerization is substantially, or even completely, balanced with the heat absorbed by the ethanol dehydration.

[00110] A second portion of the heated ethanol is introduced into the adiabatic multistage reactor 106 as a second inlet feed 102b. Upon exiting the first reaction stage, the first reaction mixture (not shown) is mixed with the second inlet feed 102b within the adiabatic multistage reactor 106 to produce a first effluent (not shown). The first effluent then comes into contact with the second reactor bed 110 to maintain a second reactor bed temperature within a second temperature range and to produce from this Petition 870250078935, dated 04 / 09 / 2025, page 55 / 101 46 / 61 mode a second reaction mixture (not shown). The second reactor bed 110 is designed in such a way that the heat produced from the expected exothermic olefin oligomerization is substantially, or even completely, balanced with the heat absorbed by the dehydration of ethanol to ethylene.

[00111] A third portion of the heated ethanol is introduced into the adiabatic multistage reactor 106 as a third inlet feed 102c. Upon exiting the second reaction stage, the second reaction mixture (not shown) is mixed with the second inlet feed 102c within the adiabatic multistage reactor 106 to produce a second effluent (not shown). The second effluent then comes into contact with the third reactor bed 112 to maintain a second reactor bed temperature 112 within a third temperature range and thereby produce a third reaction mixture 120. The third reactor bed 112 is designed such that the heat produced from the expected exothermic olefin oligomerization is substantially, or completely, balanced with the heat absorbed by the dehydration of ethanol to ethylene.The third reaction mixture 120 then exits the adiabatic multistage reactor 106 at a second end 122 (i.e., an outlet) which is opposite the first end 118. A person skilled in the art should appreciate that the first end 118 and the second end 122 can be placed in various positions in the adiabatic multistage reactor and are therefore not limited to their positions illustrated in FIGURE 1.

[00112] As also shown in FIGURE 1, the system 100 includes a first heat exchanger 124, a single-stage reactor 126, a separation subsystem 128 and a second heat exchanger 130. In use, the third reaction mixture 120 is first introduced into the first heat exchanger 124 in such a way that the temperature Petition 870250078935, dated 04 / 09 / 2025, page 56 / 101 47 / 61 The temperature of the third reaction mixture 120 is reduced. The resulting cooled third reaction mixture 121 is then introduced as feed feed into the single-stage reactor 126. The single-stage reactor 126 includes a reactor bed 32 with one or more catalysts such that at least a portion of the ethylene in the third reaction mixture 120 is converted into higher-carbon olefins (e.g., C3 to C5 olefins). In other words, when the third reaction mixture 120 comes into contact with the reactor bed 132 of the single-stage reactor 126, an output stream 134 is produced. The output stream 134 includes one or more product olefins (e.g., C3 to C5 olefins) and ethylene.

[00113] The output stream 134 can then optionally be introduced first into the condenser of the heat integration subsystem 104. The condensed output stream 136 can then be introduced into the separation subsystem 128 which produces a first stream 138 and a second stream 140 (C3+ olefins). The first stream 138 includes ethylene, and the second stream includes C3-C5 olefins, water and by-products (e.g., aromatic(s) and / or saturated(s)). In the illustrated system, the first stream 138 is then introduced into the second heat exchanger 130 to increase the temperature of the ethylene, then mixed with the ethanol portion 102a to form the first input stream 116.Thus, at the beginning of the process, the first inlet feed 116 includes only the first portion of 102a, but as the process continues, the first stream 138 (e.g., the recycled ethylene produced) is combined with the first portion of ethanol 102a upstream of the multistage reactor 106 in such a way that the first inlet stream 116 then includes a combination of ethanol 102a and the recycled ethylene produced 138.

[00114] In some respects, most ethylene is extracted from Petition 870250078935, dated 04 / 09 / 2025, p. 57 / 101 48 / 61 system, instead of being recycled back into the system, and thus recycled back into the multistage reactor. In this way, in examples where most of the ethylene is extracted from the outflow stream, it may be desirable to heat the first inflow charge, for example, to a temperature of about 450°C, before introducing the ethanol portions into the multistage reactor. The heating of the ethanol can be carried out, for example, in a furnace, an electric heater, or another heat source, which is implemented in the system.

[00115] As noted above, in some respects, the first stream 138 may consist of ethylene (e.g., ethylene is the highest concentration component of the first stream). In other respects, it may be desirable to limit or avoid the separation of olefins. In such respects, the first stream may include a variety of olefin mixtures. For example, in some respects, the first stream may include ethylene and propylene (e.g., ethylene and propylene are the highest concentration components of the first stream). In other respects, the first stream may include C2-C4 olefins (e.g., C2-C4 olefins are the highest concentration components). In still other respects, the first stream may include C2-C5 olefins. In some respects, a portion of the condensed outlet stream may be added to the first stream before being separated by means of the separation subsystem.

[00116] In certain aspects, one or more olefins can be generated directly from C2+ alcohols in a separate reactor using a specific dehydration catalyst and then used as part of the first feed without separately forming unconverted alcohols, generated water, or any co-products.

[00117] In some respects, the reactor may have additional current Petition 870250078935, dated 04 / 09 / 2025, p. 58 / 101 49 / 61 which are introduced into the reactor, wherein the first feed charge may also include methanol and / or dimethyl ether. An exemplary schematic diagram of the ethanol feed and a methanol and / or dimethyl ether feed system for the conversion of oxygenates is illustrated in FIGURE 2. For simplification purposes only, this exemplary system 200 is discussed with respect to two streams that are combined to form the first feed stream that is introduced into the adiabatic reactor. More specifically, the first stream consisting of ethanol and the second stream consisting of methanol and / or dimethyl ether. A person skilled in the art should appreciate that this exemplary system can be used for other oxygenates and olefins and is therefore not limited to methanol, dimethyl ether or ethanol.

[00118] In the illustrated system 200, the system 200 includes a methanol source 201, an optional first heat exchanger 203, an ethanol source 202, an optional heat integration subsystem 204, and an adiabatic multistage reactor 206. Although the adiabatic multistage reactor 206 may have two or more reaction stages, in this illustrated example the adiabatic multistage reactor includes three reaction stages. The first reaction stage includes a first reactor bed 208, the second reaction stage includes a second reactor bed 210, and the third reaction stage includes a third reactor bed 212. Each reactor bed 208, 210, and 212 includes one or more catalysts. As will be described in more detail below, in this illustrated system, heated methanol is fed into the adiabatic multistage reactor 206 in one portion and heated ethanol is fed into the adiabatic multistage reactor 206 in three portions.In other respects, additional portions of heated methanol can be fed into the adiabatic multistage reactor, for example, downstream of the first reactor bed. Although. Petition 870250078935, dated 04 / 09 / 2025, page 59 / 101 50 / 61 The first heat exchanger 203 may have a variety of configurations; in this illustrated system, the first heat exchanger is configured to preheat methanol, for example, to a temperature of about 450°C to 550°C (e.g., about 450°C). Furthermore, although the heat integration subsystem 204 may have a variety of configurations, the second heat integration subsystem includes a preheater that is configured to preheat ethanol, for example, to a temperature of about 450°C, and a condenser that is configured to condense an output stream (e.g., the output stream from the single-stage reactor) as a condensed output stream.

[00119] In use, methanol 201 is introduced into the preheater (not shown) and heated, and ethanol 102 is introduced into the preheater (not shown) and heated. A first portion of heated ethanol 102a is then combined with a heated methanol stream 205 (e.g., a first stream) to generate a first inlet charge 216, which is then introduced at a first end 218 (e.g., a first inlet) of the adiabatic multistage reactor 206. In other respects, the first portion of heated ethanol 202a and the heated methanol stream 205 do not have to be introduced into the adiabatic multistage reactor 106 as a combined stream, but rather as two separate streams.The first feed 216 then comes into contact with the first reactor bed 208 to maintain a first reactor bed temperature 208 within a first temperature range and thereby produce a first reaction mixture (not shown). The first reactor bed 208 is designed in such a way that the heat produced from the exothermic conversion of methanol to dimethyl ether, from the conversion of methanol and dimethyl ether to olefins, and from the expected olefin oligomerization is substantially... Petition 870250078935, dated 04 / 09 / 2025, pages 60 / 101 51 / 61 or completely balanced with the heat absorbed by the dehydration of ethanol.

[00120] A second portion of heated ethanol is introduced into the adiabatic multistage reactor 206 as a second feed 202b. Upon exiting the first reaction stage, the first reaction mixture (not shown) is mixed with the second feed 202b within the adiabatic multistage reactor 206 to produce a first effluent (not shown). The first effluent then comes into contact with the second reactor bed 210 to maintain a second reactor bed temperature within a second temperature range and thereby produce a second reaction mixture (not shown). The second reactor bed 210 is designed such that the heat produced from the exothermic conversion of methanol to dimethyl ether, from the conversion of methanol and dimethyl ether to olefins, and from the expected oligomerization is substantially, or even completely, balanced with the heat absorbed by the dehydration of ethanol to ethylene.

[00121] A third portion of heated ethanol is introduced into the adiabatic multistage reactor 206 as a third inlet feed 202c. Upon exiting the second reaction stage, the second reaction mixture (not shown) is mixed with the second inlet feed 202c within the adiabatic multistage reactor 206 to produce a second effluent (not shown). The second effluent then comes into contact with the third reactor bed 212 to maintain a second reactor bed temperature 212 within a third temperature range and thereby produce a third reaction mixture 220. The third reactor bed 212 is designed such that the heat produced from the expected exothermic olefin oligomerization is substantially, or even completely, balanced with the heat absorbed by the dehydration of ethanol into ethyl Petition 870250078935, dated 04 / 09 / 2025, pages 61 / 101 52 / 61 leno. The third reaction mixture 220 then exits the adiabatic multistage reactor 206 at a second end 222 (e.g., an outlet) which is opposite the first end 218. A person skilled in the art should appreciate that the first end 218 and the second end 222 can be placed in various positions in the adiabatic multistage reactor and are therefore not limited to their positions illustrated in FIGURE 2.

[00122] As also shown in FIGURE 2, the system 200 includes a second heat exchanger 224 and a single-stage reactor 226. In use, the third reaction mixture 220 is first introduced into the second heat exchanger 224 in such a way that the temperature of the third reaction mixture 220 is lowered. The resulting cooled third reaction mixture 221 is then introduced as feed feed into the single-stage reactor 226. The single-stage reactor 226 includes a reactor bed 232 with one or more catalysts so that at least a portion of the ethylene in the third reaction mixture 220 is converted into higher-carbon olefins (e.g., C3 to C5 olefins). In other words, when the third reaction mixture 220 comes into contact with the reactor bed 232 of the single-stage reactor 126, an outlet stream 234 is produced. The outlet stream 134 includes one or more product olefins (e.g., C3 to C5 olefins) and ethylene.

[00123] The output stream 234 can then optionally be introduced first into the condenser of the heat integration subsystem 204. Subsequently, the condensed output stream 236 can be introduced into a separation subsystem. Although not shown, the separation subsystem may be similar to separation subsystem 128. Furthermore, although not shown, a recycled ethanol stream, for example, 114 in FIGURE 1, can be produced in system 200 and introduced into the adiabatic reactor 206 such that Petition 870250078935, dated 04 / 09 / 2025, page 62 / 101 53 / 61 as discussed above with respect to FIGURE 1.

[00124] An exemplary process for converting one or more oxygenates into one or more olefins may include introducing an initial feedstock that includes ethanol, water, and methanol and / or olefin(s) into an adiabatic multistage reactor, where the temperature of the initial feedstock may be from about 400°C to 480°C. In this exemplary process, ethanol may be present in the initial feedstock at about 20 to 25% by weight of the initial feedstock, while methanol, ethylene, or other mixed olefins may be present in the initial feedstock at about 60 to 70% by weight of the initial feedstock, and the remainder of the initial feedstock may consist of water. The temperature of the first reactor bed can be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > temperature of the first reactor bed < 480°C).Once the first reaction mixture is formed, it can be combined with a second inlet charge of ethanol to form a first effluent, where the other portion of the ethanol is at a temperature above about 300°C. The ethanol present in the first effluent comprises about 15 to 30% by weight of the first effluent. Water may optionally be added to the second inlet charge such that the total water in the first effluent does not exceed about 60% by weight. The temperature of the second reactor bed may be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > first reactor bed temperature < 480°C). Once the second reaction mixture is formed, it can be combined with a third inlet charge of ethanol to form a second effluent, where the ethanol is at a temperature above about 300°C.The ethanol present in the second effluent comprises approximately 10 to 25% by weight of the second effluent. The water may be... Petition 870250078935, dated 04 / 09 / 2025, page 63 / 101 Optionally, 54 / 61 is added to the third inlet feed in such a way that the total water in the second effluent does not exceed about 60% by weight. The temperature of the third reactor bed may be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > reactor bed temperature < 480°C). Once the third reaction mixture is formed, it can then exit the adiabatic multistage reactor as an outlet stream.

[00125] In cases where additional downstream reactor beds are present in the multi-stage reactor, the process may also include the following. Once the third reaction mixture is formed, it may be combined with a fourth inlet charge of ethanol to form a third effluent, where the ethanol is at a temperature above about 300°C. The ethanol present in the second effluent comprises about 8 to 22% by weight of the third effluent. Water may optionally be added to the fourth inlet charge such that the total water in the third effluent does not exceed about 60% by weight. The temperature of the fourth reactor bed may be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > temperature of the first reactor bed < 480°C). Once the fourth reaction mixture is formed, it may exit the multi-stage reactor as an exhaust vapor.Optionally, the outlet stream can be cooled through a heat exchanger and fed as a fifth inlet feed into the multistage reactor in a fifth reactor bed at an inlet temperature, for example, of about 350°C to 400°C. Water can optionally be added to the fifth inlet stream in such a way that the total water in the fifth inlet feed does not exceed about 60% by weight.

[00126] Another example process for converting one or Petition 870250078935, dated 04 / 09 / 2025, p. 64 / 101 55 / 61 more oxygenated in one or more olefins may involve the introduction of an initial feedstock that includes ethanol, water, and methanol and / or olefin(s) into an adiabatic multistage reactor, where the temperature of the initial feedstock may be about 400°C to 480°C. In this exemplary process, ethanol may be present in the initial feedstock at about 25 to 30% by weight of the initial feedstock, while methanol, ethylene, or other mixed olefins may be present in the initial feedstock at about 50 to 60% by weight of the initial feedstock, and the remainder of the initial feedstock may consist of water. The temperature of the first reactor bed can be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > temperature of the first reactor bed < 480°C).Once the first reaction mixture is formed, it can be combined with a second inlet charge of ethanol to form a first effluent, where the other portion of the ethanol is at a temperature above 300°C. The ethanol present in the first effluent comprises about 20 to 30% by weight of the first effluent. Water can optionally be added to the second inlet charge such that the total water in the first effluent does not exceed about 50% by weight. The temperature of the second reactor bed can be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > first reactor bed temperature < 480°C). Once the second reaction mixture is formed, it can be combined with a third inlet charge of ethanol to form a second effluent, where the ethanol is at a temperature above about 300°C. The ethanol present in the second effluent comprises approximately 15 to 25% by weight of the second effluent.Water may optionally be added to the third inlet load in such a way that the total water in the second effluent does not exceed approximately 50%. Petition 870250078935, dated 04 / 09 / 2025, p. 65 / 101 56 / 61 by weight. The temperature of the third reactor bed may be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > temperature of the first reactor bed < 480°C). Once the third reaction mixture is formed, it can then exit the adiabatic multistage reactor as an outlet stream.

[00127] In cases where additional downstream reactor beds are present in the multistage reactor, the process may also include the following. Once the third reaction mixture is formed, it may be combined with a fourth inlet charge of ethanol to form a third effluent, where the ethanol is at a temperature above about 300°C. The ethanol present in the second effluent comprises about 15 to 25% by weight of the third effluent. Water may optionally be added to the fourth inlet charge such that the total water in the third effluent does not exceed about 50% by weight. The temperature of the fourth reactor bed may be equal to or greater than about 350°C and equal to or less than about 480°C (350°C > temperature of the first reactor bed < 480°C). Once the fourth reaction mixture is formed, it may exit the multistage reactor as an exhaust vapor.Optionally, the outlet stream can be cooled through a heat exchanger and fed as a fifth inlet feed into the multistage reactor in a fifth reactor bed at an inlet temperature, for example, of about 350°C to 400°C. Water can optionally be added to the fifth inlet stream in such a way that the total water in the fifth inlet feed does not exceed about 60% by weight.

[00128] In any of the exemplary processes described above, in cases where the first inlet stream includes at least one or more primary oxygenates and one or more primary oxygenates Petition 870250078935, dated 04 / 09 / 2025, p. 66 / 101 57 / 61 olefins, the net molar ratio between ethylene and ethanol fed through all reaction stages can be, for example, 1:1. Based on the number of reactor beds within the adiabatic multistage reactor, this molar ratio can increase or decrease. For example, in some aspects where the multistage reactor has more than 5 reactor beds, the net molar ratio between ethylene and ethanol fed through all reaction stages can be, for example, 1:5 or 1:9.

[00129] The terminology used in this document is for the purpose of describing particular modalities and implementations only and is not intended to be limited. For example, as used in this document, the singular forms a, an and the also lend themselves to including the plural forms, unless the context clearly indicates otherwise.

[00130] In the descriptions above and in the claims, expressions such as at least one of or one or more of may occur followed by a conjunctive list of elements or characteristics. The term and / or may also occur in a list of two or more elements or characteristics. Unless otherwise contradicted implicitly or explicitly by the context in which it is used, such a term lends itself to indicating individually either any of the listed elements or characteristics or any of the recited elements or characteristics in combination with any of the other recited elements or characteristics. For example, each of the expressions at least one of A and B; one or more of A and B; and A and / or B lends itself to indicating only A, only B, or A and B together. A similar interpretation is also indicated for lists that include three or more items.For example, each of the expressions at least one of A, B and C; one or more of A, B and C; and A, B and / or C lends itself to indicating only A, only B, only C, A and B, A and C. Petition 870250078935, dated 04 / 09 / 2025, p. 67 / 101 58 / 61 C together, B and C together, or A and B and C together. The use of the term "based on," "above," and "in the claims" lends itself to indicating "based at least in part on," in such a way that an unstated feature or element is also permissible.

[00131] Although the terms first and second may be used in this document to describe various features / elements (including steps), these features / elements should not be limited by these terms unless the context indicates otherwise. These terms may be used to distinguish one feature / element from another feature / element. Thus, a first feature / element discussed below may be referred to as a second feature / element, and similarly, a second feature / element discussed below may be referred to as a first feature / element without deviating from the teachings provided in this document.

[00132] As used in this document in the descriptive report and claims, including as used in the examples and unless expressly specified otherwise, all numbers may be read as if preceded by the expression about or approximately, even if the term does not appear explicitly. The expression about or approximately may be used in the description of magnitude and / or position to indicate that the value and / or position described is within a reasonable expected range of values ​​and / or positions. The expression about or approximately, when immediately preceding a numerical value, refers to a range of plus or minus 10% of that value, for example, about 50 means 45 to 55, about 25,000 means 22,560 to 27,500, etc. In addition, expressions less than about a value or more than about a value should be understood Petition 870250078935, dated 04 / 09 / 2025, pp. 68 / 101 59 / 61 of the definition of the term "about" provided in this document. It should also be understood that when a value is disclosed, less than or equal to the value, greater than or equal to the value, and the possible ranges between values ​​are also disclosed, as appropriately understood by a person skilled in the art. For example, if the value X is disclosed, less than or equal to X, as well as greater than or equal to X (for example, where X is a numeric value) are also disclosed. It should also be understood throughout the patent application that data are provided in a number of different formats, and that this data represent endpoints and starting points, and the ranges for any combination of data points.For example, if a particular data point 10 and a particular data point 15 are disclosed, it should be understood that more than, greater than or equal to, less than, less than or equal to, and equal to 10 and 15 are considered disclosed, as well as between 10 and 15. It should also be understood that each unit between two particular units is also disclosed. For example, if 10 and 15 are disclosed, then 11, 12, 13, and 14 are also disclosed.

[00133] Although several illustrative embodiments are described above, any of a number of changes can be made to various embodiments without departing from the teachings in this document. For example, the order in which various steps of the described method are performed can often be altered in alternative embodiments, and in other alternative embodiments, one or more steps of the method can be skipped at once. Optional features of various device and system embodiments may be included in some embodiments and not in others. Therefore, the above description is provided primarily for illustrative purposes and should not be interpreted as limiting the scope of the re Petition 870250078935, dated 04 / 09 / 2025, p. 69 / 101 60 / 61 claims.

[00134] The examples and illustrations included in this document show, by way of illustration and not limitation, the specific embodiments in which the object may be implemented. As mentioned, other embodiments may be used and derived from them, such that structural and logical substitutions and alterations may be made without departing from the scope of the present invention. Such embodiments of the object of the invention may be indicated in this document both individually and collectively by the term invention merely for convenience and without the intention of willfully limiting the scope of this patent application to any single invention or inventive concept, if more than one is in fact disclosed. Thus, although specific embodiments have been illustrated and described in this document, any arrangement calculated to achieve the same purpose may be substituted in place of the specific embodiments shown.This disclosure is intended to cover any and all adaptations or variations of various embodiments. Combinations of the above embodiments, and other embodiments not specifically described herein, will be apparent to those versed in the prior art upon review of the above description. The use of the expression "based on" in this document and in the claims is intended to indicate "based at least in part on," such that such an unmentioned feature or element is also permissible.

[00135] The object described in this document can be incorporated into systems, devices, methods, and / or items, depending on the desired configuration. The implementations presented in the description above do not represent all implementations consistent with the object described in this document. Instead, they are merely some examples consistent with the related aspects. Petition 870250078935, dated 04 / 09 / 2025, pp. 70 / 101 61 / 61 of the described object. Although some variations are described in detail in this document, other modifications or additions are possible. In particular, other features and / or additional variations may be provided beyond those presented in this document. For example, the implementations described in this document may be directed to various combinations and subcombinations of disclosed features and / or combinations and subcombinations of various other features disclosed in this document. Furthermore, the logical flows described in the attached figures and / or described in this document do not necessarily require the particular order shown, or the sequential order, to achieve the desired results. Other implementations may fall within the scope of the following claims. Petition 870250078935, dated 04 / 09 / 2025, pp. 71 / 101

Claims

1 / 16 CLAIMS 1. Process for converting one or more oxygenates into one or more olefins, characterized in that it comprises: the introduction of a first feedstock at a first end of an adiabatic multistage reactor, wherein the first feedstock comprises one or more first oxygenates and one or more first olefins, wherein the multistage reactor has at least one first reaction stage and a second reaction stage, wherein the first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed; placing the first feedstock in contact with the first reactor bed to maintain a first reactor bed temperature within a first temperature range of about 300°C to 550°C and thereby producing a first reaction mixture;The introduction of a second feed into the multi-stage reactor downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feed to produce a first effluent having a different composition from the first reaction mixture, and the second feed comprises one or more second oxygenates; and the placement of the first effluent in contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of about 300°C to 550°C and thereby produce a second reaction mixture.

2. Process according to claim 1, characterized in Petition 870250078935, dated 04 / 09 / 2025, page 72 / 101 2 / 16, in that the multistage reactor has a third reaction stage, and the third reaction stage has a third reactor bed, and the process also comprises introducing a third inlet feed into the multistage reactor downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture is mixed with the third inlet feed to produce a second effluent that has a different composition relative to the second reaction mixture, and the third inlet feed comprises one or more oxygenated thirds; and placing the second effluent in contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and thereby produce a third reaction mixture.

3. A process according to any one of claims 1 or 2, characterized in that, during each reaction stage and between reaction stages, no external heat is added to the multi-stage reactor.

4. A process according to any one of claims 1 or 2, characterized in that, during each reaction stage and between reaction stages, heat is not removed from the multi-stage reactor.

5. Process according to any one of claims 1 to 4, characterized in that the first effluent is not removed from the multistage reactor.

6. Process according to any one of claims 1 to 5, characterized in that the second effluent is not removed from the multistage reactor.

7. Process in accordance with any of claims 1, 2, 5 and 6, characterized in that heat is not removed from the first reaction mixture before it is mixed with the second input charge.

8. Process according to any one of claims 1, 2, 5, 6 and 7, characterized in that the heat is not removed from the second reaction mixture before being removed from the multistage reactor or subsequently mixed with the third inlet feed.

9. Process according to any one of claims 2, 5, 6, 7 and 8, characterized in that the heat is not removed from the third reaction mixture before being removed from the multistage reactor or subsequently mixed with a fourth inlet charge.

10. Process according to any one of claims 1 to 9, characterized in that one or more first oxygenates comprise a predominant first oxygenate, and one or more first olefins comprise a predominant first olefin, wherein the predominant first oxygenate is ethanol and the predominant first olefin is ethylene.

11. Process according to claim 10, characterized in that the molar ratio of ethylene:ethanol is from about 0.25 to 10 in the first inlet charge.

12. Process according to claim 11, characterized in that the molar ratio of ethylene:ethanol is from about 0.25 to 5 in the first inlet charge.

13. Process according to any one of claims 1 to 12, characterized in that the first temperature range is from about 350°C to 500°C.

14. Process according to any one of claims 1 to 13, characterized in that the second temperature range is about 350°C to 500°C.

15. Process according to any one of claims 2 to 14, characterized in that the third temperature range is from about 350°C to 500°C.

16. Process according to any one of claims 1 to 15, characterized in that at least one of the first reactor bed or the second reactor bed is a fixed bed.

17. Process according to any one of claims 2 to 16, characterized in that the third bed of the reactor is a fixed bed.

18. Process according to any one of claims 1 to 15, characterized in that at least one of the first reactor bed or the second reactor bed is a fluidized bed.

19. Process according to any one of claims 2 to 15, characterized in that the third bed of the reactor is a fluidized bed.

20. A process according to any one of claims 1 to 15, characterized in that at least one of the first reactor bed or the second reactor bed is a moving bed.

21. Process according to any one of claims 2 to 15, characterized in that the third bed of the reactor is a moving bed.

22. Process according to any one of claims 1 to 21, characterized in that one or more first oxygenates and one or more second oxygenates are the same.

23. Process according to any one of claims 2 to 22, characterized in that one or more first oxygenates, one or more second oxygenates and one or more third oxygenates are the same. Petition 870250078935, dated 04 / 09 / 2025, p. 75 / 101 5 / 16 24. Process according to any one of claims 1 to 23, characterized in that one or more first oxygenates comprise one or more C2+ alcohols.

25. Process according to any one of claims 1 to 24, characterized in that one or more second oxygenates comprise one or more C2+ alcohols.

26. Process according to any one of claims 2 to 25, characterized in that one or more oxygenated third parties comprise one or more C2+ alcohols.

27. A process according to any one of claims 1 to 26, characterized in that one or more first oxygenates comprise a predominant first oxygenate, wherein the predominant oxygenate is ethanol.

28. A process according to any one of claims 1 to 27, characterized in that one or more second oxygenates comprise a second predominant oxygenate, wherein the predominant oxygenate is ethanol.

29. A process according to any one of claims 2 to 28, characterized in that one or more third oxygenates comprise a predominant third oxygenate, wherein the predominant oxygenate is ethanol.

30. Process according to any one of claims 1, 3 to 22, 24, 25, 27 and 28, characterized in that it further comprises introducing the second reaction mixture into a single-stage reactor, wherein the single-stage reactor comprises one or more catalysts, and bringing the second reaction mixture into contact with one or more catalysts to produce an output stream comprising one or more product olefins.

31. Process according to claim 30, characterized in that it further comprises, before the introduction of the second reaction mixture in the single-stage reactor, lowering the temperature of the second reaction mixture.

32. A process according to any one of claims 30 or 31, characterized in that it further comprises introducing the output stream into a separation subsystem to produce a first stream and a second stream.

33. Process according to claim 31, characterized in that the second stream comprises at least one C3+ olefin.

34. Process according to claim 33, characterized in that the first stream is combined with one or more first oxygenates to produce the first inlet charge.

35. Process according to any one of claims 32 to 34, characterized in that the first stream comprises a predominant olefin, wherein the predominant olefin is ethylene.

36. A process according to any one of claims 30 or 31, characterized in that it further comprises condensing the output stream into a condensed output stream and introducing the condensed output stream into a separation subsystem to produce a first stream and a second stream.

37. Process according to claim 36, characterized in that the first stream is combined with one or more first oxygenates to produce the first inlet charge.

38. Process according to any one of claims 36 or 37, characterized in that the first stream comprises a predominant olefin, wherein the predominant olefin is ethylene.

39. Process in accordance with any of the claims 36 to 38, characterized in that the second stream comprises at least one C3+ olefin. Petition 870250078935, dated 04 / 09 / 2025, page 77 / 101 7 / 16 40. A process according to any one of claims 2 to 29, characterized in that it further comprises introducing the third reaction mixture into a single-stage reactor, wherein the single-stage reactor comprises one or more catalysts, and bringing the third reaction mixture into contact with one or more catalysts to produce an output stream comprising one or more product olefins.

41. Process according to claim 40, characterized in that it further comprises, before the introduction of the third reaction mixture into the single-stage reactor, lowering the temperature of the third reaction mixture.

42. Process according to any one of claims 40 or 41, characterized in that it further comprises introducing the output stream into a separation system to produce a first stream and a second stream.

43. Process according to claim 34, characterized in that the first stream is combined with one or more first oxygenates to produce the first inlet charge.

44. Process according to any one of claims 42 or 43, characterized in that the first stream comprises a predominant olefin, wherein the predominant olefin is ethylene.

45. Process according to any one of claims 42 to 44, characterized in that the second stream comprises at least one C3+ olefin.

46. ​​Process according to any one of claims 40 or 41, characterized in that it further comprises condensing the output stream into a condensed output stream and introducing the condensed reaction mixture into a separation subsystem to produce a first stream and a second stream.

47. Process according to claim 47, characterized in that the first stream is combined with one or more first oxygenates to produce the first inlet charge.

48. Process according to any one of claims 46 or 47, characterized in that the first stream comprises a predominant olefin, wherein the predominant olefin is ethylene.

49. Process according to any one of claims 46 to 48, characterized in that the second stream comprises at least one C3+ olefin.

50. Process according to any one of claims 1 to 49, characterized in that it further comprises, before the introduction of the first inlet stream into the adiabatic multistage reactor, the heating of one or more first oxygenates.

51. A process according to any one of claims 1 to 50, characterized in that it further comprises, before the introduction of the second inlet stream into the adiabatic multistage reactor, the heating of one or more oxygenated seconds.

52. A process according to any one of claims 2 to 51, characterized in that it further comprises, before the introduction of the third inlet stream into the adiabatic multistage reactor, the heating of one or more third oxygenates.

53. Process according to any one of claims 1 to 52, characterized in that the multiple reactor is Petition 870250078935, dated 04 / 09 / 2025, page 79 / 101 9 / 16 gios at a gauge pressure of 0 to about 30 bar.

54. Process according to any one of claims 1 to 53, characterized in that the multistage reactor has a weight-hour space velocity (WHSV) of about 0.25 to 15.

55. Process according to any one of claims 1 to 54, characterized in that at least one of the first reactor bed or the second reactor bed comprises a mixture of catalysts.

56. Process according to claim 55, characterized in that the catalyst mixture comprises a zeolite and an alcohol dehydration catalyst.

57. Process according to any one of claims 2 to 56, characterized in that the third reactor bed comprises a mixture of catalysts.

58. Process according to claim 57, characterized in that the catalyst mixture of the reactor's third bed comprises a zeolite and an alcohol dehydration catalyst.

59. Process according to any one of claims 1 to 58, characterized in that the second inlet charge is introduced into the adiabatic multistage reactor at a temperature that is higher than the temperature of the first reaction mixture.

60. Process according to any one of claims 2 to 58, characterized in that the third inlet charge is introduced into the adiabatic multistage reactor at a temperature that is higher than the temperature of the second reaction mixture.

61. Process according to any of the claims 2 to 60, characterized in that the multistage reactor comprises one or more additional reaction stages downstream of the third reaction stage, wherein each of the one or more additional reaction stages has a respective reactor bed, and the process further comprises the introduction of a subsequent inlet feed downstream of the previous multistage reactor reaction stages in such a way that, upon exiting the previous reaction stage, a previous reaction mixture is mixed with the subsequent inlet feed to produce an additional effluent having a different composition than the previous reaction mixture, wherein the subsequent inlet feed comprises one or more additional oxygenates;and the placement of the preceding effluent in contact with the respective reactor bed of one or more additional reaction stages to maintain a temperature of the respective reactor bed within a temperature range of about 300°C to 550°C and to thereby produce an additional reaction mixture downstream of the preceding reaction stages.

62. Process according to any of the preceding claims, characterized in that one or more first oxygenates comprise ethanol and methanol.

63. Process according to any one of claims 1 to 9, 13 and 34, 36, 37, 39 to 43, 45 to 47, and 49 to 62, characterized in that one or more first olefins comprise ethylene, propylene, butene, or any combination thereof.

64. Process according to any one of claims 1 to 61 and 63, characterized in that one or more of the first oxygenates do not comprise methanol.

65. Process according to any of the preceding claims, characterized in that one or more of the oxygenated compounds do not comprise methanol. Petition 870250078935, dated 04 / 09 / 2025, page 81 / 101 11 / 16 66. A process according to any of the preceding claims, characterized in that one or more oxygenated third parties do not comprise methanol.

67. Process for converting one or more oxygenates into one or more olefins, wherein the process is characterized in that it comprises: the introduction of a first feedstock at a first end of an adiabatic multistage reactor, wherein the first feedstock comprises one or more first oxygenates, wherein one or more first oxygenates comprise ethanol and at least one of methanol or dimethyl ether, the multistage reactor having at least one first reaction stage and a second reaction stage, wherein the first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed;the placement of the first feed in contact with the first reactor bed to maintain a first reactor bed temperature within a first temperature range of about 300°C to 550°C and thereby produce a first reaction mixture; the introduction of a second feed into the multistage reactor downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feed to produce a first effluent which has a different composition from the first reaction mixture, wherein the second feed comprises one or more second oxygenates;and placing the first effluent in contact with the second effluent of the reactor bed to maintain a second temperature of the second reactor bed within a second temperature range of approximately 300°C to 550°C and thereby produce a second reaction mixture.

68. Process according to claim 67, characterized in that the multistage reactor has a third reaction stage, wherein the third reaction stage has a third reactor bed, and the process further comprises introducing a third inlet feed into the multistage reactor downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture is mixed with the third inlet feed to produce a second effluent having a different composition relative to the second reaction mixture, wherein the third inlet feed comprises one or more oxygenated thirds; and placing the second effluent in contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of about 300°C to 550°C and thereby producing a third reaction mixture.

69. Process according to any one of claims 67 or 68, characterized in that one or more first oxygenates comprise ethanol and methanol.

70. Process according to any one of claims 67 or 68, characterized in that one or more first oxygenates comprise ethanol or dimethyl ether.

71. Process according to claim 70, characterized in that one or more first oxygenates also comprise methanol.

72. Process in accordance with any of the claims in Petition 870250078935, dated 04 / 09 / 2025, pages 83 / 101 13 / 16, characterized in that one or more second oxygenates comprise ethanol, methanol, or a combination thereof.

73. Process according to any one of claims 67 to 72, characterized in that one or more secondary oxygenates do not comprise methanol.

74. Process according to any one of claims 67 to 73, characterized in that one or more oxygenated third parties comprise ethanol, methanol, or a combination thereof.

75. Process according to any one of claims 67 74, characterized in that one or more oxygenated third parties do not comprise methanol.

76. System, characterized in that it comprises the adiabatic multistage reactor of any one of claims 1 to 75.

77. Process for converting one or more oxygenates into one or more olefins, characterized in that it comprises: the introduction of a first feedstock at one end of a multi-stage adiabatic reactor assembly, wherein the first feedstock comprises one or more first oxygenates and at least one or more first olefins and methanol, wherein the multi-stage reactor assembly has at least one first reaction stage and a second reaction stage, wherein the first reaction stage is upstream of the second reaction stage, and the first reaction stage has a first reactor bed, and the second reaction stage has a second reactor bed; placing the first feedstock in contact with the first reactor bed to maintain a first temperature of the primary Petition 870250078935, dated 04 / 09 / 2025, p.84 / 101 14 / 16 first reactor bed within a first temperature range of about 300°C to 550°C and thereby produce a first reaction mixture; the introduction of a second feed into the multi-stage reactor set downstream of the first reaction stage in such a way that, upon exiting the first reaction stage, the first reaction mixture is mixed with the second feed to produce a first effluent having a different composition from the first reaction mixture, wherein the second feed comprises one or more second oxygenates; and placing the first effluent in contact with the second reactor bed to maintain a second reactor bed temperature within a second temperature range of about 300°C to 550°C and thereby produce a second reaction mixture.

78. Process according to claim 77, characterized in that the multi-stage reactor assembly has a third reaction stage, wherein the third reaction stage has a third reactor bed, and the process further comprises introducing a third inlet feed into the multi-stage reactor assembly downstream of the second reaction stage in such a way that, upon exiting the second reaction stage, the second reaction mixture is mixed with the third inlet feed to produce a second effluent having a different composition relative to the second reaction mixture, wherein the third inlet feed comprises one or more oxygenated thirds; and placing the second effluent in contact with the third reactor bed to maintain a third reactor bed temperature within a third temperature range of approximately Petition 870250078935, dated 04 / 09 / 2025, p.85 / 101 15 / 16 300°C to 550°C and thus produce a third reaction mixture.

79. A process according to any one of claims 77 or 78, characterized in that the multi-stage reactor assembly includes two or more reactors, wherein the first and second stages are loaded into the first reactor and the third stage is loaded into the second reactor.

80. Process according to any one of claims 77 or 78, characterized in that the multi-stage reactor assembly includes two or more reactors, wherein the first reactor bed is positioned in a first reactor and the second reactor bed is positioned in a second reactor.

81. Process according to claim 80, characterized in that the third reactor bed is positioned in a third reactor.

82. Process according to any one of claims 77 to 81, characterized in that the first feedstock comprises one or more first oxygenates, one or more first olefins, and methanol.

83. Process according to any one of claims 77 to 81, characterized in that the first feedstock comprises one or more oxygenates and methanol.

84. Process according to any one of claims 77 to 81, characterized in that the first feedstock comprises one or more first oxygenates and one or more first olefins.

85. Process according to any one of claims 77 to 84, characterized in that one or more secondary oxygenates do not comprise methanol.

86. Process in accordance with any of the claims Petition 870250078935, dated 04 / 09 / 2025, pp. 86 / 101 16 / 16 tions 78 to 85, characterized by the fact that one or more oxygenated third parties do not comprise methanol.

87. Process according to any of the preceding claims, characterized in that one or more first olefins comprise one or more recycled olefins, wherein one or more recycled olefins comprise ethylene, propylene, butenes, pentenes, or any combination thereof. Petition 870250078935, dated 04 / 09 / 2025, p. 87 / 101

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