TW575559B - High pressure separation of dimethyl ether from an olefin stream - Google Patents

Description

575559 Α7 Β7 V. Description of the Invention (i) Field of the Invention = The present invention relates to a method for removing charged oxidation pollutants from an olefin stream. In particular, the present invention relates to a method for removing dimethyl ether from a stream containing ethylene and / or propylene.

BACKGROUND OF THE INVENTION Z olefins, especially (2 and C3 olefins), are suitable feed sources for the manufacture of derivative products such as oligomers (eg, higher olefins) and polymers such as polyethylene and polypropylene. Olefin feed Sources have traditionally been produced by cracking petroleum feedstocks. US 5,090,977 discloses a method for the production of olefins by continuous cracking. The method includes dividing the olefin product into methane, hydrogen, ethane, ethylene, propylene, and C 5 + streams. Revealed The separation action preferentially produces propylene, and no propane, butane, butene or butadiene streams are produced. In any case, oxygenated feedstocks are becoming an option for the production of olefins from petroleum feedstocks, especially large quantities of ethylene and propylene. For higher carbon number olefins and plasticized raw materials. Generally, olefins are formed by contacting oxygenated components with molecular sieve catalysts to catalyze the conversion of oxygenated compounds to olefins. For example, US 4,499,3 27 discloses A method for producing olefins from methanol using any type of silicoaluminophosphate (SAPO) molecular sieve catalyst. The method is at a temperature between 300 ° C and 500 ° C and pressure It is carried out at 0.1 atmosphere pressure and 100 atmosphere pressure and weight space-time velocity (WHS V between 0.1 and 40hr). This method is highly selective for the production of ethylene and propylene. US 6,121,504 also discloses a catalyst using molecular sieve The paper size made from oxygen-filled paper is applicable to China's National Standard (CNS) A4 specification (210X 297 mm) '" ~~~ 一 (Please read the precautions on the back before filling this page) Today, 1T Ministry of Economy Wisdom Printed by the Consumer Cooperative of the Property Bureau 575559 A7 B7 V. Description of the invention (2) (Please read the precautions on the back before filling this page) Method for producing olefin products. Water and other unwanted by-products are produced by quenching with It is removed from the olefin product by contact. After contact with the quenching medium, a light product fraction is obtained, which includes the desired olefin, but also includes dimethyl ether, methane, C0, C02, ethane, propane And other minor ingredients, such as water and unreacted oxygenated feedstocks. To further process olefins, it is often necessary to reduce or remove undesirable by-products present in the olefin composition. For example, US 4,474,647 discloses two Ethers may have an adverse effect on the oligomerization of certain olefins. This patent describes a method for removing dimethyl ether from a C% and / or C5 olefin stream by distillation. The stream is distilled and divided into overhead And bottoms streams. The overhead stream contains dimethyl ether, water, and various hydrocarbons, and the bottoms stream contains purified olefins. US 5,9 1 4, 4 3 3 discloses a method for producing an olefin composition. And a system for removing non-olefin by-products such as C00. The dehydrated olefin composition is washed with caustic soda to remove C02, and the washed olefin composition is dried to reduce the added water This is the result of washing with caustic. US 5,720,929 printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economics discloses a method that includes making isobutene from isobutane. Isobutylene is cooled and water is stripped from the product. Extra water was removed by washing the product with methanol.

Eng et a 1. , " Integration of the UOP / HYDRO MTO Process into Ethylene Plants / 5 10th Ethylene Producers5 Conference, 1 998, discloses a process for producing olefin compositions from methanol. This scheme shows a scheme for distilling off ethane first. EP-B 1-0060 103 discloses a methanol washing system that applies the Chinese National Standard (CMS) A4 specification (210X 297 mm) to the paper containing vinyl paper. 575559 B7 5. Description of the invention (3) and the vapor stream of propylene Method for extracting dimethyl ether. Methanol scrubbing removes significant amounts of dimethyl ether, but also removes significant amounts of ethylene and propylene. (Please read the Weeping Matters on the back before filling out this page.) Find additional ways to remove unwanted components from the olefin stream. In particular, it is important to find an invention that will remove oxidized hydrocarbons (especially dimethyl ether) and reduce the CO and water in the olefin product stream to ppm levels without removing significant amounts of bar hydrocarbons. In the present invention, dimethyl ether is separated from the olefin stream containing ethylene and / or propylene using high pressure separation, preferably high pressure distillation. In one embodiment, the present invention provides a method for separating dimethyl ether from an olefin stream, the method comprising providing an olefin stream comprising ethylene, ethane, propylene, propane, and dimethyl ether. The supplied stream is divided into a first part and a second part at a pressure of at least 200 psig (l, 480 kPa absolute). The first part contains at least most of the ethylene and propylene present in the hydrocarbon burn stream, and the second part contains at least most of the dimethyl ether present in the olefin stream. In another specific example, the provided olefin stream further comprises water in an amount not greater than about 15,000 wppm. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economics The present invention is particularly effective for olefin streams containing at least about 500 w p p m dimethyl ether. Preferably, the olefin stream comprises no more than about 50% by weight of dimethyl ether. In a specific example, the separation is such that the first portion contains at least most of the propane present in the olefin stream, and preferably no greater than about 1000 wppm of dimethyl ether. Separation. The effect can be that a large amount of propane present in the olefin stream can be in the first or second part. Separation can also result in the presence of a large amount of propane in the olefin stream; C may be in the first or second part. In order to obtain the paper standard from the olefin stream, the Chinese national standard ϋN-S) A4 specification mm) 1 ~-575559 A7 B7 V. Description of the invention (4) High-purity propylene stream Any amount of allene and propane in the olefin feed can be separated in the second part. In another specific example, the olefin stream is divided into a first portion and a second portion in a distillation column. Preferably, a water absorbent is added to the distillation column. The water absorbent can be added to the distillation column at a molar ratio of the water absorbent to the total olefin stream from about 4: 1 to about 1: 5,000. In another embodiment of the present invention, the first portion is treated with an acid gas. The acid gas-treated stream can then be washed with water and contacted with a solid adsorbent. The ethylene and propylene separated from the olefin stream can be used for any ethylene or propylene derivative processing due to the high quality of the recovered stream. Preferred specific examples include polymerization into polyethylene and polypropylene. In a specific example, the present invention provides a method for separating dimethyl ether from an olefin stream, the method comprising contacting an oxygenate with a molecular sieve catalyst to form an olefin stream, wherein the olefin stream comprises ethylene, ethane, propylene, propane And dimethyl ether. The olefin stream is divided into the first and second sections at a pressure of at least 200 psig (l, 480 kPa absolute). The first part contains at least most of the ethylene and propylene present in the olefin stream, and the second part contains at least most of the dimethyl ether present in the olefin stream. In a specific example of the present invention, the olefin stream formed by contacting an oxygenate with a molecular sieve catalyst is contacted with a water absorbent before being divided into the first and second parts. The water absorbent is contacted with the olefin stream at a molar ratio of water absorbent to total olefins of from about 1: 2 to about 1: 200. Preferably, contact with water absorbent This paper size is applicable + national and national standards YCNS) A4 specification (210X297 mm) '~~~ (Please read the precautions on the back before filling this page). Participants, 11 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 575559 A7 B7 V. Description of the invention (5) The olefin stream contains water not greater than about 15,000 w p p m. (Please read the notes on the back before filling this page) The present invention also provides a method for separating dimethyl ether from an olefinic smoke stream, which method comprises contacting an oxygenate with a molecular sieve catalyst to form an olefin stream, wherein the olefin stream Contains ethylene, ethane, propylene, propane, dimethyl ether and water. The water is then removed from the olefin stream so that the olefin stream contains no more than about 15,000 w p p ni. Thereafter, the olefin stream containing no more than about 15,000 wppm water is divided into a first part and a second part at a pressure of at least 200 psig (1,4 80 kPa), wherein the first part contains at least Most of ethylene and propylene. , And the second part contains at least most of the dimethyl ether present in the olefin stream. The invention further provides a method for stripping dimethyl ether from an olefin stream, the method comprising providing an olefin stream comprising ethylene, ethane, propylene, propane, propadiene and dimethyl ether. The olefin stream is divided into a first portion 'containing at least most of the ethylene and propylene present in the olefin stream and a second portion containing at least most of the dimethyl ether and propadiene present in the olefin stream. Separation is performed at a pressure of at least 200 psig (1,480 kPa absolute), and the temperature of the second part is not greater than about 121 ° C ° Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs The attached drawings illustrate various specific examples of the present invention, in which: FIG. 1 is a flow chart showing a method for reacting methanol to form an olefin. The olefin is divided into a first part containing ethylene and propylene, and The second part of the ether and Co hydrocarbon components. -8- This paper size is in accordance with Chinese National Standard (CNS) A4 (210X297 mm) 575559 Μ B7___ V. Description of the invention (6) Figure 2 is a flow chart showing caustic washing solution, water and adsorption Processing of ethylene and propylene. (Please read the precautions on the back before filling this page) Component comparison table 100: Conveyor pipe 102: Reactor 104: Conveyor pipe 106: Quench tower 108: Conveyor pipe 110: Conveyor pipe 112: Conveyor pipe 114: Compressor 1 1 6: Conveying pipe 11 8: Absorption pipe column 120: Conveying pipe 122: Conveying pipe 124: Conveying pipe 125: Conveying pipe 126: Distillation pipe column 128: Conveying pipe 130: Conveying pipe 200: Caustic decontamination pipe column 202: Conveying pipe 204: Conveying pipe 206: Conveying pipe 208: Water washing column 210: Conveying pipe 212: Conveying pipe 214: Conveying pipe 21 6: Dryer 218: Conveyor pipe DETAILED DESCRIPTION OF THE INVENTION The present invention provides a method for removing an oxidized hydrocarbon component (eg, dimethicone) from an olefin stream. Such components are intended to be removed because they poison the catalyst used to further process the hydrocarbon burn in the olefin stream. The present invention is particularly advantageous for removing dimethyl ether from the logistics of dioxin and / or propylene, so that B ---- ^ 575575 A7 B7 printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs 7) Shaoxi and / or propylene can be polymerized without poisoning the catalyst used for the polymerization reaction. In the present invention, the oxidized pollutants, particularly dimethyl ether, are removed from the provided olefin stream at high pressure. The advantage of using high pressure separation is that olefins can be separated at higher temperatures. In terms of the advantages of higher temperature separations, less cooling is required to recover light olefins such as ethylene and propylene. The net effect is substantial energy savings. Another advantage of high-pressure separation is that inclusion complexes and free water structures are easier to control in the separation plant. This is particularly advantageous when a distillation column with an inner fractionation tray serves as a separation device, as the inner fractionation tray is apt to collect water and inclusions. If excess water and / or clathrates are collected, the fractionation trays may be broken or disintegrated, causing severe equipment damage. Generally, the process of the present invention includes providing an olefin stream containing ethylene, ethane, propylene, propane, and dimethyl ether, followed by separating the dimethyl ether present in at least a majority (i.e., greater than 50%) of the olefin stream. The olefin stream can come from any conventional source. However, the present invention is particularly effective for separating dimethyl ether from an olefin stream in the production of olefins from free oxygenates. In a specific example, the provided olefin stream includes not more than about 50% by weight of dimethyl ether, preferably not more than about 20% by weight of dimethyl ether, and more preferably not more than about 10% by weight of dimethyl ether. Ether, and most preferably no more than about 5 weight percent dimethyl ether. Of course, for dimethyl ether to be removed from the olefin stream, some measurable amount must be present. Desirably, dimethyl ether is preferably at least about 50 wppn], and more preferably at least about 1,000 wppm. In another specific example, the provided olefin stream includes at least about 25 weight percent ethylene. Preferably, the provided olefin stream includes from about 25% by weight of B (please read the notes on the back before filling this page) This paper size is applicable to China National Standard (CNS) A4 specification (210X297 mm) _ 575559 DESCRIPTION OF THE INVENTION (8) Alkenes to about 75% by weight of ethylene, more preferably from about 30% to about 60% by weight, and most preferably from about 35% to about 50% by weight propylene. (Please read the notes on the back before filling out this page.) In another specific example, the olefin stream provided also includes at least about 20% by weight of propylene. Preferably, the olefin stream provided comprises from about 20% by weight ethylene to about 70% by weight propylene, more preferably from about 25% by weight to about 50% by weight, and most preferably from about 30% by weight to about 40% % By weight of propylene. The olefin stream provided contains a relatively low concentration of ethane, and preferably, the concentration of ethane is lower than the concentration of propane, which is desirable. Preferably, the olefin stream includes no more than about 4% by weight ethane, more preferably no more than about 3% by weight ethane, and most preferably no more than 2% by weight ethane. It is also desirable that the olefin stream provided contains a relatively low concentration of propane. Preferably, the olefin stream includes no more than about 5 weight percent propane, more preferably no more than about 4 weight percent propane, and most preferably no more than 3 weight percent propane. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs In another embodiment of the present invention, the olefin stream provided includes both ethylene and propylene. Desirably, the olefin stream contains at least about 50% by weight ethylene and propylene. Preferably, the olefin stream comprises from about 50% to about 95% by weight ethylene and propylene, more preferably from about 55% to about 90% by weight ethylene and propylene, and most preferably from about 60% to about 85 % By weight of ethylene and propylene. The olefin stream provided may also contain some amount of water. However, it is satisfactory that any river water present in the olefin stream will be at a concentration 'so that the free water structure (ie, forming a separated water phase) or gas hydration will not significantly hinder the separation process . Gas hydration results in the formation of clathrate compounds. These compounds are solids, and these solids can be cited during the separation process. -11-This paper size applies Chinese National Standard (CNS) A4 specifications (2) 0X 297 mm. 575559 Printed by A7, Consumer Cooperatives, Bureau of Intellectual Property, Ministry of Economic Affairs B7_V. The description of the invention (g) causes obvious operational problems. The water present in the provided olefin stream should be at a concentration low enough 'so that a separated aqueous phase is not formed during the separation process. When a distillation column with a fractionation tray is used to separate monomethyl ether from olefins, recovery is very important because the separated water formed in the fractionation tray will prevent mass transfer. Distillation columns with mash are advantageous at high concentrations of water because such columns will not tend to collect the separated aqueous phase. Desirably, the olefin stream provided by 'in the present invention contains no more than about 15,000 wppm water. Preferably, the olefin stream contains no more than about 10,000 wppm water. More preferably, it is not more than 5,000 wppm of water, and most preferably, it is not more than about 1,000 wppm of water. In the present invention, the olefin stream need not be completely dried. That is, the olefin stream may contain some water. The advantage of an olefin stream containing some water is that no additional and / or complicated drying equipment will be required before the dimethyl ether is separated from the olefin stream. Preferably, the olefin stream comprises at least about 10 wppm water, more preferably, at least about 100 w p p m, and most preferably, at least about 200 w p p m of water. If the olefin stream contains an unacceptably high concentration of water, a sufficient amount of water can be removed, either before or during the separation of dimethyl ether using a water absorbent. . Examples of water-absorbing agents include alcohols, amines, amidines, nitriles, heterocyclic nitrogen-containing compounds, or any combination of the foregoing. Either monohydric or polyhydric alcohols can also act as alcohol absorbents. Specific examples of absorbents include methanol, ethanol, propanol, ethylene glycol, diethylene glycol, triethylene glycol 'ethanolamine, diethanolamine, triethanolamine, hindered cyclic amines, acetonitrile, n-methylpyrrolidone, dibenzyl Paper size applies Chinese National Standard (CNS) A4 specification (2) 0X 297 mm -12-(Please read the precautions on the back before filling out this page) 575559 A7 B7 Printed by the Consumer Cooperative of Intellectual Property Bureau, Ministry of Economic Affairs V. Description of the invention (10) Amidomethoxamine and combinations thereof. In order to obtain a substantial effect, the water absorbent should contain a small amount of non-aqueous absorbing component. For example, the water absorbent should contain at least about 75% by weight of water absorbing components. Desirably, the water absorbent comprises at least about 90% by weight, preferably at least about 95% by weight, and most preferably, at least about 98% by weight. A decontamination process using a decontamination vessel may be used when a water absorbent is used to reduce the concentration of water in the olefin stream before the dimethyl ether is separated. In essence, the decanting process involves contacting the olefinic stream with a water absorbent to remove a large amount of water from the olefin stream, that is, to wash it off. The amount of the absorbent added to the decontamination container should be sufficient to reduce the free water structure (i.e., the structure of the separated water), especially in the container, where separation of dimethyl ether from olefins occurs. In this specific example, it is satisfactory. The water absorbent is added to the rinse vessel at a molar ratio of the absorbent compound to the total olefin feed to the rinse vessel of about 1: 2 to about 1: 200. More preferably, the absorbent is added at a molar ratio from about 1: 5 to about 1: 00, and more preferably from about 1; 10 to about 1:50. Although the olefin stream may come from any conventional source that contains dimethyl ether, the present invention is particularly suitable for removing dimethyl ether from the olefin stream in the process of producing olefins from oxygenates. In a specific example of the present invention, the dimethyl ether-containing smoke stream is obtained by contacting an oxygenated raw material with a molecular sieve catalyst. In a preferred embodiment of the method of the present invention, the oxygenate raw material comprises one or more oxygenates, and more particularly, one or more organic compounds containing at least one oxygen atom. In the most preferred embodiment of the method of the present invention, the oxygenate in the raw material is one or more alcohols, preferably aliphatic alcohols, wherein the aliphatic portion of the alcohol has 1 to 20 carbon atoms, preferably from 1 to 10 carbon atoms, (please read the notes on the back before filling this page) This paper size applies Chinese National Standard (CNS) A4 specification (210X 297 mm) 575559 A7 B7 V. Description of Invention (M) and optimally from 1 to 4 carbon atoms. Alcohols serving as starting materials for the method of the present invention include lower straight or branched chain aliphatic alcohols and their unsaturated counterparts. Non-limiting examples of oxygenates include methanol, ethanol, n-propanol, isopropanol, methyl ethyl ether, dimethyl ether, diethyl ether, diisopropyl ether, formaldehyde, dimethyl carbonate, dimethyl Ketones, acetic acid and mixtures thereof. In a preferred embodiment, the raw material is one or more selected from the group consisting of methanol, ethanol, dimethyl ether, diethyl ether, or a combination thereof, preferably methanol and dimethyl ether, and most preferably methanol. The feedstock in a specific example includes one or more diluents, which are typically used to reduce the concentration of the feedstock and are generally non-reactive with the feedstock and molecular sieve catalyst composition. Non-limiting ranges of diluents include ammonia, argon, nitrogen, carbon monoxide, carbon dioxide, water, essentially non-reactive paraffins (especially the class' e.g. methane, ethane and propane), essentially non-reactive aromatic Compounds and mixtures thereof. The best diluents are water and nitrogen, with water being particularly preferred. The diluent is either added directly to the feedstock into the reactor, or directly into the reactor, or to the molecular sieve catalyst composition. In a specific example, the content of the diluent in the raw material is in a range from about 1 to about 99 mole percentages, preferably from about 1 to 80 mole percentages, based on the total amount of the raw materials and the diluent. Preferably from about 5 to about 50, and most preferably from about 5 to about 25. In a specific example, 'other hydrocarbons are added to the raw material, whether directly or indirectly, and include hydrocarbon burning, paraffins' aromatics (please refer to US 4,677,242, addition of aromatics) or mixtures thereof, preferably propylene , Butene, pentene, and other hydrocarbons having 4 or more carbon atoms, or mixtures thereof. Molecular sieves with the ability to convert oxygenates to olefinic compounds include zeolites (please read the precautions on the back before filling out this page) This paper size applies Chinese National Standard (CNS) Α4Ϊ 格 (2IGX-297 mm) -14-575559 A7 B7 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs. 5. Description of the invention (12) 'and non-zeolitic molecular sieves, and they are large, medium and small pore types. Non-limiting examples of these molecular sieves are small-pore molecular sieves, AEI, AFT, APC, ATN, ATT, ATV, AWW, BIK, CAS, CHA, CHI, DAC, DDR, EDI, ERI, G〇〇, KFI, LEV, L〇V, LTA, MON, PAU, PHI, RH〇, ROG, TH〇, and their substituted forms; mesoporous molecular sieve 'AF〇, AEL, EU〇, HEU, FER, MEL, MFI, MTW, MTT, TON and their substituted forms; and macroporous molecular sieves, EMT, FAU and their substituted forms. Other molecular sieves include ANA, BEA, CFI, CL0, DON, GIS, LTL, MER, MOR, MWW and SOD. Non-limiting examples of preferred molecular sieves, especially conversion of oxygenated feedstocks to olefins' including AEL, AFY, BEA, CHA, EDI, FAU, FER, GIS, LTA, LTL, MER, MFI, MOR, MTT, MWW, TAM and TON. In a preferred embodiment, the molecular sieve of the present invention has AEI topology or CHA topology or a mixture thereof, and most preferably is CHA topology. The molecular sieve substances all have a 3-dimensional, 4-connected skeleton structure of a TO4 tetrahedron with shared vertices, where T is any tetrahedral coordinated cation. These molecular sieves are typically described in terms of ring sizes defining pores, where size is calculated as the number of T atoms in the ring. Other skeleton type features include shape. Arrangement of caged rings, and when present, the dimension of channels, and the spaces ^ between the cages0 see van Bekkum, e t al. , Introduction to Zeolite Science and Practice, Second Completely Revised and Expanded Edition, Volume 137, pages 1-67, elsevier Science, B.  V. , Amsterdam, Netherlands (2001) (Please read the notes on the back before filling out this page) This paper size is applicable to the Chinese National Standard (CNS) A4 (210X 297 mm) 575559 A7 B7 13 V. Description of the invention ((please first Read the notes on the reverse side and fill out this page) Small, medium and large pore molecular sieves have a skeleton 颏 type from 4-ring to 12-ring or larger. In a preferred embodiment, 'molecular sieves have 8-, 10-, or 12 + Ring structure or larger 'average pore size ranges from about 3 A to about 15 A. In the best denier, the molecular sieve of the present invention, preferably the silicoaluminophosphate molecular sieve, has 8_rings and the average pores The size is less than about 5A, preferably from about 3A to about 5a, and more preferably from 3A to about 4. 5A, and best from 3. 5A to about 4. 2A. Molecular sieves, especially zeolites and zeolite-type molecular sieves, preferably have a molecular framework of 1 ', preferably 2 or more apex sharing [T04] tetrahedral units. These molecular sieves with silicon, aluminum and phosphorus as substrates and metal-containing sand, aluminum and phosphorus as substrates have been described in detail in most publications, for example, US 4,567,029 (MeAPO where Me is Mg, Μη, Zη or Co), US 4,440,87 1 (SAP〇), EP-Α-0 1 59624 (ELAPSO where El is As, Be, B, Cr, Co, Ga, Ge, Fe, Li, Mg, Mn , Ti or Zn), US 4,5 54, 143 (FeAP〇), US 4,822,47 8, 4,683,2 1 7, 4,744,885 (FeAPSO), EP-A-0 1 5 8975 and US 4,935,2 1 6 (ZnAPSO), EP-A-0 1 61489 (CoAPSO), EP-A-0 1 58976 (ELAP〇, whose EL is Co, Fe, Mg, Mn, Ti, or Zn) 'Employee Consumer Cooperative of Intellectual Property Bureau, Ministry of Economic Affairs Printed US 4,31〇, 440 (A1P〇4), EP-A-0 1 5 8350 (SENAPSO), US 4,973,460 (LiAPSO) 'US 4,888,1 67 (GeAPO), US 5,057,295 (BAPSO), US 4,738,837 (CrAPSO), US 4,759,9 1 9 and US 4,851,106 (CrAPO), US 4,758,4 19, 4,882,03 8, 5,434,326 and 5,478,787 (MgAPSO), US 4,554,143 (FeAPO), US 4,894,2 1 3 (AsAPSO), US 4,9 1 3,888 (AsAPO), US 4,686,092, 4,846,95 6 and 4,793,833 (MnAPSO), this paper size applies Chinese National Standard (CMS) A4 specification (210X297 mm) 575559 A7 B7 V. Description of invention () US 5,345,0 1 1 R 6,1 56,93 1 (MnAPO) '' US 4,7 3 7,3 5 3 (BeAPSO), US 4,940,570 (BeAPO), US 4,80 1,309, 4,684,6 1 7 and 4,880,5 20 (TiAPSO), US 4,500,65 1 ^ 4,55 1,236 and 4,605,492 (TiAPO), US 4,824,554, 4,744,970 (CoAPSO), US 4,735,806 (GaAPSO), EP-A-0 293937 (QAPSO, where Q is the framework oxide unit [Q〇2]), and US 4,567,029, 4,686,093, 4,781,814, 4,793,984, 4,801,364, 4,853,197, 4,9 1 7,876, 4,952,3 84, 4,956,164, 4,956, 165, 4,973,785, 5,241,093, 5,493,066, and 5,675,050 are all incorporated herein Reference. Other molecular sieves include those disclosed in EP-0 888 1 87 Bl (microporous crystalline metal phosphate, (SAP〇4 (UI〇-6)), US 6,004,898 (molecular sieves and alkaline earth metals), February 24, 2000 U.S. Patent Application Serial No. 09/5 1 1,94 3 (combined hydrocarbon co-catalyst) filed daily, PCT WO 0 1/64340 (molecular sieve containing thallium) published on September 7, 2001, and R.  Szostak, Handbook of Molecular Sieves, Van Nostrand Rein hold, New York (1992), all of which are incorporated herein by reference. Better molecular sieves containing silicon, aluminum and / or phosphorus and molecular sieves containing aluminum, phosphorus and any silicon include aluminophosphate (ALP0) molecular sieves and silicoaluminophosphate (SAPO) molecular sieves and substituted, preferably metal substituted Yes, ALP0 and SAP0 molecules. The best molecular sieves are SAP0 molecular sieves and metal substituted SAP0 molecular sieves. In a specific example, the metal is an alkali metal of Group IA of the Periodic Table of the Elements, an alkaline earth metal of Group IIIA of the Periodic Table of the Elements, and a rare earth metal of Group IIIB.釓, 钺, 镝, “, bait, table, mirror, and distillate; and 铳 or yttrium of the periodic table, ---------— * '(Please read the precautions on the back before filling this page) 11, 11 Printed by the Consumers' Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs The paper size is applicable to the Chinese National Standard (CNS) A4 (210X 297 mm) 575559 A7 B7 V. Description of the invention (15) ^ — (Please read the notes on the back first (Fill on this page again.) Periodic Table of Elements IVB, VB, VIB, VIIB, VIIIB, and transition metals of Group IB, or any mixture of these metals. In a preferred embodiment, the metal system is selected from the group consisting of Co, Cr, Cu, Fe, Ga, Ge, Mg, M11, Ni, S11, T i, Z n, and Z l ·, and mixtures thereof. In another preferred embodiment, these metal atoms are inserted into the skeleton of the molecular sieve through a tetrahedral unit, such as [Me〇2], and have a net charge according to the valence state of the metal substituent. For example, in a specific example, when the metal substituent has a valence state of +2, +3, +4, +5, or +6, the net charge of the tetrahedral unit is between _2 and +2. In a specific example, as described in the above US patent case, molecular sieves are expressed in the experimental form of anhydrous substance: mR: (MxAhPz :) 〇2. Printed by the Consumer Cooperative of Intellectual Property Bureau of the Ministry of Economic Affairs where R represents at least one template Temp 1 ating agent, preferably an organic templating agent; m is the number of moles relative to R per mol (MxAlyPz), and m has a number from 0 to 1, preferably 0 to 0. 5 and best from 0 to 0. 3; X, y, and z represent mole fractions of a, P, and M serving as tetrahedral oxides, where M is a metal selected from the periodic table of the elements Ια, ΙΑΑ, IB, ΙΙΙΒ, IVB, VB One of VIB, VIIB, VIIIB, and the lanthanide group, preferably M is selected from the group consisting of Co, Cr, Cu, Fe, Ga, Ge, Mg, Mη, Ni, Sn, Ti, Zn, and Zr. In a specific example, m is greater than or equal to 0 · 2, and x, y, and z 焉 are greater than or equal to 0. 〇1. In another specific example, m is greater than 0.  1 to about 1, x is greater than 0 to about 0. 25, y is from 0. 4 to 0. 5, and z is from 0. 25 to 0. 5, more preferably, m is from 0. 15 to 〇7, X is from 〇. 〇1 to 0. 2, y is from 0. 4 to 0. 5, and z is from 0. 3 to 0. 5. Non-limiting example package of SAPO and ALP0 molecular sieves used in the present invention ^ Paper size conforms to China's National Standard (CNS) A4 specification (210 '乂 ~ 297gt): 18-~ 575559 A7 B7 Intellectual Property Bureau, Ministry of Economic Affairs Printed by Employee Consumer Cooperatives V. Invention Description (16) Includes SAPO-5, SAP0-8, SAP0-1 1, SAP0-16, SAP0-17, SAP0-18, SAPO-20, SAP0-31, SAPO-34, SAPO-35, SAPO-36, SAPO-37, SAPO-40, SAP0-41, SAPO-42, SAPO-44 (US 6,162,415), SAPO-47, SAPO-56, ALP0-5, ALP0-1 1 , ALP0-18, ALP0-31, ALPO-34, ALPO-36, ALPO-37, ALP0-46, or a combination thereof, and a metal-containing molecular coating. More preferred zeolite type molecular sieves include one or a combination of SAP0-18, SAPO-34, SAPO-35, SAPO-44, SAPO-56, ALP0-18, and ALP0-34, and more preferably, SAP0-18 , SAPO-34, ALPO-34 and ALP0-18, or a combination thereof, and a metal-containing molecular layer, and preferably SA. PO-34 and AL. One or a combination of P0-18, and a molecular sieve containing the metal. In a specific example, the molecular sieve is an internally growing substance having 2 or more unique phases having a crystalline structure in a molecular sieve composition. In particular, internally grown molecular sieves are described in US Patent Application Serial No. 09 / 924,01 6 filed on August 7, 2001 and PCT W0 98/15496 published on April 16, 998, both of which are This article is incorporated herein by reference. In another specific example, the molecular sieve includes at least one internal growth phase of AEI and CHA framework type. For example, SAPO-18, ALPO-18, and RUW-18 have the AEI framework type, and SAPO-34 has the CHA framework type. In a specific example, the molecular sieve used in the present invention is combined with one or more other molecular species. In another specific example, the preferred ammonium phosphonate or phosphonium molecular sieve, or a combination thereof, is combined with one or more non-limiting exemplary zeolites below, such as / 5 (US 3,305 8,069), ZSM- 5 (US 3,702,886 (Please read the notes on the back before filling this page) This paper size applies to China National Standard (CNS) A4 specifications (2) 0X 297 mm) 575559 A7 B7 5. Description of the invention (17) (please first Read the notes on the back and fill out this page), 4,797,267 R 5,7 8 3,3 21), ZSM-1 1 (US 3,709,9790, ZSM-1 2 (US 3,832,449), ZSM-12 and ZSM-38 ( US 3,94 8,7 5 8), Z SM-2 2 (US 5,336,478), ZSM-23 (US 4,076,842), ZSM-34 (US 4,086,186), ZSM_35 (US 4,01 6,245), ZSM- 48 (US 4,397,827), ZSM-58 (US 4,698,21 7), MCM-1 (US 4,639,3 5 8), MCM-2 (US 4,673,559), MCM-3 (US 4,632,8 1 1), MCM -4 (US 4,664,897), MCM-5 (US 4,639,357), MCM-9 (US 4,880,61 1), MCM-10 (US 4,623,527), MCM-14 (US 4,619,818), MCM-22 (US 4,954,325), MCM-41 (US 5,098,684), M-41S (US 5,102,643), MCM-48 (US 5,198,203) MCM-49 (US 5,236,575), MCM-56 (US 5,362,697), ALP0-11 (US 4,310,440), titanium aluminosilicate (butyl AS0), TASO-45 (EP-A-0229, -295), boron Silicate (US 4,254,297), titanium aluminophosphate (TAP〇) (US 4,500,65 1), a mixture of ZSM-5 and ZSM-11 (US 4,229,424), ECR-18 (US 5,278,345), bound to ALPO- 5 of SAPO-34 (printed by the Consumer Cooperative of the Intellectual Property Office of the Ministry of Economic Affairs US 5,97 2,203), PCT published on December 23, 1988 (¥ 98/57743 (molecular sieve and Fischer-Tropsch), 1 ^ 6,300,535 (combined with 1 \ ^ 1 zeolite) and mesoporous molecular sieves (US 6,284,696, 5,098,684, 5, 102,643, and 5,1 08,725), all of which are incorporated herein by reference. Molecular sieves are prepared or formulated as catalysts by mixing synthetic molecular sieves with adhesives and / or matrix materials to form sieving catalyst compositions or formulated molecular sieve catalyst compositions. The formulated molecular sieve catalyst composition is manufactured by conventional techniques, such as spray drying, pelletization, extrusion, etc. The paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 575559 Ministry of Economic Affairs Printed by the Consumer Goods Cooperative of Intellectual Property Bureau A7 A_B7 V. Invention Description (18) Useful shapes and sizes of particles. There are many different adhesives used to form molecular sieve catalyst compositions. Non-limiting ranges of adhesives used alone or in combination include various types of hydrated alumina, silica, and / or other inorganic oxide solvents. A sol containing a preferred oxide name is aluminuni chlorhydrol. Inorganic oxide sols act like glues to stick together synthetic molecular sieves and other materials, such as substrates, especially after heat treatment. Upon heating, the inorganic oxide sol, preferably having a low viscosity, is converted into an inorganic oxide matrix component. For example, an alumina sol will be converted to an alumina matrix after heat treatment. [005 8] A sol with 211111 ^ 11111116111〇147 center 01, hydroxylated aluminum as a substrate has the general formula: AUCMHOHCl1x (H2O), where m is 1 to 20, n is 1 to 8, and 5 to 40, p is 2 to 15 and X is 0 to 30. The dispersion contains counter ions. In a specific example, the adhesive is Ali3 04 (〇H) 24Cl7 · 12 (Η 2〇), which is described in G. M.  Wolterman, et al., Stud, Surf, Sci, and Catal, 76, pages 1 05-144 (1 993), which are incorporated herein by reference. In another specific example, one or more adhesives are mixed with one or more other non-limiting examples of alumina materials, such as aluminum oxyhydroxide, r-alumina, boehmite, boehmite, and transition oxides such as α-oxidation. g, yS-oxidation oxide, r-oxidation bromide, 6-oxidation insulation, ε-alumina, / c-alumina and p-alumina, aluminum trihydroxide, such as hydrotalcite, bayerite, nordstrandite, doyelite and others mixture. In another specific example, the adhesive is an alumina sol, preferably including oxidized oxide, and any anthracene including some sand. In another specific example, the adhesive is peptized alumina, which is made by using acid, preferably acid-free paper, which does not include halogens. The paper size is in accordance with Chinese national standards (CNsTa4 specification (210X 297 mm) — (Please read the notes on the back before filling out this page) 575559 A7 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs ______________ B7 V. Invention Description (19) 'Process oxidation hydrates, such as pse U d 〇b 〇hemite, To prepare a sol or anion solution. Non-limiting examples of commercially available colloidal alumina sols include those purchased from Nalco Chemical Co. Nalco 8676 from Naperville, Illinois and Nyacol from PQ Corporation, Valley Forge, Pennsylvania. In a preferred embodiment, the molecular sieve is mixed with one or more matrix materials. The matrix material is typically effective in reducing the total cost of the catalyst, acting as a heat sink to assist in masking the heat from the catalyst composition, such as hardening the catalyst composition during regeneration, increasing the catalyst strength, such as crushing strength and resistance to wear, And control the slew rate in a special method. Non-limiting examples of the matrix material include one or more rare earth metals, metal oxides including titanium dioxide, oxide pins, gold oxide, hafnium oxide, beryllium oxide, quartz, sand oxide or sol, and mixtures thereof 'For example, sand oxide-magnesium oxide, sand dioxide-hafnium oxide, stone oxide _ titanium oxide, silica-alumina, and silica-alumina-hafnium oxide. In a specific example, the 'matrix material is natural clay, such as those from montmorillonite and Shangtong soil. Suitable natural clays include sabbentonites and other known local territories ’such as D i X i e, Mc N a mee, G e 〇 r g i a and F 1 〇 r i d a clay. Non-limiting examples of other matrix materials include halosite, kaolinite, dickite, nacdte, or vermiculite. In a specific example, the matrix material, preferably any clay, is subjected to known improvements such as calcination and / or acid treatment and / or chemical treatment. In a preferred embodiment, the matrix material is a clay or clay-type composition 'preferably clay or clay with a low content of iron or titanium dioxide (please read the precautions on the back before filling this page) This paper The scale is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 public attack) 575559 A7 B7 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs V. Invention Description (20) type composition, and the best matrix material is kaolin. Kaolin was found to form a pumpable, high solids slurry. Kaolin has a low fresh surface area ' and is easy to integrate into piles because of its slab structure. The preferred average particle size of the matrix material (most preferably kaolin) is from about 0. 1 / zm to about 0. 6 // m ′ and the D 9 0 particle size distribution is below about 1 // m. In another specific example, the weight ratio of the adhesive used to form the molecular sieve composition to the matrix material is from 0: 1 to 1:15, preferably from 1:15 to 1: 5, more preferably from 1:10 to 1: 4, and preferably from 1: 6 to 1: 5. It has been found that higher sieve content and lower matrix content will increase the effectiveness of the molecular sieve catalyst composition, and lower sieve content and higher matrix content will improve the wear resistance of the paper product. In another specific example, the formulated radon sieve catalyst composition comprises from about 1% to about 99%, more preferably from about 5% to about 90%, and most preferably from about 10% to about 80%. The molecular weight of molecular sieve is calculated by the total weight of molecular sieve catalyst composition. In another specific example, the weight percentage of the adhesive in the spray-dried molecular sieve catalyst composition is calculated from the total weight of the adhesive, the molecular sieve and the matrix material, and is from about 2% by weight to about 30% by weight. It is preferably from about 5% to about 20% by weight, and more preferably from about 7% to about 15% by weight. Once the molecular sieve catalyst composition is formed in a substantially dry or dried state, in order to further harden and / or activate the formed catalyst composition, heat treatment, such as calcination, is usually performed at a high temperature. A conventional calcination environment is air, which typically includes a small amount of water vapor. In a preferred calcination environment such as air, nitrogen, ammonia, flue gases (combustion products in lean oxygen), or any combination thereof, typical calcination temperatures range from about 400 ° C to about this paper size. China National Standard (0 milk) into 4 specifications (210 \ 297 mm) 13-(Please read the precautions on the back before filling out this page) 575559 A7 _ B7 V. Description of the invention (21) 1,000 ° C 'Preferably from about 500 ° C to about 800 ° C, and most preferably from about 550 ° C to about 700 ° C. (Please read the precautions on the back before filling in this page) The method of converting raw materials, especially raw materials containing one or more oxygenates, in the presence of the molecular sieve catalyst composition of the present invention is carried out in a reactor This method is a fixed bed method, a fluidized bed method (including a turbulent bed method), a continuous fluidized bed method is preferred, and a continuous high velocity fluidized bed method is most preferred. The reaction method can occur in various catalytic reactors, such as a mixed reactor, which has a tight or fixed bed reaction zone and / or a fast flowing bed reaction zone connected together, a circulating fluid bed reactor, a riser Reactors and the like. Suitable conventional reactor types are described in, for example, US 4,076; 796, US 6,287,522 (dual riser) and Fluidization Engineering, D.  Kunii and Levenspiel, Robert E.  Krieger Publishing Company, New York, New York 1 977, all of which are incorporated herein by reference. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. The preferred reactor type is a riser reactor, which is usually described in Riser Reactor, Fluidization and Fluid-Particle Systems, pp. 48-59, F. A.  Zen z and D. F. 〇t homo, Rein hold Publishing Corporation, New York, 1960, and US 6,1 66,282 (fast fluid bed reactor) and US patent application serial number 09 / 564,613 (multiple riser reactor) filed on May 4, 2000 , Which are incorporated herein by reference. In a preferred embodiment, the fluid bed method or the high-speed fluid bed method includes a reactor system, a regeneration system, and a recovery system. The reaction system is preferably a fluidized bed reactor system, which has one or more riser reactors with the first paper size applicable to Chinese National Standard (CNS) A4 specifications (2) 0X 297 mm. 575559 A7 B7 5 2. Description of the invention (22) A reaction region and a second reaction region are provided in at least one separation container preferably including one or more cyclones. In a specific example, one or more riser reactors and separation vessels are contained in a single reactor vessel. Fresh raw materials, which preferably contain one or more oxygenates, optionally one or more diluents, are entrained into one or more riser reactors, in which a zeolite or zeolite-type molecular sieve catalyst composition or its coke form is introduced . In a specific example, the molecular sieve catalyst composition or its coke form is contacted with a liquid or a gas or a combination thereof before being introduced into a riser reactor. Preferably, the liquid is water or methanol, and the gas is an inert gas. , Such as nitrogen. In a specific example, the content of fresh raw materials fed separately or in conjunction with gaseous raw materials to the reactor system ranges from 0. 1% to about 85% by weight, preferably from about 1% to about 75% by weight, and more preferably from about 5% to about 65% by weight, based on the total weight of the raw materials containing any diluent. The liquid and gas raw materials are preferably the same composition or the same or different 'raw materials containing different proportions, and the raw materials have the same or different diluents. The feedstock entering the reactor system is preferably partially or fully converted into a gaseous effluent in the first reactor area, which effluent enters the separation vessel with the coked molecular sieve catalyst composition. In a preferred embodiment, the cyclone in the separation vessel is designed to separate the molecular sieve catalyst composition from the gaseous effluent containing one or more olefins in the separation region, preferably a coke-based molecular sieve catalyst composition. . The cyclone is better, but the gravity effect in the separation vessel will also separate the catalyst composition from the gas effluent. Other methods of separating the catalyst composition from the gas effluent include the use of plates, caps, elbows, and the like. {Please read the notes on the back before filling this page)-This paper is printed by the Consumers' Cooperative of the Intellectual Property Bureau of the Ministry of Economy. The paper size is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm) 575559 A7 B7 V. Invention Explanation (23) In a specific example of the separation system, the separation system includes a separation container, and a typical lower part of the separation container is a stripping area. In the stripping zone, the coked molecular sieve catalyst composition is in contact with a gas, which is preferably a water vapor, methane, carbon dioxide, carbon monoxide, hydrogen or an inert gas such as argon, or a combination thereof, preferably water vapor In order to recover the adsorbed hydrocarbon from the coked molecular sieve catalyst composition, the composition is then introduced into a regeneration system. In another specific example, the stripping zone is a separation vessel from a separation vessel, and when the gas system calculates the volume of the coke-based molecular sieve catalyst composition by the gas volume, the gas surface velocity (GHSV) is from lhr · 1 To about 20,000111 ^, preferably at a high temperature from 250 ° C to about 750 ° C, preferably from about 35 ° C to 650 ° C, through a coke-based molecular sieve catalyst composition. Conversion methods, particularly in reactor systems, use conversion temperatures ranging from about 200 ° C to about 1,000 ° C, preferably from about 250 ° C to about 800 ° C, and more preferably from about 250 ° C to about 750 ° C, more preferably from about 30CTC to about 650 ° C, more preferably from about 350 ° C to about 600 ° C, and most preferably from about 35CTC to about 550 ° C. The conversion method ', especially in the reactor system, does not matter which conversion pressure is used. The conversion pressure is calculated as the partial pressure of the raw material without any diluent. The transition pressure used in the method typically ranges from about 0.1 kPaa to about 5 MPaa, preferably from about 5 kPaa to about 1 MPaa, and most preferably from about 20 kPaa to about 500 kPaa. In particular, in the method of converting a raw material containing one or more oxygenates in the presence of a molecular sieve catalyst composition in the reaction zone, the weight space-time velocity (WHS V) is defined as the total weight of the raw material in the reaction zone without any diluent. The weight of the molecular sieve in the molecular sieve catalyst composition per reaction area per hour. WHS V is applicable to the Chinese National Standard (CNS) A4 specification (210X 297 mm)-this _.  . ------ (Please read the notes on the back before filling this page) Order ΦΙ.  Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs 575559 Μ B7 V. Description of the Invention (24) The catalyst composition maintained in a sufficient amount to keep the flow in the reactor. (Please read the precautions on the back before filling in this (Pages) WHSV typically ranges from about 1hr · 1 to about 50,000hr ·, preferably from about 2hri to about 3000hr · 1, and more preferably from about 5hr · 1 to about 1500hr. i, and preferably from about 1 Ohr 1 to about 1000 hr · 1. In a specific example, V is greater than 20 hi ·· 1 ′ to convert the WHSV of the raw material containing methanol and dimethyl ether to a range from about 2011Γ1 to about 300 hi · -1. The surface gas velocity (SGV) of the raw material containing the diluent and the reaction product in the reactor system is preferably sufficient to flow the catalyst composition through the molecules in the reaction area in the reactor. In the method, 'especially in the reactor system, more preferably in the riser reactor, the SGV is at least 0. per second. 1 meter (m / sec), preferably greater than 0. 5 m / sec, more preferably lm / sec, more preferably 2 m / sec, more preferably 3 m / sec, and most preferably 4 m / sec. Reference is made to US Patent Application Serial No. 09 / 708,753, filed November 8, 2000, which is incorporated herein by reference. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. In a preferred embodiment of a method for converting oxygenates to olefins using a silicoaluminophosphate molecular sieve catalyst composition, the method is based on a WHSV of at least 201η ·· 1 and The corrected normalized methane selectivity (TCNMS) is below 0. 016, preferably lower than or equal to 0. 01 to operate. Reference is made to US 5,952,5 3 8, which is incorporated herein by reference. In another preferred embodiment of the method of using a molecular sieve catalyst composition to convert an oxygenate (such as methanol) into one or more olefins, WHSV is from 0. 01 hi ·· 1 to about 100hr1, at a temperature of from about 350 t to 55 (TC and silicon dioxide to MeaCMMe are group IIIA or VIII of the periodic table) Mohr ratio from 300 to this paper standard applies Chinese national standard (CNS ) A4 specification (210X297) 575559 A7 B7 25 5. Description of the invention (2500. Refer to EP_0642485B1, which is incorporated herein by reference. (Please read the precautions on the back before filling this page) In the use of molecular sieve catalyst composition Other methods to convert oxygenates (such as methanol) to one or more olefins are described in PCT WO 0/23 5 00 published on April 5, 2001 (at least 1. 〇, reduce propane); which is incorporated herein by reference. According to a specific example, the conversion of a major oxygenate (such as methanol) is from 90% to 98% by weight. According to another specific example, the conversion of methanol is from 92% to 98% by weight, preferably from 94% to 98% by weight. According to another specific example, the conversion of methanol is greater than 98% by weight and less than 100% by weight. According to another specific example, the conversion of methanol is from 98. 1% by weight to less than 100% by weight, preferably from 98. 2% by weight to 99. 8% by weight. According to another specific example, the conversion of methanol is from 98. 2% by weight to less than 99. 5% by weight, preferably from 98. 2% to 99% by weight. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs The process of converting oxygenates to olefins forms a large amount of water as a by-product. Most of the water can be removed by cooling the olefin stream from the oxygenate reactor to a temperature below the condensation temperature of the water in the stream. Preferably, for the oxygenate to olefin conversion process, the temperature of the product stream is cooled to a temperature below the condensation temperature of the oxygenate feed. In a particular embodiment, it is desirable to cool the product stream below the condensation temperature of methanol. The quench column is an arrangement that is effective for cooling the olefin stream from the oxygenate to olefin reaction process. In a quench column, the quench fluid is in direct contact with the olefin stream to cool the stream to the desired condensation temperature. Condensation produces concentrated water containing the stream, which usually comes from the quenched tubing column and serves as the bottom stream. The olefins usually come from the column as an overhead stream. The paper size of the top distillation is applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) 575559 A7 B7 V. Description of the invention (26) (Please read the precautions on the back before filling this page) Ether, the dimethyl ether must be isolated according to the invention. If high concentrations of water still remain in the overhead distillate, an absorbent can be used to reduce the water concentration as described above. In a particular embodiment of the invention, the quenched olefin stream is further compressed by compression, preferably multi-stage compression. Two, three, four or more stages can be used, with two or three stages being preferred. During or after multi-stage compression, if desired, the olefin stream can be rinsed with a water absorbent as described above. Rinse using a water absorbent can alleviate problems associated with gas hydration and / or separation of aqueous phases. Preferably, multi-stage compression using a water absorbent, and washing between stages is preferred. Dimethyl and C 4 + smoke components are separated from the olefin stream. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. In a specific example of the present invention, the olefin stream is divided into the first part and the second part. the second part. Desirably, the separation is performed at a pressure below 200 psig (l, 480 kPa absolute). Preferably, the separation is performed at a pressure from about 200 psig (l, 480 kPa absolute) to about 290 psig (2, 100 kPa absolute), more preferably from about 250 psig (l, 825 kPa absolute) to about 290 psig (2, 100 kPa absolute). . The actual higher pressure limit in the separation process will typically depend on the temperature 'at which the second part is separated. The second part will contain dimethyl ether and other hydrocarbons with a boiling point greater than methyl ether, such as C4 + olefins. Desirable. Yes' The compounds that remain in the second part at temperatures as low as possible will not cause chemical degradation or blockage problems in other downstream separation and processing units. In a specific example, the separation will cause the average temperature of the second part to be no greater than about 250 -29- This paper size applies the Chinese National Standard (CNS) A4 specification (210X297 mm) 575559 A7 ___ B7 V. Description of the invention ( 27) ° F (121 ° C), preferably not more than about 240 ° F (116 ° C), and more preferably not more than about 230 ° F (1 1 (TC). In the present invention, as described above, the water absorbent It can be optionally added to the container ', in which the separation of the oxidized pollutants from the provided hydrocarbon stream;): the hydrocarbon stream can be carried out. Adding the water absorbent directly to the separation vessel may have the additional advantage of reducing the free water and / or inclusion structure in the vessel. In a specific example of the present invention, the water absorbent is added to the oxygenated substance separation container in a sufficient amount to greatly reduce the oxygenated substance content (such as dimethyl ether) or the formation of inclusion compounds. Preferably, the water absorbent is added to the container in a manner such that the molar ratio of the water absorbent to the total weight of the olefin feed entering the separation vessel is from about 4: 1 to about 1: 5,000,000. The high molar ratio of the water absorbent to the total weight of the olefin feed is suitable for reducing the oxygenate content, preferably from about 4: 1 to about 1: 1, more preferably from about 3: 丨 to about 1.2: 1 'and Optimally from about 2.5: 1 to about 1.5: 1. The low molar ratio of the water absorbent to the total weight of the olefin feed is suitable for reducing clathrate formation, preferably from about 1: 丨 to about 1: 5,00, more preferably from about 1: 100 to about 1 : 4,00, and most preferably from about 1: 0 to about 1: 3,000. In a specific example of the present invention, the separation is performed by conventional distillation. Distillation is carried out using vessels or towers with internal mash or trays, which vessels or towers produce different temperatures from the top to the bottom of the tower. The top layer of the column, ρβ, is the colder fraction, and the higher volatile components in the feed come from the top of the column. In the present invention, it is desirable to obtain a high concentration of ethylene and propylene 'from an olefin stream containing monomethyl ether. In a specific example, the paper size of dimethyl ether from olefins is applicable to the Chinese National Standard (CNS) A4 specification (21 Οχ 297 mm) Γ30---Clothing-(Please read the precautions on the back before filling in this Page), printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs, printed 575559 A7 B7 V. Ethylene and propylene were separated from the description of the invention (28) (please read the precautions on the back before filling this page). In this specific example, ethylene and propylene are recovered in the first part, and dimethyl ether is recovered in the second part. Typically, the first portion will be the overhead or side portion of the distillation column, and the second portion will be the bottom portion of the distillation column or another side portion. In a specific example of the present invention, a large amount of ethylene and propylene in the provided olefin stream will be separated in the first part, and a large amount of dimethyl ether in the provided olefin stream will be separated in the second part. Separation. Preferably, the first part will contain at least about 75% of the ethylene and propylene in the provided olefin stream, more preferably at least about 85%, and most preferably at least about 95%. In another specific example, at least about 75% of the dimethyl ether in the provided olefin stream will be separated in the second section. Preferably, at least about 85%, more preferably at least about 95%, and most preferably at least about 99% of the dimethyl ether in the provided olefin stream will be separated in the second section. The large amount of propane printed in the provided olefin stream by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs can be separated in either the first or the second part. If a large amount of propane is contained in the first part, the heavier products required in the second part will have less separation. However, when a large amount of propane is in the first part, the amount of dimethyl ether in the first part may be slightly increased. In this specific example, the propane in the provided olefin stream is at least about 60%, preferably at least about 70%, more preferably at least about 80%, which will be in the first part, and the first part will contain no more than about 50 w ρ pm, preferably no more than about 25 wppm, more preferably no more than about 10 wppm dimethyl ether, and most preferably no more than about 5 wppm dimethyl ether. If a significant amount of propane in the provided olefin stream is separated in the second part, the concentration of dimethyl ether in the first part will be significantly lower. -一 31 _ This paper rule jade applies the Chinese National Standard (CNS) A4 specification (210X 297mm) 575559 Α7 Β7 V. Description of the invention (29) (Please read the precautions on the back before filling this page) In this specific example In the provided olefin stream, the propane is at least about 60%, preferably at least about 70%, more preferably at least about 80%, which will be in the second part, and the second part will contain not more than about 25 wppm, preferably No more than about 15 wpp, more preferably no more than about 5 wppm ether, and most preferably no more than about 1 w ρ pm dimethyl ether. In another embodiment of the present invention, the second part will also include some having 4 or more Hydrocarbon compounds of one carbon atom. These compounds are also known as C4 + ingredients. The content of the C4 + component in the second part can vary, especially depending on the propane content in the second part. For example, the second portion may contain from about 5 wt% to about 90 wt% of a C4 + ingredient. Preferably, the second part contains C4 + ingredients from about 25% to about 80% by weight, and more preferably from about 35% to about 75% by weight of C4 + ingredients. Another advantage of the invention printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economics is that the separation vessel is operated at temperature and pressure to separate at least most (ie, at least 50%) of the propadiene from the provided olefin stream. Allene may be present. In this specific example, allene is preferably separated in the second part with dimethyl ether. Preferably, at least about 75%, more preferably at least about 85%, and most preferably at least about 95% of the allene may be separated. Separation of any propadiene in this manner will necessarily include separation of any large amount of methylacetylene, which may also be present in the olefin stream provided. This is because methylacetylene has a lower boiling point than propadiene and dimethyl ether. Removal of allene and methylacetylene from the provided olefin stream will provide a substantial advantage because the first part containing ethylene and / or propylene has a high concentration of monoolefin compounds. If any hydrogen is processed, this logistics will require a little bit. This logistics may be typically reduced by the two papers recovered in the first part. Applicable to China National Standard (CNS) A4 specification (2IOX 297 mm) Γ32 ~: ~ ~ 575559 A7 B7 V. Description of the invention (30) Number of olefins or olefinic compounds. (Please read the notes on the back before filling out this page) The present invention is particularly useful for processing the ethylene and propylene streams contained in the first part to remove the acid gas such as CO2 which is taken away. portion. The advantage is that the separated ethylene and propylene streams in the present invention will contain a relatively small amount of hydrocarbon components which will cause blocking problems in this acid gas processing system. A solid or liquid acid gas processing system can be used in the present invention. In another system, the acid gas system is removed from the ethylene and / or propylene stream in the first portion by contacting the first portion with an acid gas absorbent or adsorbent. Examples of the absorbent or adsorbent include amines, potassium carbonate, caustic compounds, alumina, molecular sieves, and membranes, particularly those formed from polymill, polyimide, polyamidine, transparent polymers, and cellulose acetate membrane. Solutions containing amines and caustic compounds are preferred, and caustic compounds are more preferred. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs The aqueous amine solution used in the present invention may contain any amine compound suitable for acid gas absorption. Examples include alkanolamines such as triethanolamine (TEA), methyldiethanolamine (MDEA), diethanolamine (DEA), monoethanolamine (MEA), diisopropanolamine (DIPA), and hydroxyaminoethyl ether (DGA) ). Effective concentrations can be from about 0. A range of 5 to about 8 moles per liter of aqueous solution. Piperazine and / or monomethylethanolamine (MMEA) can be added to the aqueous amine solution to enhance its absorption capacity. These additives may be included in an aqueous solution at a concentration of from about 0. 04 to about 2 moles per liter of aqueous solution. Caustic compounds useful in the present invention are basic compounds which are effective in removing acid gases from olefin streams. Examples of this basic compound include sodium hydroxide and potassium hydroxide. -33-This paper size applies Chinese National Standard (CNS) A4 specification (210X 297mm) 575559 A7 _____B7 V. Description of the invention (31) (Please read the precautions on the back before filling this page) The acid gas treatment below, It is desirable to use water rinsing to simultaneously remove the entrained material in the treated ethylene / propylene. Can be used with conventional equipment. However, it is desirable to further remove additional water from the separated ethylene and / or propylene stream. In a specific example of the present invention, the ethylene and propylene in the first part are washed with water, that is, in contact with the water stream before the acid gas treatment. This contact is particularly advantageous when the water absorbent is added to the oxygenate separation vessel, and the water absorbent can continue to exist to the first or overhead distillate portion. Water scrubbing will be performed to remove most of the water absorbent carried. In the case of acid gas treatment, the present invention further includes any specific examples of drying. In this specific example, a solid or liquid drying system may be used that has removed water and / or additional charged oxidized hydrocarbons from the first section. Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs in a solid drying system, ethylene and / or propylene are contacted with a solid adsorbent to further remove water and charged oxidized hydrocarbons to a very low level. Separated in the first part and optionally treated with acid gas and washed with water. Typically, the adsorption process is carried out on one or more fixed beds containing a suitable solid adsorbent. Adsorption is used to remove water and oxidized hydrocarbons to very low concentrations, and to remove oxidized hydrocarbons that cannot normally be removed using other processing systems. Preferably, the adsorption system as part of the invention has multiple adsorbent beds. Multiple beds allow continuous separation without the need to stop the method to regenerate the solid adsorbent. For example, in a three-bed system, typically one bed is on-line, one bed is off-line regeneration, and the third bed is spare. ^^ scales are applicable to Chinese national standards ((^^ Eight 4 specifications (21 ^ 297 mm) --- Do not-575559 A7 B7 V. Invention description (32) (Please read the precautions on the back before filling this page)) Used for The specific sorbent solids of the sorbent bed are determined by the type of pollutants removed. Examples of solid sorbents for the removal of water and various polar organic compounds (such as oxidized hydrocarbon rescue liquids) include alumina, silica :: 3A molecular residue, 4A molecular sieve and aluminate salt. The bed containing these sieves or multiple beds with different adsorbent solids can be used to remove water and various charged oxidized hydrocarbons. In the present invention, one or Multiple adsorption beds can be arranged in series or in parallel. In one example of a series arrangement, the first bed is used to remove the smallest and most polar molecule, which is the most solution-removed. For larger removals and less polarities The subsequent bed of the oxidized species is in the second position in series. As a specific example of an arrangement, water is the first choice to be removed, using a 3A molecular sieve. Following this bed is one or more Low selective suction One or more beds of the adsorbent, such as a larger pore molecular sieve, such as 1 3X, and / or a high surface area active oxide, such as S e 1 e X ο 1 · d CD (A1 c 〇a tradename) ° Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs. In another specific example, the first bed is the third with selective removal of both water and methanol. 6 A molecular shop. This bed is followed by one or more 1 X or activated alumina beds, as described above. If desired, the sorbent bed can be operated at room temperature or at elevated temperatures, regardless of upward or downward flow. The regeneration of the sorbent material can be carried out by conventional methods which include treatment with a dry inert gas (eg nitrogen) at high temperature. In a liquid drying system, a water absorbent is used to remove water from the first part. The water absorbent can be any liquid that is effective in removing water from the hydrocarbon stream. This paper is sized to the Chinese National Standard (CNS) A4 (210 X 297 mm) 575559 A7 _ B7 V. Description of the invention (33). Preferably, the water absorbent is the same as previously described. Preferably, the olefin from the adsorption bed contains less than about 1000 wppm of water ', more preferably less than about 10 wppm, and most preferably less than about 1 wppm. Preferably ' less than about 1 Owppm of dimethyl ether is present in the stream leaving the adsorption bed, more preferably less than about 5 w p p m, and most preferably less than about 1 w p p m. The ethylene and propylene streams processed and separated in accordance with the present invention can be polymerized to form plastic compositions such as polyolefins, particularly polyethylene and polypropylene. Any conventional method for forming polyethylene or polypropylene may be used. Catalytic methods are preferred. Particularly preferred are metallocene, Zieg / Natta, chromium oxide and acid catalyst systems. References, for example, US 3,25 8,45 5 + 3,305,5 38, 3,364,190, 5,892,079, 4,659,685, 4,076,698, 3,645,992, 4,302,5 65, and 4,243,691, the catalyst and method descriptions of each article are clearly described This article is incorporated by reference. Generally, these methods involve contacting an ethylene or propylene product with a polyolefin-forming catalyst at an effective pressure and temperature to form a polyolefin product. In one embodiment of the invention, the ethylene or propylene product is contacted with a metallocene catalyst to form a polyolefin. Desirably, the method of forming a polyolefin is carried out at a temperature ranging from about 50 ° C to about 3 20 ° C. The reaction can be carried out at any low, medium or high pressure ranging from about 1 bar to about 3200 bar. For carrying out the method in solution, an inert diluent can be used. In this type of operation, it is desirable to have a pressure range from about 10 bar to about 150 bar, and a preferred temperature range from about 120 ° C to about 250 ° C. For the gas phase method, it is preferable that the temperature is usually in the range of about 60 ° C to 120 ° C, and the operating pressure is from about 5 b a 1 · to 50 0 b a 1 ·. (Please read the notes on the back before filling this page).  Printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, the Consumer Cooperatives printed the paper standard applicable to the Chinese National Standard (CNS) A4 specification (210X297 mm) 575559 A7 Printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, the Consumer Cooperatives printed B7 ^ " " " " One · ——— One -—— —--_____--------------- —--________ V. Description of the Invention (34) In addition to polyolefins, many other olefins Derivatives can be formed from the ethylene, propylene, and C4 + olefins, especially butene, isolated according to the present invention. The olefins isolated according to the present invention can be used to make such compounds, such as' aldehydes, acids such as C2-Cm monocarboxylic acids, alcohols such as C2-C " monoalcohols, C2-C " monocarboxylic acids and C2-C〗 2 Ester, linear alpha olefin, vinyl acetate, ethylene dichloride and ethylene chloride, ethylbenzene, ethylene oxide, cumene, acrolein, allyl chloride , Propylene oxide, acrylic acid, ethylene-propylene rubber and acrylonitrile, and terpolymers and dimers of ethylene and propylene. C4 + _ hydrocarbons, especially butene, are particularly suitable for the production of aldehydes, acids, alcohols, esters and linear alpha olefins made from C5-C! 3 monocarboxylic acids and monoalcohols. An example of the separation of dimethyl ether from an olefin stream is shown in FIG. This example demonstrates one way to obtain an ethylene and propylene stream that has substantially removed dimethyl ether and C% + components. However, the common factor of the present invention is that the dimethyl ether and C4 + components are largely removed from the stream containing ethylene and / or propylene before the caustic treatment. This means that both ethylene and propylene can be recovered in the first part, and dimethyl ether and c% + can be recovered in the second part. The propane present in the olefin stream can be recovered in the first or second part, depending on how low the dimethyl ether concentration in the first part is desired. Both ethylene and propylene can be recovered and further processed, for example, caustic scrubbing or water scrubbing, together or separately and separately. Fig. 1 shows a specific example in which an olefin to be treated is prepared in an oxygenated oxygen to olefin reaction system. In the figure, methanol is transported to a reactor 102 for converting oxygenates to olefins via a transfer pipe '100, where the methanol is converted to containing methane, ethylene, ethane, propylene, propane, and dimethyl ether. Paper size applies Chinese National Standard (CNS) A4 specification (210X297 mm) ----- clothing-m ·-(please read the precautions on the back before filling this page) Order f 575559 A7 B7 V. Description of the invention (35) (Please read the notes on the back before filling this page), olefin flow of C4 + component, water and other hydrocarbon components. The olefin stream is conveyed to the quench tower 106 via a conveying pipe 104, in which the olefin is cooled and water and other condensable components are condensed. The condensed component containing a large amount of water is extracted from the quench tower 106 via the bottom duct 108. A part of the condensed components is circulated back to the top of the quench tower 106 via the transfer pipe 110. The transfer pipe 110 contains a cooling unit, such as an exchanger (not shown), to further cool the condensed component ' to provide a cooling medium to further cool the component in the quench tower 106. The olefin vapor leaves the top of the quench tower 106 via the transfer pipe 112. The olefin vapor is compressed in the compressor 114, and the compressed olefin is transported to the water absorption pipe string 118 via a transfer pipe 116. In this specific example, methanol acts as a water absorbent, and is fed to the top of the water absorption pipe string 118 via a transfer pipe 120. Methanol, taken water, and some charged oxidized hydrocarbons' are separated into a bottom stream via a transfer pipe 1 2 2. The olefin is recovered via a transfer pipe 124. Arbitrarily, the olefin is sent to another compressor (not shown), and is then fed into the distillation column 126 °. The distillation column 126 printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs is produced from dimethyl ether and contains C4 + ingredients and from Ethylene and propylene and lower boiling point components were separated from the higher boiling point components of methanol remaining in the methanol washing. Additional methanol is added to the distillation column 126 via the transfer line 125 to reduce inclusions and / or free water structures in the distillation column. The stream containing ethylene and propylene leaves the distillation column 12 26 through the transfer pipe 1 28, and the higher boiling point components containing dimethyl ether and Cd components leave the distillation column 126 through the transfer pipe 1 30. Figure 2 shows the subsequent processing and drying of the logistics containing ethylene and propylene. The paper size is in accordance with the Chinese National Standard (CNS) Λ4 specification (210X 297 mm) 575559 M ______ B7 V. Description of the invention (36). Ethylene and propylene flow to the caustic decontamination tubing column 200 via a conduit 1 28. The caustic solution is conveyed to the top of the caustic decontamination column 200 via the conveying pipe 202 to remove CCh. Co2 is also contained in the stream containing ethylene and propylene. The used caustics exits the caustic decontamination tubing via the transfer tube 204. The caustic treated ethylene and propylene leave the caustic decontamination column 200 via the conveying pipe 206 to the water decontamination column 208. Water enters the water washing column through the conveying pipe 210, and water and absorbed components leave the water washing column 208 through the conveying pipe 2 1 2. The water-washed ethylene and propylene leave the water-washing pipe column 208 through the conveying pipe 214 and pass through the dryer 216. The dried ethylene and acrylic strips leave the dryer 216 via a transfer tube 218. Now that the present invention has been fully described, those skilled in the art will understand that the present invention can be implemented within a wide range of parameters within the scope of the patent application, without departing from the spirit and scope of the present invention. (Please read the precautions on the back before filling this page} Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs

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Claims (1)

575SS9- A8 B8 C8 D8 Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 6. Application for patent scope 1 1. A method for separating dimethyl ether from an olefin stream, including: providing a solution containing ethylene, ethane, propylene, propane An olefin stream of dimethyl ether; and the olefin stream is divided into a first part and a second part at a pressure of at least 1,480 kPa, wherein the first part contains at least most of the ethylene and propylene present in the olefin stream, and the second part contains At least most of the dimethyl ether is present in the olefin stream. 2. The method of claim 1 in which the olefin stream provided additionally includes water not exceeding 15,000 wpm. '3. The method according to the scope of the patent application, wherein the water is present in an amount of at least 10 wppm 〇' 4. The method according to the scope of the patent application, wherein the olefin stream provided additionally comprises at least 50 wppm Dimethyl ether. 5. As the method of applying for the scope of the first item of the patent, the pressure is from ι, 480 · kPa to 2,100 kPa 〇6. As the method of applying for the scope of the fifth item of the patent, the pressure is from ι, 825 kPa to 2 100 kPa 〇7. The method according to item 1 of the patent application range, wherein the provided smoke stream contains not more than 50% by weight of dimethyl ether. 8. The method of claim 1 in the scope of the patent application, wherein the first part comprises at least most of the propane present in the olefin stream. 9. The method according to item 1 of the patent application scope, wherein the first part includes a Dimethyl @ 迷 that is not greater than 100 wppm. 10 · If the method of applying for the first item of the patent scope, the second part contains (please read the precautions on the back before filling this page) ----------:-, I _ 装 --- --- Order -----: #j This paper size applies to the Chinese National Standard (CNS) A4 specification (210 X 297 mm) -40- 575559 A8 B8 C8 ___ D8 VI. The scope of patent application 2 exists in the olefin stream At least most of the propane. (Please read the notes on the back before filling out this page) 11 · If the method of patent application No. 1 method, the olefin stream is divided into the first part and the second part in the distillation column. 12. A method according to claim 11 in which a water absorbent is added to the distillation column. 1 3 · The method according to item 11 of the patent application, wherein the average temperature of the second part is not greater than 250 ° F. 14 · The method as claimed in item 13 of the patent application, wherein the average temperature of the second part is not greater than 240 ° F. · 1 · The method according to item 14 in the scope of patent application, wherein the average temperature of the second part is not greater than 230 ° F. 〇1 6 · The method according to item 12 in the scope of patent application, wherein the water absorbent absorbs water. The mole ratio of the agent to the total olefin stream to be separated was added from the steaming crane column from 4: 1 to 1: 5,000. 1 7. The method of claim 1 in which the olefin stream provided comprises from 50% to 95% by weight of ethylene and propylene. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 1 8. The method according to item 1 of the scope of patent application, wherein the olefin stream provided contains from 25% to 75% by weight of ethylene. 19. The method of claim 1, wherein the olefin stream provided comprises from 25% to 75% by weight of propylene. 20. The method of claim 1 in which the olefin stream provided additionally includes Co2 ' and the first part contains at least most of Co in the provided olefin stream. 21. For the method of applying for the scope of patent application item 20, it also includes the first paper size applicable to the Chinese National Standard (CNS) A4 (210X297 mm) _ 41-Printed by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs 575559 Sixth, the scope of patent application 3 part of the acid gas. 2 2 The method of claim 1 in the scope of patent application, wherein the olefin stream provided additionally includes a C4 + hydrocarbon component, and the second portion additionally includes at least a majority of the C4 + hydrocarbon component in the provided olefin stream. 23. The method according to item 1 of the scope of patent application, further comprising separating ethylene and propylene in the first part, and polymerizing ethylene. 24. The method according to item 1 of the scope of patent application, further comprising separating ethylene and propane in the first part, and polymerizing propane. 2 5 · The method according to item 12 of the scope of patent application, further comprising contacting the first part with water, treating the first part with water with an acid gas, and drying the first part treated with an acid gas. 26. A method of separating dimethyl ether from an olefin stream, comprising: contacting an oxygenate with a molecular sieve catalyst to form an olefin stream, wherein the olefin stream comprises ethylene, ethane, propylene, propane, and dimethyl ether; and At a pressure of at least 1,480 kPa, the olefin stream is divided into a first part and a second part, where the first part contains at least a majority of the ethylene and propylene present in the olefin stream, and the second part contains at least a majority of the olefin stream Dimethyl ether. 27. If applying, please apply the method of item 26 of the patent, further comprising contacting an olefin stream formed by contacting an oxygenate with a molecular sieve catalyst with a water absorbent before dividing the olefin stream into the first part and the second part. 2 8 · The method according to item 27 of the scope of patent application, in which the water absorbent uses a molar ratio of water absorbent to the total olefin ratio of 1: 2 to 1: 200 and contacts the olefin stream (please read the note on the back first) (Fill in this page again) This paper size applies to Chinese National Standard (CNS) A4 specification (210X297 mm) -42-575559 A8 B8 C8 D8 VI. Application for patent scope 4 29. If the method of item 26 of the patent scope is applied, the contact with water absorbent The hydrocarbon burning stream contains no more than 1 5,000 wppm water. (Please read the notes on the back before filling out this page) 3 0. The method of claim 26 in which the olefin stream in contact with the water absorbent contains at least 500 wppm of dimethyl ether. 3 1. The method according to item 26 of the patent application, wherein the pressure is from 1,480 kPa to 2,100 kPa 〇, 3 2. The method according to item 31 of the patent application, wherein the pressure is from 1,825 kPa to 2,100kPa. 3 3 · The process according to item 26 of the patent application, wherein the first part contains at least a large part of the propane present in the olefin stream. 34. The method of claim 26, wherein the first part contains dimethyl ether not greater than 100 w p p m. 35. The method as claimed in item 26 of the patent application, in which the second part contains the third house which is present in at least the majority of the olefin stream. 36. The method of claim 26, wherein the olefin stream is divided into a first part and a second part in a distillation column. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 37. For the method of applying for item 36 in the scope of patent application, the water absorbent is added to the steam column. 38. The method according to item 36 of the patent application, wherein the average temperature of the second part is not greater than 250 ° F. 39. The method of claim 38, wherein the average temperature of the second part is not greater than 240 ° F. 40. The method of claim 39, wherein the average temperature of the second part is not greater than 230 ° F. This paper size applies Chinese National Standard (CNS) A4 specification (210 x 297 mm) -43-575559 8 8 8 8 ABCD 々, patent application scope 5 (Please read the precautions on the back before filling this page) 41 · If applying for a patent The method of item 37, wherein the water absorbent is added to the distillation column with a molar ratio of the water absorbent to the total olefin stream to be separated from 4: 1 to 1: 5,00. 4 2 · The method according to item 26 of the patent application scope, wherein the olefin stream provided additionally comprises CO2, and the first part additionally comprises at least most of the CO2 in the provided olefin stream. 4 3 · The method according to item 42 of the patent application scope, further comprising treating the first part with an acid gas. 44. The method of claim 26, wherein the olefin stream provided additionally includes a C4 + hydrocarbon component, and the second portion additionally includes at least a majority of the C4 + hydrocarbon component in the provided olefin stream. 4 5 · The method of item 26 of the patented vehicle E, including the separation of ethylene and propylene in the first part, and the polymerization of ethylene. 4 6. The method in item 1 of patent application No. 26, which additionally includes separating ethylene and propylene in the first part, and polymerizing propylene. Printed by the Consumers' Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs 4 7 · If the method of applying for patent No. 26 is applied, it also includes contacting the first part with water, treating the first part that has been in contact with water with acid gas, and drying and receiving acid The first part of the gas treatment. 48 · A method for separating dimethyl ether from an olefin stream, comprising: contacting an oxygenate with a molecular sieve catalyst to form an olefin stream, wherein the olefin stream includes ethylene, ethane, propylene, propane, dimethyl ether, and water; Remove water from the olefin stream so that the olefin stream contains no more than 15,000 wppm of water; and at a pressure of at least 1,480 kPa, make less than 1 5,000 wppm water. Standard (CNS) A4 specification (210X297 mm) -44-575559 AB3CD 々, patent application scope 6 (Please read the notes on the back before filling this page) The olefin flow is divided into the first part and the second part, where the first part contains At least most of the ethylene and propylene present in the olefin stream, and the second portion contains at least most of the dimethyl ether present in the olefin stream. 49. The method of claim 48, wherein water is removed from the olefin stream by contacting the olefin stream with a water absorbent with a molar ratio of water absorbent to the total olefin of 1: 2 to 1: 200. Remove it. 50. The method of claim 48, wherein the olefin is divided into a first part and a second part in a distillation column. 51. The method of claim 50, wherein a water absorbent is added to the distillation column. 5 2 · The method according to item 51 of the scope of patent application, wherein the water absorbent, the molar ratio of the water absorbent to the total olefin stream separated from the paper from 4: 1 to 1: 5,000, is added to the distillation column . 53. The method of claim 52, wherein the olefin stream is separated at a pressure of from 1,480 kPa to 2,100 kPa. Printed by the Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 5 4 · If the method in the scope of patent application No. 48 is applied, the olefin stream provided additionally includes CO2, and the first part is also included in the provided olefin stream at least. Partial CO2. 55. The method according to item 54 of the patent application, further comprising treating the first part with an acid gas. 56. The method of claim 48, wherein the olefin stream provided additionally includes a C4 + hydrocarbon component, and the second portion additionally includes at least a majority of the C4 + hydrocarbon component in the provided olefin stream. 5 7 · If the method of item 48 of the scope of patent application is applied, it also includes the application of the Chinese National Standard (CNS) A4 specification (210 X 297 mm) in the first paper size. 575559 A8 B8 C8 ______ D8 6. The scope of patent application Separate ethylene and propylene in 7 minutes, and polymerize ethylene. 58 • The method under the scope of patent application, which additionally includes separating ethylene and propylene in the first part, and polymerizing acrylic. 5 9. The method of claim 50 in the scope of patent application, further comprising contacting the first part with water, treating the first part with water with an acid gas, and drying the first part treated with the acid gas. 60. A method of separating dimethyl ether from an olefin stream, comprising: providing an olefin stream containing ethylene, ethane, propylene, propane, and dimethyl ether; and dividing the olefin stream into at least a majority of the olefin stream The first part of ethylene and propylene, and the second part containing at least most of the dimethyl ether present in the olefin stream, where the olefin stream is separated at a pressure of at least 1,480 kPa, and the average temperature of the second part is not greater than 250 ° F. 61. The method of claim 60, wherein the olefin stream is divided into a first part and a second part in a steam-saturated 'column. 62. The method according to item 61 of the application, wherein the water absorbent is forced to the distillation column. 63. The method of claim 60, wherein the average temperature of the second part is not greater than 240 ° F. 64. The method of claim 63, in which the average temperature of the second part is not greater than 230 ° F. 65. The method according to item 62 of the patent application, wherein the water absorbent's molar ratio of the water absorbent to the total olefin stream to be separated from 4: 1 to 1: 5,000,000 is added to the distillation Tubing. This paper size applies to China National Standard (CNS) A4 specification (210X297 mm) -46-(Please read the notes on the back before filling this page), tT printed by the Intellectual Property Bureau of the Ministry of Economic Affairs, Consumer Cooperatives 575559 A8 B8 C8 D8 VI. Patent application range 8 " 6 6 · The method of item 61 of the patent application range of Rushen i, where j: Greek hydrocarbon stream is separated at a pressure from 1,4 80 kPa to 2,100 kPa . (Please read the notes on the back before filling out this page) 67 · If the method of applying for the scope of patent No. 60, the olefin stream provided additionally includes C 0 2 and the first part is additionally included in the provided olefin stream at least Most of Co2. 68. The method of claim 67, further comprising treating the first part with an acid gas. 69. The method of claim 60, wherein the provided olefin stream additionally includes a C4 + hydrocarbon component, and the second portion additionally contains at least a majority of the Cd hydrocarbon component in the provided olefin stream. 70 • The method according to item 60 of the scope of patent application, further comprising separating ethylene and propylene in the first part, and polymerizing ethylene. 7 1 · The method according to item 60 of the scope of patent application, further comprising separating ethylene and propylene in the first part, and polymerizing propylene. 72. The method of claim 61, further comprising contacting the first portion with water, treating the first portion with water with an acid gas, and drying the first portion treated with the acid gas. 73. A method for separating dimethyl ether from an olefin stream by the Consumer Cooperative of the Intellectual Property Bureau of the Ministry of Economic Affairs, including: providing an olefin stream containing ethylene, ethane, propylene, propane, propadiene and dimethyl ether; And dividing the olefin stream into a first part containing at least most of the ethylene and propylene present in the olefin stream, and a second part containing at least most of the dimethyl ether and propadiene present in the olefin stream, wherein the olefin stream is under pressure Separated at least 1,480 kPa, and the average temperature of the second part is not greater than 250 ° F. ^ Zhang scale is applicable to China National Standard (CNS) A4 specification (210X297 mm) -47-Printed by the Employee Consumer Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs 575559 A8 B8 C8 D8 ___ VI. Patent Application Range 9 74. The method of item 73, wherein the olefin stream is divided into a first part and a second part in the distillation column. 75. The method of claim 74, wherein a water absorbent is added to the distillation column. 76. The method of claim 74, wherein the average temperature of the second part is not greater than 240 ° F. 77. The method of applying scope 76 of the patent application, wherein the average temperature of the second part is not greater than 230 ° F. 78. The method of claim 75, wherein the water absorbent is added to the steamed salt column with a molar ratio of the water absorbent to the total olefin stream to be separated from 4: 1 to 1: 5,000. 79. The method of claim 74, wherein the olefin stream is separated at a pressure of from 1,480 kPa to 2,100 kPa. 80. The method of claim 73, wherein the olefin stream provided additionally comprises CO2, and the first part additionally comprises at least a majority of CO2 in the provided olefin stream. 8 1 · The method according to item 80 of the scope of patent application, further comprising treating the first part with an acid gas. 82. The method of claim 73, wherein the olefin stream provided additionally includes a C4 + hydrocarbon component, and the second portion additionally includes at least a majority of the C4 + hydrocarbon component in the provided olefin stream. 8 3 · The method according to item 73 of the scope of patent application, further comprising separating ethylene and propylene in the first part, and polymerizing ethylene. 84. If you apply for the method of item 73 of the patent scope, it also includes the application of the Chinese National Standard (CNS) A4 specification (210 X 297 mm) in the first paper size. -48-(Please read the precautions on the back before filling (This page) 575559 A8 B8 C8 D8 VI. Patent application scope 10 points to separate ethylene and propylene, and polymerize propylene. 85. The method of claim 74, further comprising contacting the first part with water, treating the first part with water with an acid gas, and drying the first part with acid gas. (Please read the precautions on the back before filling in this tribute) Printed by the Employees' Cooperatives of the Intellectual Property Bureau of the Ministry of Economic Affairs This paper is sized to the Chinese National Standard (CNS) A4 (210X297 mm) -49-