CN109336726B - Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol - Google Patents
Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol Download PDFInfo
- Publication number
- CN109336726B CN109336726B CN201811440587.2A CN201811440587A CN109336726B CN 109336726 B CN109336726 B CN 109336726B CN 201811440587 A CN201811440587 A CN 201811440587A CN 109336726 B CN109336726 B CN 109336726B
- Authority
- CN
- China
- Prior art keywords
- reaction
- enters
- reactor
- cracking
- catalytic cracking
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 88
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 37
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 title claims abstract description 22
- 229910052799 carbon Inorganic materials 0.000 title claims abstract description 22
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 17
- HQQADJVZYDDRJT-UHFFFAOYSA-N ethene;prop-1-ene Chemical group C=C.CC=C HQQADJVZYDDRJT-UHFFFAOYSA-N 0.000 title claims abstract description 12
- 230000008878 coupling Effects 0.000 title claims abstract description 11
- 238000010168 coupling process Methods 0.000 title claims abstract description 11
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 11
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 53
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 53
- 239000002994 raw material Substances 0.000 claims abstract description 52
- 238000005899 aromatization reaction Methods 0.000 claims abstract description 37
- 238000000926 separation method Methods 0.000 claims abstract description 21
- 238000011069 regeneration method Methods 0.000 claims abstract description 20
- 238000000034 method Methods 0.000 claims abstract description 19
- 230000008569 process Effects 0.000 claims abstract description 14
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 10
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 10
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 10
- 125000004432 carbon atom Chemical group C* 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 90
- 238000005336 cracking Methods 0.000 claims description 44
- 238000006243 chemical reaction Methods 0.000 claims description 41
- 239000003054 catalyst Substances 0.000 claims description 39
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 26
- 238000010521 absorption reaction Methods 0.000 claims description 26
- 239000007795 chemical reaction product Substances 0.000 claims description 23
- 239000003381 stabilizer Substances 0.000 claims description 22
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims description 17
- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 claims description 17
- 230000008929 regeneration Effects 0.000 claims description 17
- 238000010438 heat treatment Methods 0.000 claims description 16
- 239000000047 product Substances 0.000 claims description 15
- 239000001294 propane Substances 0.000 claims description 15
- BZLVMXJERCGZMT-UHFFFAOYSA-N Methyl tert-butyl ether Chemical compound COC(C)(C)C BZLVMXJERCGZMT-UHFFFAOYSA-N 0.000 claims description 13
- 230000000087 stabilizing effect Effects 0.000 claims description 12
- 239000001273 butane Substances 0.000 claims description 11
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 claims description 11
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 claims description 11
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 claims description 10
- 238000005261 decarburization Methods 0.000 claims description 10
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 9
- 239000005977 Ethylene Substances 0.000 claims description 9
- 239000000203 mixture Substances 0.000 claims description 9
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 8
- 238000002156 mixing Methods 0.000 claims description 8
- 239000002184 metal Substances 0.000 claims description 6
- 239000002808 molecular sieve Substances 0.000 claims description 6
- 229910052755 nonmetal Inorganic materials 0.000 claims description 6
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 6
- 230000006641 stabilisation Effects 0.000 claims description 6
- 238000011105 stabilization Methods 0.000 claims description 6
- 230000015572 biosynthetic process Effects 0.000 claims description 5
- 238000002360 preparation method Methods 0.000 claims description 5
- 238000003786 synthesis reaction Methods 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 4
- 239000000571 coke Substances 0.000 claims description 3
- 230000000694 effects Effects 0.000 claims description 3
- 230000009471 action Effects 0.000 claims description 2
- 230000001808 coupling effect Effects 0.000 claims description 2
- 238000007323 disproportionation reaction Methods 0.000 claims description 2
- 238000005194 fractionation Methods 0.000 claims description 2
- 239000001257 hydrogen Substances 0.000 claims description 2
- 229910052739 hydrogen Inorganic materials 0.000 claims description 2
- 125000004435 hydrogen atom Chemical class [H]* 0.000 claims description 2
- 230000000977 initiatory effect Effects 0.000 claims description 2
- 238000006317 isomerization reaction Methods 0.000 claims description 2
- 239000003915 liquefied petroleum gas Substances 0.000 claims description 2
- 230000001105 regulatory effect Effects 0.000 claims description 2
- 238000011049 filling Methods 0.000 claims 1
- 238000005086 pumping Methods 0.000 claims 1
- 238000006276 transfer reaction Methods 0.000 claims 1
- 238000010992 reflux Methods 0.000 description 29
- 239000003921 oil Substances 0.000 description 11
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 10
- 238000003795 desorption Methods 0.000 description 9
- 238000000605 extraction Methods 0.000 description 9
- 239000007788 liquid Substances 0.000 description 9
- 239000007791 liquid phase Substances 0.000 description 9
- 238000005262 decarbonization Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 230000002745 absorbent Effects 0.000 description 2
- 239000002250 absorbent Substances 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000006356 dehydrogenation reaction Methods 0.000 description 2
- 239000003546 flue gas Substances 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 description 2
- 238000004227 thermal cracking Methods 0.000 description 2
- 150000001335 aliphatic alkanes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000010692 aromatic oil Substances 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- KOYGZROXUOTUEE-UHFFFAOYSA-N butane;but-1-ene Chemical compound CCCC.CCC=C KOYGZROXUOTUEE-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000007233 catalytic pyrolysis Methods 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000013067 intermediate product Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Natural products C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 1
- -1 naphtha Chemical class 0.000 description 1
- 238000005839 oxidative dehydrogenation reaction Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
- C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
- C07C2/864—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an alcohol
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2529/00—Catalysts comprising molecular sieves
- C07C2529/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
- C07C2529/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- C07C2529/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil (containing naphtha, stable light hydrocarbon, straight-run gasoline, raffinate oil, gasoline and the like) and methanol. The process comprises a raw material pretreatment unit, a catalytic cracking reaction-regeneration unit, a separation unit and a dry gas aromatization unit. The invention mainly solves the problem of heat coupling in the process of preparing propylene ethylene by catalytic cracking of light oil with four carbon atoms and preparing propylene ethylene by methanol, realizes the comprehensive utilization of various raw materials and can ensure the continuity of production. The invention can be used in industrial devices for producing propylene ethylene, can relieve the contradiction between supply and demand of propylene and can improve the economic benefit of petrochemical enterprises.
Description
Technical Field
The invention relates to a process for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol, which is applied to the field of petrochemical industry.
Background
Propylene is always in a scarce state as an important chemical raw material, the price is very high, and along with the increasing shortage of petroleum resources, raw materials for preparing propylene are also becoming more rare. Generally, the propylene is obtained by adopting the methods of naphtha cracking, catalytic cracking, propylene preparation from methanol, propane dehydrogenation and the like in industry. In recent years, research on propylene production by butene cracking has been paid attention to, but due to limited sources, it has not been applied to industry on a large scale.
The naphtha thermal cracking is a common and traditional method for preparing ethylene and simultaneously producing propylene by a byproduct, the thermal cracking method is adopted for preparing ethylene and propylene, and according to the reaction mechanism of free radicals, the high temperature of more than 800 ℃ is needed, and the proportion of propylene in the product is low, so researchers hope to improve the propylene yield by adopting a catalytic cracking method according to a carbocation mechanism, reduce the energy consumption, and the current catalytic cracking temperature is about 500-600 ℃ and the propylene yield is about 15-38%.
CN102603457B discloses a device and process for deep processing of liquefied gas for producing propylene from C3 and C4. The process mainly comprises the following steps: the device comprises a cracking unit, an absorption stabilizing unit, a gas separation unit and a dehydrogenation unit. The method comprises the steps of sending a raw material liquefied gas containing propane and butane and a liquefied gas rich in butene to a butene cracking unit for producing propylene, preparing propylene and a butene unit by oxidative dehydrogenation of butane and propane, generating propylene and butene through high-temperature reaction under the action of a catalyst, sending the propylene to an absorption stabilizing and gas separating unit for finally obtaining refined propylene, and sending the butene as an intermediate product to the butene cracking unit for cracking to generate propylene.
CN101844960B discloses a method for producing propylene by catalytic cracking of liquefied gas, which comprises the steps of carrying out pretreatment such as depropanization, extraction rectification and the like on common civil liquefied gas, then carrying out heat exchange with a reaction product, heating to 500-600 ℃, carrying out cracking reaction under the conditions of 0.4MPa and weight airspeed of 0.8h -1, carrying out heat exchange cooling on the reaction product, and then carrying out absorption, stabilization and other systems to obtain the liquefied gas rich in high-octane gasoline and propylene and butylene.
CN107355508B discloses a process for preparing hydrocarbon by using liquefied gas, which comprises a cracking reaction system, an absorption stabilization system, an aromatization reaction system, a gas separation raw material gas concentration system and an aromatic hydrocarbon purification system.
Disclosure of Invention
The invention aims to thermally couple the reactions in the preparation of propylene ethylene by catalytic pyrolysis of light oil and propylene ethylene by methanol, is convenient for controlling the reaction temperature, and is suitable for various raw materials.
The technical problems to be solved by the invention are realized by adopting the following technical scheme:
a process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol is specifically characterized by comprising the following steps:
the raw material C four enters a pretreatment unit, light components such as propylene, propane and the like contained in the C four are distilled out from the top of the tower through a decarburization three tower and are sent to a deethanizer of a gas separation system; and light hydrocarbon components with four or more carbon atoms are used as raw materials for catalytic cracking reaction and enter a cracking reaction system.
The pretreated carbon four is mixed with light oil and methanol, the mixture is pumped into a preheater of a catalytic cracking reaction unit by a feed pump, the temperature is increased, then the mixture is heated to the reaction initiation temperature of 450-650 ℃, the high-temperature mixed raw material enters a cracking catalyst bed layer from the top of a cracking reactor to carry out reactions such as cracking, hydrogen transfer, disproportionation and aromatization, the catalytic cracking reaction of the carbon four and the light oil is mainly carried out with heat absorption, and the reaction of the methanol to propylene ethylene is mainly carried out with heat release. The coupling effect of the two reaction heat effects can be adjusted by adjusting the proportion of raw materials, so that the temperature of the bed layer is controlled. The reaction product flows out of the bottom of the reactor and enters the raw material preheater to provide heat for the reaction product. The catalytic cracking catalyst in the process gradually grows coke after a period of reaction, and a regeneration system is required to regenerate the catalyst in the process, and has two functions: firstly, the catalyst provides regeneration service for the cracking catalyst containing carbon, and secondly, the catalyst provides regeneration service for the aromatization catalyst containing carbon. Both catalysts are metal or nonmetal modified catalysts based on ZSM-5 molecular sieve, and the scorch temperature ranges from 380 ℃ to 520 ℃. The regeneration process flow is as follows: mixing air and nitrogen according to a certain proportion (the control range of the air content is 0-100V%), then pressurizing and preheating by a circulating gas compressor, heating to 380-520 ℃, and feeding into a catalyst bed from the top of a reactor for burning regeneration. In order to balance the heat of reaction, part of the regeneration air may enter the reactor directly from the side feed inlet of the reactor from the compressor outlet without passing through the furnace.
The two reaction products of the catalytic cracking reaction and the dry gas aromatization reaction are cooled and compressed and then enter a separation unit, the separation unit consists of an absorption stabilization system and a gas fractionation system, the reaction products firstly enter the absorption stabilization system, the dry gas in the products is absorbed, a part of the dry gas is discharged from the top of the absorption tower, and a part of the dry gas returns to the dry gas aromatization reactor. The liquefied gas component in the reaction product is desorbed, enters the stabilizing tower, and is discharged from the top of the stabilizing tower through rectification and is pumped to a gas separation system through pump pressurization. The cracking reaction product contains isobutene, and can enter a stabilizer along with liquefied gas components, a section of MTBE synthesis catalyst is arranged at the middle upper part of the stabilizer, and another raw material methanol for MTBE synthesis is fed from the middle part of the stabilizer and reacts with isobutene on the MTBE synthesis catalyst to generate MTBE, and the MTBE and gasoline come out of the bottom of the stabilizer together as gasoline blending components and are sent to a tank area. The liquefied gas from the stabilizer contains propylene, propane, butene, butane and a small amount of C2 components, and enters a gas separation system, propylene is purified in a propylene rectifying tower A, B according to the rectification principle, the purity can reach 99.7%, the purity of propane can reach more than 95%, butane and butene come out from the bottom of the depropanizer, a part of the butane and the butene are delivered to a tank area as products, and a part of the butane and the butene are returned to a cracking reactor to participate in the propylene preparation reaction by cracking the butene.
The dry gas coming out of the top of the absorption tower enters a dry gas aromatization unit, after being preheated, enters a heating furnace, is heated to the dry gas aromatization reaction temperature, and then enters an aromatization reactor from the top of the aromatization reactor, wherein the reactor is provided with side line feeding, the dry gas is subjected to superposition, aromatization, isomerization and other reactions on an aromatization catalyst bed layer to generate gasoline blending components with RON more than 94, liquefied petroleum gas and lean-olefin dry gas, and the reaction product flows out from the bottom of the reactor and enters a dry gas raw material preheater to provide heat for the dry gas, and is mixed with a catalytic cracking reaction product through a heat exchange device and enters a separation unit.
The process for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol is characterized by comprising the following steps of: the raw material light oil is light hydrocarbon (including naphtha, straight-run gasoline, raffinate oil, stable light hydrocarbon, gasoline and the like) which takes carbon five to carbon ten as a main component.
The process for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol is characterized by comprising the following steps of: the catalyst for cracking reaction is prepared with ZSM-5 molecular sieve as main component and through metal or non-metal modification, and has bulk density of 0.63-0.73 ton/cubic meter, reaction temperature of 450-650 deg.c, pressure of 0.1-1.0 MPa and airspeed of 0.1-5 h -1.
The process for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol is characterized by comprising the following steps of: the catalytic cracking reactor is a fixed bed and is divided into two or more sections to be filled, namely, two or more reaction areas are arranged, a propylene ethylene catalyst is prepared by catalytic cracking, and the number of the reactors is 2 or more than 2, so that the production continuity is ensured.
Drawings
FIG. 1 is a process flow diagram of a feedstock pretreatment unit, a catalytic cracking reaction-regeneration unit, a separation unit, and a dry gas aromatization unit of the present invention.
1-Raw material liquefied gas feeding tank, 2-raw material liquefied gas feeding pump, 3-decarbonization three-tower feeding preheater, 4-decarbonization three-tower, 5-decarbonization three-tower top cooler, 6-decarbonization three-tower top reflux tank, 7-decarbonization three-tower reflux pump, 8-decarbonization three-tower reboiler, 9-raw material methanol feeding tank, 10-raw material methanol feeding pump, 11-raw material C5C6 feeding tank, 12-raw material C5C6 feeding pump, 13-cracking raw material preheater, 14-cracking heating furnace, 15-cracking reactor, 16-cracking heating furnace, 17-cracking reactor, 18-cracking raw material preheater, 19-aromatization heating furnace, 20-aromatization reactor, 21-aromatization raw material preheater, 22-air cooler, 23-water cooler, 24-rich gas compressor, 25-rich gas water cooler, 26-liquid separating tank, 27-absorption tower and 28-desorption tower reboiler; 29-stabilizer feed pump, 30-stabilizer, 31-stabilizer overhead cooler, 32-stabilizer overhead reflux drum, 33-stabilizer overhead reflux drum, 34-stabilizer reboiler, 35-stabilizer bottom pump, 36-gasoline water cooler, 37-depropanizer feed heat exchanger, 38-depropanizer, 39-depropanizer overhead cooler, 40-depropanizer overhead reflux drum, 41-depropanizer overhead reflux drum, 42-depropanizer reboiler; 43-liquefied gas product water cooler, 44-deethanizer, 45-deethanizer overhead cooler, 46-deethanizer overhead reflux drum, 47-deethanizer overhead reflux pump, 48-deethanizer reboiler, 49-propylene rectifying tower A, 50-propylene rectifying tower A reboiler, 51-propane product pump, 52-propane product cooler, 53-propylene rectifying tower B bottom pump, 54-propylene rectifying tower B, 55-propylene rectifying tower B overhead cooler, 56-propylene rectifying tower B reflux drum; 57-propylene rectifying tower B reflux pump, 58-absorption tower middle section extraction cooler, 59-absorption tower middle section extraction reflux pump, 60-reaction product liquid separating tank, 61-reaction product liquid pump.
FIG. 2 is a flow chart of the regeneration system of the present invention.
62-Regenerated air water cooler, 63-recycle gas compressor inlet buffer tank, 64-recycle gas compressor.
Detailed Description
The invention will be further described with reference to the following detailed drawings, in order to facilitate understanding of technical means, authoring features, achieving objects and effects achieved by the invention.
The embodiment is a 30 ten thousand ton/year stable light hydrocarbon liquefied gas methanol catalytic cracking propylene preparation device built in a refinery, and the process comprises a raw material pretreatment unit, a catalytic cracking reaction-regeneration unit, a separation unit and a dry gas aromatization unit. The adopted process flow chart is shown in fig. 1, and the regeneration flow chart is shown in fig. 2.
The raw materials are stable light hydrocarbon, liquefied gas and methanol, and the properties of the raw materials are as follows:
table 1 stable light hydrocarbon properties of feedstock
| Carbon number | N-alkanes | Isoparaffin(s) | Total alkane |
| C3 | 0.3 | 0.0 | 0.3 |
| C4 | 2.5 | 2.2 | 4.7 |
| C5 | 9.6 | 4.6 | 14.2 |
| C6 | 15.6 | 6.2 | 21.8 |
| C7 | 17.4 | 8.9 | 26.2 |
| C8 | 15.1 | 10.2 | 25.3 |
| C9 | 1.3 | 6.1 | 7.5 |
| C10 | 0.0 | 0.1 | 0.1 |
| Sum total | 61.8 | 38.2 | 100.0 |
TABLE 2 liquefied gas Properties of raw materials
TABLE 3 raw methanol Properties
| Project | Properties of (C) |
| Purity of | ＞99.5％ |
| Molecular formula | CH3OH |
| Molecular weight | 32 |
| Density (0 ℃), g/ml | 0.8100 |
| Boiling point, DEG C | 64.6 |
| Specific heat, kcal/. Degree.C. Mol | 18.4 |
| Combustion heat, kcal/mol | 174 |
| Flash point, C | 9.5 (Closed), 16 (open) |
Raw material liquefied gas enters a raw material liquefied gas feeding tank (1) from a tank area or other units, is pressurized by a raw material liquefied gas feeding pump (2), enters a decarburization three-tower feeding preheater (3), enters a decarburization three-tower (4) after being preheated, and C3 and light components below enter a decarburization three-tower top cooler (5) after being rectified from the top, enter a decarburization three-tower top reflux tank (6) after being cooled to normal temperature, return C3 and light components below at normal temperature, a part of the light components returns to the tower top, and a part of the light components enter a depropanizer of a gas separation system. The C4 component mainly comprising butane and butene comes out from the bottom of the decarbonization three tower (4), enters the decarbonization three tower feeding preheater (3) for heat exchange, and then enters the catalytic cracking reaction system. The decarburization three tower (4) is provided with a decarburization three tower reboiler (8).
Raw material methanol enters a raw material methanol feeding tank (9) from a tank field, and is pressurized by a raw material methanol feeding pump (10) to enter a catalytic cracking reaction system.
Raw material C5C6 is sent to a raw material C5C6 feeding tank (11) from a tank area or other units, is pressurized by a raw material C5C6 feeding pump (12), is mixed with raw material methanol and butane butene at the bottom of a decarburization three tower (4), then enters a cracking raw material preheater (13) or (18), is preheated, enters a cracking heating furnace (16) or (19) after the temperature is increased to 450-650 ℃, then enters a cracking reactor (17) or (20), is reacted on a catalyst bed layer, reaction products come out from the bottom of the cracking reactor, enter the cracking raw material preheater (13) or (18) for heat exchange, then enter an air cooler (22) and a water cooler (23) in sequence, is cooled to normal temperature, then enters a reaction product liquid separating tank (60), is sent out from the top of the tank, enters a rich gas compressor (24), and is sent to a stabilizing tower (30) after being pressurized. The materials from the compressor pass through a rich gas water cooler (25), are cooled to normal temperature, and then enter a liquid separating tank (26) for liquid separation. The gas phase comes out from the top of the liquid separating tank (26), enters the absorption and desorption tower (27), and the liquid phase comes out from the bottom of the liquid separating tank (26), is pressurized by the stabilizing tower feeding pump (29), and enters the stabilizing tower (30).
The absorbent of the absorption and desorption tower (27) is gasoline coming out from the bottom of the stabilizing tower (30), and is sent to the top of the absorption and desorption tower (27) by a stabilizing tower bottom pump (35) after being cooled. The absorption and desorption tower (27) is provided with a middle-section extraction reflux, and after the middle-section extraction liquid is extracted from the side part of the tower, the middle-section extraction reflux enters an absorption tower middle-section extraction cooler (58), the temperature is cooled to 35 ℃, and the middle-section extraction reflux enters an absorption tower middle-section extraction reflux pump (59) to be pressurized and then returns to the tower. The absorption/desorption column (27) is provided with a desorption column reboiler (28). And the dry gas is discharged from the top of the tower, a part of the dry gas is discharged from the device, a part of the dry gas enters the dry gas aromatization unit, and the mixed aromatic oil at the bottom of the tower enters the stabilizer (30).
The middle part of the stabilizer (30) is provided with a section of MTBE synthetic catalyst, methanol is fed from the middle part of the stabilizer, and is subjected to synthetic reaction with isobutene in liquefied gas on the MTBE catalyst, and the generated MTBE is mixed with gasoline at the bottom of the stabilizer and is discharged out of the device. The bottom of the tower is provided with a stabilizer reboiler (34). The liquefied gas component is rectified from the top of the tower, passes through a stable tower top cooler (31), is cooled to normal temperature, enters a stable tower top reflux tank (32), the liquid phase component is discharged from the bottom of the stable tower top reflux tank (32), is pressurized by a stable tower top reflux pump (33), and one part of the liquid phase component is refluxed into the tower, and the other part of the liquid phase component enters a gas separation system. The gasoline comes out from the bottom of the tower, is cooled to normal temperature by a gasoline water cooler (36), and part of the gasoline is taken as a product outlet device and the other part of the gasoline is taken as an absorbent to enter an absorption and desorption tower (27).
And (3) preheating part of dry gas coming out of the top of the absorption and desorption tower (27) by an aromatization raw material preheater (21), then entering an aromatization heating furnace (19), raising the temperature to 160-350 ℃, entering an aromatization reactor (20), coming out of the bottom of the reactor, entering the aromatization raw material preheater (21), exchanging heat, and then mixing with a cracking reaction product and entering an air cooler (22).
C4 and following components from the decarburization three-tower reflux pump (7) and the stabilizing tower top reflux pump (33) are mixed and enter a depropanizer feeding heat exchanger (37) for preheating, then enter a depropanizer (38), C3 and following components are distilled out from the tower top, enter a depropanizer top cooler (39), enter a depropanizer top reflux tank (40) after the temperature is cooled to normal temperature, and enter a deethanizer (44) after being pressurized by a depropanizer top reflux pump (41). And the C4 component is discharged from the bottom of the tower, enters a depropanizer feeding heat exchanger (37) for heat exchange, one part returns to the cracking reactor, and the other part enters a liquefied gas product water cooler (43) and is discharged from the device after being cooled to normal temperature. C3 and following components enter a deethanizer (44), C2 and following components are distilled out from the top of the deethanizer, enter a deethanizer cooler (45), enter a deethanizer reflux tank (46) after being cooled to normal temperature, and gas phase exits from the top of the tank and enters a gas system. The liquid phase comes out of the bottom of the tank, is pressurized by a deethanizer overhead reflux pump (47), and enters a column for reflux, and the column is provided with a reboiler (48). The C3 component is discharged from the bottom of the deethanizer (44) and enters a propylene rectifying tower A (49), the propylene rectifying tower A (49) and a propylene rectifying tower B (54) are a set of distillation system, the two towers cooperate to complete the separation of propane and propylene, a reboiler (50) is arranged at the bottom of the propylene rectifying tower A (49), a gas phase at the top of the propylene rectifying tower A (49) enters a tower kettle of the propylene rectifying tower B (54), a liquid phase at the bottom of the propylene rectifying tower B (54) is discharged from the bottom of the tower, after being pumped by a tower bottom pump (53) of the propylene rectifying tower B, the gas phase at the top of the propylene rectifying tower B (54) enters a tower top cooler (55) of the propylene rectifying tower B, after being cooled to normal temperature, enters a reflux tank (56) of the propylene rectifying tower B, the liquid phase is discharged from the bottom of the tower, and after passing through the reflux pump (57) of the propylene rectifying tower B, part of the liquid phase is taken as a reflux to enter the tower, and the other part of the liquid phase is taken as a product propylene discharging device. The propane comes out from the bottom of the propylene rectifying tower A (49), passes through a propane product pump (51), enters a propane product cooler (52), is cooled to normal temperature, and enters a tank area.
After deactivation of the catalyst in one reactor, the reactor was cut into a regeneration system, which was operated as follows: air and nitrogen are regulated according to the range of 0-100% (V) of air ratio through respective flow meters, then enter a circulating gas compressor (64) for pressure increasing, then enter a cracking raw material preheater (13) or (18) or an aromatization raw material preheater (21), are preheated, then enter a cracking heating furnace (14) or (16) or an aromatization heating furnace (19) for temperature increasing to 380-480 ℃, then enter a cracking reactor (15) or (17) or an aromatization reactor (20), a burning reaction occurs on a catalyst bed layer, high-temperature regenerated flue gas comes out of the bottom of the reactor, enters the cracking raw material preheater (13) or (18) or the aromatization raw material preheater (21) for heat exchange, then enters a regenerated air water cooler (62) for temperature cooling to normal temperature, enters a circulating gas compressor inlet buffer tank (63), and the buffered regenerated air enters the circulating gas compressor (64) to form a circulating regeneration system with fresh air and nitrogen. The top of the circulating gas compressor inlet buffer tank (63) is provided with a vent, and redundant flue gas can be discharged from a top vent line.
The catalyst used in the cracking reaction is a ZSM-5 molecular sieve catalyst modified by metal or nonmetal, and the space velocity is 0.2-5 h -1. The single-pass period is 20-25 days, and the regeneration period is less than 7 days.
The catalyst adopted by the dry gas aromatization reactor is a metal or nonmetal modified ZSM-5 molecular sieve catalyst, and the space velocity is 0.5-3 h -1. The single-pass period is 60-90 days, and the regeneration period is less than 7 days.
By adopting the flow and the catalyst, the following product distribution is obtained:
| Sequence number | Product(s) | Composition (w)% | Description of the invention |
| 1 | Dry gas + loss + coke | 6 | |
| 2 | Propylene | 19 | |
| 3 | Propane | 5 | |
| 4 | Liquefied gas | 17 | |
| 5 | Gasoline | 53 | RON82 |
| Totals to | 100 |
The various devices used in the present invention are conventional devices used in the art production process, and the operating parameters of the devices and the like are performed according to conventional operations, without any particular limitation.
The foregoing has outlined and described the basic principles, features, and advantages of the present invention. It will be understood by those skilled in the art that the present invention is not limited to the foregoing embodiments, which have been described in the foregoing description merely illustrates the principles of the invention, and that various changes and modifications may be effected therein without departing from the spirit and scope of the invention as defined in the appended claims and their equivalents.
Claims (2)
1. A process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol is specifically characterized by comprising the following steps:
(1) The light component in the carbon four enters a pretreatment unit, is distilled out from the top of the tower through a decarburization three tower and is sent to a deethanizer of a gas separation system; light hydrocarbon components with four or more carbon atoms are used as raw materials for catalytic cracking reaction and enter a cracking reaction system;
(2) Mixing the pretreated carbon four, light oil and methanol, pumping the mixture to a preheater of a catalytic cracking reaction unit through a feed pump, increasing the temperature, then feeding the mixture into a heating furnace, heating the mixture to the reaction initiation temperature of 450-650 ℃, feeding the high-temperature mixed raw material into a cracking catalyst bed layer from the top of the cracking reactor, and carrying out cracking, hydrogen transfer, disproportionation and aromatization reactions, wherein the catalytic cracking reaction of the carbon four and the light oil is mainly carried out with heat absorption, and the reaction of the methanol to propylene and ethylene is mainly carried out with heat release; the coupling effect of the two reaction heat effects is regulated by adjusting the proportion of raw materials, so that the temperature of a bed layer is controlled; the reaction product flows out from the bottom of the reactor and enters a raw material preheater to provide heat for the reaction product; the raw material light oil is light hydrocarbon with five to ten carbon atoms as main components;
The catalytic cracking catalyst in the process gradually grows coke after a period of reaction, and a regeneration system is required to regenerate the catalyst in the process, and has two functions: firstly, providing a regeneration service for a cracking catalyst containing carbon, and secondly, providing a regeneration service for an aromatization catalyst containing carbon; both catalysts are metal or nonmetal modified catalysts based on ZSM-5 molecular sieve, and the scorch temperature ranges from 380 ℃ to 520 ℃; wherein the catalyst used in the cracking reaction is prepared by modifying ZSM-5 molecular sieve with metal or nonmetal, the bulk density is 0.63-0.73 ton/cubic meter, the reaction temperature is 450-650 ℃, the pressure is 0.1-1.0 MPa, and the airspeed is 0.1-5 h -1;
the regeneration process flow is as follows: mixing air and nitrogen according to a certain proportion, then pressurizing and preheating the mixture by a circulating gas compressor, heating the mixture to 380-520 ℃ by a heating furnace, and feeding the mixture into a catalyst bed from the top of a reactor for burning regeneration; in order to balance the reaction heat, part of regenerated air directly enters the reactor from a side feed inlet of the reactor from a compressor outlet without passing through a heating furnace; (3) The two reaction products of the catalytic cracking reaction and the dry gas aromatization reaction are cooled and compressed and then enter a separation unit, the separation unit consists of an absorption stabilization system and a gas fractionation system, the reaction products firstly enter the absorption stabilization system, the dry gas in the products is absorbed, a part of the dry gas is discharged from the top of the absorption tower, and a part of the dry gas returns to the dry gas aromatization reactor; the liquefied gas component in the reaction product is desorbed, enters a stabilizing tower, is discharged from the top of the stabilizing tower under the action of rectification, and is pressurized by a pump and sent to a gas separation system; the cracking reaction product contains isobutene, and enters a stabilizer along with a liquefied gas component, a section of MTBE synthesis catalyst is arranged at the middle upper part of the stabilizer, and another raw material methanol synthesized by MTBE is fed from the middle part of the stabilizer and reacts with the isobutene on the MTBE synthesis catalyst to generate MTBE, and the MTBE and gasoline come out of the bottom of the stabilizer together as gasoline blending components and are sent to a tank area; the liquefied gas from the stabilizer contains propylene, propane, butene, butane and a small amount of C2 components, and enters a gas separation system, propylene is purified in a propylene rectifying tower A, B according to the rectification principle, the purity can reach 99.7%, the purity of propane can reach more than 95%, butane and butene come out from the bottom of the depropanizer, a part of the butane and the butene are sent to a tank area as products, and a part of the butane and the butene are returned to a cracking reactor to participate in the propylene preparation reaction by cracking the butene;
(4) The dry gas coming out of the top of the absorption tower enters a dry gas aromatization unit, after being preheated, enters a heating furnace, is heated to the dry gas aromatization reaction temperature, and then enters an aromatization reactor from the top of the aromatization reactor, wherein the reactor is provided with side line feeding, the dry gas is subjected to superposition, aromatization and isomerization reactions on an aromatization catalyst bed layer to generate gasoline blending components with RON more than 94, liquefied petroleum gas and lean-olefin dry gas, and the reaction product flows out from the bottom of the reactor and enters a dry gas raw material preheater to provide heat for the dry gas, and is mixed with a catalytic cracking reaction product through a heat exchange device and enters a separation unit.
2. The process for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol according to claim 1, wherein the process is characterized in that: the catalytic cracking reactor is a fixed bed and is divided into more than two sections of filling, namely more than two reaction areas are provided, and a catalyst for preparing propylene and ethylene by catalytic cracking is arranged in the reactor, wherein the number of the reactors is more than 2, so that the production continuity is ensured.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811440587.2A CN109336726B (en) | 2018-11-29 | 2018-11-29 | Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201811440587.2A CN109336726B (en) | 2018-11-29 | 2018-11-29 | Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109336726A CN109336726A (en) | 2019-02-15 |
| CN109336726B true CN109336726B (en) | 2024-05-31 |
Family
ID=65319264
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201811440587.2A Active CN109336726B (en) | 2018-11-29 | 2018-11-29 | Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109336726B (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111718230B (en) * | 2019-03-22 | 2023-04-11 | 中国石油化工股份有限公司 | Method and system for producing propylene |
| CN110183296B (en) * | 2019-06-04 | 2022-07-01 | 国家能源投资集团有限责任公司 | Method for producing low-carbon olefin and co-producing gasoline by using Fischer-Tropsch synthetic oil |
| CN111139114A (en) * | 2019-12-27 | 2020-05-12 | 安徽海德化工科技有限公司 | Propane removing device |
| CN111554356B (en) * | 2020-05-08 | 2023-02-28 | 中国石油化工股份有限公司 | Dynamic modeling method for coupling reaction of light hydrocarbon and methanol |
| CN114524412B (en) * | 2022-03-13 | 2023-09-19 | 武汉轻工大学 | Methanol and light hydrocarbon combined aromatization and hydrogen production system and method |
Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101070260A (en) * | 2007-06-21 | 2007-11-14 | 复旦大学 | Zeolite catalyzing and separating method for increasing yield of preparing olefin by methyl alcohol dewatering |
| CN101343568A (en) * | 2008-03-25 | 2009-01-14 | 北京惠尔三吉绿色化学科技有限公司 | Method for preparing gasoline with petroleum cracking of dry gas |
| CN101516811A (en) * | 2006-09-21 | 2009-08-26 | 三菱化学株式会社 | Process for production of propylene |
| CN101629091A (en) * | 2009-08-14 | 2010-01-20 | 山西恒扬科技有限公司 | Technique for preparing low carbon mixed hydrocarbon rich in propylene and gasoline fraction by methanol |
| CN101844960A (en) * | 2009-03-23 | 2010-09-29 | 上海傲佳能源科技有限公司 | Method for producting propylene by catalytic pyrolysis of liquefied gas |
| CN102146010A (en) * | 2010-02-10 | 2011-08-10 | 江苏煤化工程研究设计院有限公司 | Process for producing low carbon olefin and arene parallel cogeneration gasoline by using methanol as raw material |
| CN102276399A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for producing lower olefins from methanol and naphtha |
| CN102329181A (en) * | 2011-08-01 | 2012-01-25 | 天津市泰源工业气体有限公司 | Method for preparing isobutylene by etherification |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
| CN102531821A (en) * | 2010-12-28 | 2012-07-04 | 中国科学院大连化学物理研究所 | Method for catalyzing catalytic cracking reaction of methanol coupled with naphtha using modified ZSM-5 molecular sieve based catalyst |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| CN102675020A (en) * | 2011-03-17 | 2012-09-19 | 江苏煤化工程研究设计院有限公司 | Process for preparing low-carbon olefin, aromatic hydrocarbon and functional alkane from multi-element carbon-containing raw material by using fixed bed reactor |
| CN102851063A (en) * | 2012-09-19 | 2013-01-02 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing high-octane rating clean gasoline by dry gas and liquefied gas aromatization |
| CN103242884A (en) * | 2013-05-20 | 2013-08-14 | 易高环保能源研究院有限公司 | Process for preparing high-octane high-cleanness gasoline with methanol by using multi-element catalysis method |
| CN104193574A (en) * | 2014-08-13 | 2014-12-10 | 中石化上海工程有限公司 | Method for coupling MTO (methanol to olefin) process with process of preparing ethylene by cracking naphtha steam |
| CN104370676A (en) * | 2014-11-11 | 2015-02-25 | 中国石油天然气集团公司 | Method for producing propylene and coproducing ethylene from C4 olefins |
-
2018
- 2018-11-29 CN CN201811440587.2A patent/CN109336726B/en active Active
Patent Citations (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101516811A (en) * | 2006-09-21 | 2009-08-26 | 三菱化学株式会社 | Process for production of propylene |
| CN101070260A (en) * | 2007-06-21 | 2007-11-14 | 复旦大学 | Zeolite catalyzing and separating method for increasing yield of preparing olefin by methyl alcohol dewatering |
| CN101343568A (en) * | 2008-03-25 | 2009-01-14 | 北京惠尔三吉绿色化学科技有限公司 | Method for preparing gasoline with petroleum cracking of dry gas |
| CN101844960A (en) * | 2009-03-23 | 2010-09-29 | 上海傲佳能源科技有限公司 | Method for producting propylene by catalytic pyrolysis of liquefied gas |
| CN101629091A (en) * | 2009-08-14 | 2010-01-20 | 山西恒扬科技有限公司 | Technique for preparing low carbon mixed hydrocarbon rich in propylene and gasoline fraction by methanol |
| CN102146010A (en) * | 2010-02-10 | 2011-08-10 | 江苏煤化工程研究设计院有限公司 | Process for producing low carbon olefin and arene parallel cogeneration gasoline by using methanol as raw material |
| CN102276399A (en) * | 2010-06-11 | 2011-12-14 | 中国石油化工股份有限公司 | Method for producing lower olefins from methanol and naphtha |
| CN102531821A (en) * | 2010-12-28 | 2012-07-04 | 中国科学院大连化学物理研究所 | Method for catalyzing catalytic cracking reaction of methanol coupled with naphtha using modified ZSM-5 molecular sieve based catalyst |
| CN102675020A (en) * | 2011-03-17 | 2012-09-19 | 江苏煤化工程研究设计院有限公司 | Process for preparing low-carbon olefin, aromatic hydrocarbon and functional alkane from multi-element carbon-containing raw material by using fixed bed reactor |
| CN102329181A (en) * | 2011-08-01 | 2012-01-25 | 天津市泰源工业气体有限公司 | Method for preparing isobutylene by etherification |
| CN102531824A (en) * | 2011-12-29 | 2012-07-04 | 北京惠尔三吉绿色化学科技有限公司 | Process method for preparing propylene and ethylene from liquid gas including butylene |
| CN102603457A (en) * | 2012-01-17 | 2012-07-25 | 马俊杰 | Production device and process for generating propylene by utilizing C3 and C4 in liquid gas deep processing |
| CN102851063A (en) * | 2012-09-19 | 2013-01-02 | 北京惠尔三吉绿色化学科技有限公司 | Method for producing high-octane rating clean gasoline by dry gas and liquefied gas aromatization |
| CN103242884A (en) * | 2013-05-20 | 2013-08-14 | 易高环保能源研究院有限公司 | Process for preparing high-octane high-cleanness gasoline with methanol by using multi-element catalysis method |
| CN104193574A (en) * | 2014-08-13 | 2014-12-10 | 中石化上海工程有限公司 | Method for coupling MTO (methanol to olefin) process with process of preparing ethylene by cracking naphtha steam |
| CN104370676A (en) * | 2014-11-11 | 2015-02-25 | 中国石油天然气集团公司 | Method for producing propylene and coproducing ethylene from C4 olefins |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109336726A (en) | 2019-02-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109336726B (en) | Process for preparing propylene ethylene by coupling catalytic cracking of carbon four, light oil and methanol | |
| TW460483B (en) | Improved process for saturated oligomer production | |
| CN101844960B (en) | Method for producting propylene by catalytic pyrolysis of liquefied gas | |
| US8324441B2 (en) | Pentane catalytic cracking process | |
| CN101617028B (en) | Method and system for producing synthetic fuels | |
| AU2010320947B2 (en) | Method for generating hydrocarbons, in particular gasoline, from synthesis gas | |
| CN105152840B (en) | Process for refining C-4 hydrocarbon fluid | |
| CN102356053A (en) | Process for the production of olefins | |
| JPS59206484A (en) | Catalytic conversion of olefin to higher hydrocarbon | |
| RU138334U1 (en) | INSTALLATION FOR PRODUCING HIGH-OCTANE GASOLINE FROM GASOLINE FRACTIONS AND METHANOL | |
| CN106488897A (en) | The method preparing dimethylbenzene | |
| CN105308008A (en) | Dual riser fluid bed process and reactor | |
| CN112321379B (en) | Energy-saving and environment-friendly method for preparing ethylbenzene from dry gas | |
| CN101875851B (en) | Non-hydrogenation upgrading method for liquefied gas fractions | |
| CN101333461B (en) | Method for producing cleaning fuel oil form petroleum cracking dry gas and C4 component | |
| CN101544905B (en) | Light hydrocarbon isomerization method | |
| CN106831288B (en) | The MTP method of mixed alcohol side entry feed | |
| CN101497815B (en) | Isomerization method for light hydrocarbon | |
| CN103864564B (en) | Technique for processing methanol-to-propylene by-products | |
| CN103333040A (en) | Low energy consumption propylene production technology | |
| CN102851063B (en) | Method for producing high-octane rating clean gasoline by dry gas and liquefied gas aromatization | |
| CN104557368A (en) | System for preparing ethylene, ethylene and arene from kinds of raw materials by coupling and transformation and method for system | |
| CN104525057B (en) | A kind of synthesis gas two-step method prepares the device and technique of gasoline | |
| CN110041157B (en) | Method for improving yield of propylene prepared from methanol and prolonging service life of catalyst | |
| CN210825992U (en) | Device for preparing propylene and ethylene by coupling catalytic cracking of carbon four, light oil and methanol |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |