CN113788735A - Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period - Google Patents
Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period Download PDFInfo
- Publication number
- CN113788735A CN113788735A CN202111165163.1A CN202111165163A CN113788735A CN 113788735 A CN113788735 A CN 113788735A CN 202111165163 A CN202111165163 A CN 202111165163A CN 113788735 A CN113788735 A CN 113788735A
- Authority
- CN
- China
- Prior art keywords
- tower
- ethylene
- propylene
- deethanizer
- tank
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 171
- 238000011084 recovery Methods 0.000 title claims abstract description 113
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 79
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 77
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 75
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 32
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims abstract description 232
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims abstract description 220
- 239000005977 Ethylene Substances 0.000 claims abstract description 205
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 197
- 239000007791 liquid phase Substances 0.000 claims abstract description 51
- 229910052799 carbon Inorganic materials 0.000 claims abstract description 39
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 37
- 239000000463 material Substances 0.000 claims abstract description 35
- 239000003507 refrigerant Substances 0.000 claims abstract description 28
- 150000001336 alkenes Chemical class 0.000 claims abstract description 21
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 claims abstract description 20
- 238000007599 discharging Methods 0.000 claims abstract description 8
- 239000007788 liquid Substances 0.000 claims description 86
- 238000010992 reflux Methods 0.000 claims description 61
- 230000006835 compression Effects 0.000 claims description 47
- 238000007906 compression Methods 0.000 claims description 47
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 45
- 238000005406 washing Methods 0.000 claims description 37
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 34
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 20
- 239000003513 alkali Substances 0.000 claims description 20
- 239000012071 phase Substances 0.000 claims description 16
- 239000001569 carbon dioxide Substances 0.000 claims description 10
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 10
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 9
- 238000004458 analytical method Methods 0.000 claims description 9
- 238000004064 recycling Methods 0.000 claims description 9
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 8
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 8
- 238000005336 cracking Methods 0.000 claims description 8
- 239000006200 vaporizer Substances 0.000 claims description 6
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims description 5
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims description 5
- 239000001294 propane Substances 0.000 claims description 5
- KAKZBPTYRLMSJV-UHFFFAOYSA-N Butadiene Chemical compound C=CC=C KAKZBPTYRLMSJV-UHFFFAOYSA-N 0.000 claims description 4
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims description 4
- 229910002091 carbon monoxide Inorganic materials 0.000 claims description 4
- 238000012545 processing Methods 0.000 claims description 4
- 238000000605 extraction Methods 0.000 claims description 3
- IYABWNGZIDDRAK-UHFFFAOYSA-N allene Chemical compound C=C=C IYABWNGZIDDRAK-UHFFFAOYSA-N 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- MWWATHDPGQKSAR-UHFFFAOYSA-N propyne Chemical compound CC#C MWWATHDPGQKSAR-UHFFFAOYSA-N 0.000 claims description 2
- 125000000383 tetramethylene group Chemical group [H]C([H])([*:1])C([H])([H])C([H])([H])C([H])([H])[*:2] 0.000 claims description 2
- 238000004523 catalytic cracking Methods 0.000 abstract description 13
- 150000001993 dienes Chemical class 0.000 abstract description 5
- 238000007670 refining Methods 0.000 abstract description 5
- 238000004904 shortening Methods 0.000 abstract 1
- 239000007789 gas Substances 0.000 description 144
- 238000000926 separation method Methods 0.000 description 17
- 238000005516 engineering process Methods 0.000 description 9
- 238000005057 refrigeration Methods 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 description 3
- 239000006227 byproduct Substances 0.000 description 3
- 230000007613 environmental effect Effects 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- 238000011144 upstream manufacturing Methods 0.000 description 3
- 238000005520 cutting process Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- BDAGIHXWWSANSR-UHFFFAOYSA-N methanoic acid Natural products OC=O BDAGIHXWWSANSR-UHFFFAOYSA-N 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000006467 substitution reaction Methods 0.000 description 2
- OSWFIVFLDKOXQC-UHFFFAOYSA-N 4-(3-methoxyphenyl)aniline Chemical compound COC1=CC=CC(C=2C=CC(N)=CC=2)=C1 OSWFIVFLDKOXQC-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 239000002253 acid Substances 0.000 description 1
- 230000004075 alteration Effects 0.000 description 1
- 239000002585 base Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- -1 ethylene, propylene Chemical group 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 235000019253 formic acid Nutrition 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 230000000630 rising effect Effects 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/11—Purification; Separation; Use of additives by absorption, i.e. purification or separation of gaseous hydrocarbons with the aid of liquids
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
-
- 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
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/40—Ethylene production
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Water Supply & Treatment (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a light hydrocarbon recovery start-up method suitable for a methanol-to-olefin reverse short-time shutdown period, which is characterized in that during the reverse-to-olefin short-time shutdown period of the methanol-to-olefin, crude propylene gas, liquid-phase propylene and liquid-phase ethylene are conveyed to a light hydrocarbon recovery part to simulate a reverse-to-olefin small-flow supply process gas, a part to be reversed is started in advance to supply qualified process gas, unqualified propylene and unqualified ethylene can be recycled, liquid-phase ethylene is conveyed at the same time, a refrigerant which is lacked before a first cooler of a deethanizer is started is supplemented, the deethanizer system can stably operate, and qualified intermediate materials are conveyed to the downstream as quickly as possible at the tower top and the tower bottom. The invention is started under the conditions that the S-MTO reaction is partially stopped again and the light hydrocarbon recovery part does not return materials, thereby not only shortening the start-up time, avoiding the process gas from discharging a torch, refining unqualified ethylene and propylene, reducing the diene loss amount, reducing the carbon emission amount and the like, but also realizing the continuous operation of the olefin catalytic cracking device.
Description
Technical Field
The invention relates to the technical field of methanol-to-olefin, in particular to a light hydrocarbon recovery and start-up method suitable for a methanol-to-olefin reaction short-time shutdown period.
Background
The methanol-to-olefin (MTO) technology which carries on the processes of upstream coal-to-methanol and downstream olefin polymerization is a key technology for realizing coal-to-olefin and an important ring for realizing a petroleum substitution strategy, and opens up a new way for producing petrochemical products by using coal to replace petroleum. MTO is by the part of turning over again and the light hydrocarbon recovery part is constituteed, and the light hydrocarbon recovery part separates the refining with the process gas that the part methanol catalytic cracking produced of turning over again, rectifies polymerization level ethylene and polymerization level propylene product, produces byproducts such as heavy hydrocarbon, carbon mixture four, propane and fuel gas simultaneously. At present, the technology for preparing olefin from methanol mainly comprises an MTO technology developed by UOP company, a D-MTO technology of a large chemical company institute of Chinese academy of sciences and an S-MTO technology of a China Shanghai petrochemical institute of petrochemical technology.
The light hydrocarbon recovery part of the S-MTO technology comprises a process gas compression unit, a cold separation unit, a heat separation unit, a propylene refrigeration unit and the like. The process gas compression unit is compressed in four sections, and a water scrubber and an alkali scrubber are arranged at the outlet of the three sections, so that the CO in the process gas can be removed under the pressure2Acid gases such as formic acid and acetic acid, the pressure of the process gas is increased by compression, and the water content of the materials is reduced by a dryer so as to enter a cold separation unit. Because the content of methane hydrogen in the coal-to-olefin process gas is low and the content of heavy components of carbon three or more is high, the cold separation technology adopts a front deethanizing process, and a deethanizer cuts the process gas into carbon two and light components and carbon three and heavy components. The demethanizer continues to cut the deethanizer overhead gas into a carbon-one and light-component and carbon-two mixture. By utilizing the principle of similar phase and phase dissolution, the bottom liquid of the depropanization tower is used as the carbon four washing liquid of the ethylene recovery tower,absorbing and dissolving ethylene in the gas extracted from the top of the demethanizer, and then feeding the C-C washing liquid into a deethanizer for separating and recovering ethylene. Rectifying the carbon dioxide component in the demethanizer kettle in an ethylene tower to refine ethane and polymerization-grade ethylene; feeding the carbon III and heavy components in the kettle of the deethanizer into a depropanizer of a thermal separation unit for continuous rectification and separation; enabling the carbon three components at the top of the depropanizing tower to enter a 1/2# propylene rectifying tower, refining to obtain propane and polymerization-grade propylene, enabling the residue of the depropanizing tower to enter a depentanizing tower, and further separating out a mixed liquid containing four carbon five and a heavy hydrocarbon product containing six carbon and more heavy components; the propylene refrigeration unit provides three propylene refrigerants of 7 ℃, 25 ℃ and 40 ℃ below zero and a reboiling heat source of 25 ℃ for the light hydrocarbon recovery part. An Olefin Catalytic Cracking (OCC) device is a matched device of S-MTO, the byproduct carbon four-carbon five-mixed liquid is utilized to carry out catalytic cracking to generate process gas rich in ethylene and propylene, crude propylene gas consisting of carbon three and light components is separated out by a rectification system and enters an S-MTO light hydrocarbon recovery part to be continuously rectified so as to increase the production of polymerization-grade propylene and ethylene.
The existing start-up scheme has the technical problems of long start-up time, serious environment protection pressure and diene loss caused by a process gas discharge torch and the like. However, the S-MTO reverse part short stop operation has the following problems during the S-MTO reverse part short stop: (1) if the Olefin Catalytic Cracking (OCC) device is partially stopped and started along with the reaction, the process of the device is accompanied with the discharge of crude propylene gas of a product to a torch, and certain loss and environmental protection pressure are caused. (2) During the reverse part of the parking, most systems of the light hydrocarbon recovery part are in a self-circulation or pressure-maintaining and liquid-maintaining state, the process gas is fed slowly, the loss and the environmental protection pressure of the process gas discharge torch are increased, meanwhile, the time for extracting qualified products is long, more unqualified ethylene and propylene products are generated, and the energy consumption of the recycling treatment is increased. (3) In the process of receiving a large amount of upstream process gas, the process gas is taken as a deethanizer after starting, a first condenser of the deethanizer on the top of the deethanizer is short of refrigerant at the early stage of starting, so that the temperature of the top of the deethanizer is higher, the reflux quantity is insufficient, the tower system releases a torch under an overpressure condition, the heavy component of the material on the top of the deethanizer is higher, and the tower system cannot be quickly adjusted to a normal state; the tower top material with excessive heavy components in the deethanizer enters the demethanizer, so that the carbon content and the heavy component content in the material in the demethanizer kettle are not qualified, a torch needs to be discharged after heat exchange of a first condenser of the deethanizer, the heat exchange effect of a reboiler of the demethanizer kettle is poor, and the torch needs to be discharged at the bottom of the reboiler of the demethanizer kettle; when an unstable deethanizer system is operated, qualified tower kettle materials are difficult to provide for a thermal separation unit, and a torch needs to be put at the top of a reflux tank of a depropanizer after the contents of carbon dioxide and light components in the depropanizer materials exceed the standard and enter the downstream; meanwhile, the depropanizer is unstable in operation, and cannot timely convey qualified C-C washing liquid to the ethylene recovery tower and the deethanizer, so that the depropanizer is not favorable for stable operation; the heavy components fed into the ethylene tower exceed the standard, so that the extraction of polymer-grade ethylene is not qualified for a long time, and the heavy components in the tower kettle exceed the standard, so that the heating effect of the ethylene tower reboiler is poor, and a torch needs to be placed at the bottom of the ethylene tower reboiler when the heating effect is serious. The light components fed into the 1# propylene rectifying tower exceed the standard, so that the polymer-grade propylene is not qualified for a long time.
Therefore, the traditional starting scheme is used for solving the problems of long starting period, long time of a spark torch, large diene loss and large environmental protection pressure when the S-MTO reaction is partially stopped after the start is carried out.
Disclosure of Invention
The invention aims to solve the technical problem of providing a light hydrocarbon recovery start-up method suitable for the reaction-to-olefin short-time shutdown period of methanol, which has the characteristics of short start-up time, no torch discharge and small diene loss, and solves the problems of short shutdown of the reaction-to-olefin part, maintenance of the light hydrocarbon recovery part and the olefin catalytic cracking device.
The technical scheme of the invention is as follows:
a light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period specifically comprises the following steps:
(1) and during the short-time shutdown period of the reverse recycling part, the processing steps of the light hydrocarbon recovery part are as follows:
a) the olefin cracking device normally operates, the olefin cracking device conveys qualified crude propylene gas to a process gas compression unit of a light hydrocarbon recovery part, and the crude propylene gas is added behind a water scrubber and in front of an alkali scrubber between a compressor three-section and a compressor four-section of the process gas compression unit;
b) adjusting a three-return anti-surge valve between the three sections of the compressor and the first section of the compressor to ensure the flow of the suction inlet of the first section of the suction tank;
c) after a first ethylene delivery pump and a propylene delivery pump are started, respectively introducing unqualified liquid-phase ethylene in an ethylene unqualified tank and unqualified liquid-phase propylene in a propylene unqualified tank to the input ends of three sections of aftercondensers of a process gas compression unit by the first ethylene delivery pump, normally adjusting a compressor of the process gas compression unit, increasing the pressure of an outlet of the four sections of the compressor to be more than 2.9MPa, normally adjusting a water scrubber and an alkali scrubber, reducing the using amount of fresh alkali of the boiler water of the water scrubber and the alkali scrubber, and adjusting the temperature of an outlet of the process gas of a second aftercooler of the four sections to be 14-16 ℃;
d) before the liquid level of the four-section discharge tank is not established, the process gas discharged from the four-section discharge tank is dried by a gas phase dryer and enters a deethanizer after being qualified, and after the liquid level of the four-section discharge tank is established, the liquid phase of the four-section discharge tank enters the deethanizer after being qualified by condensate condensation of a condensate dryer;
e) leading the unqualified liquid-phase ethylene in the unqualified ethylene tank to a first condenser of a deethanizer by a second ethylene delivery pump to be used as an ethylene refrigerant for heat exchange, so that the process medium at the top of the deethanizer is condensed to be below 20 ℃ below zero;
f) adjusting the dosage of a-25 ℃ propylene refrigerant in a second condenser of the deethanizer to ensure that the temperature of the process medium is below-21 ℃ after the process medium is condensed in the second condenser of the deethanizer;
g) adjusting the reboiling amount of a reboiler of the deethanizer to ensure that non-condensable gas discharged from a reflux tank of the deethanizer slowly enters the demethanizer, controlling the pressure of the deethanizer to be 2.8-3.0 MPa, and adjusting the temperature at the top of the tower to be below-17 ℃;
h) the liquid level of a reflux tank of the deethanizer rises, the tower top reflux amount of the deethanizer is increased, and materials collected at the tower bottom of the deethanizer are sent to a depropanizer after the liquid level of the tower bottom of the deethanizer rises;
i) after the material is fed into the depropanizing tower, the material is normally adjusted, after the liquid level is established at the tower bottom of the depropanizing tower, the carbon four washing liquid at the tower bottom of the depropanizing tower is cooled and then is sent to an ethylene recovery tower, the flow is gradually increased, and the carbon four washing liquid is not sent to a depentanizing tower system;
j) the gas phase discharged from the top of the deethanizer directly enters a demethanizer after being condensed, the demethanizer starts to be adjusted, a torch does not need to be discharged from a reflux tank of the demethanizer, the non-condensable gas at the top of the demethanizer enters an ethane vaporizer for heat exchange, the liquid phase after heat exchange returns to the reflux tank of the demethanizer through self-flowing, the gas phase enters an ethylene recovery tower, and the material at the bottom of the demethanizer directly enters the ethylene tower without discharging the torch after heat exchange through a first condenser of the deethanizer;
k) controlling the pressure in the ethylene recovery tower to be 2.4-2.6 MPa, and after the liquid level of the ethylene recovery tower is established, sending a C-C washing liquid in the ethylene recovery tower to a deethanizer and gradually increasing the flow;
l) adjusting the using amount of 25 ℃ propylene and-40 ℃ propylene refrigerant in the ethylene tower, controlling the pressure at the top of the ethylene tower to be 1.6-1.7 MPa, the temperature at the top of the ethylene tower to be-37 ℃ to-31 ℃, controlling the reflux ratio to be 3.9-4.1, and extracting ethylene from the side line of the ethylene tower to an ethylene qualified tank;
m) adjusting the using amount and the reboiling amount of propylene at 7 ℃ in a depropanizing tower, controlling the pressure at the top of the depropanizing tower to be 0.7-0.9 MPa, the temperature at the top of the depropanizing tower to be 10-18 ℃, the temperature of a sensitive plate to be 35-45 ℃, establishing a liquid level at the top of the depropanizing tower, and then sending the liquid level to a No. 1 propylene rectifying tower;
n) normally adjusting a 1# propylene rectifying tower and a 2# propylene rectifying tower, controlling the pressure at the top of the 2# propylene rectifying tower to be 1.6-1.9 MPa, the temperature at the top of the tower to be 42-45 ℃, the temperature of a kettle of the 1# propylene rectifying tower to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower and the 2# propylene rectifying tower to be 12-14, and collecting propylene from the top of the 2# propylene rectifying tower to a propylene qualified tank;
(2) after the reverse recycling part is started to supply qualified process gas, the light hydrocarbon recovery part is started:
o) opening a process gas material inlet valve at an inlet of the light hydrocarbon recovery part, introducing the process gas formed by reverse partial conversion into a process gas compression unit of the light hydrocarbon recovery part, and normally adjusting the process gas compression unit;
p) after the process gas compression unit introduces the process gas, the first ethylene delivery pump and the propylene delivery pump stop delivering the liquid-phase ethylene and the liquid-phase propylene to the process gas compression unit, the compressors of the process gas compression unit are normally adjusted, and the water washing tower and the alkaline washing tower are normally adjusted, so that the consumption of boiler water of the water washing tower and fresh alkaline of the alkaline washing tower is increased;
q) increasing the ethylene refrigerant dosage of the first condenser of the deethanizer, and normally adjusting the deethanizer;
r) the depropanizing tower is normally adjusted after feeding, after the liquid level at the tower kettle of the depropanizing tower rises, one part of the liquid is sent to an ethylene recovery tower after passing through a carbon four washing liquid cooler, and the other part of the liquid is sent to a depentanizing tower system;
s) increasing the pressure in the ethylene recovery tower to 2.6-2.8 MPa, and increasing the flow of the C-C washing liquid sent to the deethanizer;
t) normally adjusting the ethylene tower, leading the ethylene extracted from the side line of the ethylene tower to an ethylene unqualified tank, leading the ethylene to an ethylene qualified tank after the ethylene is qualified through analysis, normally adjusting a 1# propylene rectifying tower and a 2# propylene rectifying tower, leading the propylene extracted from the top of the 2# propylene rectifying tower to a propylene unqualified tank, and leading the propylene to a propylene qualified tank after the propylene is qualified through analysis.
The pressure of the qualified crude propylene gas in the step a) is more than 1.8MPa, and the sum of the gas contents of propylene and ethylene in the qualified crude propylene gas is 75 percent.
The temperature of the unqualified liquid-phase ethylene in the ethylene unqualified tank is below minus 32 ℃, the pressure is above 2.2MPa, the volume content of carbon dioxide in the unqualified liquid-phase ethylene is below 5ppm, and the volume content of water is below 1 ppm.
The pressure of the unqualified liquid phase propylene in the unqualified propylene tank is more than 3.1MPa, the volume content of carbon dioxide in the unqualified liquid phase propylene is less than 5ppm, and the volume content of water is less than 1 ppm.
The temperature of the tower kettle of the deethanizer is always controlled to be 93-96 ℃ in the whole feeding process, so that the qualified extraction of the tower kettle of the deethanizer is ensured.
The content of ethylene in the material extracted from the tower bottom of the deethanizer is below 20ppm, and the content of ethane is below 150 ppm.
The temperature of the process gas formed by the reverse and re-partial conversion is below 50 ℃, and the volume content of dimethyl ether in the process gas is below 3000 ppm.
In the qualified ethylene in the ethylene qualified tank, the volume content of ethylene is more than 99.95 percent, the volume content of carbon monoxide is less than 1ppm, the volume content of carbon dioxide is less than 5ppm, the volume content of heavy components of carbon three or more is less than 10ppm, the volume content of acetylene is less than 5ppm, the volume content of methanol is less than 4ppm, and the volume content of water is less than 1 ppm.
In the qualified propylene in the propylene qualified tank, the volume content of propylene is more than 99.6 percent, the volume content of carbon monoxide is less than 2ppm, the volume content of carbon dioxide is less than 1ppm, the volume content of propane is less than 0.4 percent, the volume content of ethylene is less than 10ppm, the volume content of methanol is less than 5ppm, the volume content of water is less than 2ppm, the sum of the volume contents of propyne and propadiene is less than 5ppm, the sum of the volume contents of butylene and butadiene is less than 2ppm, the volume content of acetylene is less than 2ppm, and the volume content of dimethyl ether is less than 2 ppm.
The invention has the advantages that:
(1) the invention supplies crude propylene gas, unqualified liquid phase propylene and unqualified liquid phase ethylene substances to the light hydrocarbon recovery part, imitates the small flow supply process gas of the reverse-recycle part, and supplies qualified process gas to the reverse-recycle part after the start in advance.
(2) The crude propylene gas generated by the catalytic cracking of the olefin catalytic cracking device contains three or less carbon components, and is similar to the three or less carbon components in the process gas;
(3) the invention conveys unqualified liquid-phase propylene to the light hydrocarbon recovery part, firstly, the propylene is supplemented to the light hydrocarbon recovery part system, the adjustment is convenient, and secondly, the unqualified propylene with overproof hydrocarbons and oxides can be recycled;
(4) the invention conveys unqualified liquid-phase ethylene to the light hydrocarbon recovery part, supplements the cryogen which is lacked before the first cooler of the deethanizer is started, is beneficial to the stable operation of the deethanizer system, simultaneously conveys qualified intermediate materials to the downstream as fast as possible at the tower top and the tower kettle, and can recycle unqualified ethylene with over-standard ethane and acetylene.
The invention not only shortens the start-up time, avoids process gas flare, recycles unqualified ethylene and propylene, reduces the diene loss amount, reduces the carbon emission amount and the like, but also realizes the continuous operation of an olefin catalytic cracking device (OCC device). The method is operated under the conditions that the S-MTO reaction is partially and temporarily stopped and the light hydrocarbon recovery part does not return materials, so that the method obtains good practical application, the whole process from the process gas entering the light hydrocarbon recovery part to the production of qualified polymer-grade ethylene and polymer-grade propylene lasts for 6 hours, the phenomenon of torch discharge does not occur, and a good technical effect is obtained.
Drawings
FIG. 1 is a schematic flow diagram of the recovery section of light hydrocarbons from methanol to olefins according to the present invention.
Reference numerals: 1A-reaction-recycle process gas, 1B-fuel gas system, 1C-propylene spherical tank (comprising a propylene unqualified tank and a propylene qualified tank), 1D-olefin catalytic cracking device (OCC device), 1E-boiler water system, 1F-fresh alkali injection system, 2A-torch system, 2B-ethylene spherical tank (comprising an ethylene unqualified tank and an ethylene qualified tank), 3A-depentanizer system and 3B-propane spherical tank; f101-process gas inlet valve, F102-three-return one-surge prevention valve, F103-four-return four-surge prevention valve, F104-four-section outlet pressure control valve, F201-flare valve at outlet of first condenser of deethanizer, F202-flare valve at top of deethanizer, and F301-depropanizer pressure control;
1-1-first compressor section, 1-2-second compressor section, 1-3-third compressor section, 1-4-four compressor section, 101-first suction tank, 102-first aftercooler, 103-propylene delivery pump, 104-second suction tank, 105-second aftercondensation, 106-third suction tank, 107-third aftercondenser, 108-third discharge tank, 109-water scrubber, 110-process gas heater, 111-alkali scrubber, 112-fourth suction condenser, 113-fourth suction tank, 114-fourth first aftercooler, 115-fourth aftercooler (with 7 ℃ propylene inside), 116-fourth discharge tank, 117-process gas drier, 118-condensate drier, 119-weak base circulating pump, 120-medium alkali circulating pump, 121-strong alkali circulating pump, and 122-four-section condensate pump;
201-deethanizer, 202-deethanizer first condenser, 203-deethanizer second condenser (with-25 deg.C propylene refrigerant inside), 204-deethanizer reflux drum; 205-deethanizer reflux pump, 206-deethanizer reboiler, 207-demethanizer, 208-demethanizer reboiler (provided with propylene at 25 ℃), 209-demethanizer reflux pump, 210-demethanizer condenser (provided with propylene refrigerant at-40 ℃), 211-demethanizer reflux tank, 212-ethane vaporizer, 213-ethylene recovery tower, 214-carbon four-wash liquid cooler, 215-ethylene recovery tower kettle pump, 216-ethylene tower, 217-ethylene tower condenser (provided with propylene at-40 ℃), 218-ethylene tower reflux tank, 219-ethylene tower reflux pump, 220-ethylene tower reboiler (provided with propylene at 25 ℃), 221-first ethylene delivery pump, 222-second ethylene delivery pump;
301-depropanizer, 302-depropanizer reboiler, 303-depropanizer top condenser (with 7 ℃ propylene in it), 304-depropanizer top reflux tank, 305-depropanizer reflux pump, 306-propylene tower feed pump, 307-depropanizer kettle pump, 308-1# propylene rectifying tower, 309-1# propylene rectifying tower kettle reboiler, 310-2# propylene rectifying tower, 311-1# propylene rectifying tower reflux pump, 312-2# propylene rectifying tower reflux tank, 313-2# propylene rectifying tower reflux pump, 314-2# propylene rectifying tower condenser.
Detailed Description
The technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the drawings in the embodiments of the present invention, and it is obvious that the described embodiments are only a part of the embodiments of the present invention, and not all of the embodiments. All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.
Example 1
The methanol-to-olefin process comprises a re-reaction part and a light hydrocarbon recovery part, wherein the re-reaction part is a process for converting methanol into process gas containing ethylene, propylene and the like, and the light hydrocarbon recovery part is used for separating and refining the upstream process gas; the light hydrocarbon recovery part comprises a process gas compression unit, a cold separation unit, a heat separation unit and a propylene refrigeration unit.
Referring to fig. 1, the start-up method of the light hydrocarbon recovery part for preparing olefin from methanol is a process from the time when process gas enters the light hydrocarbon recovery part to the time when qualified polymer-grade ethylene and polymer-grade propylene are produced. When the process gas enters the light hydrocarbon recovery part, the reverse part is normally started to produce qualified process gas; when the process gas enters the light hydrocarbon recovery part, an industrial gas material inlet valve F101 of the process gas compression unit is closed, a first section 1-1 of a compressor, a second section 1-2 of the compressor, a third section 1-3 of the compressor and a fourth section 1-4 of the compressor of the process gas compression unit normally operate, and a water scrubber 109 and an alkaline scrubber 111 start to circulate automatically; when the process gas 1A enters the light hydrocarbon recovery part, the ethylene recovery tower 213 of the cold separation unit maintains pressure and liquid, and the deethanizer 201, the demethanizer 207 and the ethylene tower 216 are completely refluxed and established; when the process gas enters the light hydrocarbon recovery part, the depropanizer system (depropanizer 301, a depropanizer reboiler 302, a depropanizer top condenser 303, a depropanizer top reflux tank 304, a depropanizer reflux pump 305), the depentanizer system 3A and the propylene rectifying tower system (1# propylene rectifying tower 308, 1# propylene rectifying tower kettle reboiler 309, 2# propylene rectifying tower 310, 1# propylene rectifying tower reflux pump 311, 2# propylene rectifying tower reflux tank 312, 2# propylene rectifying tower reflux pump 313 and 2# propylene rectifying tower condenser 314) of the thermal separation unit establish total reflux.
A light hydrocarbon recovery and start-up method suitable for methanol to olefin specifically comprises the following steps:
a) opening a material inlet valve F101 of the process gas, introducing the process gas into a process gas compression unit, and normally adjusting the process gas compression unit through a three-return one-surge valve F102 and a four-return four-surge valve F103, so that the consumption of boiler water of a water scrubber 109 and fresh alkali of an alkali scrubber 111 is reduced, the outlet pressure of four sections 1-4 of a compressor is increased to be more than 2.9MPa, and when the pressure is too high, the process gas is released to a torch through a four-section outlet pressure control valve F104;
b) starting a second ethylene delivery pump 222, introducing unqualified liquid-phase ethylene to a first condenser 202 of a deethanizer for heat exchange, and condensing a tower top process medium of the deethanizer 201 to be below 20 ℃ below zero;
c) the amount of the-25 ℃ propylene refrigerant in the second condenser 203 of the deethanizer is adjusted, the temperature of the process medium after the process medium is condensed in the second condenser 203 of the deethanizer is ensured to be below-21 ℃, and meanwhile, a refrigeration unit of the-25 ℃ propylene refrigerant is adjusted;
d) the reboiling amount of the deethanizer reboiler 206 is increased, the non-condensable gas in the deethanizer reflux tank 204 slowly enters the demethanizer 207, the pressure in the deethanizer 201 is controlled to be 2.8-3.0 MPa, and the temperature at the top of the tower is adjusted to be below minus 17 ℃;
e) the reflux quantity at the top of the deethanizer 201 is increased, and materials extracted from the bottom of the deethanizer 201 are sent to the depropanizer 301 after the liquid level at the bottom of the deethanizer 201 rises;
f) after the material is fed into the depropanizing tower 201, the adjustment is started, after the liquid level is established at the bottom of the depropanizing tower 301, the carbon four washing liquid at the bottom of the depropanizing tower 301 is cooled by the carbon four washing liquid cooler 214 and then is sent to the ethylene recovery tower 213, and the flow is gradually increased;
g) the gas phase discharged from the top of the deethanizer 201 is condensed by the second condenser 203 of the deethanizer and then directly enters the demethanizer 207, the demethanizer 207 starts to adjust, the reflux tank 211 of the demethanizer is not ignited, the non-condensable gas at the top of the demethanizer 207 enters the ethane vaporizer 212 for heat exchange through the reflux tank 211 of the demethanizer, the liquid phase after heat exchange returns to the reflux tank 211 of the demethanizer by gravity flow, the gas phase enters the ethylene recovery tower 213, and the material at the bottom of the demethanizer 207 directly enters the ethylene tower 216 after heat exchange through the first condenser 202 of the deethanizer;
h) controlling the pressure in the ethylene recovery tower 213 to be 2.6-2.8 MPa, and after the liquid level is established at the tower kettle of the ethylene recovery tower 213, sending the carbon four washing liquid at the tower kettle to the deethanizer 201 and gradually increasing the flow;
i) adjusting the dosage of 25 ℃ propylene and the dosage of-40 ℃ propylene refrigerant in the ethylene tower 216, controlling the pressure at the top of the ethylene tower 216 to be 1.6-1.7 MPa, the temperature at the top of the ethylene tower to be-37-31 ℃, controlling the reflux ratio to be 3.9-4.1, collecting ethylene from the side line of the ethylene tower 216 to an ethylene unqualified tank, and introducing the ethylene qualified tank after the ethylene qualified tank is analyzed;
j) adjusting the using amount and the reboiling amount of propylene at 7 ℃ in the depropanizing tower 301, controlling the pressure at the top of the depropanizing tower 301 to be 0.7-0.9 MPa, the temperature at the top of the depropanizing tower to be 10-18 ℃, the temperature of a sensitive plate to be 35-45 ℃, establishing a liquid level at the top of the depropanizing tower, and sending the liquid level to a No. 1 propylene rectifying tower 308;
k) normally adjusting the propylene rectifying tower, controlling the pressure at the top of the 2# propylene rectifying tower (310) to be 1.6-1.9 MPa, the top temperature to be 42-45 ℃, the kettle temperature of the 1# propylene rectifying tower to be 50-60 ℃, controlling the reflux ratio to be about 13, extracting propylene from the top of the tower to an unqualified propylene tank, and transferring to a qualified propylene tank after the propylene is qualified through analysis.
Normally adjusting a 1# propylene rectifying tower 308 and a 2# propylene rectifying tower 310, controlling the pressure at the top of the 2# propylene rectifying tower 310 to be 1.6-1.9 MPa, the temperature at the top of the tower to be 42-45 ℃, the temperature at the bottom of a tower of the 1# propylene rectifying tower 308 to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310 to be 12-14, and extracting propylene from the top of the 2# propylene rectifying tower 310 to a propylene qualified tank;
in this embodiment 1, only the unqualified liquid-phase ethylene is delivered to the cold separation unit, and is used as the refrigerant of the first cooler 202 of the deethanizer, the process gas is supplied at a small flow rate without simulating the reverse part, and the qualified process gas is supplied at a part of the light hydrocarbon without being started in advance to be reversed. The whole process from the process gas entering the light hydrocarbon recovery part to the production of qualified polymer-grade ethylene and polymer-grade propylene lasts for 8 hours, and the time of torch discharge lasts for 1.5 hours.
Example 2
The methanol-to-olefin comprises a re-reaction part, a light hydrocarbon recovery part and a matched olefin catalytic cracking device (OCC device). The light hydrocarbon recovery part is used for separating and refining the reverse regeneration process gas, and the olefin catalytic cracking device (OCC device) is used for generating crude propylene gas rich in ethylene and propylene through catalytic cracking of a byproduct of the light hydrocarbon recovery part, and returning the crude propylene gas to the light hydrocarbon recovery part for separation and purification. The light hydrocarbon recovery part comprises a process gas compression unit, a cold separation unit, a heat separation unit and a propylene refrigeration unit.
Referring to fig. 1, a light hydrocarbon recovery and start-up method suitable for a methanol-to-olefin reaction short-time shutdown period specifically comprises the following steps:
(1) and during the short-time shutdown period of the reverse recycling part, the processing steps of the light hydrocarbon recovery part are as follows:
a) the olefin cracking device (OCC device) normally operates, the olefin cracking device conveys qualified crude propylene gas 1D to a process gas compression unit of a light hydrocarbon recovery part, and the crude propylene gas 1D is added behind a water scrubber 109 and in front of an alkaline scrubber 111 between a compressor three-section 1-3 and a compressor four-section 1-4 of the process gas compression unit, namely the input end of a process gas heater 110;
b) adjusting a three-return anti-surge valve F102 between the three sections 1-3 of the compressor and the section 1-1 of the compressor to ensure the flow of a suction inlet of the section of the suction tank 101;
c) after the first ethylene delivery pump 221 and the propylene delivery pump 103 are started, the first ethylene delivery pump 221 respectively introduces unqualified liquid-phase ethylene in an ethylene unqualified tank and unqualified liquid-phase propylene in a propylene unqualified tank to the input ends of the condenser 107 in the three sections of the process gas compression unit, the compressor of the process gas compression unit is normally adjusted, the outlet pressure of the four sections 1-4 of the compressor is increased to be more than 2.9MPa, the water scrubber 109 and the alkaline tower 111 are normally adjusted, the boiler water and alkaline tower 111 fresh alkali consumption of the water scrubber 109 is reduced, and the outlet temperature of the process gas of the four sections of the second aftercooler 115 is adjusted to be 14-16 ℃;
d) before the liquid level of the four-section discharge tank 116 is not established, the process gas discharged from the four-section discharge tank 116 enters the deethanizer 201 after being dried and qualified by the gas phase dryer 117, and after the liquid level of the four-section discharge tank 116 is established, the liquid phase of the four-section discharge tank 116 enters the deethanizer after being condensed and qualified by the condensate dryer 118;
e) the amount of the-25 ℃ propylene refrigerant in the second condenser 203 of the deethanizer is adjusted, the temperature of the process medium after the process medium is condensed in the second condenser 203 of the deethanizer is ensured to be below-21 ℃, and meanwhile, a refrigeration unit of the-25 ℃ propylene refrigerant is adjusted;
f) the reboiling amount of a reboiler 206 of the deethanizer is adjusted, so that the non-condensable gas discharged from a reflux tank 204 of the deethanizer slowly enters a demethanizer 207, the pressure of the deethanizer 201 is controlled to be 2.8-3.0 MPa, and the temperature at the top of the tower is adjusted to be below-17 ℃;
g) the liquid level of the reflux tank 204 of the deethanizer rises, the tower top reflux amount of the deethanizer 201 is increased, and materials extracted from the tower bottom of the deethanizer 201 are sent to the depropanizer 301 after the tower bottom liquid level of the deethanizer 201 rises;
h) the depropanizing tower 301 is normally adjusted after feeding, after the liquid level of the tower kettle of the depropanizing tower 301 is established, carbon four washing liquid at the tower kettle of the depropanizing tower 301 is cooled by a carbon four washing liquid cooler 214 and then is sent to an ethylene recovery tower 213, the flow is gradually increased, and the carbon four washing liquid is not sent to a depentanizing tower system 3A;
i) the gas phase discharged from the top of the deethanizer 201 directly enters the demethanizer 207 after being condensed, the demethanizer 207 starts to be adjusted, the reflux tank 211 of the demethanizer does not need to discharge a torch, the non-condensable gas at the top of the demethanizer 207 enters the ethane vaporizer 212 for heat exchange through the reflux tank 211 of the demethanizer, the liquid phase after heat exchange automatically flows back to the reflux tank 211 of the demethanizer, the gas phase enters the ethylene recovery tower 213, and the material at the bottom of the demethanizer 207 directly enters the ethylene tower 216 without discharging the torch after heat exchange through the first condenser 202 of the deethanizer;
j) controlling the pressure in the ethylene recovery tower 213 to be 2.4-2.6 MPa, and after the liquid level of the ethylene recovery tower 213 is established, sending the C4 washing liquid in the ethylene recovery tower 213 to the deethanizer 201 and gradually increasing the flow;
k) adjusting the dosage of 25 ℃ propylene and the dosage of-40 ℃ propylene refrigerant in the ethylene tower 216, controlling the pressure at the top of the ethylene tower 216 to be 1.6-1.7 MPa, the temperature at the top of the ethylene tower to be-37 ℃ to-31 ℃, controlling the reflux ratio to be 3.9-4.1, and collecting ethylene from the side line of the ethylene tower 216 to an ethylene qualified tank;
l) adjusting the using amount and the reboiling amount of propylene at 7 ℃ in the depropanizing tower 301, controlling the pressure at the top of the depropanizing tower 301 to be 0.7-0.9 MPa, the temperature at the top of the depropanizing tower to be 10-18 ℃, the temperature of a sensitive plate to be 35-45 ℃, establishing a liquid level at the top of the depropanizing tower, and sending the liquid level to a No. 1 propylene rectifying tower 308;
m) normally adjusting a 1# propylene rectifying tower 308 and a 2# propylene rectifying tower 310, controlling the pressure at the top of the 2# propylene rectifying tower 310 to be 1.6-1.9 MPa, the temperature at the top of the tower to be 42-45 ℃, the temperature of a kettle of the 1# propylene rectifying tower 308 to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310 to be 12-14, and collecting propylene at the top of the 2# propylene rectifying tower 310 to a propylene qualified tank;
(2) after the reverse recycling part is started to supply qualified process gas, the light hydrocarbon recovery part is started:
n) opening a process gas material inlet valve F101 at an inlet of a light hydrocarbon recovery part, introducing process gas 1A formed by reverse partial conversion into a process gas compression unit of the light hydrocarbon recovery part, normally adjusting a compressor of the process gas compression unit through a three-return one-surge-proof valve F102 and a four-return four-surge-proof valve F103, increasing the consumption of boiler water of a water scrubber 109 and fresh alkali of an alkali scrubber 111, and discharging the process gas from a four-section outlet pressure control valve F104 to release a torch when the outlet pressure of the four sections 1-4 of the compressor is overhigh;
o) after the process gas compression unit introduces the process gas 1A, stopping conveying the liquid-phase ethylene and the liquid-phase propylene to the process gas compression unit by the first ethylene conveying pump 221 and the propylene conveying pump 103, normally adjusting compressors of the process gas compression unit, normally adjusting the water scrubber 109 and the alkaline tower 111, and increasing the boiler water consumption of the water scrubber 109 and the fresh alkaline consumption of the alkaline tower 111;
p) increasing the consumption of a-25 ℃ propylene refrigerant in the second condenser 203 of the deethanizer, ensuring that the temperature of a process medium is below-14 ℃ after the process medium is condensed in the second condenser 203 of the deethanizer, adjusting the reboiling amount of a reboiler 206 of the deethanizer, enabling one part of non-condensable gas discharged from a reflux tank 204 of the deethanizer to slowly enter a demethanizer 207, controlling the pressure of the deethanizer to be 2.8-3.0 MPa through a torch valve F202 arranged on the top of the deethanizer, and adjusting a refrigeration unit of the-25 ℃ propylene refrigerant;
q) the liquid level of the reflux tank 204 of the deethanizer rises, the reflux quantity at the top of the deethanizer 201 is increased, the temperature of the kettle of the deethanizer 201 is controlled to be 93-96 ℃, and after the liquid level of the kettle of the deethanizer 201 rises, the kettle of the deethanizer 201 is sent to the depropanizer 301;
r) the demethanizer 207 is adjusted normally, the non-condensable gas at the top of the demethanizer 207 enters an ethylene recovery tower 213, the materials at the bottom of the demethanizer 207 are subjected to heat exchange by a first condenser 202 of a deethanizer, then a flare is directly discharged through a flare discharging valve F201 at the outlet of the first condenser of the deethanizer, when all the process gas and the condensed liquid discharged from the four-section discharge tank 106 enter the deethanizer 201, and the temperature at the top of the deethanizer is reduced to below-14 ℃, the flare discharging valve F201 at the outlet of the first condenser of the deethanizer is gradually closed, and the materials are fed into an ethylene tower 216;
s) the depropanizing tower 301 is normally adjusted after feeding, after the liquid level at the tower bottom of the depropanizing tower 301 rises, the carbon four washing liquid at the tower bottom is cooled by the carbon four washing liquid cooler 214, then sent to the ethylene recovery tower 213 and gradually increased in flow, and then sent to the depentanizing tower system 3A;
t) after the liquid level of the ethylene recovery tower 213 is established, the carbon four washing liquid at the tower bottom of the ethylene recovery tower 213 is sent to the deethanizer 201, and the flow is gradually increased;
u) after feeding of the ethylene tower 216, normally adjusting, taking out ethylene from a side line of the ethylene tower 216 to an ethylene unqualified tank, and cutting to an ethylene qualified tank after analysis is qualified;
v) adjusting the propylene dosage and the reboiling amount at 7 ℃ in the depropanizing tower 301, before the tower system parameters of the depropanizing tower 301 are not adjusted to the proper level, establishing a liquid level at the top of the depropanizing tower 301 by adjusting a pressure control valve, sending the liquid level to a No. 1 propylene rectifying tower 308, preferentially sending the liquid level at the bottom of the depropanizing tower 301 to an ethylene recovery tower 213 after rising, and sending the redundant part to a depentanizing tower system 3A;
w) normally adjusting the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310, controlling the pressure at the top of the 2# propylene rectifying tower 310 to be 1.6-1.9 MPa, the top temperature to be 42-45 ℃, the temperature of a tower kettle of the 1# propylene rectifying tower 308 to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310 to be 12-14, collecting propylene at the top of the 2# propylene rectifying tower 310 to a propylene unqualified tank, and cutting the propylene qualified tank after the propylene is qualified through analysis.
In this embodiment 2, the OCC apparatus normally operates, the crude propylene gas produced by the OCC apparatus returns to the light hydrocarbon recovery part, and liquid-phase ethylene and liquid-phase propylene are delivered to the process gas compression unit, so as to simulate a reverse re-reaction part to supply the process gas at a small flow rate, the light hydrocarbon part is driven in advance to supply qualified process gas to the reverse re-reaction part, and the liquid-phase ethylene is not delivered to the cold separation unit and used as the first cooler refrigerant of the deethanizer. The whole process from the process gas entering the light hydrocarbon recovery part to the production of qualified polymer-grade ethylene and polymer-grade propylene lasts for 12 hours, and the time of torch discharge lasts for 6 hours.
Example 3
Referring to fig. 1, a light hydrocarbon recovery and start-up method suitable for a methanol-to-olefin reaction short-time shutdown period specifically comprises the following steps:
(1) and during the short-time shutdown period of the reverse recycling part, the processing steps of the light hydrocarbon recovery part are as follows:
a) the olefin cracking device (OCC device) normally operates, the olefin cracking device conveys qualified crude propylene gas 1D to a process gas compression unit of a light hydrocarbon recovery part, and the crude propylene gas 1D is added behind a water scrubber 109 and in front of an alkaline scrubber 111 between a compressor three-section 1-3 and a compressor four-section 1-4 of the process gas compression unit, namely the input end of a process gas heater 110;
b) adjusting a three-return anti-surge valve F102 between the three sections 1-3 of the compressor and the section 1-1 of the compressor to ensure the flow of a suction inlet of the section of the suction tank 101;
c) after the first ethylene delivery pump 221 and the propylene delivery pump 103 are started, the first ethylene delivery pump 221 respectively introduces unqualified liquid-phase ethylene in an ethylene unqualified tank and unqualified liquid-phase propylene in a propylene unqualified tank to the input ends of the condenser 107 in the three sections of the process gas compression unit, the compressor of the process gas compression unit is normally adjusted, the outlet pressure of the four sections 1-4 of the compressor is increased to be more than 2.9MPa, the water scrubber 109 and the alkaline tower 111 are normally adjusted, the boiler water and alkaline tower 111 fresh alkali consumption of the water scrubber 109 is reduced, and the outlet temperature of the process gas of the four sections of the second aftercooler 115 is adjusted to be 14-16 ℃;
d) before the liquid level of the four-section discharge tank 116 is not established, the process gas discharged from the four-section discharge tank 116 enters the deethanizer 201 after being dried and qualified by the gas phase dryer 117, and after the liquid level of the four-section discharge tank 116 is established, the liquid phase of the four-section discharge tank 116 enters the deethanizer after being condensed and qualified by the condensate dryer 118;
e) the second ethylene transfer pump 222 introduces the unqualified liquid-phase ethylene in the unqualified ethylene tank to the first condenser 202 of the deethanizer as an ethylene refrigerant for heat exchange, so that the process medium at the top of the deethanizer 201 is condensed to be below 20 ℃ below zero;
f) adjusting the dosage of a-25 ℃ propylene refrigerant in the second condenser 203 of the deethanizer to ensure that the temperature of the process medium is below-21 ℃ after the process medium is condensed in the second condenser 203 of the deethanizer;
g) the reboiling amount of a reboiler 206 of the deethanizer is adjusted, so that the non-condensable gas discharged from a reflux tank 204 of the deethanizer slowly enters a demethanizer 207, the pressure of the deethanizer 201 is controlled to be 2.8-3.0 MPa, and the temperature at the top of the tower is adjusted to be below-17 ℃;
h) the liquid level of the reflux tank 204 of the deethanizer rises, the tower top reflux amount of the deethanizer 201 is increased, and materials extracted from the tower bottom of the deethanizer 201 are sent to the depropanizer 301 after the tower bottom liquid level of the deethanizer 201 rises;
i) the depropanizing tower 301 is normally adjusted after feeding, after the liquid level of the tower kettle of the depropanizing tower 301 is established, carbon four washing liquid at the tower kettle of the depropanizing tower 301 is cooled by a carbon four washing liquid cooler 214 and then is sent to an ethylene recovery tower 213, the flow is gradually increased, and the carbon four washing liquid is not sent to a depentanizing tower system 3A;
j) the gas phase discharged from the top of the deethanizer 201 directly enters the demethanizer 207 after being condensed, the demethanizer 207 starts to be adjusted, the reflux tank 211 of the demethanizer does not need to discharge a torch, the non-condensable gas at the top of the demethanizer 207 enters the ethane vaporizer 212 for heat exchange through the reflux tank 211 of the demethanizer, the liquid phase after heat exchange automatically flows back to the reflux tank 211 of the demethanizer, the gas phase enters the ethylene recovery tower 213, and the material at the bottom of the demethanizer 207 directly enters the ethylene tower 216 without discharging the torch after heat exchange through the first condenser 202 of the deethanizer;
k) controlling the pressure in the ethylene recovery tower 213 to be 2.4-2.6 MPa, and after the liquid level of the ethylene recovery tower 213 is established, sending the C4 washing liquid in the ethylene recovery tower 213 to the deethanizer 201 and gradually increasing the flow;
l) adjusting the dosage of 25 ℃ propylene and the dosage of-40 ℃ propylene refrigerant in the ethylene tower 216, controlling the pressure at the top of the ethylene tower 216 to be 1.6-1.7 MPa, the temperature at the top of the ethylene tower to be-37 ℃ to-31 ℃, controlling the reflux ratio to be 3.9-4.1, and collecting ethylene from the side line of the ethylene tower 216 to an ethylene qualified tank;
m) adjusting the using amount and the reboiling amount of propylene at 7 ℃ in the depropanizing tower 301, controlling the pressure at the top of the depropanizing tower 301 to be 0.7-0.9 MPa, the temperature at the top of the depropanizing tower to be 10-18 ℃, the temperature of a sensitive plate to be 35-45 ℃, establishing a liquid level at the top of the depropanizing tower, and sending the liquid level to a No. 1 propylene rectifying tower 308;
n) normally adjusting a 1# propylene rectifying tower 308 and a 2# propylene rectifying tower 310, controlling the pressure at the top of the 2# propylene rectifying tower 310 to be 1.6-1.9 MPa, the temperature at the top of the tower to be 42-45 ℃, the temperature of a kettle of the 1# propylene rectifying tower 308 to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310 to be 12-14, and collecting propylene at the top of the 2# propylene rectifying tower 310 to a propylene qualified tank;
(2) after the reverse recycling part is started to supply qualified process gas, the light hydrocarbon recovery part is started:
o) opening a process gas material inlet valve F101 at an inlet of the light hydrocarbon recovery part, introducing the process gas formed by reverse partial conversion into a process gas compression unit of the light hydrocarbon recovery part, and normally adjusting the process gas compression unit;
p) after the process gas compression unit introduces the process gas, the first ethylene delivery pump 221 and the propylene delivery pump 103 stop delivering the liquid-phase ethylene and the liquid-phase propylene to the process gas compression unit, the compressors of the process gas compression unit are normally adjusted, the water scrubber 109 and the alkaline tower 111 are normally adjusted, and the boiler water consumption of the water scrubber 109 and the fresh alkali consumption of the alkaline tower 111 are increased;
q) increasing the ethylene refrigerant usage of the first condenser 202 of the deethanizer, with the deethanizer 201 normally adjusted;
r) after the feed of the depropanizing tower 301 is normally adjusted, after the liquid level at the bottom of the depropanizing tower 301 rises, one part of the feed is sent to the ethylene recovery tower 213 after passing through the carbon four-washing liquid cooler 214, and the other part of the feed is sent to the depentanizing tower system 3A;
s) increasing the pressure in the ethylene recovery tower 213 to 2.6-2.8 MPa, and increasing the flow of the C4 washing liquid sent to the deethanizer 201;
t) normally adjusting the ethylene tower 216, leading the ethylene extracted from the side line of the ethylene tower 216 to an ethylene unqualified tank, leading the ethylene to an ethylene qualified tank after the ethylene is qualified through analysis, normally adjusting the 1# propylene rectifying tower 308 and the 2# propylene rectifying tower 310, leading the propylene extracted from the top of the 2# propylene rectifying tower 310 to a propylene unqualified tank, and leading the propylene to a propylene qualified tank after the propylene is qualified through analysis.
In this embodiment 3, the OCC apparatus normally operates, the crude propylene gas produced by the OCC apparatus returns to the light hydrocarbon recovery part, and liquid-phase ethylene and liquid-phase propylene are delivered to the process gas compression unit, so as to simulate the reverse re-reaction part to supply the process gas at a small flow rate, and the light hydrocarbon part is driven in advance to wait for the reverse re-reaction part to supply the qualified process gas, and the liquid-phase ethylene is delivered to the cold separation unit to be used as the first cooler refrigerant of the deethanizer. The whole process from the process gas entering the light hydrocarbon recovery part to the production of qualified polymer-grade ethylene and polymer-grade propylene lasts for 6 hours without the phenomenon of flame-off.
Although embodiments of the present invention have been shown and described, it will be appreciated by those skilled in the art that changes, modifications, substitutions and alterations can be made in these embodiments without departing from the principles and spirit of the invention, the scope of which is defined in the appended claims and their equivalents.
Claims (9)
1. A light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period is characterized in that: the method specifically comprises the following steps:
(1) and during the short-time shutdown period of the reverse recycling part, the processing steps of the light hydrocarbon recovery part are as follows:
a) the olefin cracking device normally operates, the olefin cracking device conveys qualified crude propylene gas to a process gas compression unit of a light hydrocarbon recovery part, and the crude propylene gas is added behind a water scrubber and in front of an alkali scrubber between a compressor three-section and a compressor four-section of the process gas compression unit;
b) adjusting a three-return anti-surge valve between the three sections of the compressor and the first section of the compressor to ensure the flow of the suction inlet of the first section of the suction tank;
c) after a first ethylene delivery pump and a propylene delivery pump are started, respectively introducing unqualified liquid-phase ethylene in an ethylene unqualified tank and unqualified liquid-phase propylene in a propylene unqualified tank to the input ends of three sections of aftercondensers of a process gas compression unit by the first ethylene delivery pump, normally adjusting a compressor of the process gas compression unit, increasing the pressure of an outlet of the four sections of the compressor to be more than 2.9MPa, normally adjusting a water scrubber and an alkali scrubber, reducing the using amount of fresh alkali of the boiler water of the water scrubber and the alkali scrubber, and adjusting the temperature of an outlet of the process gas of a second aftercooler of the four sections to be 14-16 ℃;
d) before the liquid level of the four-section discharge tank is not established, the process gas discharged from the four-section discharge tank is dried by a gas phase dryer and enters a deethanizer after being qualified, and after the liquid level of the four-section discharge tank is established, the liquid phase of the four-section discharge tank enters the deethanizer after being qualified by condensate condensation of a condensate dryer;
e) leading the unqualified liquid-phase ethylene in the unqualified ethylene tank to a first condenser of a deethanizer by a second ethylene delivery pump to be used as an ethylene refrigerant for heat exchange, so that the process medium at the top of the deethanizer is condensed to be below 20 ℃ below zero;
f) adjusting the dosage of a-25 ℃ propylene refrigerant in a second condenser of the deethanizer to ensure that the temperature of the process medium is below-21 ℃ after the process medium is condensed in the second condenser of the deethanizer;
g) adjusting the reboiling amount of a reboiler of the deethanizer to ensure that non-condensable gas discharged from a reflux tank of the deethanizer slowly enters the demethanizer, controlling the pressure of the deethanizer to be 2.8-3.0 MPa, and adjusting the temperature at the top of the tower to be below-17 ℃;
h) the liquid level of a reflux tank of the deethanizer rises, the tower top reflux amount of the deethanizer is increased, and materials collected at the tower bottom of the deethanizer are sent to a depropanizer after the liquid level of the tower bottom of the deethanizer rises;
i) after the material is fed into the depropanizing tower, the material is normally adjusted, after the liquid level is established at the tower bottom of the depropanizing tower, the carbon four washing liquid at the tower bottom of the depropanizing tower is cooled and then is sent to an ethylene recovery tower, the flow is gradually increased, and the carbon four washing liquid is not sent to a depentanizing tower system;
j) the gas phase discharged from the top of the deethanizer directly enters a demethanizer after being condensed, the demethanizer starts to be adjusted, a torch does not need to be discharged from a reflux tank of the demethanizer, the non-condensable gas at the top of the demethanizer enters an ethane vaporizer for heat exchange, the liquid phase after heat exchange returns to the reflux tank of the demethanizer through self-flowing, the gas phase enters an ethylene recovery tower, and the material at the bottom of the demethanizer directly enters the ethylene tower without discharging the torch after heat exchange through a first condenser of the deethanizer;
k) controlling the pressure in the ethylene recovery tower to be 2.4-2.6 MPa, and after the liquid level of the ethylene recovery tower is established, sending a C-C washing liquid in the ethylene recovery tower to a deethanizer and gradually increasing the flow;
l) adjusting the using amount of 25 ℃ propylene and-40 ℃ propylene refrigerant in the ethylene tower, controlling the pressure at the top of the ethylene tower to be 1.6-1.7 MPa, the temperature at the top of the ethylene tower to be-37 ℃ to-31 ℃, controlling the reflux ratio to be 3.9-4.1, and extracting ethylene from the side line of the ethylene tower to an ethylene qualified tank;
m) adjusting the using amount and the reboiling amount of propylene at 7 ℃ in a depropanizing tower, controlling the pressure at the top of the depropanizing tower to be 0.7-0.9 MPa, the temperature at the top of the depropanizing tower to be 10-18 ℃, the temperature of a sensitive plate to be 35-45 ℃, establishing a liquid level at the top of the depropanizing tower, and then sending the liquid level to a No. 1 propylene rectifying tower;
n) normally adjusting a 1# propylene rectifying tower and a 2# propylene rectifying tower, controlling the pressure at the top of the 2# propylene rectifying tower to be 1.6-1.9 MPa, the temperature at the top of the tower to be 42-45 ℃, the temperature of a kettle of the 1# propylene rectifying tower to be 50-60 ℃, controlling the reflux ratio between the 1# propylene rectifying tower and the 2# propylene rectifying tower to be 12-14, and collecting propylene from the top of the 2# propylene rectifying tower to a propylene qualified tank;
(2) after the reverse recycling part is started to supply qualified process gas, the light hydrocarbon recovery part is started:
o) opening a process gas material inlet valve at an inlet of the light hydrocarbon recovery part, introducing the process gas formed by reverse partial conversion into a process gas compression unit of the light hydrocarbon recovery part, and normally adjusting the process gas compression unit;
p) after the process gas compression unit introduces the process gas, the first ethylene delivery pump and the propylene delivery pump stop delivering the liquid-phase ethylene and the liquid-phase propylene to the process gas compression unit, the compressors of the process gas compression unit are normally adjusted, and the water washing tower and the alkaline washing tower are normally adjusted, so that the consumption of boiler water of the water washing tower and fresh alkaline of the alkaline washing tower is increased;
q) increasing the ethylene refrigerant dosage of the first condenser of the deethanizer, and normally adjusting the deethanizer;
r) the depropanizing tower is normally adjusted after feeding, after the liquid level at the tower kettle of the depropanizing tower rises, one part of the liquid is sent to an ethylene recovery tower after passing through a carbon four washing liquid cooler, and the other part of the liquid is sent to a depentanizing tower system;
s) increasing the pressure in the ethylene recovery tower to 2.6-2.8 MPa, and increasing the flow of the C-C washing liquid sent to the deethanizer;
t) normally adjusting the ethylene tower, leading the ethylene extracted from the side line of the ethylene tower to an ethylene unqualified tank, leading the ethylene to an ethylene qualified tank after the ethylene is qualified through analysis, normally adjusting a 1# propylene rectifying tower and a 2# propylene rectifying tower, leading the propylene extracted from the top of the 2# propylene rectifying tower to a propylene unqualified tank, and leading the propylene to a propylene qualified tank after the propylene is qualified through analysis.
2. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the pressure of the qualified crude propylene gas in the step a) is more than 1.8MPa, and the sum of the gas contents of propylene and ethylene in the qualified crude propylene gas is 75 percent.
3. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the temperature of the unqualified liquid-phase ethylene in the ethylene unqualified tank is below minus 32 ℃, the pressure is above 2.2MPa, the volume content of carbon dioxide in the unqualified liquid-phase ethylene is below 5ppm, and the volume content of water is below 1 ppm.
4. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the pressure of the unqualified liquid phase propylene in the unqualified propylene tank is more than 3.1MPa, the volume content of carbon dioxide in the unqualified liquid phase propylene is less than 5ppm, and the volume content of water is less than 1 ppm.
5. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the temperature of the tower kettle of the deethanizer is always controlled to be 93-96 ℃ in the whole feeding process, so that the qualified extraction of the tower kettle of the deethanizer is ensured.
6. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the content of ethylene in the material extracted from the tower bottom of the deethanizer is below 20ppm, and the content of ethane is below 150 ppm.
7. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: the temperature of the process gas formed by the reverse and re-partial conversion is below 50 ℃, and the volume content of dimethyl ether in the process gas is below 3000 ppm.
8. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: in the qualified ethylene in the ethylene qualified tank, the volume content of ethylene is more than 99.95 percent, the volume content of carbon monoxide is less than 1ppm, the volume content of carbon dioxide is less than 5ppm, the volume content of heavy components of carbon three or more is less than 10ppm, the volume content of acetylene is less than 5ppm, the volume content of methanol is less than 4ppm, and the volume content of water is less than 1 ppm.
9. The light hydrocarbon recovery startup method suitable for the methanol-to-olefin reaction short-time shutdown period of claim 1, wherein: in the qualified propylene in the propylene qualified tank, the volume content of propylene is more than 99.6 percent, the volume content of carbon monoxide is less than 2ppm, the volume content of carbon dioxide is less than 1ppm, the volume content of propane is less than 0.4 percent, the volume content of ethylene is less than 10ppm, the volume content of methanol is less than 5ppm, the volume content of water is less than 2ppm, the sum of the volume contents of propyne and propadiene is less than 5ppm, the sum of the volume contents of butylene and butadiene is less than 2ppm, the volume content of acetylene is less than 2ppm, and the volume content of dimethyl ether is less than 2 ppm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111165163.1A CN113788735B (en) | 2021-09-30 | 2021-09-30 | Light hydrocarbon recovery start-up method suitable for short-time shutdown period of methanol-to-olefin reaction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202111165163.1A CN113788735B (en) | 2021-09-30 | 2021-09-30 | Light hydrocarbon recovery start-up method suitable for short-time shutdown period of methanol-to-olefin reaction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113788735A true CN113788735A (en) | 2021-12-14 |
| CN113788735B CN113788735B (en) | 2024-05-10 |
Family
ID=78877751
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202111165163.1A Active CN113788735B (en) | 2021-09-30 | 2021-09-30 | Light hydrocarbon recovery start-up method suitable for short-time shutdown period of methanol-to-olefin reaction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113788735B (en) |
Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1983004249A1 (en) * | 1982-06-03 | 1983-12-08 | Linde Aktiengesellschaft | Method for the preparation of olefins with lower molecular weigth |
| CN1833017A (en) * | 2003-08-06 | 2006-09-13 | 埃克森美孚化学专利公司 | Recovery of ethylene and propylene from a methanol to olefin reaction system |
| CN103626619A (en) * | 2013-12-02 | 2014-03-12 | 中国天辰工程有限公司 | Light hydrocarbon separation method used in methanol to olefin device |
| CN207973691U (en) * | 2018-01-31 | 2018-10-16 | 中国寰球工程有限公司 | The lighter hydrocarbons piece-rate system of MTO product mix gas |
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
| CN111072438A (en) * | 2019-12-09 | 2020-04-28 | 久泰能源(准格尔)有限公司 | Methanol-to-olefin (MTO) reverse recycling process and product separation method |
| CN210825990U (en) * | 2019-10-15 | 2020-06-23 | 久泰能源(准格尔)有限公司 | Pressure release light hydrocarbon recovery system of MTO device |
| CN113943200A (en) * | 2021-11-15 | 2022-01-18 | 中安联合煤化有限责任公司 | Methanol-to-olefin light hydrocarbon recovery part cold separation unit and light hydrocarbon separation method thereof |
| CN216513606U (en) * | 2021-11-15 | 2022-05-13 | 中安联合煤化有限责任公司 | Methanol-to-olefin light hydrocarbon recovery part cold separation unit |
| CN115193343A (en) * | 2022-07-27 | 2022-10-18 | 天津渤化化工发展有限公司 | Methanol-to-olefin device and start-up method thereof |
| CN218742012U (en) * | 2022-12-08 | 2023-03-28 | 中国石化中原石油化工有限责任公司 | Ethylene recovery system in methanol-to-olefin device |
| CN218740300U (en) * | 2022-08-30 | 2023-03-28 | 中煤陕西榆林能源化工有限公司 | Light hydrocarbon recovery device in methanol-to-olefin system |
-
2021
- 2021-09-30 CN CN202111165163.1A patent/CN113788735B/en active Active
Patent Citations (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1983004249A1 (en) * | 1982-06-03 | 1983-12-08 | Linde Aktiengesellschaft | Method for the preparation of olefins with lower molecular weigth |
| CN1833017A (en) * | 2003-08-06 | 2006-09-13 | 埃克森美孚化学专利公司 | Recovery of ethylene and propylene from a methanol to olefin reaction system |
| CN103626619A (en) * | 2013-12-02 | 2014-03-12 | 中国天辰工程有限公司 | Light hydrocarbon separation method used in methanol to olefin device |
| CN207973691U (en) * | 2018-01-31 | 2018-10-16 | 中国寰球工程有限公司 | The lighter hydrocarbons piece-rate system of MTO product mix gas |
| CN110092701A (en) * | 2018-01-31 | 2019-08-06 | 中国寰球工程有限公司 | The lighter hydrocarbons separation system and method for MTO product mix gas |
| CN210825990U (en) * | 2019-10-15 | 2020-06-23 | 久泰能源(准格尔)有限公司 | Pressure release light hydrocarbon recovery system of MTO device |
| CN111072438A (en) * | 2019-12-09 | 2020-04-28 | 久泰能源(准格尔)有限公司 | Methanol-to-olefin (MTO) reverse recycling process and product separation method |
| CN113943200A (en) * | 2021-11-15 | 2022-01-18 | 中安联合煤化有限责任公司 | Methanol-to-olefin light hydrocarbon recovery part cold separation unit and light hydrocarbon separation method thereof |
| CN216513606U (en) * | 2021-11-15 | 2022-05-13 | 中安联合煤化有限责任公司 | Methanol-to-olefin light hydrocarbon recovery part cold separation unit |
| CN115193343A (en) * | 2022-07-27 | 2022-10-18 | 天津渤化化工发展有限公司 | Methanol-to-olefin device and start-up method thereof |
| CN218740300U (en) * | 2022-08-30 | 2023-03-28 | 中煤陕西榆林能源化工有限公司 | Light hydrocarbon recovery device in methanol-to-olefin system |
| CN218742012U (en) * | 2022-12-08 | 2023-03-28 | 中国石化中原石油化工有限责任公司 | Ethylene recovery system in methanol-to-olefin device |
Non-Patent Citations (2)
| Title |
|---|
| 王子宗: "甲醇制丙烯产品气分离工艺的开发", 《石油化工》, vol. 44, no. 3, 1 March 2015 (2015-03-01), pages 5 - 10 * |
| 马颖足: "甲醇制烯烃工艺烯烃分离开停工与运行优化", 《石化技术》, vol. 27, no. 7, 31 July 2020 (2020-07-31), pages 95 - 97 * |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113788735B (en) | 2024-05-10 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN1727317B (en) | Secondary deethanizer to debottleneck an ethylene plant | |
| US4979966A (en) | Process and apparatus for the dehydration, deacidification, and separation of a condensate from a natural gas | |
| KR100338407B1 (en) | Compound Condensation-Absorbing Method to Recover Olefin | |
| CN109111336B (en) | Deep cooling recovery device and process for waste towed synthetic tail gas | |
| CN107827698B (en) | Non-cryogenic separation method and system for ethylene-containing pyrolysis gas | |
| CN216513606U (en) | Methanol-to-olefin light hydrocarbon recovery part cold separation unit | |
| CN216536963U (en) | Separation system of sulfuric acid alkylation reaction product | |
| RU2688533C1 (en) | Ltdr plant for integrated gas preparation and production of lng and its operation method | |
| CN113788735A (en) | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period | |
| CN110407658B (en) | Low-energy-consumption cryogenic separation process method for ethane pyrolysis gas | |
| CN111320523B (en) | Method and device for separating ethylene from refinery dry gas | |
| CN111004079B (en) | Separation method and device for reaction gas for preparing ethylene by oxidative coupling of methane | |
| CN110590490B (en) | System and method for recovering hydrocarbons in liquefied natural gas | |
| CN104342205A (en) | Ethylene device driving method of front-end deethanization process | |
| CN113943200A (en) | Methanol-to-olefin light hydrocarbon recovery part cold separation unit and light hydrocarbon separation method thereof | |
| CN111320524A (en) | Method and device for separating ethylene and propylene from pyrolysis gas and/or dry gas | |
| CN113354501B (en) | Separation method for recovering C1, C2 and C3 in catalytic rich gas by combined absorption method | |
| CN111320522B (en) | Method and device for separating ethylene from refinery dry gas | |
| CN111004081B (en) | Separation method and device for reaction gas for preparing ethylene by oxidative coupling of methane | |
| CN101792679B (en) | Energy-saving method for vaporizing feed of propylene depolymerization oil tower by stepped utilization of low-temperature wastewater and device thereof | |
| CN112028734A (en) | Recovery device and recovery process for reaction product of propane dehydrogenation propylene preparation | |
| CN110701485A (en) | Recycling method and system of fuel gas of methanol-to-olefin device byproduct | |
| CN112760127B (en) | Oil-gas separation and recovery device and method | |
| CN111470933B (en) | C3 separation method capable of saving energy and reducing equipment | |
| CN112374957B (en) | Ethylene recycling method |
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 |