CN113943200A - Methanol-to-olefin light hydrocarbon recovery part cold separation unit and light hydrocarbon separation method thereof - Google Patents
Methanol-to-olefin light hydrocarbon recovery part cold separation unit and light hydrocarbon separation method thereof Download PDFInfo
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- 238000011084 recovery Methods 0.000 title claims abstract description 65
- 238000000926 separation method Methods 0.000 title claims abstract description 50
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 38
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 37
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 36
- 239000005977 Ethylene Substances 0.000 claims abstract description 157
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims abstract description 150
- 238000010992 reflux Methods 0.000 claims abstract description 66
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims abstract description 35
- 239000006200 vaporizer Substances 0.000 claims abstract description 34
- 239000000463 material Substances 0.000 claims abstract description 24
- 239000003507 refrigerant Substances 0.000 claims abstract description 11
- 238000000034 method Methods 0.000 claims description 32
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 30
- 239000007789 gas Substances 0.000 claims description 29
- 239000007788 liquid Substances 0.000 claims description 26
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 claims description 19
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 claims description 19
- 229910052799 carbon Inorganic materials 0.000 claims description 18
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 17
- 239000007791 liquid phase Substances 0.000 claims description 16
- 238000005406 washing Methods 0.000 claims description 16
- 239000002737 fuel gas Substances 0.000 claims description 15
- 239000012071 phase Substances 0.000 claims description 13
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 claims description 12
- LCGLNKUTAGEVQW-UHFFFAOYSA-N Dimethyl ether Chemical compound COC LCGLNKUTAGEVQW-UHFFFAOYSA-N 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 8
- 239000013589 supplement Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 7
- 229910002092 carbon dioxide Inorganic materials 0.000 claims description 6
- 239000001569 carbon dioxide Substances 0.000 claims description 6
- 238000004458 analytical method Methods 0.000 claims description 2
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 6
- 230000008901 benefit Effects 0.000 abstract description 3
- 238000004064 recycling Methods 0.000 abstract description 2
- 239000002699 waste material Substances 0.000 abstract description 2
- 150000001336 alkenes Chemical class 0.000 description 6
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 5
- 230000006835 compression Effects 0.000 description 4
- 238000007906 compression Methods 0.000 description 4
- 150000001993 dienes Chemical class 0.000 description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 238000005057 refrigeration Methods 0.000 description 4
- 239000003245 coal Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000001502 supplementing effect Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 239000001294 propane Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000005215 recombination Methods 0.000 description 1
- 230000006798 recombination Effects 0.000 description 1
- 239000010117 shenhua Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
- C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
-
- 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
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- 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
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- 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
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- Engineering & Computer Science (AREA)
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- Oil, Petroleum & Natural Gas (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a methanol-to-olefin light hydrocarbon recovery part cold separation unit and a light hydrocarbon separation method thereof, and the unit comprises a deethanizer, a demethanizer, an ethane vaporizer, an ethylene rectifying tower, an ethylene recovery tower and other devices, wherein the ethane vaporizer can collect noncondensable gas containing ethylene in a reflux tank of the demethanizer and reuse the ethylene contained in the reflux tank of the demethanizer on one hand; on the other hand, the ethane in the tower bottom material can be gasified and separated after the tower bottom material of the ethylene rectifying tower enters the ethane vaporizer, and the separated material is conveyed to the ethylene recovery tower for recycling, so that the yield of ethylene can be increased, the resource waste is reduced, and the ethylene rectifying tower has good economic benefit. In addition, the invention also adds an ethylene replenishing pipeline to the first condenser of the deethanizer, and can provide enough refrigerant for the first condenser of the deethanizer in the early stage of start-up, so that the deethanizer can enter a stable operation state in a short time, the start-up time is shortened, and the production efficiency is improved.
Description
Technical Field
The invention belongs to the technical field of coal chemical industry, and particularly relates to a methanol-to-olefin light hydrocarbon recovery part cold separation unit and a light hydrocarbon separation method thereof.
Background
The methanol-to-olefin (MTO) process is a pivotal technology of a process route for preparing olefin from coal, realizes important conversion of coal into ethylene and propylene through methanol, is an important supplement to a traditional route for preparing olefin by taking petroleum as a raw material, and is a breakthrough of a petroleum substitution strategy. D-MTO developed by a large-connected substance in 8 months in 2010 is built and put into production in Shenhua Baotou, and the national petrochemical independent intellectual property S-MTO technology is built and put into production in the original petrochemical for the first time in 10 months in 2011, so that more than 40 methanol-to-olefin plants which are built or put into production in China currently have large capacity.
The methanol-to-olefin light hydrocarbon recovery part comprises a process gas compression unit, a cold separation unit, a heat separation unit, a propylene refrigeration unit and the like, wherein the process of the cold separation unit refers to the process from the step that materials enter the cold separation unit to the step that qualified polymer-grade ethylene is produced through rectification. At present, in the process of starting a cold separation unit of the Chinese petrochemical S-MTO technology, a first condenser at the top of a deethanizer does not contain refrigerant during starting, so that the temperature at the top of the deethanizer is higher, the reflux quantity is insufficient, the tower is subjected to overpressure flare discharge, the content of carbon III and recombination in materials at the top of the tower exceeds the standard, the tower cannot be quickly adjusted to a normal state, and the flare needs to be discharged from an outlet valve of a first cooler of the deethanizer; the contents of carbon dioxide and light components in materials from the tower kettle of the deethanizer to the depropanizer exceed standards, a torch needs to be put from the top of the depropanizer to maintain the tower pressure, and meanwhile, the depropanization operation is unstable, so that qualified carbon four washing liquid cannot be timely conveyed to the ethylene recovery tower and the deethanizer, and the deethanization stable operation is not facilitated. In addition, the heavy components fed into the ethylene rectifying tower exceed the standard, so that the polymer-grade ethylene is not extracted for a long time, the heavy components in the tower kettle exceed the standard, so that the heating effect of a reboiler is poor, and a torch needs to be placed at the bottom of the reboiler when the reboiler is serious. Because the top of the deethanizer is free of refrigerant, heating of a tower kettle is necessarily reduced in normal operation, and the tower kettle is cooled, so that part of light components are substituted into a thermal separation unit, and finally, the carbon four washing liquid cannot be circulated at the highest speed, and the rapid establishment of circulation of an ethylene recovery tower and the deethanizer is influenced. In addition, in the operation process of the existing cold separation unit, the components discharged from the top of the demethanizer and the tower bottom materials of the ethylene tower both contain a certain amount of ethylene, and if the materials are treated again to improve the recovery rate of the ethylene, the cold separation unit has important significance for reducing the cost and improving the production efficiency.
How to enable the top of the deethanizer tower to be cooled more quickly without reducing the heating quantity of the tower kettle; how to shorten the time of the flare and reduce the loss of diene products, and simultaneously, the carbon four-washing liquid of the back system returns to the deethanizer as soon as possible is an important technical subject. The start-up scheme of the traditional methanol-to-olefin light hydrocarbon recovery part cold separation unit has long start-up period, long time of a flame, large diene loss and large environmental protection pressure.
Disclosure of Invention
Aiming at the defects of the prior art, the invention aims to provide a methanol-to-olefin light hydrocarbon recovery part cold separation unit and a light hydrocarbon separation method thereof, wherein an ethylene supplement pipeline is connected to a first condenser of a deethanizer to quickly enable the deethanizer to enter a stable operation state in the early stage of start-up and shorten the start-up time; the ethane vaporizer is arranged among the demethanizer, the ethylene rectifying tower and the ethylene recovery tower, so that the ethylene yield is improved.
In order to achieve the purpose, the invention adopts the technical scheme that:
a methanol-to-olefin light hydrocarbon recovery part cold separation unit comprises a deethanizer, a demethanizer, an ethane vaporizer, an ethylene rectifying tower and an ethylene recovery tower, wherein:
the system comprises a deethanizer, a deethanizer reflux tank, a deethanizer reflux pump and a deethanizer reflux pump, wherein the deethanizer reflux tank is connected with the deethanizer; the top gas phase outlet of the deethanizer reflux tank is connected with the tower body inlet of the demethanizer; and a deethanizer reboiler is arranged at the lower part of the deethanizer.
The outlet of the top of the demethanizer is sequentially connected with a demethanizer condenser, a demethanizer reflux tank and an ethane vaporizer; the ethane vaporizer comprises a first inlet, a first outlet, a second inlet, a second outlet, and a fuel gas outlet; a top gas phase outlet of the demethanizer reflux tank is connected with a first inlet of an ethane vaporizer, a first outlet of the ethane vaporizer is connected with a liquid phase inlet of the demethanizer reflux tank, a liquid phase outlet of the demethanizer reflux tank is connected with a top inlet of the demethanizer, and a demethanizer reflux pump is arranged between the liquid phase outlet of the demethanizer reflux tank and the top inlet of the demethanizer; a fuel gas outlet of the ethane vaporizer is connected with a fuel gas pipe network; a second outlet of the ethane vaporizer is connected with an inlet at the lower part of the tower body of the ethylene recovery tower; the lower part of the demethanizer is provided with a demethanizer reboiler; .
The outlet of the bottom of the demethanizer is connected with a demethanizer discharge pipeline, and the demethanizer discharge pipeline passes through a first condenser of the deethanizer and then is connected with the inlet of the ethylene rectifying tower; the tower bottom outlet of the ethylene rectifying tower is connected with the second inlet of the ethane vaporizer; collecting qualified polymerization-grade ethylene from a discharge hole at the upper part of the ethylene rectifying tower; further, an outlet at the top of the ethylene rectifying tower is sequentially connected with an ethylene rectifying tower condenser and an ethylene rectifying tower reflux tank, and an outlet at the bottom of the ethylene rectifying tower reflux tank is connected with an inlet at the top of the ethylene rectifying tower through an ethylene rectifying tower reflux pump; the lower part of the ethylene rectifying tower is provided with an ethylene rectifying tower reboiler;
an outlet at the top of the ethylene recovery tower is connected with a fuel gas pipe network, and an outlet at the bottom of the ethylene recovery tower is connected with an inlet at the body of the deethanizer; and a kettle pump of the ethylene recovery tower is arranged on a pipeline between the ethylene recovery tower and the deethanizer.
As a preferable technical scheme, the methanol-to-olefin light hydrocarbon recovery part cold separation unit further comprises an ethylene make-up line, an outlet end of the ethylene make-up line is combined with a demethanizer discharge line and then introduced into a first condenser of a deethanizer, and an inlet end of the ethylene make-up line is connected with an ethylene ball tank through an ethylene delivery pump. The ethylene is conveyed to the first condenser of the deethanizer as a refrigerant through the ethylene supplementing pipeline in the early stage of start-up, so that the deethanizer can rapidly enter a stable operation state, and the start-up time is shortened.
As a preferred technical scheme, a tower bottom outlet of the deethanizer is connected with a tower body inlet of the depropanizer, and a tower bottom discharge pipeline of the deethanizer is provided with a deethanizer kettle cooler; the tower bottom outlet of the depropanizing tower is connected with the tower body inlet of the ethylene recovery tower through a depropanizing tower discharging pipeline; and a depropanizing tower reboiler is arranged at the lower part of the depropanizing tower. Furthermore, a depropanizing tower kettle pump and a carbon four-washing liquid cooler are arranged on a depropanizing tower discharge pipe line.
The invention also provides a method for separating light hydrocarbon of a cold separation unit of a light hydrocarbon recovery part of olefin from methanol, which is characterized in that low-temperature high-pressure ethylene is conveyed to a first condenser of a deethanizer through an ethylene supplement pipeline in the early stage of starting up to be used as a refrigerant, so that the deethanizer can quickly enter a stable operation state, qualified intermediate materials are conveyed to the downstream of the top and the bottom of the deethanizer as quickly as possible, the start-up time is shortened, the process gas flare amount is reduced, and the diene loss amount is reduced; the scheme is operated under the condition that the cold separation unit does not return materials, and good practical application is obtained.
Compared with the prior art, the invention has the beneficial effects that:
(1) the ethane vaporizer in the methanol-to-olefin light hydrocarbon recovery part cold separation unit provided by the invention has the following two functions: on one hand, noncondensable gas containing ethylene and methane hydrogen in a reflux tank of the demethanizer can be collected, after the noncondensable gas exchanges heat in an ethane vaporizer, the generated liquid phase automatically flows back to the reflux tank of the demethanizer, the gas phase enters the lower part of an ethylene recovery tower, the carbon four washing liquid at the tower bottom of the depropanizer is used as absorption liquid to dissolve the ethylene by utilizing the similar phase-dissolving principle of the carbon four washing liquid and the ethylene, and enters a deethanizer to recover the ethylene, and the methane hydrogen enters a fuel gas pipe network; the method has the advantages that while the yield of ethylene is improved, the material in the bottom of the demethanizer is directly fed into an ethylene rectifying tower without discharging a torch after heat exchange through a first condenser at the top of the deethanizer; on the other hand, the ethane in the tower bottom material can be gasified and separated after the tower bottom material of the ethylene rectifying tower enters the ethane vaporizer, and the separated material is conveyed to the ethylene recovery tower for recycling, so that the yield of ethylene can be increased, the resource waste is reduced, and the ethylene rectifying tower has good economic benefit.
(2) According to the cold separation unit for the light hydrocarbon recovery part of the olefin prepared from methanol, provided by the invention, the ethylene supplement pipeline is additionally arranged on the first condenser of the deethanizer, so that enough refrigerant can be provided for the first condenser of the deethanizer in the early stage of start-up, the deethanizer can enter a stable operation state in a short time, the start-up time is shortened, and the production efficiency is improved.
Drawings
FIG. 1 is a schematic structural diagram of a partial cold separation unit for recovering light hydrocarbons from methanol to olefins according to the present invention;
reference numerals: 1-a deethanizer; 2-a deethanizer first condenser; 3-deethanizer second condenser (-25 ℃ propylene refrigerant); 4-deethanizer reflux drum; 5-a demethanizer; 6-an ethylene recovery column; 7-an ethylene rectification column; 8-depropanizer; 9-an ethylene transfer pump; 10-demethanizer condenser (-40 ℃ propylene refrigerant); 11-demethanizer reflux drum; a 12-ethane vaporizer; 1201-first inlet, 1202-first outlet, 1203-second inlet, 1204-second outlet, 1205-fuel gas outlet, 13-deethanizer reboiler; 14-a deethanizer column kettle cooler; 15-deethanizer reflux pump; a 16-depropanizer reboiler; 17-depropanizer kettle pump; 18-demethanizer reboiler (25 ℃ propylene); a 19-carbon four wash cooler; 20-demethanizer reflux pump; 21-ethylene recovery column kettle pump; 22-ethylene rectifier reboiler (25 ℃ propylene); 23-ethylene rectification column condenser (-40 ℃ propylene); 24-ethylene rectification column reflux drum; 25-ethylene rectification column reflux pump; 26-ethylene supplement pipeline, 27-depropanizer discharge pipeline, 28-demethanizer discharge pipeline and A-fuel gas pipe network; b-ethylene ball tank.
Detailed Description
The invention is further described with reference to the following figures and examples.
In the present invention, unless otherwise expressly stated or limited, the terms "mounted," "connected," and the like are to be construed broadly and can include, for example, fixed connections, removable connections, or integral connections; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
In the description of the present invention, it is to be understood that the terms "upper", "lower", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, and are used only for convenience in describing the present invention and for simplicity in description, and do not indicate or imply that the referenced devices or elements must have a specific orientation, be constructed and operated in a specific orientation, and thus, are not to be construed as limiting the present invention. The terms "first," "second," and "third" as used herein do not denote any particular order or quantity, but rather are used to distinguish one element from another.
Referring to fig. 1, a methanol-to-olefin light hydrocarbon recovery part cold separation unit includes a deethanizer 1, a demethanizer 5, an ethane vaporizer 12, an ethylene rectification tower 7, and an ethylene recovery tower 6, wherein:
the tower top outlet of the deethanizer 1 is sequentially connected with a deethanizer first condenser 2, a deethanizer second condenser 3 and a deethanizer reflux tank 4, the bottom liquid phase outlet of the deethanizer reflux tank 4 is connected with the tower top inlet of the deethanizer 1, and further, a deethanizer reflux pump 4 is arranged between the bottom liquid phase outlet of the deethanizer reflux tank 4 and the tower top inlet of the deethanizer 1; the top gas phase outlet of the deethanizer reflux tank 4 is connected with the tower body inlet of the demethanizer 5; the lower part of the deethanizer 1 is provided with a deethanizer reboiler 13.
The outlet of the top of the demethanizer 5 is sequentially connected with a demethanizer condenser 10, a demethanizer reflux tank 11 and an ethane vaporizer 12; the ethane vaporizer 12 comprises a first inlet 1201, a first outlet 1202, a second inlet 1203, a second outlet 1204, and a fuel gas outlet 1205; the top gas phase outlet of the demethanizer reflux tank 11 is connected with the first inlet 1201 of the ethane vaporizer, the first outlet 1202 of the ethane vaporizer is connected with the liquid phase inlet of the demethanizer reflux tank 11, the liquid phase outlet of the demethanizer reflux tank 11 is connected with the top inlet of the demethanizer 5, and further, a demethanizer reflux pump 20 is installed between the liquid phase outlet of the demethanizer reflux tank 11 and the top inlet of the demethanizer 5; a fuel gas outlet 1205 of the ethane vaporizer 12 is connected with a fuel gas pipe network A; a second outlet 1204 of the ethane vaporizer is connected with an inlet at the lower part of the tower body of the ethylene recovery tower 6; the lower part of the demethanizer 5 is provided with a demethanizer reboiler 18, and propylene at 25 ℃ is introduced into the demethanizer reboiler 18.
A demethanizer discharging pipeline 28 is connected to the outlet of the bottom of the demethanizer 5, and the demethanizer discharging pipeline 28 passes through the first condenser 2 of the deethanizer and is connected with the inlet of the ethylene rectifying tower 7; the outlet at the bottom of the ethylene rectifying tower 7 is connected with a second inlet 1203 of an ethane vaporizer; qualified polymer-grade ethylene is collected from a discharge hole at the upper part of the ethylene rectifying tower 7; further, an outlet at the top of the ethylene rectifying tower 7 is sequentially connected with an ethylene rectifying tower condenser 23 and an ethylene rectifying tower reflux tank 24, and an outlet at the bottom of the ethylene rectifying tower reflux tank 24 is connected with an inlet at the top of the ethylene rectifying tower 7 through an ethylene rectifying tower reflux pump 25; an ethylene rectifying tower reboiler 22 is arranged at the lower part of the ethylene rectifying tower 7, and propylene at 25 ℃ is introduced into the ethylene rectifying tower reboiler 22;
an outlet at the top of the ethylene recovery tower 6 is connected with a fuel gas pipe network A, and an outlet at the bottom of the ethylene recovery tower 6 is connected with an inlet at the body of the deethanizer 1; and an ethylene recovery tower kettle pump 21 is arranged on a pipeline between the ethylene recovery tower 6 and the deethanizer 1.
As a preferred technical scheme, a tower bottom outlet of the deethanizer 1 is connected with a tower body inlet of the depropanizer 8, and a deethanizer kettle cooler 14 is installed on a tower bottom discharge pipeline of the deethanizer 1; the tower bottom outlet of the depropanizing tower 8 is connected with the tower body inlet of the ethylene recovery tower 6 through a depropanizing tower discharging pipeline 27; the lower part of the depropanizer 8 is provided with a depropanizer reboiler 16. Further, a depropanizer kettle pump 17 and a carbon four-washing liquid cooler 19 are arranged on the depropanizer discharge pipeline 27.
As a preferable technical scheme, the methanol-to-olefin light hydrocarbon recovery part cold separation unit further comprises an ethylene make-up line 26, an outlet end of the ethylene make-up line 26 is combined with a demethanizer discharge line 28 and then introduced into the first condenser 2 of the deethanizer, and an inlet end of the ethylene make-up line 26 is connected with the ethylene spherical tank B through an ethylene transfer pump 9. Low-temperature high-pressure ethylene is conveyed to a first condenser 2 of the deethanizer through an ethylene supplementing pipeline 26 as a refrigerant in the early stage of start-up, so that the deethanizer 1 can quickly enter a stable operation state, qualified intermediate materials are conveyed to the downstream direction from the top and the bottom of the deethanizer as quickly as possible, the start-up time is shortened, the process gas flare amount is reduced, and the diene loss amount is reduced; the scheme is operated under the condition that the cold separation unit does not return materials, and good practical application is obtained.
The recovery part of light hydrocarbon from olefin preparation by methanol comprises a process gas compression unit, a cold separation unit, a heat separation unit, a propylene refrigeration unit and the like, wherein the process of the cold separation unit refers to the process from the material entering the cold separation unit to the rectification for producing qualified polymer grade ethylene, when the process gas compression unit introduces feed, a torch is put at an outlet of four sections, the full reflux of the heat separation unit is established, when the propylene refrigeration unit operates stably, the cold separation unit maintains pressure and keeps liquid in an ethylene recovery tower, the full reflux of a deethanizer 1, a demethanizer 5 and an ethylene rectification tower 7 is established, and when the process gas (the methanol content of the process gas is below 15ppm, the water content is below 1ppm, the dimethyl ether is below 500ppm and the carbon dioxide is below 2 ppm) and condensate (the methanol content of the condensate is below 15ppm, the water content is below 1ppm and the dimethyl ether is below 500 ppm) enter the deethanizer 1 after the process gas compression unit dries and is qualified, the treatment is carried out according to the following steps:
a) starting an ethylene delivery pump 9, introducing ethylene to a first condenser 2 of the deethanizer for heat exchange, and condensing the process medium at the top of the deethanizer to be below 20 ℃ below zero; further, the ethylene temperature is below 32 ℃ below zero, the pressure is above 2.2MPa, the carbon dioxide content is below 5ppm, and the water content is below 1 ppm;
b) adjusting the dosage of a propylene refrigerant at-25 ℃ of a second condenser of the deethanizer, ensuring that the temperature of a process medium is below-21 ℃ after the process medium is cooled in the second condenser 3 of the deethanizer, and simultaneously adjusting a propylene refrigeration unit;
c) the reboiling amount of a reboiler 13 of the deethanizer is increased, the non-condensable gas in a reflux tank 4 of the deethanizer slowly enters a demethanizer 5, the pressure of the deethanizer 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 ℃;
d) the liquid level of the reflux tank 4 of the deethanizer rises, and the reflux quantity at the top of the deethanizer is increased;
e) after the liquid level of the tower bottom of the deethanizer 1 rises, the tower bottom materials (C3 and heavy components) are sent to a depropanizer 8;
f) after the material is fed into the depropanizing tower 8, the adjustment is started, after the liquid level is established in the tower kettle, the carbon four washing liquid in the tower kettle is preferentially sent to the ethylene recovery tower 6, the flow is gradually increased, and then the normal extraction is carried out; the content of propylene in the carbon four-washing liquid 6 is less than 0.1 percent (mass fraction), and the content of propane is less than 0.1 percent (mass fraction);
g) the gas phase at the top of the deethanizer 1 directly enters a demethanizer 5 after heat exchange and condensation through a deethanizer first condenser 2 and a deethanizer second condenser 3, the demethanizer 5 starts to adjust, a torch does not need to be placed in a demethanizer reflux tank 11, the non-condensable gas at the top of the demethanizer 5 enters an ethane vaporizer 12 for heat exchange, the liquid phase automatically flows back to the demethanizer reflux tank 11, the gas phase enters an ethylene recovery tower 6, and the gas phase entering the ethylene recovery tower 6 is absorbed and recycled by the action of a carbon four washing liquid; the material in the bottom of the demethanizer is directly sent into an ethylene rectifying tower 7 without discharging a torch after heat exchange by a first condenser 2 of the deethanizer;
h) after the liquid level of the ethylene recovery tower 6 is established, the C-C washing liquid in the tower is sent to the deethanizer 1, and the flow is gradually increased;
i) the ethylene rectifying tower 7 adjusts the dosage of propylene at 25 ℃ and the dosage of propylene at minus 40 ℃, controls the pressure at the top of the tower to be 1.6MPa-1.7MPa, the top temperature to be minus 37 ℃ to minus 31 ℃, controls the reflux ratio to be about 4, extracts ethylene from a side line to an unqualified ethylene tank, and cuts the ethylene tank to an ethylene spherical tank B after the ethylene is qualified in analysis.
In the above process, in order to ensure that the material extracted from the tower bottom of the deethanizer is qualified (the qualified index refers to the carbon dioxide in the material and the following components less than 170ml/m3) The temperature of the deethanizer kettle is always controlled to be 93-96 ℃ in the whole feeding process; the obtained qualified ethylene indexes are that the volume fraction of ethylene in the product is more than or equal to 99.95 percent, the water content is less than 1ppm, CO is less than 1ppm, and CO is2The content is less than 5ppm, and the methanol content is less than 4ml/m3More than three carbon components less than 10ml/m3(ii) a By the process, the invention can effectively improve the product yield of ethylene and obviously shorten the start-up time of the cold separation unit; the whole start-up process treatment time was 8 hours and the torch discharge time was 4 hours.
It is to be understood that the above-described embodiments are only a few, but not all, embodiments of the present invention. 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.
Claims (10)
1. A methanol-to-olefin light hydrocarbon recovery part cold separation unit is characterized in that: comprises a deethanizer, a demethanizer, an ethane vaporizer, an ethylene rectification column, and an ethylene recovery column, wherein:
the outlet of the top of the deethanizer is sequentially connected with a first condenser of the deethanizer, a second condenser of the deethanizer and a reflux tank of the deethanizer, and the liquid phase outlet of the bottom of the reflux tank of the deethanizer is connected with the inlet of the top of the deethanizer; the top gas phase outlet of the deethanizer reflux tank is connected with the tower body inlet of the demethanizer;
the outlet of the top of the demethanizer is sequentially connected with a demethanizer condenser, a demethanizer reflux tank and an ethane vaporizer; the ethane vaporizer comprises a first inlet, a first outlet, a second inlet, a second outlet, and a fuel gas outlet; the top gas phase outlet of the demethanizer reflux tank is connected with the first inlet of an ethane vaporizer, the first outlet of the ethane vaporizer is connected with the liquid phase inlet of the demethanizer reflux tank, and the liquid phase outlet of the demethanizer reflux tank is connected with the top inlet of the demethanizer; a fuel gas outlet of the ethane vaporizer is connected with a fuel gas pipe network; a second outlet of the ethane vaporizer is connected with an inlet at the lower part of the tower body of the ethylene recovery tower;
the outlet of the bottom of the demethanizer is connected with a demethanizer discharge pipeline, and the demethanizer discharge pipeline passes through a first condenser of the deethanizer and then is connected with the inlet of the ethylene rectifying tower; the tower bottom outlet of the ethylene rectifying tower is connected with the second inlet of the ethane vaporizer; collecting qualified polymerization-grade ethylene from a discharge hole at the upper part of the ethylene rectifying tower;
the outlet at the top of the ethylene recovery tower is connected with a fuel gas pipe network, and the outlet at the bottom of the ethylene recovery tower is connected with the inlet of the tower body of the deethanizer.
2. The methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 1, wherein: the cold separation unit for the light hydrocarbon recovery part of the methanol-to-olefin hydrocarbon further comprises an ethylene supplement pipeline, the outlet end of the ethylene supplement pipeline is merged with the discharge pipeline of the demethanizer and then is introduced into the first condenser of the deethanizer, and the inlet end of the ethylene supplement pipeline is connected with the ethylene ball tank through an ethylene delivery pump.
3. The methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 1, wherein: the tower bottom outlet of the deethanizer is connected with the tower body inlet of the depropanizer, and a deethanizer tower kettle cooler is arranged on a tower bottom discharge pipeline of the deethanizer; the tower bottom outlet of the depropanizing tower is connected with the tower body inlet of the ethylene recovery tower through a depropanizing tower discharging pipeline; and a depropanizing tower reboiler is arranged at the lower part of the depropanizing tower.
4. The methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 3, wherein: and a depropanizing tower kettle pump and a carbon four-washing liquid cooler are arranged on a depropanizing tower discharge pipe line.
5. The methanol-to-olefin light hydrocarbon recovery section cold separation unit of any one of claims 1 to 4, wherein: a deethanizer reboiler is arranged at the lower part of the deethanizer; a deethanizer reflux pump is arranged between the bottom liquid phase outlet of the deethanizer reflux tank and the tower top inlet of the deethanizer.
6. The methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 5, wherein: the lower part of the demethanizer is provided with a demethanizer reboiler; and a demethanizer reflux pump is arranged between the liquid phase outlet of the demethanizer reflux tank and the tower top inlet of the demethanizer.
7. The methanol-to-olefins light hydrocarbon recovery section cold separation unit of claim 6, wherein: an outlet at the top of the ethylene rectifying tower is sequentially connected with an ethylene rectifying tower condenser and an ethylene rectifying tower reflux tank, and an outlet at the bottom of the ethylene rectifying tower reflux tank is connected with an inlet at the top of the ethylene rectifying tower through an ethylene rectifying tower reflux pump; and the lower part of the ethylene rectifying tower is provided with an ethylene rectifying tower reboiler.
8. A method for separating light hydrocarbons in a methanol-to-olefin light hydrocarbon recovery part cold separation unit is carried out based on the methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 7, and is characterized in that: the method comprises the following steps:
a) conveying the process gas and the condensate into a deethanizer, starting an ethylene conveying pump, introducing ethylene into a first condenser of the deethanizer for heat exchange, and condensing a process medium at the top of the deethanizer to be below-20 ℃;
b) adjusting the dosage of a propylene refrigerant at-25 ℃ in a second condenser of the deethanizer to ensure that the temperature of the process medium is below-21 ℃ after the process medium is cooled in the second condenser of the deethanizer;
c) increasing reboiling amount of a reboiler of the deethanizer, slowly introducing non-condensable gas in a reflux tank of the deethanizer into the demethanizer, controlling the pressure of the deethanizer to be 2.8-3.0 MPa, and adjusting the temperature of the tower top to be below-17 ℃;
d) the liquid level of the reflux tank of the deethanizer rises, and the reflux quantity at the top of the deethanizer is increased;
e) after the liquid level of the tower kettle of the deethanizer rises, the tower kettle material is sent to a depropanizer;
f) after the depropanizing tower is fed, the depropanizing tower starts to adjust, after the liquid level is established in the tower kettle, the carbon four washing liquid in the tower kettle is preferentially sent to the ethylene recovery tower, the flow is gradually increased, and then the carbon four washing liquid is normally extracted;
g) the gas phase at the top of the deethanizer directly enters a demethanizer after heat exchange and condensation through a first condenser of the deethanizer and a second condenser of the deethanizer, the demethanizer starts to be adjusted, a torch does not need to be placed in 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 returns to the reflux tank of the demethanizer through self-flowing, the gas phase enters an ethylene recovery tower, and the gas phase entering the ethylene recovery tower is absorbed and recycled by the action of carbon four washing liquid; directly feeding the material in the bottom of the demethanizer into an ethylene rectifying tower without discharging a torch after heat exchange by a first condenser of the deethanizer;
h) after the liquid level of the ethylene recovery tower is established, sending carbon four washing liquid in the tower to a deethanizer and gradually increasing the flow;
i) the ethylene rectifying tower adjusts the dosage of propylene at 25 ℃ and the dosage of propylene at minus 40 ℃, controls the pressure at the top of the tower to be 1.6MPa-1.7MPa, the top temperature to be minus 37 ℃ to minus 31 ℃, draws ethylene to an unqualified ethylene tank at a lateral line, and cuts the ethylene to an ethylene spherical tank B after the analysis is qualified.
9. The light hydrocarbon separation method of the methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 8, wherein: in the step (1), the methanol content in the process gas is below 15ppm, the water content is below 1ppm, the dimethyl ether content is below 500ppm, and the carbon dioxide content is below 2 ppm; the methanol content in the condensate is below 15ppm, the water content is below 1ppm, and the dimethyl ether content is below 500 ppm; the ethylene has a temperature below-32 ℃, a pressure above 2.2MPa, a carbon dioxide content below 5ppm and a water content below 1 ppm.
10. The light hydrocarbon separation method of the methanol-to-olefin light hydrocarbon recovery part cold separation unit of claim 8, wherein: the temperature of a tower kettle of the deethanizer is 93-96 ℃.
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| CN113788735A (en) * | 2021-09-30 | 2021-12-14 | 中安联合煤化有限责任公司 | Light hydrocarbon recovery and start-up method suitable for methanol-to-olefin reaction short-time shutdown period |
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