CN104892340A - Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption - Google Patents
Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption Download PDFInfo
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- CN104892340A CN104892340A CN201510314992.XA CN201510314992A CN104892340A CN 104892340 A CN104892340 A CN 104892340A CN 201510314992 A CN201510314992 A CN 201510314992A CN 104892340 A CN104892340 A CN 104892340A
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- 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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- 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
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G70/00—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00
- C10G70/04—Working-up undefined normally gaseous mixtures obtained by processes covered by groups C10G9/00, C10G11/00, C10G15/00, C10G47/00, C10G51/00 by physical processes
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C11/00—Aliphatic unsaturated hydrocarbons
- C07C11/02—Alkenes
- C07C11/04—Ethylene
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C9/00—Aliphatic saturated hydrocarbons
- C07C9/02—Aliphatic saturated hydrocarbons with one to four carbon atoms
- C07C9/06—Ethane
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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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Abstract
The invention relates to a three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption. The method comprises the following steps: pressurizing and cooling the dry gas through a compressor, mixing the dry gas with rich liquid from an absorption tower and desorbed gas from a desorption tower, enabling the mixture to enter a heat exchanger for cooling so as to enable the temperature of the mixture to reach absorbent temperature; enabling the mixture to enter a flash drum for single flash, and enabling a gas phase used as a gas phase feeding material of the absorption tower to enter from the tower bottom; enabling a liquid phase used as a feeding material of the desorption tower to enter from the tower top; refining products at the bottom of the desorption tower through a rectifying tower so as to obtain the products of ethylene and ethane; enabling the products at the bottom of the rectifying tower to be supplemented and cooled, and then returned to the rectifying tower top to be used as an absorbent. An intercondenser is arranged in the absorption tower, so that heat generated can be absorbed timely. According to the invention, the contents of methane and other light components are adjusted through the desorption tower, the content of the methane is 0.05% lower than that of the ethylene and polymer grade ethylene can be obtained directly from an ethylene tower. The method provided by the invention is suitable for separating and recycling C2 component from catalytic cracking dry gas and has the high potential of replacing a deep-cooling method.
Description
Technical field
The present invention relates to catalytic cracked dry gas separating technology, particularly relate to the technique recover ethylene of oil absorption, the equipment of ethane and method, its principal feature is that product directly can enter deethanizing column acquisition polymer grade ethylene.Belong to Chemical Engineering Technology.
Background technology
Catalytic cracked dry gas, be the gas that a kind of generation of producing in petroleum refining process is larger, its main component comprises hydrogen, nitrogen, oxygen, methane, ethene, ethane etc.In most cases, due to the shortage of dry-gas recovery means, dry gas is all directly burn as fuel gas.This is a kind of waste greatly to the valuable gas being wherein representative with ethene, ethane.Meanwhile, along with the Deep Catalytic Cracking process of producing in high-yield olefin is continually developed, the content of the amount of dry gas and wherein ethene is all in increase.Therefore, reclaim dry gas, the ethene especially reclaimed wherein just seems extremely important, the important channel that this Ye Shi oil refining enterprise increases ethylene yield, economizes on resources.
The ethene reclaimed in oil refinery dry gas has following several scheme at present: low temperature separation process, absorption, pressure-variable adsorption etc.Deep cooling recovery technology is representative by Shi Wei company of the U.S., is reached the object of recovered ethylene by partial condenser.But because Deep Cooling Method exists the shortcoming that working pressure is high, energy consumption is high, application relates to certain patent fee at home simultaneously, so there is more difficulty in application at home.Pressure swing adsorption process is mainly through adsorption/desorption circulation by recovery such as the ethylene-ethane in dry gas, and the ethene generally obtained, ethane concentration are more than 80%.The method at home Maoming Petrochemical etc. is applied to some extent.
Oil-absorption process general butane, pentane or aromatic hydrocarbons, as absorption agent, absorb the above component of ethene in dry gas, then with rectification method, each component absorbed are separated one by one.In the product that current absorption process obtains, the content of methane is higher, and product gas also needs to enter splitting gas low temperature separation process system to carry out separation and could obtain polymer grade ethylene, this greatly limits the range of application of absorption process.For the enterprise not having deep cooling demethanizing, it is very large that the investment obtaining polymer grade ethylene becomes.
Summary of the invention
The present invention is directed to the deficiencies in the prior art, propose a kind of oil and absorb dry-gas recovery ethene, three tower apparatus of ethane product and method.Dry gas enters interchanger and cools after compressor pressurizes, cooling with after mixing from the rich solution on absorption tower and the stripping gas of desorption tower, reaches absorption temperature; Enter flash tank afterwards and carry out single flash, gas phase, as the gas-phase feed on absorption tower, enters at the bottom of tower; Liquid phase enters from tower top as the charging of desorption tower; Desorption tower bottom product, after rectifying tower is refining, obtains C2 product.Rectifying tower bottom product returns absorption tower top, as absorption agent after supplementing, cooling.Be provided with intermediate condenser in absorption tower and remove the heat absorbing and produce in time.Its advantage is by the content regulating desorption tower to control the light constituents such as methane, to reclaim absorption agent, controlled the temperature absorbed by interchanger by rectifying tower.In the C2 product obtained like this, the content of methane relative ethylene, lower than 0.05%, directly can enter ethylene column and obtain polymer grade ethylene.Method of the present invention is applicable to Separation and Recovery C2 component from catalytic cracked dry gas, is expected to replace Deep Cooling Method.
Technical scheme of the present invention is as follows:
A kind of oil absorbs three tower apparatus of dry-gas recovery high-purity ethylene, ethane: comprise compressor, absorption tower, desorption tower and rectifying tower; It is characterized in that the outlet of compressor is connected with the entrance of raw material one-level water cooler, the outlet of raw material one-level water cooler is connected with an entrance of raw material secondary coolers; The outlet of raw material secondary coolers is connected with the entrance of separating tank, and the gaseous phase outlet of separating tank is connected with the gas phase entrance on absorption tower, and the liquid-phase outlet of separating tank is connected with the liquid phase entrance of desorption tower tower top; The liquid-phase outlet on absorption tower is connected with two other entrance of raw material secondary coolers with the gaseous phase outlet of desorption tower; Liquid-phase outlet at the bottom of the tower of desorption tower is connected with the cold stream inlet of preheater, and the cold stream outlet of preheater is connected with the opening for feed of rectifying tower; At the bottom of the tower of rectifying tower, liquid-phase outlet is connected with the entrance of force (forcing) pump, and pressurization pump outlet is connected with the hot stream inlet of preheater; The hot stream outlet of preheater is connected with the entrance of absorption agent one-level water cooler, and the outlet of absorption agent one-level water cooler is connected with the entrance of absorption agent secondary coolers; The outlet of absorption agent secondary coolers is connected with an entrance of absorption agent mixing tank, and the outlet of absorption agent mixing tank is connected with the liquid phase entrance on absorption tower; Absorption tower tower top arranges fuel exhaust gas outlet, and rectifying tower tower top produces and arranges ethene, ethane product outlet.
A kind of oil of the present invention absorbs three tower recovery methods of dry-gas recovery ethene, ethane, and unstripped gas is within the compressor after supercharging, through the cooling of raw material one-level water cooler, with absorption liquid incoming stock secondary coolers together with stripping gas; Secondary cooling charging enters separating tank and carries out vapor-liquid separation, produces and absorbs gas and stripping liquid; Absorb gas and enter bottom, absorption tower, stripping liquid enters desorption tower top; Stripping liquid, after extraction bottom desorption tower, forms pre-hydrothermal solution and enters rectifying tower after entering preheater preheats; Rectifying tower tower top output ethene, ethane product, extraction heat absorbent at the bottom of tower; Heat absorbent forms pressurizing absorption agent after force (forcing) pump; Pressurizing absorption agent is lowered the temperature after preheater heat exchange, forms precooling absorption agent; Precooling absorption agent, after absorption agent one-level water cooler and absorption agent secondary coolers, forms the agent of secondary cooling and absorbing; The agent of secondary cooling and absorbing and supplementary absorption agent are mixed to form cyclic absorption agent 2 and enter top, absorption tower 2 in absorption agent mixing tank; Absorption tower tower top output fuel exhaust gas.
Concrete technical qualification are preferably as follows:
Described compressor delivery pressure is 2.8 ~ 3.4Mpa;
Described raw material one-level cooler outlet temperature is 32 ~ 40 DEG C; Raw material secondary coolers temperature out is-20 ~-10 DEG C.
Described absorption tower pressure is 2.8 ~ 3.4MPa, and number of theoretical plate is 18 ~ 24.
The working pressure of described desorption tower is 2.9 ~ 3.5MPa, and number of theoretical plate is 10 ~ 16.
The cold material temperature out of described preheater is 130 ~ 140 DEG C.
The working pressure of described rectifying tower is 2.2 ~ 2.8MPa, and reflux ratio is 1.8 ~ 2.2, and number of theoretical plate is 16 ~ 24.
The temperature out of described absorption agent one-level water cooler is 32 ~ 40 DEG C, and the temperature out of absorption agent secondary coolers is-20 ~-10 DEG C.
The present invention has the following advantages:
(1) three tower process that a kind of oil absorbs dry-gas recovery ethene, ethane are proposed.When reclaiming the ethene in dry gas by the absorption process of routine, owing to not having steam stripped effect, in ethene, ethane product, the foreign gas content such as methane is higher, directly cannot enter the ethene that deethanizing column obtains polymerization-grade; And can only match with deep cooling or other technique and use, extra investment can be brought like this.And new flow process only needs to absorb the ethylene raw that just can obtain polymerization-grade, the rate of recovery reaches more than 90%.
(2) present method make use of flexible, strong to the adaptability to raw material feature of absorption process, and the catalytic cracked dry gas complicated for composition has assimilation effect preferably.Compare Deep Cooling Method, this method avoid ethylene refrigeration machine, save energy consumption and investment.
Accompanying drawing explanation
Fig. 1 is present invention process schematic flow sheet.
Embodiment
Below in conjunction with accompanying drawing and specific embodiments, the present invention is introduced in more detail, but any restriction can not formed by practical range to of the present invention.
Device is as shown in Figure 1: the outlet of compressor 2 is connected with the entrance of raw material one-level water cooler 4, and the outlet of raw material one-level water cooler 4 is connected with a dry gas gas phase entrance of raw material secondary coolers 6.The outlet of raw material secondary coolers 6 is connected with the entrance of separating tank 8, and the gaseous phase outlet of separating tank 8 is connected with the gas phase entrance on absorption tower 29, and liquid-phase outlet is connected with the liquid phase entrance of desorption tower 13 tower top.The liquid-phase outlet on absorption tower 29 is connected with the liquid phase entrance of raw material secondary coolers 6, and the gaseous phase outlet of desorption tower 13 is connected with the stripping gas entrance of raw material secondary coolers 6.Liquid-phase outlet at the bottom of the tower of desorption tower 13 is connected with the cold stream inlet of preheater 15, and the cold stream outlet of preheater 15 is connected with the opening for feed of rectifying tower 17.At the bottom of the tower of rectifying tower 17, liquid-phase outlet is connected with the entrance of force (forcing) pump 19, and the outlet of force (forcing) pump 19 is connected with the hot stream inlet of preheater 15.The hot stream outlet of preheater 15 is connected with the entrance of absorption agent one-level water cooler 22, and the outlet of absorption agent one-level water cooler 22 is connected with the entrance of absorption agent secondary coolers 24.The outlet of absorption agent secondary coolers 24 is connected with an entrance of absorption agent mixing tank 27, and the outlet of absorption agent mixing tank 27 is connected with the liquid phase entrance on absorption tower 29.
A kind of oil that the present invention proposes absorbs three tower methods of dry-gas recovery ethene, ethane, and its separation process is: unstripped gas 1 after supercharging, cools through raw material one-level water cooler 4 in compressor 2, with absorption liquid 12 incoming stock secondary coolers 6 together with stripping gas 11.Secondary cooling charging 7 enters separating tank 8 and carries out vapor-liquid separation, produces and absorbs gas 10 and stripping liquid 9.Absorb gas 10 and enter bottom, absorption tower 29, stripping liquid 9 enters desorption tower 13 top.Stripping liquid 14, after extraction bottom desorption tower 13, forms pre-hydrothermal solution 16 and enters rectifying tower 17 after entering preheater 15 preheating.Rectifying tower 17 tower top output ethene, ethane product 31, extraction heat absorbent 18 at the bottom of tower.Heat absorbent 18 forms pressurizing absorption agent 20 after force (forcing) pump 19.Pressurizing absorption agent 20 is lowered the temperature after preheater 15 heat exchange, forms precooling absorption agent 21.Precooling absorption agent 21, after absorption agent one-level water cooler 21 and absorption agent secondary coolers 24, forms secondary cooling and absorbing agent 25.Secondary cooling and absorbing agent 25 and supplementary absorption agent 26 are mixed to form cyclic absorption agent 28 and enter top, absorption tower 29 in absorption agent mixing tank 27.Absorption tower 29 tower top output fuel exhaust gas 30.
Concrete technical qualification are: compressor 2 top hole pressure is 2.8 ~ 3.4Mpa; Raw material one-level water cooler 4 temperature out is 32 ~ 40 DEG C; Raw material secondary coolers 6 temperature out is-20 ~-10 DEG C; Absorption tower 29 pressure is 2.8 ~ 3.4MPa, and number of theoretical plate is 18 ~ 24.In absorption tower 29, the heavy constituents such as most of ethene, ethane absorb by absorption agent, concentrate at the bottom of tower, and the foreign gases such as methane concentrate on tower top.The working pressure of desorption tower 13 is 2.9 ~ 3.5MPa, and number of theoretical plate is 10 ~ 16.In desorption tower 13, the foreign gases such as methane concentrate on tower top by desorption, and ethene and other Concentration of matters are at the bottom of tower.The cold material temperature out of preheater 15 is 130 ~ 140 DEG C.The working pressure of rectifying tower 17 is 2.2 ~ 2.8MPa, and reflux ratio is 1.8 ~ 2.2, and number of theoretical plate is 16 ~ 24.The temperature out of absorption agent one-level water cooler 22 is 32 ~ 40 DEG C, and the temperature out of absorption agent secondary coolers 24 is-20 ~-10 DEG C.Absorption agent in whole flow process adopts C 5 fraction.
Embodiment 1.
Unstripped gas 1 mole consist of 21.1%H
2+ 24.5%N
2+ 24.3%CH
4+ 21%C
2h
4+ 7.8%C
2h
6+ 0.2C
3h
6+ 0.4%O
2+ 0.6%CO, mass rate is 7.5tons/hr, temperature 40 DEG C.Adopt C5 as absorption agent in technique, the amount of cyclic absorption agent is 20tons/hr.
Unstripped gas 1 is compressed to 3.05Mpa by compressor 2, and compressed gas 3 is cooled to 32 DEG C by raw material one-level water cooler 4, and absorption liquid 12, one-level cold gas 5, stripping gas 11 are cooled to-15 DEG C by raw material secondary coolers 6.Separating tank 8 is at 3.05MPa adiabatic flash.Absorption tower 29 number of theoretical plate is 12, and working pressure is 3MPa; Desorption tower 13 number of theoretical plate is 10, and working pressure is 3.05MPa.Stripping liquid 14 is preheated to 132 DEG C by preheater 15.Rectifying tower 17 number of theoretical plate is 20, and working pressure is 2.6MPa, and reflux ratio is 2, and pre-hydrothermal solution 16 is from the 10th piece of charging.Heat absorbent 18 is forced into 3MPa through force (forcing) pump 19.Precooling absorption agent 21 is cooled to 32 DEG C by absorption agent one-level water cooler 22, and one-level cooling and absorbing agent 23 is cooled to-15 DEG C by absorption agent secondary coolant 24.Cooling twice absorption agent 25 and supplementary absorption agent 26, after absorption agent mixing tank 27 mixes, form first piece of theoretical stage that cyclic absorption agent 28 enters absorption tower 29.Form 1 shows, and in ethene, ethane product 31, methane accounts for the mark of both methane ethene molar flow is 0.045%, can obtain polymer grade ethylene after deethanizing.
Form 1 typical catalyst dry gas absorption extraction result:
Can calculate from table, CH4 and the C2H4 molar flow in ethene, ethane product is respectively 0.03kmol and 66.64kmol.The molar fraction that CH4 accounts for both sums is 0.00045, namely less than 0.05%.Such gaseous products, after the process of deethanizing column, directly can obtain the ethene of polymerization-grade.
Claims (9)
1. oily three tower apparatus absorbing dry-gas recovery high-purity ethylene, ethane: comprise compressor, absorption tower, desorption tower and rectifying tower; It is characterized in that the outlet of compressor is connected with the entrance of raw material one-level water cooler, the outlet of raw material one-level water cooler is connected with an entrance of raw material secondary coolers; The outlet of raw material secondary coolers is connected with the entrance of separating tank, and the gaseous phase outlet of separating tank is connected with the gas phase entrance on absorption tower, and the liquid-phase outlet of separating tank is connected with the liquid phase entrance of desorption tower tower top; The liquid-phase outlet on absorption tower is connected with two other entrance of raw material secondary coolers with the gaseous phase outlet of desorption tower; Liquid-phase outlet at the bottom of the tower of desorption tower is connected with the cold stream inlet of preheater, and the cold stream outlet of preheater is connected with the opening for feed of rectifying tower; At the bottom of the tower of rectifying tower, liquid-phase outlet is connected with the entrance of force (forcing) pump, and pressurization pump outlet is connected with the hot stream inlet of preheater; The hot stream outlet of preheater is connected with the entrance of absorption agent one-level water cooler, and the outlet of absorption agent one-level water cooler is connected with the entrance of absorption agent secondary coolers; The outlet of absorption agent secondary coolers is connected with an entrance of absorption agent mixing tank, and the outlet of absorption agent mixing tank is connected with the liquid phase entrance on absorption tower; Absorption tower tower top arranges fuel exhaust gas outlet, and rectifying tower tower top produces and arranges ethene, ethane product outlet.
2. oil absorbs three tower recovery methods of dry-gas recovery ethene, ethane, it is characterized in that: unstripped gas is within the compressor after supercharging, through the cooling of raw material one-level water cooler, with absorption liquid incoming stock secondary coolers together with stripping gas; Secondary cooling charging enters separating tank and carries out vapor-liquid separation, produces and absorbs gas and stripping liquid; Absorb gas and enter bottom, absorption tower, stripping liquid enters desorption tower top; Stripping liquid, after extraction bottom desorption tower, forms pre-hydrothermal solution and enters rectifying tower after entering preheater preheats; Rectifying tower tower top output ethene, ethane product, extraction heat absorbent at the bottom of tower; Heat absorbent forms pressurizing absorption agent after force (forcing) pump; Pressurizing absorption agent is lowered the temperature after preheater heat exchange, forms precooling absorption agent; Precooling absorption agent, after absorption agent one-level water cooler and absorption agent secondary coolers, forms the agent of secondary cooling and absorbing; The agent of secondary cooling and absorbing and supplementary absorption agent are mixed to form cyclic absorption agent 2 and enter top, absorption tower 2 in absorption agent mixing tank; Absorption tower tower top output fuel exhaust gas.
3. method as claimed in claim 2, is characterized in that described compressor delivery pressure is 2.8 ~ 3.4Mpa.
4. method as claimed in claim 2, is characterized in that described raw material one-level cooler outlet temperature is 32 ~ 40 DEG C; Raw material secondary coolers temperature out is-20 ~-10 DEG C.
5. method as claimed in claim 2, it is characterized in that described absorption tower pressure is 2.8 ~ 3.4MPa, number of theoretical plate is 18 ~ 24.
6. method as claimed in claim 2, it is characterized in that the working pressure of described desorption tower is 2.9 ~ 3.5MPa, number of theoretical plate is 10 ~ 16.
7. method as claimed in claim 2, is characterized in that the cold material temperature out of described preheater is 130 ~ 140 DEG C.
8. method as claimed in claim 2, it is characterized in that the working pressure of described rectifying tower is 2.2 ~ 2.8MPa, reflux ratio is 1.8 ~ 2.2, and number of theoretical plate is 16 ~ 24.
9. method as claimed in claim 2, it is characterized in that the temperature out of described absorption agent one-level water cooler is 32 ~ 40 DEG C, the temperature out of absorption agent secondary coolers is-20 ~-10 DEG C.
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201510314992.XA CN104892340A (en) | 2015-06-10 | 2015-06-10 | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption |
| PCT/CN2015/090879 WO2016197487A1 (en) | 2015-06-10 | 2015-09-28 | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption |
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| CN201510314992.XA CN104892340A (en) | 2015-06-10 | 2015-06-10 | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption |
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| WO (1) | WO2016197487A1 (en) |
Cited By (6)
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| WO2016197487A1 (en) * | 2015-06-10 | 2016-12-15 | 天津大学 | Three-tower device and method for recycling ethylene and ethane from dry gas through oil absorption |
| CN107022378A (en) * | 2016-02-01 | 2017-08-08 | 中国石化工程建设有限公司 | The technique of the dry-gas recovery system and recovery dry gas of hydrocracking unit or hydro-upgrading unit |
| CN109627136A (en) * | 2017-10-09 | 2019-04-16 | 中国石油化工股份有限公司 | The separator and separation method of ethylene-ethane in a kind of dry gas or cracking gas |
| CN112299942A (en) * | 2019-08-02 | 2021-02-02 | 中国石化工程建设有限公司 | Method and system for recovering carbon dioxide fraction in refinery dry gas |
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