WO2016197487A1 - 一种油吸收干气回收乙烯、乙烷的三塔装置与方法 - Google Patents

一种油吸收干气回收乙烯、乙烷的三塔装置与方法 Download PDF

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WO2016197487A1
WO2016197487A1 PCT/CN2015/090879 CN2015090879W WO2016197487A1 WO 2016197487 A1 WO2016197487 A1 WO 2016197487A1 CN 2015090879 W CN2015090879 W CN 2015090879W WO 2016197487 A1 WO2016197487 A1 WO 2016197487A1
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absorbent
outlet
tower
absorption
column
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French (fr)
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李鑫钢
王珏
陈超
李优
辛峰
李永红
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Tianjin University
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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
    • 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
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C11/00—Aliphatic unsaturated hydrocarbons
    • C07C11/02—Alkenes
    • C07C11/04—Ethene
    • 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
    • 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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  • the invention relates to a catalytic cracking dry gas separation process, in particular to an oil absorption process for recovering ethylene and ethane.
  • the main feature is that the product can directly enter the deethanizer to obtain polymer grade ethylene. Belongs to chemical technology.
  • Catalytic cracking dry gas is a kind of gas produced in the petroleum refining process. Its main components include hydrogen, nitrogen, oxygen, methane, ethylene, ethane and so on. In most cases, dry gas is directly burned as fuel gas due to lack of dry gas recovery means. This is a great waste for the valuable gas represented by ethylene and ethane. At the same time, as the catalytic cracking process for producing olefins continues to develop, the amount of dry gas and the amount of ethylene therein are increasing. Therefore, recycling dry gas, especially the recovery of ethylene, is very important, which is also an important way for refining companies to increase ethylene production and save resources.
  • Ethylene in the dry gas of the refinery is currently recycled as follows: cryogenic separation, absorption, pressure swing adsorption, and the like.
  • the cryogenic recycling technology is represented by American Shiwei Company, and the purpose of recycling ethylene is achieved by a condenser.
  • the pressure swing adsorption method mainly recovers ethylene ethane in the dry gas through an adsorption desorption cycle, and generally has a concentration of ethylene and ethane of 80% or more. This method has application in domestic Maoming Petrochemical.
  • the oil absorption method generally uses butane, pentane or an aromatic hydrocarbon as an absorbent to absorb the above components of ethylene in the dry gas, and then separates the absorbed components one by one by distillation.
  • the content of methane is high, and the product gas needs to enter the cracking gas cryogenic separation system for separation to obtain the polymerization grade ethylene, which greatly limits the application range of the absorption method.
  • the investment in polymer grade ethylene is very large.
  • the invention aims at the deficiencies of the prior art, and proposes a three-column device and method for recovering ethylene and ethane products from oil absorption dry gas.
  • the dry gas is pressurized by the compressor, cooled, mixed with the rich liquid from the absorption tower and the desorbed gas of the desorption tower, and then enters the heat exchanger to be cooled to reach the absorption temperature; then enters the flash tank for one flash, and the gas phase serves as an absorption tower.
  • the gas phase feed enters from the bottom of the column; the liquid phase enters from the top of the column as a feed to the desorption column; the bottom product of the desorber is refined through a rectification column to obtain a C2 product.
  • the bottom product of the distillation column is replenished, cooled, and returned to the top of the absorption tower as an absorbent.
  • An intermediate condenser is arranged in the absorption tower to remove the heat generated by the absorption in time.
  • the advantage is that the content of light components such as methane can be controlled by adjusting the desorption column, the absorbent is recovered by the rectification column, and the absorption temperature is controlled by the heat exchanger.
  • the content of methane relative to ethylene is less than 0.05%, and it is possible to directly enter the ethylene column to obtain polymer grade ethylene.
  • the method of the present invention is suitable for separating and recovering C2 components from catalytic cracking dry gas, and is expected to replace the cryogenic method.
  • a three-column device for recovering high-purity ethylene and ethane by oil absorption dry gas comprises: a compressor, an absorption tower, a desorption tower and a rectification tower; wherein the outlet of the compressor is connected with the inlet of the raw material primary cooler, The outlet of the raw material primary cooler is connected to an inlet of the raw material secondary cooler; the outlet of the raw material secondary cooler is connected to the inlet of the separation tank, the separation tank
  • the gas phase outlet is connected to the gas phase inlet of the absorption tower, and the liquid phase outlet of the separation tank is connected to the liquid phase inlet of the top of the desorption column; the liquid phase outlet of the absorption tower and the gas phase outlet of the desorption column and the other two of the raw material secondary coolers
  • the inlets of the desorption column are connected to the cold stream inlet of the preheater, the cold stream outlet of the preheater is connected to the feed port of the rectification column; the bottom liquid phase outlet of the rectification column is added
  • the invention relates to a three-column recovery method for recovering ethylene and ethane from oil absorption dry gas. After the raw material gas is pressurized in the compressor, it is cooled by the raw material primary cooler, and enters the secondary cooling of the raw material together with the absorption liquid and the desorbed gas.
  • the secondary cooling feed enters the separation tank for vapor-liquid separation to generate absorption gas and desorption liquid; the absorption gas enters the lower part of the absorption tower, and the desorbed liquid enters the upper part of the desorption tower; the desorption liquid is taken out from the bottom of the desorption tower and enters the preheater After preheating, preheating liquid is formed into the rectification column; ethylene and ethane products are produced at the top of the distillation column, and heat absorbent is produced at the bottom of the column; the heat absorbent forms a pressure absorbent after being pressurized by the pump; The agent is cooled by the preheater to form a pre-cooling absorbent; the pre-cooling absorbent passes through the first-stage cooler of the absorbent and the secondary cooler of the absorbent to form a secondary cooling absorbent; the secondary cooling absorbent and the supplement The absorbent is mixed in an absorbent mixer to form a circulating absorbent 2 which enters the upper portion of the absorption tower 2; the top of the absorption tower produces
  • the compressor outlet pressure is 2.8 ⁇ 3.4Mpa
  • the raw material primary cooler outlet temperature is 32 to 40 ° C; the raw material secondary cooler outlet temperature is -20 to -10 ° C.
  • the absorption tower pressure is 2.8 to 3.4 MPa, and the theoretical number of plates is 18 to 24.
  • the operating pressure of the desorption column is 2.9 to 3.5 MPa, and the number of theoretical plates is 10 to 16.
  • the cold material outlet temperature of the preheater is 130 to 140 °C.
  • the distillation column has an operating pressure of 2.2 to 2.8 MPa, a reflux ratio of 1.8 to 2.2, and a theoretical plate number of 16 to 24.
  • the outlet temperature of the absorbent primary cooler is 32-40 ° C, and the outlet temperature of the secondary cooler of the absorbent is
  • a three-tower process for recovering ethylene and ethane from oil absorption dry gas is proposed.
  • the ethylene in the dry gas is recovered by the conventional absorption method, since there is no stripping effect, the content of impurity gases such as methane in the ethylene and ethane products is high, and it is impossible to directly enter the deethanizer to obtain the polymerization grade ethylene; Used in conjunction with cryogenic or other processes, this will result in additional investment.
  • the new process requires only absorption to obtain a polymer grade ethylene feedstock with a recovery rate of over 90%.
  • the method utilizes the characteristics of flexible absorption method and strong adaptability to raw materials, and has a good absorption effect on the composition of complex catalytic cracking dry gas. Compared with the cryogenic method, this method avoids the ethylene refrigerator and saves energy and investment.
  • Figure 1 is a schematic view of the process flow of the present invention.
  • the outlet of the compressor 2 is connected to the inlet of the raw material primary cooler 4, and the outlet of the raw material primary cooler 4 is connected to a dry gas phase inlet of the raw material secondary cooler 6.
  • the outlet of the raw material secondary cooler 6 is connected to the inlet of the separation tank 8
  • the gas phase outlet of the separation tank 8 is connected to the gas phase inlet of the absorption column 29, and the liquid phase outlet is connected to the liquid phase inlet of the top of the desorption column 13.
  • the liquid phase outlet of the absorption column 29 is connected to the liquid phase inlet of the raw material secondary cooler 6, and the gas phase outlet of the desorption column 13 is connected to the desorption gas inlet of the raw material secondary cooler 6.
  • the bottom liquid phase outlet of the desorber 13 is connected to the cold stream inlet of the preheater 15, and the cold stream outlet of the preheater 15 is connected to the feed port of the rectification column 17.
  • the bottom liquid phase outlet of the rectification column 17 is connected to the inlet of the pressurizing pump 19, and the outlet of the pressurizing pump 19 is connected to the hot stream inlet of the preheater 15.
  • the hot stream outlet of the preheater 15 is connected to the inlet of the absorbent primary cooler 22, and the outlet of the absorbent primary cooler 22 is connected to the inlet of the absorbent secondary cooler 24.
  • the outlet of the absorbent secondary cooler 24 is connected to an inlet of the absorbent mixer 27, and the outlet of the absorbent mixer 27 is connected to the liquid phase inlet of the absorption tower 29.
  • the invention provides a three-column method for recovering ethylene and ethane by oil absorption dry gas, wherein the separation process is: after the raw material gas 1 is pressurized in the compressor 2, it is cooled by the raw material primary cooler 4, and the absorption liquid 12 Together with the desorbed gas 11, it enters the raw material secondary cooler 6.
  • the secondary cooling feed 7 enters the separation tank 8 for vapor-liquid separation to produce the absorption gas 10 and the desorption liquid 9.
  • the absorption gas 10 enters the lower portion of the absorption tower 29, and the desorbed liquid 9 enters the upper portion of the desorption column 13.
  • the desorbed liquid 14 is taken out from the bottom of the desorption column 13, it is preheated into the preheater 15 to form the preheated liquid 16 and enters the rectification column 17.
  • the top of the rectification column 17 produces ethylene and ethane product 31, and the bottom of the column produces a heat absorbent 18.
  • the heat absorbent 18 passes through the pressurizing pump 19 to form a pressurized absorbent 20.
  • the pressurized absorbent 20 is cooled by the heat exchange of the preheater 15 to form a pre-cooling absorbent 21.
  • the pre-cooling absorbent 21 passes through the absorbent primary cooler 21 and the absorbent secondary cooler 24 to form a secondary cooling absorbent 25.
  • the secondary cooling absorbent 25 is mixed with the supplemental absorbent 26 in the absorbent mixer 27 to form a circulating absorbent 28 which enters the upper portion of the absorption tower 29.
  • the fuel tail gas 30 is produced at the top of the absorption tower 29.
  • the outlet pressure of the compressor 2 is 2.8 ⁇ 3.4Mpa; the outlet temperature of the raw material primary cooler 4 is 32 ⁇ 40 ° C; the outlet temperature of the raw material secondary cooler 6 is -20 ⁇ -10 ° C; the pressure of the absorption tower 29 It is 2.8 to 3.4 MPa, and the number of theoretical plates is 18 to 24.
  • the absorbent absorbs most of the heavy components such as ethylene and ethane, and concentrates on the bottom of the column, while impurity gases such as methane are concentrated at the top of the column.
  • the operating pressure of the desorption column 13 is 2.9 to 3.5 MPa, and the number of theoretical plates is 10 to 16.
  • the cold material outlet temperature of the preheater 15 is 130 to 140 °C.
  • the operating pressure of the rectification column 17 is 2.2 to 2.8 MPa, the reflux ratio is 1.8 to 2.2, and the number of theoretical plates is 16 to 24.
  • the outlet temperature of the absorbent primary cooler 22 is 32 to 40 ° C, and the outlet temperature of the absorbent secondary cooler 24 is -20 to -10 °C.
  • the absorbent in the entire process uses a C5 fraction.
  • the molar composition of the feed gas 1 is 21.1% H 2 + 24.5% N 2 + 24.3% CH 4 + 21% C 2 H 4 + 7.8% C 2 H 6 + 0.2 C 3 H 6 + 0.4% O 2 + 0.6% CO
  • the mass flow rate is 7.5 tons/hr and the temperature is 40 °C.
  • C5 was used as the absorbent in the process, and the amount of the circulating absorbent was 20 tons/hr.
  • the compressor 2 compresses the raw material gas 1 to 3.05 MPa, and the raw material primary cooler 4 cools the compressed gas 3 to 32 ° C.
  • the secondary cooler 6 cools the absorption liquid 12, the primary cooling gas 5, and the desorbed gas 11 to -15 °C.
  • the separation tank 8 was adiabatically flashed at 3.05 MPa.
  • the theoretical number of plates of the absorption tower 29 is 12, the operating pressure is 3 MPa; the number of theoretical plates of the desorption column 13 is 10, and the operating pressure is 3.05 MPa.
  • the preheater 15 preheats the desorbent 14 to 132 °C.
  • the number of theoretical plates of the rectification column 17 is 20, the operating pressure is 2.6 MPa, the reflux ratio is 2, and the preheating liquid 16 is fed from the 10th block.
  • the heat absorbent 18 is pressurized to 3 MPa by a pressurizing pump 19.
  • the absorbent primary cooler 22 cools the pre-cooling absorbent 21 to 32 ° C, and the absorbent secondary coolant 24 cools the primary cooling absorbent 23 to -15 ° C.
  • a first theoretical plate of the circulating absorbent 28 is introduced into the absorption tower 29.
  • Table 1 shows that the fraction of the molar flow of methane to methane ethylene in the ethylene and ethane product 31 is 0.045%, and the polymerization grade ethylene can be obtained after de-ethane removal.

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Abstract

本发明涉及一种油吸收干气回收乙烯、乙烷的三塔装置与方法；干气经过压缩机加压、冷却后与来自吸收塔的富液以及解吸塔的解吸气混合后进入换热器冷却，达到吸收温度。进入闪蒸罐进行一次闪蒸，气相作为吸收塔的气相进料，从塔底进入；液相作为解吸塔的进料从塔顶进入；解吸塔塔底产品经过精馏塔精制后，得到乙烯、乙烷产品；精馏塔塔底产品经过补充、冷却后返回吸收塔顶，作为吸收剂。吸收塔中设置了中间冷凝器及时移走吸收产生的热量。本发明通过调节解吸塔来控制甲烷等轻组分的含量，甲烷相对乙烯的含量低于0.05％，可以直接进入乙烯塔获得聚合级乙烯。本发明的方法适用于从催化裂化干气中分离回收C2组分，有望取代深冷法。

Description

一种油吸收干气回收乙烯、乙烷的三塔装置与方法 技术领域
本发明涉及催化裂化干气分离工艺，尤其涉及油吸收的工艺来回收乙烯、乙烷的设备和方法，其主要特点是产品可以直接进入脱乙烷塔获得聚合级乙烯。属于化工技术。
背景技术
催化裂化干气，是石油炼制过程中产生的一种产生量较大的气体，其主要成分包括氢气、氮气、氧气、甲烷、乙烯、乙烷等。在大部分情况下，由于干气回收手段的缺乏，干气都是作为燃料气直接燃烧。这对其中以乙烯、乙烷为代表的有价值的气体是一种极大的浪费。同时，随着多产烯烃的催化裂解工艺不断开发，干气的量以及其中乙烯的含量都在增加。因此，回收干气，尤其是回收其中的乙烯就显得非常重要，这也是炼油企业增加乙烯产量、节约资源的重要途径。
回收炼厂干气中的乙烯目前有如下几个方案：深冷分离、吸收、变压吸附等。深冷回收技术由美国石伟公司为代表，通过分凝器达到回收乙烯的目的。但是由于深冷法存在操作压力高、能耗高的缺点，同时在国内应用涉及到一定的专利费用，所以在国内应用存在较多困难。变压吸附法主要通过吸附脱附循环将干气中的乙烯乙烷等回收，一般获得的乙烯、乙烷浓度在80％以上。该方法在国内茂名石化等有所应用。
油吸收法一般利用丁烷、戊烷或芳烃作为吸收剂，吸收干气中的乙烯以上组分，再用精馏法把吸收的各个组分逐一分离。目前吸收法获得的产品中，甲烷的含量较高，产品气体还需要进入裂解气深冷分离系统进行分离才能获得聚合级乙烯，这极大地限制了吸收法的应用范围。对于没有深冷脱甲烷的企业来说，得到聚合级乙烯的投资变的非常大。
发明内容
本发明针对现有技术的不足，提出了一种油吸收干气回收乙烯、乙烷产品的三塔装置与方法。干气经过压缩机加压、冷却后与来自吸收塔的富液以及解吸塔的解吸气混合后进入换热器冷却，达到吸收温度；之后进入闪蒸罐进行一次闪蒸，气相作为吸收塔的气相进料，从塔底进入；液相作为解吸塔的进料从塔顶进入；解吸塔塔底产品经过精馏塔精制后，得到C2产品。精馏塔塔底产品经过补充、冷却后返回吸收塔顶，作为吸收剂。吸收塔中设置了中间冷凝器及时移走吸收产生的热量。其优点在于可以通过调节解吸塔来控制甲烷等轻组分的含量，通过精馏塔来回收吸收剂，通过换热器来控制吸收的温度。这样的得到的C2产品中，甲烷相对乙烯的含量低于0.05％，可以直接进入乙烯塔获得聚合级乙烯。本发明的方法适用于从催化裂化干气中分离回收C2组分，有望取代深冷法。
本发明的技术方案如下：
一种油吸收干气回收高纯度乙烯、乙烷的三塔装置：包括压缩机、吸收塔、解吸塔和精馏塔；其特征是压缩机的出口与原料一级冷却器的入口相连接，原料一级冷却器的出口与原料二级冷却器的一个入口相连；原料二级冷却器的出口与分离罐的入口相连，分离罐 的气相出口与吸收塔的气相入口连接，分离罐的液相出口与解吸塔塔顶的液相入口相连接；吸收塔的液相出口和解吸塔的气相出口与原料二级冷却器的另外两个入口相连；解吸塔的塔底液相出口与预热器的冷物流入口相连，预热器的冷物流出口与精馏塔的进料口相连；精馏塔的塔底液相出口与加压泵的入口相连，加压泵的出口与预热器的热物流入口相连；预热器的热物流出口与吸收剂一级冷却器的入口相连，吸收剂一级冷却器的出口与吸收剂二级冷却器的入口相连；吸收剂二级冷却器的出口与吸收剂混合器的一个入口相连，吸收剂混合器的出口与吸收塔的液相入口相连；吸收塔塔顶设置燃料尾气出口，精馏塔塔顶产设置乙烯、乙烷产品出口。
本发明的一种油吸收干气回收乙烯、乙烷的三塔回收方法，原料气在压缩机中增压后，经过原料一级冷却器冷却，与吸收液和解吸气一起进入原料二级冷却器；二级冷却进料进入分离罐进行汽液分离，产生吸收气和解吸液；吸收气进入吸收塔下部，解吸液进入解吸塔上部；解吸液从解吸塔底部采出后，进入预热器预热后形成预热液进入精馏塔；精馏塔塔顶产出乙烯、乙烷产品，塔底采出热吸收剂；热吸收剂经过加压泵后形成加压吸收剂；加压吸收剂经过预热器换热后降温，形成预冷吸收剂；预冷吸收剂经过吸收剂一级冷却器和吸收剂二级冷却器后，形成二级冷却吸收剂；二级冷却吸收剂与补充吸收剂在吸收剂混合器中混合形成循环吸收剂2进入吸收塔2上部；吸收塔塔顶产出燃料尾气。
具体技术条件优选如下：
所述的压缩机出口压力为2.8～3.4Mpa；
所述的原料一级冷却器出口温度为32～40℃；原料二级冷却器出口温度为-20～-10℃。
所述的吸收塔压力为2.8～3.4MPa，理论板数为18～24。
所述的解吸塔的操作压力为2.9～3.5MPa，理论板数为10～16。
所述的预热器的冷物料出口温度为130～140℃。
所述的精馏塔的操作压力为2.2～2.8MPa，回流比为1.8～2.2，理论板数为16～24。
所述的吸收剂一级冷却器的出口温度为32～40℃，吸收剂二级冷却器的出口温度为
-20～-10℃。
本发明具有以下优点：
(1)提出了一种油吸收干气回收乙烯、乙烷的三塔工艺。用常规的吸收法回收干气中的乙烯时，由于没有汽提的作用，乙烯、乙烷产品中甲烷等杂质气体含量较高，无法直接进入脱乙烷塔获得聚合级的乙烯；而只能与深冷或者其他工艺相配套使用，这样会带来额外的投资。而新的流程只需要吸收就可以获得聚合级的乙烯原料，回收率达到90％以上。
(2)本方法利用了吸收法灵活、对原料适应性强的特点，对于组成复杂的催化裂化干气有较好地吸收效果。相比深冷法，该方法避免了乙烯制冷机，节约了能耗和投资。
附图说明
图1为本发明工艺流程示意图。
具体实施方式
以下结合附图和具体实施方案对本发明进行更详细的介绍，但不对本发明的可实施范围构成任何限定。
装置如图1所示：压缩机2的出口与原料一级冷却器4的入口相连接，原料一级冷却器4的出口与原料二级冷却器6的一个干气气相入口相连。原料二级冷却器6的出口与分离罐8的入口相连，分离罐8的气相出口与吸收塔29的气相入口连接，液相出口与解吸塔13塔顶的液相入口相连接。吸收塔29的液相出口与原料二级冷却器6的液相入口相连，解吸塔13的气相出口与原料二级冷却器6的解吸气入口相连。解吸塔13的塔底液相出口与预热器15的冷物流入口相连，预热器15的冷物流出口与精馏塔17的进料口相连。精馏塔17的塔底液相出口与加压泵19的入口相连，加压泵19的出口与预热器15的热物流入口相连。预热器15的热物流出口与吸收剂一级冷却器22的入口相连，吸收剂一级冷却器22的出口与吸收剂二级冷却器24的入口相连。吸收剂二级冷却器24的出口与吸收剂混合器27的一个入口相连，吸收剂混合器27的出口与吸收塔29的液相入口相连。
本发明提出的一种油吸收干气回收乙烯、乙烷的三塔方法，其分离流程为：原料气1在压缩机2中增压后，经过原料一级冷却器4冷却，与吸收液12和解吸气11一起进入原料二级冷却器6。二级冷却进料7进入分离罐8进行汽液分离，产生吸收气10和解吸液9。吸收气10进入吸收塔29下部，解吸液9进入解吸塔13上部。解吸液14从解吸塔13底部采出后，进入预热器15预热后形成预热液16进入精馏塔17。精馏塔17塔顶产出乙烯、乙烷产品31，塔底采出热吸收剂18。热吸收剂18经过加压泵19后形成加压吸收剂20。加压吸收剂20经过预热器15换热后降温，形成预冷吸收剂21。预冷吸收剂21经过吸收剂一级冷却器21和吸收剂二级冷却器24后，形成二级冷却吸收剂25。二级冷却吸收剂25与补充吸收剂26在吸收剂混合器27中混合形成循环吸收剂28进入吸收塔29上部。吸收塔29塔顶产出燃料尾气30。
具体技术条件为：压缩机2出口压力为2.8～3.4Mpa；原料一级冷却器4出口温度为32～40℃；原料二级冷却器6出口温度为-20～-10℃；吸收塔29压力为2.8～3.4MPa，理论板数为18～24。在吸收塔29中，吸收剂将大部分乙烯、乙烷等重组分吸收下来，集中在塔底，而甲烷等杂质气体集中在塔顶。解吸塔13的操作压力为2.9～3.5MPa，理论板数为10～16。解吸塔13中，甲烷等杂质气体通过解吸作用集中在塔顶，乙烯及其他物质集中在塔底。预热器15的冷物料出口温度为130～140℃。精馏塔17的操作压力为2.2～2.8MPa，回流比为1.8～2.2，理论板数为16～24。吸收剂一级冷却器22的出口温度为32～40℃，吸收剂二级冷却器24的出口温度为-20～-10℃。整个流程中的吸收剂采用C5馏分。
实施例1.
原料气1的摩尔组成为21.1％H2+24.5％N2+24.3％CH4+21％C2H4+7.8％C2H6+0.2C3H6+0.4％O2+0.6％CO，质量流量为7.5tons/hr，温度40℃。工艺中采用C5作为吸收剂，循环吸收剂的量为20tons/hr。
压缩机2将原料气1压缩到3.05Mpa，原料一级冷却器4将压缩气3冷却至32℃，原 料二级冷却器6将吸收液12、一级冷却气5、解吸气11冷却至-15℃。分离罐8在3.05MPa绝热闪蒸。吸收塔29理论板数为12，操作压力为3MPa；解吸塔13理论板数为10，操作压力为3.05MPa。预热器15将解吸液14预热至132℃。精馏塔17理论板数为20，操作压力为2.6MPa，回流比为2，预热液16从第10块进料。热吸收剂18经过加压泵19加压至3MPa。吸收剂一级冷却器22将预冷吸收剂21冷却至32℃，吸收剂二级冷却剂24将一级冷却吸收剂23冷却至-15℃。二次冷却吸收剂25与补充吸收剂26在吸收剂混合器27混合后，形成循环吸收剂28进入吸收塔29的第一块理论板。表格1显示，乙烯、乙烷产品31中甲烷占甲烷乙烯两者摩尔流量的分数为0.045％，在经过脱乙烷之后可以获得聚合级乙烯。
表格1典型催化干气吸收分离结果：
Figure PCTCN2015090879-appb-000001
从表中可以计算得出，乙烯、乙烷产品中的CH4与C2H4摩尔流量分别为0.03kmol 和66.64kmol。CH4占两者之和的摩尔分数为0.00045，即不到0.05％。这样的气相产品经过脱乙烷塔的处理后，可以直接获得聚合级的乙烯。

Claims (9)

  1. 一种油吸收干气回收高纯度乙烯、乙烷的三塔装置：包括压缩机、吸收塔、解吸塔和精馏塔；其特征是压缩机的出口与原料一级冷却器的入口相连接，原料一级冷却器的出口与原料二级冷却器的一个入口相连；原料二级冷却器的出口与分离罐的入口相连，分离罐的气相出口与吸收塔的气相入口连接，分离罐的液相出口与解吸塔塔顶的液相入口相连接；吸收塔的液相出口和解吸塔的气相出口与原料二级冷却器的另外两个入口相连；解吸塔的塔底液相出口与预热器的冷物流入口相连，预热器的冷物流出口与精馏塔的进料口相连；精馏塔的塔底液相出口与加压泵的入口相连，加压泵的出口与预热器的热物流入口相连；预热器的热物流出口与吸收剂一级冷却器的入口相连，吸收剂一级冷却器的出口与吸收剂二级冷却器的入口相连；吸收剂二级冷却器的出口与吸收剂混合器的一个入口相连，吸收剂混合器的出口与吸收塔的液相入口相连；吸收塔塔顶设置燃料尾气出口，精馏塔塔顶产设置乙烯、乙烷产品出口。
  2. 一种油吸收干气回收乙烯、乙烷的三塔回收方法，其特征是：原料气在压缩机中增压后，经过原料一级冷却器冷却，与吸收液和解吸气一起进入原料二级冷却器；二级冷却进料进入分离罐进行汽液分离，产生吸收气和解吸液；吸收气进入吸收塔下部，解吸液进入解吸塔上部；解吸液从解吸塔底部采出后，进入预热器预热后形成预热液进入精馏塔；精馏塔塔顶产出乙烯、乙烷产品，塔底采出热吸收剂；热吸收剂经过加压泵后形成加压吸收剂；加压吸收剂经过预热器换热后降温，形成预冷吸收剂；预冷吸收剂经过吸收剂一级冷却器和吸收剂二级冷却器后，形成二级冷却吸收剂；二级冷却吸收剂与补充吸收剂在吸收剂混合器中混合形成循环吸收剂2进入吸收塔2上部；吸收塔塔顶产出燃料尾气。
  3. 如权利要求2所述的方法，其特征是所述的压缩机出口压力为2.8～3.4Mpa；
  4. 如权利要求2所述的方法，其特征是所述的原料一级冷却器出口温度为32～40℃；原料二级冷却器出口温度为-20～-10℃。
  5. 如权利要求2所述的方法，其特征是所述的吸收塔压力为2.8～3.4MPa，理论板数为18～24。
  6. 如权利要求2所述的方法，其特征是所述的解吸塔的操作压力为2.9～3.5MPa，理论板数为10～16。
  7. 如权利要求2所述的方法，其特征是所述的预热器的冷物料出口温度为130～140℃。
  8. 如权利要求2所述的方法，其特征是所述的精馏塔的操作压力为2.2～2.8MPa，回流比为1.8～2.2，理论板数为16～24。
  9. 如权利要求2所述的方法，其特征是所述的吸收剂一级冷却器的出口温度为32～40℃，吸收剂二级冷却器的出口温度为-20～-10℃。
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
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Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101602959A (zh) * 2009-07-09 2009-12-16 天津大学 催化裂化装置下游分离系统提高液化气收率的方法
CN101638584A (zh) * 2008-08-01 2010-02-03 中国石油化工股份有限公司 采用浅冷油吸收法分离炼厂催化干气的方法
CN103030494A (zh) * 2012-12-21 2013-04-10 天津大学 用于分离催化裂化干气或乙烯裂解气中的乙烯、乙烷的吸收水合耦合装置及方法
CN103068778A (zh) * 2010-08-26 2013-04-24 韩国能量技术研究院 用于从流化催化裂化废气中回收乙烯的装置和方法
CN104419464A (zh) * 2013-09-10 2015-03-18 中国石油化工股份有限公司 一种炼厂干气回收系统及干气回收方法
CN104892340A (zh) * 2015-06-10 2015-09-09 天津大学 一种油吸收干气回收乙烯、乙烷的三塔装置与方法

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103087772A (zh) * 2011-11-02 2013-05-08 中国石油化工股份有限公司 一种采用油吸收分离炼厂干气的装置及方法

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN101638584A (zh) * 2008-08-01 2010-02-03 中国石油化工股份有限公司 采用浅冷油吸收法分离炼厂催化干气的方法
CN101602959A (zh) * 2009-07-09 2009-12-16 天津大学 催化裂化装置下游分离系统提高液化气收率的方法
CN103068778A (zh) * 2010-08-26 2013-04-24 韩国能量技术研究院 用于从流化催化裂化废气中回收乙烯的装置和方法
CN103030494A (zh) * 2012-12-21 2013-04-10 天津大学 用于分离催化裂化干气或乙烯裂解气中的乙烯、乙烷的吸收水合耦合装置及方法
CN104419464A (zh) * 2013-09-10 2015-03-18 中国石油化工股份有限公司 一种炼厂干气回收系统及干气回收方法
CN104892340A (zh) * 2015-06-10 2015-09-09 天津大学 一种油吸收干气回收乙烯、乙烷的三塔装置与方法

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